Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors

*Xianhui Zhao, Kai Li, Meghan E. Lamm, Serdar Celik, Lin Wei and Soydan Ozcan*

## **Abstract**

Interest in converting waste into renewable energy has increased recently due to concerns about sustainability and climate change. This solid waste is mainly derived from municipal solid waste (MSW), biomass residue, plastic waste, and their mixtures. Gasification is one commonly applied technology that can convert solid waste into usable gases, including H2, CO, CH4, and CO2. Single- and multi-staged reactors have been utilized for solid waste gasification. Comparison in reactor dimensions, operating factors (e.g., gasification agent, temperature, and feed composition), performance (e.g., syngas yield and selectivity), advantages, and disadvantages are discussed and summarized. Additionally, discussion will include economic and advanced catalysts which have been developed for use in solid waste gasification. The multi-staged reactor can not only be applied for gasification, but also for pyrolysis and torrefaction.

**Keywords:** solid waste, gasification, single-staged reactor, multi-staged reactor, syngas, catalyst

## **1. Introduction**

Solid waste can be derived from municipal solid waste (MSW), biomass residue, plastic waste, and their mixtures. For example, MSW management has become a big challenge all over the world. Based on a World Bank report [1], the world generates 0.74 kg of waste per capita per day, and the total MSW production is projected to grow to 3.40 billion tons by 2050. 37% of this MSW ends up in landfills and 33% is openly dumped worldwide [1]. Only 19% undergoes material recovery through recycling and composting, while the remaining 11% is treated through modern incineration. This creates serious environmental problems and a huge energy waste. One sustainable strategy for waste management is to reduce landfill disposal, thus minimizing the environmental impact. Meanwhile, utilizing solid waste resources to create valueadded products has become one of the most attracting topics. The top 3 components of MSW are food and green waste (44%), paper and cardboard (17%), and rubber and leather (12%) [1]. Therefore, MSW contains a high content of organic material, which can be recovered through biochemical [2] and thermochemical processes [3]. Thermochemical processes are promising for dealing with a large quantity of MSW, especially from unsorted waste streams, as it can significantly reduce the waste in both mass (about 70–80%) and volume (about 80–90%) with a high conversion rate. Other detailed advantages can be found in Arena's review on thermochemical processes [4].

Various thermochemical processes, such as incineration, pyrolysis, and gasification, have been developed to recover energy from the organic fraction in MSW [5]. Incineration is a full oxidation of the combustible materials in the waste and generates energy in the form of heat. Incineration has been traditionally used to treat waste. However, due to the production of flue gases (CO2, H2O, O2, N2) during the process and legislation enforcement regarding gas emission, new development of incineration is needed to reduce the environmental impact. Pyrolysis is the thermal degradation of waste, under a limit or total absence of an oxidizing agent. Pyrolysis can recover part of the organic fraction as liquid fuels (e.g., hydrocarbons, alcohols), while also generating a small amount of synthesis gas (syngas, a mixture of CO, H2, CO2, CH4, etc.) and biochar. The generated syngas can be used to power gas engines or turbines to generate electricity. Although there may be some differences in yield, proportion, and exact composition, gasification is a partial oxidation of organic compounds and mainly produces syngas. Syngas can be converted into value products through processes such as the Fischer-Tropsch synthesis [6, 7], or used as a fuel for electricity and heat generation. Therefore, gasification can produce energy, energy carriers (such as H2) and chemicals from the solid waste [8], all of which creates lots of research interest. Additionally, gasification has advantages including no limitations on the size and type of waste, different applications of the gaseous fuels, and a decrease in overall pollution.

Gasification of solid waste is a complex process, including different chemical and physical transformations at high temperature (e.g., >600 °C). Based on the oxidation medium, gasification can be classified into partial oxidation with air, oxygenenriched air, pure oxygen, steam, and plasma gasification. Different gasification processes generate different gas compositions, heating values and byproduct yields. In general, there are four steps in gasification: vaporization, devolatilization/pyrolysis, secondary cracking of tars, and reactions/reduction/gasification [9]. Vaporization involves heating the waste at low temperature (ca. 160 °C) to remove water from the solid waste. Devolatilization/pyrolysis occurs at a higher temperature and generates char and volatiles, which include long chain hydrocarbon liquids and a small fraction of gases. Secondary cracking of tars (a mixture of condensable hydrocarbons) is used to further crack the tars and involves several homogeneous reactions in the gas phase and heterogeneous ones at the surface of the solid fuel or char particles. Reactions/ reduction/gasification is used to react the char with a gas species using heterogeneous reactions. The reactions which occur during gasification are complex, making it difficult to optimize the processing parameters to obtain the best quality and yield of syngas. These parameters include equivalence ratio, reactor temperature, residence time of gases and waste, waste composition and physical properties, and composition and inlet temperature of the gasifying medium. Park et al. [10] performed a two-staged gasification of high-density polyethylene (HDPE) and biomass blends, comprised of an oxidative pyrolysis reactor and a thermal plasma reactor. They found that, for higher biomass fractions, enhanced CO2 yields were produced and reversely, an increased HDPE fraction yielded a higher content of hydrocarbons.

Different reactors, including single-staged and multi-staged gasifiers, have been developed for gasification [5]. For a single-staged reactor, the pyrolysis and gasification zones are packed into one reactor (**Figure 1a**). A single-staged gasifier includes a fixed bed gasifier [11, 12], fluidized bed gasifier [13, 14], and entrained flow gasifier [15, 16]. A multi-staged reactor system is configured in two ways: a single reactor with separate, controlled pyrolysis and gasification zones, and separate pyrolysis and gasification reactors connected in series (**Figure 1b**). The multi-staged gasification technology allows for optimization of reaction conditions

**125**

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors*

for the conversion of biomass at every separate stage. Both single- and multi-staged reactors have been utilized for solid waste gasification. Single- and multi-staged reactors are illustrated in **Figure 1**. Chan et al. [18] studied the single-staged gasification of MSW, finding that the tar content in syngas could reach 7.8 g/Nm3

*Schematic of a single-staged reactor (a, fixed bed gasifier) and multi-staged reactor (b, 1: first stage [pyrolysis], 2: second stage [thermal decomposition of tar], 3: third stage [gasification], 4: fluidized bed) [17]. Reproduced* 

et al. [19] investigated the co-gasification of a MSW and switchgrass mixture in a

reactor, a multi-staged reactor system can reduce the tar yield, which is beneficial because generated tar can cause failure of gasification projects [20]. Gómez-Barea et al. [21] developed a three-staged, fluidized bed based gasification reactor and found that this three-staged system depicted a higher gasification efficiency (14%) and lower tar content, compared to a regular single-staged fluidized bed reactor. However, literature providing a comparison between single- and multi-staged reactors for solid waste gasification remains sparse. The analysis of reactor dimensions, operating factors, and performance of these reactors has not been studied systematically. It is the goal of this review to present current literature comparing

This chapter focuses on the comparison of single- and multi-staged reactors used for solid waste gasification. Solid waste resources such as MSW, biomass residue, plastic waste, and their mixtures are discussed. The reactor dimensions, operating factors (e.g., temperature, gasification agent, and feed composition), performance (e.g., syngas yield), advantages, and disadvantages of single- and multi-staged reactors are discussed and summarized. Additionally, discussion includes economic and advanced catalysts (e.g., Ni-CaO-C and Ni/Al2O3) which have been developed for use in solid waste gasification. These Ni based catalysts are promising for solid waste gasification at high conversion efficiency. The multi-staged reactor can not only be

Different reactor scales, including bench, lab, and pilot scale, have been developed for solid waste gasification. The inside diameter and length of the reactor

these reactor types and analyzing their relevant processing parameters.

applied for gasification, but also for pyrolysis and torrefaction.

**2. Solid waste gasification**

**2.1 Single-staged reactor**

*2.1.1 Reactor dimensions*

. Bhoi

of tar. Compared with a single-staged

*DOI: http://dx.doi.org/10.5772/intechopen.96157*

single-staged reactor, producing 9.9–26 g/Nm3

**Figure 1.**

*with permission from [17].*

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors DOI: http://dx.doi.org/10.5772/intechopen.96157*

**Figure 1.**

*Gasification*

mass (about 70–80%) and volume (about 80–90%) with a high conversion rate. Other detailed advantages can be found in Arena's review on thermochemical processes [4]. Various thermochemical processes, such as incineration, pyrolysis, and gasifica-

Gasification of solid waste is a complex process, including different chemical and physical transformations at high temperature (e.g., >600 °C). Based on the oxidation medium, gasification can be classified into partial oxidation with air, oxygenenriched air, pure oxygen, steam, and plasma gasification. Different gasification processes generate different gas compositions, heating values and byproduct yields. In general, there are four steps in gasification: vaporization, devolatilization/pyrolysis, secondary cracking of tars, and reactions/reduction/gasification [9]. Vaporization involves heating the waste at low temperature (ca. 160 °C) to remove water from the solid waste. Devolatilization/pyrolysis occurs at a higher temperature and generates char and volatiles, which include long chain hydrocarbon liquids and a small fraction of gases. Secondary cracking of tars (a mixture of condensable hydrocarbons) is used to further crack the tars and involves several homogeneous reactions in the gas phase and heterogeneous ones at the surface of the solid fuel or char particles. Reactions/ reduction/gasification is used to react the char with a gas species using heterogeneous reactions. The reactions which occur during gasification are complex, making it difficult to optimize the processing parameters to obtain the best quality and yield of syngas. These parameters include equivalence ratio, reactor temperature, residence time of gases and waste, waste composition and physical properties, and composition and inlet temperature of the gasifying medium. Park et al. [10] performed a two-staged gasification of high-density polyethylene (HDPE) and biomass blends, comprised of an oxidative pyrolysis reactor and a thermal plasma reactor. They found that, for higher biomass fractions, enhanced CO2 yields were produced and reversely,

an increased HDPE fraction yielded a higher content of hydrocarbons.

Different reactors, including single-staged and multi-staged gasifiers, have been developed for gasification [5]. For a single-staged reactor, the pyrolysis and gasification zones are packed into one reactor (**Figure 1a**). A single-staged gasifier includes a fixed bed gasifier [11, 12], fluidized bed gasifier [13, 14], and entrained flow gasifier [15, 16]. A multi-staged reactor system is configured in two ways: a single reactor with separate, controlled pyrolysis and gasification zones, and separate pyrolysis and gasification reactors connected in series (**Figure 1b**). The multi-staged gasification technology allows for optimization of reaction conditions

tion, have been developed to recover energy from the organic fraction in MSW [5]. Incineration is a full oxidation of the combustible materials in the waste and generates energy in the form of heat. Incineration has been traditionally used to treat waste. However, due to the production of flue gases (CO2, H2O, O2, N2) during the process and legislation enforcement regarding gas emission, new development of incineration is needed to reduce the environmental impact. Pyrolysis is the thermal degradation of waste, under a limit or total absence of an oxidizing agent. Pyrolysis can recover part of the organic fraction as liquid fuels (e.g., hydrocarbons, alcohols), while also generating a small amount of synthesis gas (syngas, a mixture of CO, H2, CO2, CH4, etc.) and biochar. The generated syngas can be used to power gas engines or turbines to generate electricity. Although there may be some differences in yield, proportion, and exact composition, gasification is a partial oxidation of organic compounds and mainly produces syngas. Syngas can be converted into value products through processes such as the Fischer-Tropsch synthesis [6, 7], or used as a fuel for electricity and heat generation. Therefore, gasification can produce energy, energy carriers (such as H2) and chemicals from the solid waste [8], all of which creates lots of research interest. Additionally, gasification has advantages including no limitations on the size and type of waste, different applications of the

gaseous fuels, and a decrease in overall pollution.

**124**

*Schematic of a single-staged reactor (a, fixed bed gasifier) and multi-staged reactor (b, 1: first stage [pyrolysis], 2: second stage [thermal decomposition of tar], 3: third stage [gasification], 4: fluidized bed) [17]. Reproduced with permission from [17].*

for the conversion of biomass at every separate stage. Both single- and multi-staged reactors have been utilized for solid waste gasification. Single- and multi-staged reactors are illustrated in **Figure 1**. Chan et al. [18] studied the single-staged gasification of MSW, finding that the tar content in syngas could reach 7.8 g/Nm3 . Bhoi et al. [19] investigated the co-gasification of a MSW and switchgrass mixture in a single-staged reactor, producing 9.9–26 g/Nm3 of tar. Compared with a single-staged reactor, a multi-staged reactor system can reduce the tar yield, which is beneficial because generated tar can cause failure of gasification projects [20]. Gómez-Barea et al. [21] developed a three-staged, fluidized bed based gasification reactor and found that this three-staged system depicted a higher gasification efficiency (14%) and lower tar content, compared to a regular single-staged fluidized bed reactor. However, literature providing a comparison between single- and multi-staged reactors for solid waste gasification remains sparse. The analysis of reactor dimensions, operating factors, and performance of these reactors has not been studied systematically. It is the goal of this review to present current literature comparing these reactor types and analyzing their relevant processing parameters.

This chapter focuses on the comparison of single- and multi-staged reactors used for solid waste gasification. Solid waste resources such as MSW, biomass residue, plastic waste, and their mixtures are discussed. The reactor dimensions, operating factors (e.g., temperature, gasification agent, and feed composition), performance (e.g., syngas yield), advantages, and disadvantages of single- and multi-staged reactors are discussed and summarized. Additionally, discussion includes economic and advanced catalysts (e.g., Ni-CaO-C and Ni/Al2O3) which have been developed for use in solid waste gasification. These Ni based catalysts are promising for solid waste gasification at high conversion efficiency. The multi-staged reactor can not only be applied for gasification, but also for pyrolysis and torrefaction.

### **2. Solid waste gasification**

#### **2.1 Single-staged reactor**

#### *2.1.1 Reactor dimensions*

Different reactor scales, including bench, lab, and pilot scale, have been developed for solid waste gasification. The inside diameter and length of the reactor

are typically in the range of 3–800 mm and 200–3500 mm, respectively, as shown in **Table 1**. Selection of the appropriate reactor dimensions is helpful for the solid waste gasification performance. For example, Xiong et al. [38] found that the reactor diameter had a negligible effect on gasification performance, but an increase in bed height (0.6–1.2 m) caused an increased heating value and carbon conversion efficiency. Basha et al. [39] found that a difference in the hydrocarbon content and methane concentration of the product gas depends on the reactor size and design. Larger reactors can increase the residence time of the product gas in the reactor, so that lighter hydrocarbons have more time to decompose or undergo oxidization into smaller molecules such as H2 and CO [39]. There are various types of reactors developed for solid waste gasification, including bubbling fluidized bed, downdraft fluidized bed, updraft fluidized bed, downdraft fixed bed, updraft fixed bed, batch, and entrained-flow reactors, some of which are shown in **Figures 2**–**4**. Different types of reactors are applicable for specific types of solid waste. For example, steam gasification of waste with a high moisture content occurs well in a bubbling fluidized bed reactor.

Other designs, such as adding a stirrer or using sorbents, have been developed to improve the solid waste gasification performance. In a study, Indrawan et al. [32] utilized a stirrer in a downdraft reactor system to create a uniform mixing feed and prevent bridging inside the reactor; a rotating ash scrapper to unload ash from the reactor and prevent ash accumulation inside the reactor; and an inclined ash screw conveyor to transport the ash into the ash drum. Pinto et al. [30] used water to cool the feeding system and avoid clogging inside, which can arise from the feedstock pyrolysis (prior to entry into the reactor). N2 was blown through the feeding system to help transfer the feedstock smoothly, avoid plugging, and prevent gas backflow. Lastly, the gas product passed through a cyclone to remove particulates [30]. Salaudeen et al. [42] used calcined eggshell as the bed material and CO2 sorbent for the steam gasification of sawdust, in a bubbling fluidized bed reactor, to improve the hydrogen content in the syngas. The sorbent-enhanced gasification enabled the reactor operation at comparatively lower temperatures, and required less equipment [42]. In summary, the reactor design and size (inside diameter of 3–800 mm and length of 200–3500 mm) need to be optimized to maximize the solid waste gasification performance.

## *2.1.2 Operating factors and performance*

During the solid waste gasification process, many parameters such as temperature, feed composition, gasification agent, and reaction time are investigated. **Table 2** shows the syngas yield (typically 1.2–2.2 Nm3 /kg) obtained from gasification under varying conditions. Temperature is a significant parameter that can affect the gasification performance and is usually in the range of 600–900 °C. For example, Bai et al. [34] studied the gasification of PP at 23 MPa and 500–800 °C, finding that an increase in temperature improved the gasification efficiency. Bai et al. [43] also studied the supercritical water gasification of polyethylene terephthalate (PET), finding that the gasification efficiency increased with an increase in temperature from 500 to 800 °C. The PET gasification reaction increased slowly with the temperature (500–700 °C). Based on the kinetics, the PET gasification reaction was complex and intense in the initial stage of gasification. Most active components gasified quickly, while inert components reacted slowly in the later stage of gasification [43]. Peng et al. [44] studied the gasification at various gasification temperatures (750, 825, and 900 °C), finding that high temperature (900 °C) was favorable for tar cracking. Xiong et al. [38] studied gasification at 400–800 °C, finding that an increase in temperature affected the heating value and improved the gasifier

**127**

*a*

*b*

*c*

**Table 1.**

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors*

Sealed quartz Inside diameter = 3 mm,

**Waste Reactor type Reactor dimension Other Ref.**

Inside diameter = 48 mm, length = 500 mm

Inside diameter = 25 mm, length = 1000 mm

Diameter = 0.08 and 0.8 m, bed height = 0.6–1.2 m

Inside diameter = 54 mm, length = 1.25 m

Inside diameter = 80 mm,

Downdraft Length = 3.2 m Feedstock flow rate:

length = 1.5 m

length = 610 mm

length = 200 mm

length = 1.8 m

length = 2.3 m

Inside diameter = 19 mm,

Inside diameter = 0.25 m,

Inside diameter = 0.2 m, length = 3.5 m

Food waste Batch Reactor volume = 200 mL Supercritical

length = 200 mm

length = 600 mm

— [22]

— [23]

— [38]

— [26]

— [29]

— [31]

— [34]

— [36]

[24]

[25]

[27]

[28]

[30]

[32]

[33]

[35]

[37]

, PEb , or

Plastic: PPa

gasification

10 kg/h

waste

5 g/min

100 kg/h

water gasification; maximum operation temperature: 600 °C, maximum operation pressure: 35 MPa

Feedstock flow rate: 0.78 g/min

Reactor capacity: 50 kg/h

composition: paper, plastic, and kitchen

Feedstock flow rate:

PCc

— Supercritical water

— Feedstock flow rate:

— Feedstock main

*DOI: http://dx.doi.org/10.5772/intechopen.96157*

horizontal tube

Stainless steel batch (autoclave)

fluidized bed

Fixed bed downdraft

Fixed bed updraft

reverse downdraft

Bench scale bubbling fluidized bed

Biomass Fluidized bed Outside diameter = 120 mm,

PP Quartz tube Inside diameter = 3 mm,

*The solid waste gasification, single-staged reactor type, and dimension.*

MSW Fixed bed Outside diameter = 219 mm,

MSW Lab scale fixed bed

Landfill waste Lab-scale

Rice husk Bubbling

Biomass Fixed bed

MSW Drop quartz

Sawdust Pilot scale

tube

Pilot-scale bubbling fluidized bed

bubbling fluidized

Lignite coal and plastic mixture

Poplar wood chips

Chicken manure and wood chip mixture

Rural solid waste

Rice production waste mixture

MSW and switchgrass mixture

MSW and biomass mixture

*Polypropylene (PP).*

*Polycarbonate (PC).*

*Polyethylene (PE).*


#### *Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors DOI: http://dx.doi.org/10.5772/intechopen.96157*

*Gasification*

are typically in the range of 3–800 mm and 200–3500 mm, respectively, as shown in **Table 1**. Selection of the appropriate reactor dimensions is helpful for the solid waste gasification performance. For example, Xiong et al. [38] found that the reactor diameter had a negligible effect on gasification performance, but an increase in bed height (0.6–1.2 m) caused an increased heating value and carbon conversion efficiency. Basha et al. [39] found that a difference in the hydrocarbon content and methane concentration of the product gas depends on the reactor size and design. Larger reactors can increase the residence time of the product gas in the reactor, so that lighter hydrocarbons have more time to decompose or undergo oxidization into smaller molecules such as H2 and CO [39]. There are various types of reactors developed for solid waste gasification, including bubbling fluidized bed, downdraft fluidized bed, updraft fluidized bed, downdraft fixed bed, updraft fixed bed, batch, and entrained-flow reactors, some of which are shown in **Figures 2**–**4**. Different types of reactors are applicable for specific types of solid waste. For example, steam gasification of waste with a high moisture content

Other designs, such as adding a stirrer or using sorbents, have been developed to improve the solid waste gasification performance. In a study, Indrawan et al. [32] utilized a stirrer in a downdraft reactor system to create a uniform mixing feed and prevent bridging inside the reactor; a rotating ash scrapper to unload ash from the reactor and prevent ash accumulation inside the reactor; and an inclined ash screw conveyor to transport the ash into the ash drum. Pinto et al. [30] used water to cool the feeding system and avoid clogging inside, which can arise from the feedstock pyrolysis (prior to entry into the reactor). N2 was blown through the feeding system to help transfer the feedstock smoothly, avoid plugging, and prevent gas backflow. Lastly, the gas product passed through a cyclone to remove particulates [30]. Salaudeen et al. [42] used calcined eggshell as the bed material and CO2 sorbent for the steam gasification of sawdust, in a bubbling fluidized bed reactor, to improve the hydrogen content in the syngas. The sorbent-enhanced gasification enabled the reactor operation at comparatively lower temperatures, and required less equipment [42]. In summary, the reactor design and size (inside diameter of 3–800 mm and length of 200–3500 mm) need to be optimized to maximize the solid waste

During the solid waste gasification process, many parameters such as temperature, feed composition, gasification agent, and reaction time are investigated. **Table 2**

temperature (500–700 °C). Based on the kinetics, the PET gasification reaction was complex and intense in the initial stage of gasification. Most active components gasified quickly, while inert components reacted slowly in the later stage of gasification [43]. Peng et al. [44] studied the gasification at various gasification temperatures (750, 825, and 900 °C), finding that high temperature (900 °C) was favorable for tar cracking. Xiong et al. [38] studied gasification at 400–800 °C, finding that an increase in temperature affected the heating value and improved the gasifier

varying conditions. Temperature is a significant parameter that can affect the gasification performance and is usually in the range of 600–900 °C. For example, Bai et al. [34] studied the gasification of PP at 23 MPa and 500–800 °C, finding that an increase in temperature improved the gasification efficiency. Bai et al. [43] also studied the supercritical water gasification of polyethylene terephthalate (PET), finding that the gasification efficiency increased with an increase in temperature from 500 to 800 °C. The PET gasification reaction increased slowly with the

/kg) obtained from gasification under

occurs well in a bubbling fluidized bed reactor.

gasification performance.

*2.1.2 Operating factors and performance*

shows the syngas yield (typically 1.2–2.2 Nm3

**126**

#### **Table 1.**

*The solid waste gasification, single-staged reactor type, and dimension.*

#### **Figure 2.**

*Illustration of the downdraft gasification of MSW integrated with a hot syngas purification system. RDF pellets were gasified to produce syngas. Some of the syngas passed through a purification system (including a tar reformer, particulate filter, and dechlorination/desulfurization reactor) to remove impurities (tar, particulates, HCl, and sulfur species). (ER: equivalence air ratio, TC1: thermocouple 1, TC2: thermocouple 2, RDF: refuse derived fuel, TR: tar reformer, DES: desulfurization reactor, GS: gasifier, SPA: solid phase adsorption) [18]. Reproduced with permission from [18].*

#### **Figure 3.**

*Schematic diagram of an H2 production plant with gasification of MSW. MSW was pre-processed and then gasified to produce syngas, which passed through a WGS reactor to produce H2. Partial MSW combustion provided heat for district heating and power grid. (WGS: water gas shift, CHP: combined heat and power) [40]. Reproduced with permission from [40].*

efficiency. Xiang et al. [26] studied the steam gasification at temperatures of 600–1000 °C, finding that the increase in temperature increased the total volume fraction of H2 and CO from 56% to 66%. From all the above studies, an appropriate temperature (e.g., 800–900 °C) should be selected for solid waste gasification based on high gasification performance and low energy consumption.

Feed composition is also a significant parameter for gasification. For example, Pio et al. [36] studied gasification using a refuse-derived fuel (from MSW) and biomass (pine chips or pine pellets) mixture. 0, 10, 20, 50, and 100 wt% of refuse-derived fuel content in the mixture was studied. An increase in the refuse-derived fuel content increased both the CH4 concentration and lower heating value (LHV) of the product gas. Therefore, the addition of refuse-derived fuel to biomass may improve

**129**

**Figure 4.**

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors*

the economic viability and environmental benefits for gasification plants. There was no agglomeration, slag, or defluidization observed during the experiment [36]. Ng et al. [27] studied the gasification of a chicken manure and wood chip mixture. The co-gasification of this chicken manure and wood chip mixture (30 wt% chicken manure) produced a syngas of similar quality (in terms of LHV) compared to that of gasification of pure wood chip. The chicken manure was found to be a compatible feedstock for gasification in the presence of wood chips [27]. Su et al. [45] studied the gasification of food waste at a food waste concentration of 10–30 wt%. When the food waste concentration increased from 10 to 30 wt%, the H2 yield largely decreased from 1.1 to 0.6 mol/kg, while the CH4 yield increased. However, higher food waste concentrations may cause the reactor to plug and catalyst to deactivate [45].

*An updraft gasification reactor (left) and a schematic diagram of the reactor interior (right). The reactor consisted of a stainless-steel cylinder with a height of 59 cm and a diameter of 8.3 cm. Biomass was transported through a feeding cochlea at the top. Four thermocouples (TH1–TH4) were used to monitor the temperature evolution during the gasification process. A perforated metal plate was used as a support for the gasification bed to allow the oxidant to flow through. A wind box was used to preheat the oxidant agent. The produced syngas was cleaned using a cyclone and a ceramic filter for particle removal. Reproduced with permission from [41].*

More researchers have studied the effect of feed composition on gasification performance. For example, Bian et al. [24] studied the supercritical water cogasification of a lignite coal and plastic (PP, PE, or PC) mixture at concentrations of 5–35 wt%. The co-gasification of lignite coal and plastic improved the gasification efficiency of each other, indicating a synergistic effect. This was also observed in other studies. Zaini et al. [23] studied the gasification of landfill waste and a landfill waste and biochar mixture. Co-gasification of landfill waste with biochar was beneficial to improve the H2 concentration in the syngas. At 800 °C, the addition of 35 wt% biochar enhanced the H2 concentration from 38 to 54 vol%, and reduced the tar yield from 0.05 to 0.01 g/g-fuel-daf (daf: dry-ash-free weight basis) [23]. It was

*DOI: http://dx.doi.org/10.5772/intechopen.96157*

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors DOI: http://dx.doi.org/10.5772/intechopen.96157*

#### **Figure 4.**

*Gasification*

**Figure 2.**

**Figure 3.**

*Reproduced with permission from [18].*

*[40]. Reproduced with permission from [40].*

**128**

efficiency. Xiang et al. [26] studied the steam gasification at temperatures of 600–1000 °C, finding that the increase in temperature increased the total volume fraction of H2 and CO from 56% to 66%. From all the above studies, an appropriate temperature (e.g., 800–900 °C) should be selected for solid waste gasification

*Schematic diagram of an H2 production plant with gasification of MSW. MSW was pre-processed and then gasified to produce syngas, which passed through a WGS reactor to produce H2. Partial MSW combustion provided heat for district heating and power grid. (WGS: water gas shift, CHP: combined heat and power)* 

*Illustration of the downdraft gasification of MSW integrated with a hot syngas purification system. RDF pellets were gasified to produce syngas. Some of the syngas passed through a purification system (including a tar reformer, particulate filter, and dechlorination/desulfurization reactor) to remove impurities (tar, particulates, HCl, and sulfur species). (ER: equivalence air ratio, TC1: thermocouple 1, TC2: thermocouple 2, RDF: refuse derived fuel, TR: tar reformer, DES: desulfurization reactor, GS: gasifier, SPA: solid phase adsorption) [18].* 

Feed composition is also a significant parameter for gasification. For example, Pio et al. [36] studied gasification using a refuse-derived fuel (from MSW) and biomass (pine chips or pine pellets) mixture. 0, 10, 20, 50, and 100 wt% of refuse-derived fuel content in the mixture was studied. An increase in the refuse-derived fuel content increased both the CH4 concentration and lower heating value (LHV) of the product gas. Therefore, the addition of refuse-derived fuel to biomass may improve

based on high gasification performance and low energy consumption.

*An updraft gasification reactor (left) and a schematic diagram of the reactor interior (right). The reactor consisted of a stainless-steel cylinder with a height of 59 cm and a diameter of 8.3 cm. Biomass was transported through a feeding cochlea at the top. Four thermocouples (TH1–TH4) were used to monitor the temperature evolution during the gasification process. A perforated metal plate was used as a support for the gasification bed to allow the oxidant to flow through. A wind box was used to preheat the oxidant agent. The produced syngas was cleaned using a cyclone and a ceramic filter for particle removal. Reproduced with permission from [41].*

the economic viability and environmental benefits for gasification plants. There was no agglomeration, slag, or defluidization observed during the experiment [36]. Ng et al. [27] studied the gasification of a chicken manure and wood chip mixture. The co-gasification of this chicken manure and wood chip mixture (30 wt% chicken manure) produced a syngas of similar quality (in terms of LHV) compared to that of gasification of pure wood chip. The chicken manure was found to be a compatible feedstock for gasification in the presence of wood chips [27]. Su et al. [45] studied the gasification of food waste at a food waste concentration of 10–30 wt%. When the food waste concentration increased from 10 to 30 wt%, the H2 yield largely decreased from 1.1 to 0.6 mol/kg, while the CH4 yield increased. However, higher food waste concentrations may cause the reactor to plug and catalyst to deactivate [45].

More researchers have studied the effect of feed composition on gasification performance. For example, Bian et al. [24] studied the supercritical water cogasification of a lignite coal and plastic (PP, PE, or PC) mixture at concentrations of 5–35 wt%. The co-gasification of lignite coal and plastic improved the gasification efficiency of each other, indicating a synergistic effect. This was also observed in other studies. Zaini et al. [23] studied the gasification of landfill waste and a landfill waste and biochar mixture. Co-gasification of landfill waste with biochar was beneficial to improve the H2 concentration in the syngas. At 800 °C, the addition of 35 wt% biochar enhanced the H2 concentration from 38 to 54 vol%, and reduced the tar yield from 0.05 to 0.01 g/g-fuel-daf (daf: dry-ash-free weight basis) [23]. It was


#### **Table 2.**

*The solid waste single-staged gasification factor and performance.*

also determined that an increase in feedstock concentration could cause problems with reactor operations, such as reactor plugging and damage, thus reducing the gasification efficiency. A suitable feedstock concentration should be selected to balance the gasification efficiency and industrial application [24].

During solid waste gasification, different gasification agents such as O2 and air can be used. For example, Pinto et al. [30] studied the gasification of rice husk, rice straw and PE at ~850 °C using different gasification agents, such as a mixture of steam, air, oxygen, and CO2. At this temperature, the heavier gaseous hydrocarbons and tar contents can be minimized, while steam can promote steam reforming reactions, thus resulting in a gas enriched in H2 and lower tar content. The use of steam and O2 was also a good gasification agent option, especially since it lacked N2 and prevented any diluting effects. The combination produces a larger gas HHV (around 42% higher) and greater energy conversion than those obtained when air was used instead of O2. However, the cost of O2 is still a disadvantage and limits its use [30].

**131**

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors*

Meng et al. [37] studied the effect of gasifying agents such as air, air–steam, oxygensteam, and oxygen-enriched air, on sawdust gasification. Compared to sawdust gasification using air, oxygen-enriched air increased LHV due to a reduction in N2 dilution, while air–steam favored H2 production due to water gas shift reaction enhancement [37]. Zheng et al. [35] studied the steam gasification of MSW using recycled CO2 at 1000 °C with a CO2/steam ratio of 0.5–3.0, and found that increasing the CO2/steam ratio from 0.5 to 2.5 increased both H2 and CO molar yields. In order to further improve the gasification performance, various catalysts have been developed and explored. For example, Wang et al. [49] studied the CO2-assisted gasification of PP at 900 °C, and discovered the catalytic (Ni/Al2O3 catalyst) gasification improved the gas evolution rate and syngas yield significantly compared to non-catalytic gasification. Irfan et al. [22] studied the catalytic gasification of MSW at 1 atm, finding that the use of waste marble powder as a catalyst was helpful to increase the H2 concentration and decrease the CO2 concentration in the gas product, compared to non-catalytic tests. Tian et al. [31] studied the gasification at 800–1000 °C, finding that the use of a catalyst (olivine) enhanced the syngas yield and reduced the cracked tar content. Peng et al. [44] studied gasification over a Ni/CeO2/Al2O3 catalyst at different Ni loadings (20, 30, and 40%), finding that a high catalyst loading (40%) was favorable for high-purity H2 production and tar cracking. The above research demonstrates that the use of an appropriate

Other parameters such as reaction time, waste pretreatment, and feed dimension have also been investigated for their influence on gasification performance. For example, Bai et al. [34] studied the gasification of PP at a reaction time of 2–60 min, finding that an increase in reaction time had a positive effect on the gasification efficiency. In another study, Bai et al. [43] studied the supercritical water gasification of PET, finding that gasification efficiency increased with the increase in reaction time from 2 to 60 min. Bai et al. [43] also found that the reaction pressure (21–29 MPa) had little impact on the gasification efficiency because the properties of the supercritical water did not change significantly at these different pressures. Su et al. [33] found that waste sorting is helpful to improve the H2-rich syngas production (or syngas yield) and gasification efficiency compared to unsorted waste. Xiang et al. [26] studied the steam gasification of MSW with two different MSW particle sizes (20 < diameter < 30 mm and 80 < diameter < 100 mm), finding that the increase of particle size decreased the total volume fraction of H2 and CO from 52% to 50%. Basha et al. [39] selected a feedstock size of 2–4 mm because a larger particle size prevented a compact fuel bed, while a smaller particle size blocked the reactor and plugged the gas outlet.

In single-staged reactor systems, different types of reactors have been utilized based on their advantages and disadvantages. The common reactors used for solid waste gasification include fixed bed, fluidized bed, and entrained flow reactors [50]. A fixed bed reactor has simple construction and operation. However, a fixed bed reactor is typically used for small size reactions with limited loading/processing flexibility because of the poor adaptability for heterogeneous materials. A fluidized bed reactor can provide high mixing and solid–gas contact, promote heat and mass transfer, increase the reaction rate and conversion efficiency, and improve the process flexibility, compared to a fixed bed reactor. However, for both fixed bed and fluidized bed reactors, tar formation is a major problem, while entrained flow

Indrawan et al. [32] studied the gasification of a MSW and switchgrass mixture, finding that the downdraft reactor (patented design) system design was selected due

reactors have a high cost and poor biomass adaptability [50].

*DOI: http://dx.doi.org/10.5772/intechopen.96157*

catalyst can improve product yield and selectivity.

*2.1.3 Advantages and disadvantages*

#### *Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors DOI: http://dx.doi.org/10.5772/intechopen.96157*

*Gasification*

**Waste Reactor** 

MSW Downdraft

Biomass Bubbling

MSW and switchgrass mixture

Palm kernel shell and PSa mixture

PE and soda lignin mixture

*a*

**Table 2.**

*Polystyrene (PS).*

**type**

fixed-bed

fluidized bed

Fixed bed downdraft

Food waste Batch 420 °C, 23 MPa,

**Reaction conditions**

850 °C, equivalence air ratio of 0.3

reaction time of 30 min

rate of 2.5 L/min

time of 30 min

time of 10 min

700–854 °C, equivalence ratio of 0.17–0.36

Downdraft 800 °C, air flow

Batch 700 °C, reaction

MSW Drop-tube 900 °C Syngas yield:

PET Quartz tube 800 °C, reaction

*The solid waste single-staged gasification factor and performance.*

**Performance Other Ref.**

MSW feed rate: 4.4 g/min; MSW moisture content: 25 wt%

Reactor volume: 200 mL; heat rate: 10 °C/min

Biomass feed rate: 7–15 kg/h

20% MSW in the feed mixture

20 wt% PS in the feed mixture

Internal volume: 10 mL; 50% PE in the feed mixture

CO2 gasification; MSW feed rate: 0.8 g/min

Supercritical water gasification [18]

[46]

[13]

[19]

[39]

[47]

[48]

[43]

Syngas yield: ~12 L/min

Gas yield: 8.4 mol/kg; H2 yield: 3.1 mol/kg

Syngas yield: 1.2–2.2 Nm3

carbon conversion efficiency: 60–88%

1.5 Nm3 /kg

Solid yield: ~17 wt%; liquid yield: ~18 wt%; tar yield: ~5 wt%; gas yield: ~60 wt%

Gas yield: 75 mol/kg

17.5 mol/kg

Carbon conversion: 98 wt%

~800 °C Syngas yield:

/kg;

**130**

also determined that an increase in feedstock concentration could cause problems with reactor operations, such as reactor plugging and damage, thus reducing the gasification efficiency. A suitable feedstock concentration should be selected to

During solid waste gasification, different gasification agents such as O2 and air can be used. For example, Pinto et al. [30] studied the gasification of rice husk, rice straw and PE at ~850 °C using different gasification agents, such as a mixture of steam, air, oxygen, and CO2. At this temperature, the heavier gaseous hydrocarbons and tar contents can be minimized, while steam can promote steam reforming reactions, thus resulting in a gas enriched in H2 and lower tar content. The use of steam and O2 was also a good gasification agent option, especially since it lacked N2 and prevented any diluting effects. The combination produces a larger gas HHV (around 42% higher) and greater energy conversion than those obtained when air was used instead of O2. However, the cost of O2 is still a disadvantage and limits its use [30].

balance the gasification efficiency and industrial application [24].

Meng et al. [37] studied the effect of gasifying agents such as air, air–steam, oxygensteam, and oxygen-enriched air, on sawdust gasification. Compared to sawdust gasification using air, oxygen-enriched air increased LHV due to a reduction in N2 dilution, while air–steam favored H2 production due to water gas shift reaction enhancement [37]. Zheng et al. [35] studied the steam gasification of MSW using recycled CO2 at 1000 °C with a CO2/steam ratio of 0.5–3.0, and found that increasing the CO2/steam ratio from 0.5 to 2.5 increased both H2 and CO molar yields.

In order to further improve the gasification performance, various catalysts have been developed and explored. For example, Wang et al. [49] studied the CO2-assisted gasification of PP at 900 °C, and discovered the catalytic (Ni/Al2O3 catalyst) gasification improved the gas evolution rate and syngas yield significantly compared to non-catalytic gasification. Irfan et al. [22] studied the catalytic gasification of MSW at 1 atm, finding that the use of waste marble powder as a catalyst was helpful to increase the H2 concentration and decrease the CO2 concentration in the gas product, compared to non-catalytic tests. Tian et al. [31] studied the gasification at 800–1000 °C, finding that the use of a catalyst (olivine) enhanced the syngas yield and reduced the cracked tar content. Peng et al. [44] studied gasification over a Ni/CeO2/Al2O3 catalyst at different Ni loadings (20, 30, and 40%), finding that a high catalyst loading (40%) was favorable for high-purity H2 production and tar cracking. The above research demonstrates that the use of an appropriate catalyst can improve product yield and selectivity.

Other parameters such as reaction time, waste pretreatment, and feed dimension have also been investigated for their influence on gasification performance. For example, Bai et al. [34] studied the gasification of PP at a reaction time of 2–60 min, finding that an increase in reaction time had a positive effect on the gasification efficiency. In another study, Bai et al. [43] studied the supercritical water gasification of PET, finding that gasification efficiency increased with the increase in reaction time from 2 to 60 min. Bai et al. [43] also found that the reaction pressure (21–29 MPa) had little impact on the gasification efficiency because the properties of the supercritical water did not change significantly at these different pressures. Su et al. [33] found that waste sorting is helpful to improve the H2-rich syngas production (or syngas yield) and gasification efficiency compared to unsorted waste. Xiang et al. [26] studied the steam gasification of MSW with two different MSW particle sizes (20 < diameter < 30 mm and 80 < diameter < 100 mm), finding that the increase of particle size decreased the total volume fraction of H2 and CO from 52% to 50%. Basha et al. [39] selected a feedstock size of 2–4 mm because a larger particle size prevented a compact fuel bed, while a smaller particle size blocked the reactor and plugged the gas outlet.

#### *2.1.3 Advantages and disadvantages*

In single-staged reactor systems, different types of reactors have been utilized based on their advantages and disadvantages. The common reactors used for solid waste gasification include fixed bed, fluidized bed, and entrained flow reactors [50]. A fixed bed reactor has simple construction and operation. However, a fixed bed reactor is typically used for small size reactions with limited loading/processing flexibility because of the poor adaptability for heterogeneous materials. A fluidized bed reactor can provide high mixing and solid–gas contact, promote heat and mass transfer, increase the reaction rate and conversion efficiency, and improve the process flexibility, compared to a fixed bed reactor. However, for both fixed bed and fluidized bed reactors, tar formation is a major problem, while entrained flow reactors have a high cost and poor biomass adaptability [50].

Indrawan et al. [32] studied the gasification of a MSW and switchgrass mixture, finding that the downdraft reactor (patented design) system design was selected due to low tar content (< 0.5 g/Nm3 ), compared to a circulating fluidized bed (up to 12 g/ Nm3 ), fluidized bed (up to 40 g/Nm3 ), and updraft fixed-bed reactor (up to 150 g/ Nm3 ). Bian et al. [24] used a sealed quartz reactor system in their study and determined that a fluidized bed reactor might be better for enhancing the mass transfer of the reactant and reducing reactor plugging problems. The fluidized bed gasifier has excellent solid–gas contact efficiency, uniform and controllable temperature distribution, and broad feedstock feasibility [51]. Based on this data, the downdraft fluidized bed is a promising reactor choice for solid waste gasification.

## **2.2 Multi-staged reactor**

## *2.2.1 Reactor dimensions*

The inside diameter and length of a multi-staged reactor is typically in the range of 3–750 mm and 150–3500 mm, respectively, shown in **Table 3**. These dimensions are similar to those of the single-staged reactor. Likewise, selection of appropriate reactor dimensions will be helpful for the solid waste gasification performance in a multi-staged reactor. There are multiple stages in a multi-staged reactor system such as pyrolysis, reforming, tar cracking, and water-gas shift. **Figure 5** shows a diagram of a two-staged gasification process. Different stages are developed for specified reactions. Parameters in each stage can be operated individually for optimization. In addition, using high temperatures in the tar cracking stage can be helpful to largely reduce tar [50].

Kuba and Hofbauer [62] studied the gasification in a dual fluid bed gasifier, where heat is supplied by the bed material circulating between the gasifier and the combustion reactor. The reactor design and the fluidization nozzle position had a significant effect on the tar formation and reduction. For example, an increase in the bed height of the gasifier can increase the residence time, leading to an overall decrease in tar. Additional fluidization nozzles in the inclined wall, located in the bubbling bed where the feedstock enters the gasifier via a conveyer screw, can improve the mixing of feedstock and bed material. A moving bed section above the inclined wall (no fluidization) can be used to reduce the tar formation. Additional fluidization nozzles can also be installed to reduce the influence of the inclined wall [62]. Chai et al. [63] studied the two-staged gasification of a mixture of LDPE and pine sawdust over catalysts, finding that N2 can be introduced into the gasifier to prevent oxidation of the catalyst in the bottom stage.

#### *2.2.2 Operating factors and performance*

**Table 4** shows the syngas yield (typically 0.7–3.0 Nm3 /kg) obtained from different gasification processes, depending on feedstock species, reactor types, and operating conditions. Temperature is one operating parameter that has a significant influence on the solid waste gasification performance in a multi-staged reactor. For example, Bai et al. [52] studied the two-staged gasification kinetics of PC in supercritical water at different temperatures (500–800 °C). An increase in temperature improved the free radical and cracking reactions of PC. The gasification reaction of PC was intense and underwent a cracking reaction, forming gas phase products and many small molecular fragments in the first stage. The gasification reaction was slow, but kept increasing in the second phase [52]. Xiao et al. [54] found the pyrolysis/gasification of pine sawdust was largely improved by increasing the reactor temperature from 700 to 850 °C. Prasertcharoensuk et al. [56] found that pyrolysis temperature significantly influenced char properties, specifically, the surface area and pore size increased with an increase in temperature from 600 to 900 °C. Liu et al. [59] studied the gasification at temperatures of 600–800 °C, finding that a higher temperature was helpful

**133**

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors*

Inside diameter = 3 mm, length = 200 mm

Central diameter = 30 mm, length = 150 mm

length = 200 mm, second stage: inside diameter = 136 mm, length = 400 mm, and third stage: inside diameter = 26 mm,

First stage: inside diameter = 80 mm,

length = 2500 mm

length = 160 mm

First stage: inside diameter = 44 mm,

length = 1.2 m

length = 3.5 m

Center diameter = 33 mm, length = 830 mm

First stage: diameter = 38 mm, length = 300 mm, and second stage: diameter = 25 mm, length = 300 mm

length = 250 mm; second stage: inside diameter = 44 mm, length = 530 mm

Inside diameter = 50 mm,

Inside diameter = 150 mm,

Two-staged Inside diameter = 0.75 m, length = 2 m

**Reactor configuration Other Ref.**

— Steam gasification [53]

700–800 °C

Two stages: 500–700 °C, and

Pyrolysis (feedstock loaded, 700 °C) and gasification (catalyst loaded, 600 °C)

First stage: pyrolysis/ gasification, second stage: reformer for tar cracked, and third stage: combustor

Pyrolysis and char gasification

First stage: pyrolysis at 600 °C, and second stage: reforming at 800 °C

First stage: pyrolysis, and second stage: tar cracking

— [56]

— [57]

— [59]

— [60]

with air

[52]

[63]

[54]

[55]

[58]

[20]

to enhance gasification performance. Khonde and Chaurasia [20] studied the twostaged gasification at different second-stage temperatures (700–900 °C). The tar yield decreased with increasing temperature, while tar cracking at higher temperatures led

Feed concentration and catalyst are important factors that have been investigated for solid waste gasification. For example, Bai et al. [52] studied the gasification kinetics of PC in supercritical water at different PC concentrations (5–25 wt%), finding that a decrease in PC concentration improved the gasification level of the unit feedstock. Chai et al. [63] studied the two-staged gasification of a mixture of

to hydrogen rich syngas production (or gas yield) [20].

*The solid waste gasification, multi-staged reactor type, and dimension.*

*DOI: http://dx.doi.org/10.5772/intechopen.96157*

two-staged tube

Two-staged fixed bed

Two-staged fixed bed

Threestaged

Two-staged fixed bed

Bench-scale two-staged fixed bed

downdraft fixed bed

Two-staged bubbling fluidized bed

Dual fluidized bed

*Low-density polyethylene (LDPE).*

Rice husk Two-staged

Biomass — Inside diameter = 22 mm,

**Waste Reactor type**

PC Quartz

Oat hull pellet

LDPEa and pine sawdust mixture

Pine sawdust

Olive oil mill residue

Waste biomass

Rice husk and PE mixture

Rice straw

Wood pellet or manure

*a*

**Table 3.**


#### **Table 3.**

*Gasification*

Nm3

Nm3

to low tar content (< 0.5 g/Nm3

**2.2 Multi-staged reactor**

*2.2.1 Reactor dimensions*

), fluidized bed (up to 40 g/Nm3

), compared to a circulating fluidized bed (up to 12 g/

). Bian et al. [24] used a sealed quartz reactor system in their study and determined that a fluidized bed reactor might be better for enhancing the mass transfer of the reactant and reducing reactor plugging problems. The fluidized bed gasifier has excellent solid–gas contact efficiency, uniform and controllable temperature distribution, and broad feedstock feasibility [51]. Based on this data, the downdraft

The inside diameter and length of a multi-staged reactor is typically in the range of 3–750 mm and 150–3500 mm, respectively, shown in **Table 3**. These dimensions are similar to those of the single-staged reactor. Likewise, selection of appropriate reactor dimensions will be helpful for the solid waste gasification performance in a multi-staged reactor. There are multiple stages in a multi-staged reactor system such as pyrolysis, reforming, tar cracking, and water-gas shift. **Figure 5** shows a diagram of a two-staged gasification process. Different stages are developed for specified reactions. Parameters in each stage can be operated individually for optimization. In addition, using high temperatures in the tar cracking stage can be helpful to largely reduce tar [50].

Kuba and Hofbauer [62] studied the gasification in a dual fluid bed gasifier, where heat is supplied by the bed material circulating between the gasifier and the combustion reactor. The reactor design and the fluidization nozzle position had a significant effect on the tar formation and reduction. For example, an increase in the bed height of the gasifier can increase the residence time, leading to an overall decrease in tar. Additional fluidization nozzles in the inclined wall, located in the bubbling bed where the feedstock enters the gasifier via a conveyer screw, can improve the mixing of feedstock and bed material. A moving bed section above the inclined wall (no fluidization) can be used to reduce the tar formation. Additional fluidization nozzles can also be installed to reduce the influence of the inclined wall [62]. Chai et al. [63] studied the two-staged gasification of a mixture of LDPE and pine sawdust over catalysts, finding that N2 can be introduced into the gasifier to

gasification processes, depending on feedstock species, reactor types, and operating conditions. Temperature is one operating parameter that has a significant influence on the solid waste gasification performance in a multi-staged reactor. For example, Bai et al. [52] studied the two-staged gasification kinetics of PC in supercritical water at different temperatures (500–800 °C). An increase in temperature improved the free radical and cracking reactions of PC. The gasification reaction of PC was intense and underwent a cracking reaction, forming gas phase products and many small molecular fragments in the first stage. The gasification reaction was slow, but kept increasing in the second phase [52]. Xiao et al. [54] found the pyrolysis/gasification of pine sawdust was largely improved by increasing the reactor temperature from 700 to 850 °C. Prasertcharoensuk et al. [56] found that pyrolysis temperature significantly influenced char properties, specifically, the surface area and pore size increased with an increase in temperature from 600 to 900 °C. Liu et al. [59] studied the gasification at temperatures of 600–800 °C, finding that a higher temperature was helpful

prevent oxidation of the catalyst in the bottom stage.

**Table 4** shows the syngas yield (typically 0.7–3.0 Nm3

*2.2.2 Operating factors and performance*

fluidized bed is a promising reactor choice for solid waste gasification.

), and updraft fixed-bed reactor (up to 150 g/

/kg) obtained from different

**132**

*The solid waste gasification, multi-staged reactor type, and dimension.*

to enhance gasification performance. Khonde and Chaurasia [20] studied the twostaged gasification at different second-stage temperatures (700–900 °C). The tar yield decreased with increasing temperature, while tar cracking at higher temperatures led to hydrogen rich syngas production (or gas yield) [20].

Feed concentration and catalyst are important factors that have been investigated for solid waste gasification. For example, Bai et al. [52] studied the gasification kinetics of PC in supercritical water at different PC concentrations (5–25 wt%), finding that a decrease in PC concentration improved the gasification level of the unit feedstock. Chai et al. [63] studied the two-staged gasification of a mixture of

#### **Figure 5.**

*Diagram of a two-staged gasification process, which mainly consists of a feeding system, two reaction zones (fluidized bed reactor and tar-cracking reactor), a char separation system (cyclone and hot filter), and a quenching system (water-cooled condensers) [61]. Reproduced with permission from [61].*


#### **Table 4.**

*The solid waste multi-staged gasification factor and performance.*

LDPE and pine sawdust, finding that the use of a Ni-CaO-C catalyst was helpful to improve the gas yield, compared with non-catalyst. Additionally, it was determined that the heat recovered from the catalyst regeneration can be used for heating

**135**

production [61].

*2.2.4 Applications of a multi-staged reactor*

varied largely between 24 and 52 wt% [69].

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors*

feedstocks in the reactor [63]. Al-Rahbi and Williams [57] studied a two-staged pyrolysis-reforming gasification, finding that the H2 production increased largely with the use of a tyre pyrolysis char as the catalyst, compared to non-catalytic test. Other parameters such as reaction time and pressure have also been investigated for gasification. For example, Bai et al. [52] studied the gasification kinetic of PC in supercritical water at different reaction time (5–60 min), finding that the increase in reaction time improved the gasification efficiency. Bai et al. [52] also studied the gasification at different pressures (21–29 MPa), finding that the pressure had no significant impact on gasification. This is likely because the properties of the supercritical water do not change significantly at these different pressures.

Compared to single-staged reactor systems, the use of multi-staged reactor systems for solid waste gasification has some advantages and disadvantages. A twostaged reactor system is convenient to investigate the specific effect of temperature at different stages [63]. The multi-staged reactor tends to be more promising and reliable in technique development [50]. For example, Al-Rahbi and Williams [57] studied two-staged pyrolysis-reforming gasification. The first stage was pyrolysis at 500 °C, and the second stage was reforming at 700–900 °C. The two-staged pyrolysis-reforming reactor was found to increase the total gas yield, compared to a single-staged reactor. One aim of this combination approach of pyrolysis and reforming is to improve the gas yield and obtain an optimum syngas ratio via shift-

In a single reactor, it is difficult to control the different gasification reactions, such as pyrolysis, char gasification, tar cracking, and water-gas shift reaction, individually [64]. Multiple reactions can occur in one reactor, making it difficult to correlate feedstock properties and downstream utilization of the gas product. Multi-staged reactors can be helpful to improve gasification performance [64]. In a three-staged reactor system, the reactions can be optimized, individually, under appropriate conditions. This can also achieve efficient tar removal [54]. However, the multi-staged reactor is significantly more complex and has a higher capital cost, compared to a single-staged reactor [67]. Furthermore, a long and steady gasification operation needs to be developed for commercial scale H2

Multi-staged reactors have some advantages, as discussed previously. They have been applied not only in gasification, but also in other technologies such as pyrolysis and torrefaction. For example, we previously studied the pyrolysis of alkali lignin to biofuel using a two-staged reactor (pyrolysis and catalytic reactor) [68]. The alkali lignin and catalyst were individually loaded into the pyrolysis and catalytic reactor, respectively. The alkali lignin was successfully converted into biofuel at a biofuel yield of 28 wt% [68]. Guzelciftci et al. [69] studied the pyrolysis of wood using a two-staged reactor system (auger and fluidized bed reactors). The auger reactor temperature varied between room temperature and 290 °C, while the fluidized bed reactor temperature varied between 500 and 700 °C. The obtained bio-oil yield

Granados et al. [70] used a two-staged rotary reactor system for torrefaction of poplar wood residues. The two-staged rotary reactor system consists of two in-series rotary drums for continuous drying (115 °C) and torrefaction (300 °C) processes. The HHV of the torrefied poplar wood residues reached 26 MJ/kg, which

*DOI: http://dx.doi.org/10.5772/intechopen.96157*

*2.2.3 Advantages and disadvantages*

ing the reaction from exothermic to endothermic [57].

#### *Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors DOI: http://dx.doi.org/10.5772/intechopen.96157*

feedstocks in the reactor [63]. Al-Rahbi and Williams [57] studied a two-staged pyrolysis-reforming gasification, finding that the H2 production increased largely with the use of a tyre pyrolysis char as the catalyst, compared to non-catalytic test.

Other parameters such as reaction time and pressure have also been investigated for gasification. For example, Bai et al. [52] studied the gasification kinetic of PC in supercritical water at different reaction time (5–60 min), finding that the increase in reaction time improved the gasification efficiency. Bai et al. [52] also studied the gasification at different pressures (21–29 MPa), finding that the pressure had no significant impact on gasification. This is likely because the properties of the supercritical water do not change significantly at these different pressures.

## *2.2.3 Advantages and disadvantages*

*Gasification*

Biomass briquette

**Figure 5.**

Pine sawdust

Pine sawdust

Wood sawdust and HDPE mixture

Two-staged (fluidized bed and swirl-melting furnace)

Three-staged (pyrolyzer, reformer, and combustor)

Three-staged (pyrolysis/ gasification, reformer, and combustor)

Two-staged (plasma gasification and folded plate)

(gasification and reforming)

(fluidized bed gasifying and tar cracking)

*The solid waste multi-staged gasification factor and performance.*

MSW Two-staged

PE Two-staged

**134**

**Table 4.**

LDPE and pine sawdust, finding that the use of a Ni-CaO-C catalyst was helpful to improve the gas yield, compared with non-catalyst. Additionally, it was determined that the heat recovered from the catalyst regeneration can be used for heating

**Waste Reactor type Conditions Performance Other Ref.**

*Diagram of a two-staged gasification process, which mainly consists of a feeding system, two reaction zones (fluidized bed reactor and tar-cracking reactor), a char separation system (cyclone and hot filter), and a* 

> Gas yield: ~1.5 Nm3 /kg

Gas yield: 1.6 Nm3 /kg; tar yield: 1.0 g/kg

Gas yield: 1.0 Nm3 /kg

~2.2 Nm3 /kg

Syngas yield: 0.7 m3 /kg

Syngas yield: 3 Nm3 /kg; char yield: 271 g/kg; tar yield: 68 g/kg

Biomass contains rice straw, plastic and paper; Biomass feed rate: 25 kg/h

Biomass feed rate: 200 g/h

Biomass feed rate: 200 g/h

40 wt% HDPE in the feed mixture

Steam gasification

— [66]

[50]

[64]

[54]

[65]

[61]

First stage: 695 °C; second stage: 1280 °C

*quenching system (water-cooled condensers) [61]. Reproduced with permission from [61].*

Pyrolyzer: 700 °C; reformer: 850 °C; combustor: 850 °C

Pyrolysis/gasification:

Gasification: 850 °C; reforming: 850 °C

Gasifying: 792 °C; cracking: 852 °C

Input power of 18 kW Gas yield:

800 °C; reformer: 850 °C; combustor: 850 °C

Compared to single-staged reactor systems, the use of multi-staged reactor systems for solid waste gasification has some advantages and disadvantages. A twostaged reactor system is convenient to investigate the specific effect of temperature at different stages [63]. The multi-staged reactor tends to be more promising and reliable in technique development [50]. For example, Al-Rahbi and Williams [57] studied two-staged pyrolysis-reforming gasification. The first stage was pyrolysis at 500 °C, and the second stage was reforming at 700–900 °C. The two-staged pyrolysis-reforming reactor was found to increase the total gas yield, compared to a single-staged reactor. One aim of this combination approach of pyrolysis and reforming is to improve the gas yield and obtain an optimum syngas ratio via shifting the reaction from exothermic to endothermic [57].

In a single reactor, it is difficult to control the different gasification reactions, such as pyrolysis, char gasification, tar cracking, and water-gas shift reaction, individually [64]. Multiple reactions can occur in one reactor, making it difficult to correlate feedstock properties and downstream utilization of the gas product. Multi-staged reactors can be helpful to improve gasification performance [64]. In a three-staged reactor system, the reactions can be optimized, individually, under appropriate conditions. This can also achieve efficient tar removal [54]. However, the multi-staged reactor is significantly more complex and has a higher capital cost, compared to a single-staged reactor [67]. Furthermore, a long and steady gasification operation needs to be developed for commercial scale H2 production [61].

#### *2.2.4 Applications of a multi-staged reactor*

Multi-staged reactors have some advantages, as discussed previously. They have been applied not only in gasification, but also in other technologies such as pyrolysis and torrefaction. For example, we previously studied the pyrolysis of alkali lignin to biofuel using a two-staged reactor (pyrolysis and catalytic reactor) [68]. The alkali lignin and catalyst were individually loaded into the pyrolysis and catalytic reactor, respectively. The alkali lignin was successfully converted into biofuel at a biofuel yield of 28 wt% [68]. Guzelciftci et al. [69] studied the pyrolysis of wood using a two-staged reactor system (auger and fluidized bed reactors). The auger reactor temperature varied between room temperature and 290 °C, while the fluidized bed reactor temperature varied between 500 and 700 °C. The obtained bio-oil yield varied largely between 24 and 52 wt% [69].

Granados et al. [70] used a two-staged rotary reactor system for torrefaction of poplar wood residues. The two-staged rotary reactor system consists of two in-series rotary drums for continuous drying (115 °C) and torrefaction (300 °C) processes. The HHV of the torrefied poplar wood residues reached 26 MJ/kg, which was a much higher value than that of the raw poplar wood residues (18 MJ/kg) [70]. Nhuchhen et al. [71] studied the torrefaction of yellow poplar in a two-staged reactor system at an angular speed of 4 rpm. Three different torrefaction temperatures (260, 290, and 320 °C) were investigated. An increase in the torrefaction temperature resulted in a decrease in solid mass yield from 93 wt% to 81 wt%. The HHV of the torrefied poplar increased from 20 to 23 MJ/kg with an increase in the torrefaction temperature from 260 to 320 °C [71]. However, further torrefaction studies on the comparison of single- and multi-staged reactors will be needed.

## **3. Conclusion**

Solid waste, including MSW, biomass residue, plastic waste, and their mixtures, has accumulated fast in recent years, leading to solid waste gasification gaining great attention. However, no systematic study has been performed to compare single-staged and multi-staged reactors. This book chapter systematically reviewed state-of-the-art research for both single- and multi-staged reactors. Discussion included analysis of the reactor dimensions, operating factors and performance, advantages, and disadvantages of these reactors. The yield of syngas generated from solid waste gasification is mainly in the range of 0.7–3.0 Nm3 /kg. Multi-staged reactors are a convenient approach to investigate the specific effect of parameters at different stages, and the reactions can be optimized individually under appropriate conditions. Additionally, a multi-staged reactor can be helpful to improve gasification performance, but is more complex and has higher capital cost, compared to a single-staged reactor.

Solid waste gasification is affected by several factors including temperature, reaction time, feed composition, and catalyst activity. An appropriate temperature (e.g., 800–900 °C) can be selected for solid waste gasification based on the elevated gasification performance and low energy consumption. A suitable feedstock concentration and reaction time should be selected to balance gasification efficiency and industrial application. Higher feedstock concentration can cause the reactor to plug and subsequent catalyst deactivation, while a longer reaction time may cause greater energy consumption. The use of a steam and O2 mixture as the gasification agent is helpful for gasification efficiency because it produces steam reforming reactions and has a lack of N2 dilution. Waste sorting is helpful to improve the gasification efficiency compared to unsorted waste. Moreover, an appropriate waste feed size should be selected because larger feed size can cause a loose bed and smaller feed size can lead to reactor blockage. The co-gasification of waste mixtures over Ni based catalysts is a promising technology due to the improved gasification efficiency derived from the synergistic effect of the feed mixture.

Additionally, multi-staged reactors have many unique advantages, which make them useful in other applications such as pyrolysis and torrefaction. However, reducing the processing cost of converting solid waste to syngas remains a major technical challenge. Pretreating solid waste, such as MSW, to remove the impurities, high energy consumption at elevated temperatures, and the use of catalysts remain the most expensive aspects of this process. In the future, a better understanding of the gasification reactions, reactor design, and catalyst development needs to be investigated to improve syngas yield and avoid tar formation.

## **Acknowledgements**

The authors acknowledge the support from the US Department of Energy (DOE), Office of Energy Efficiency and Renewable Energy, Advanced

**137**

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors*

Manufacturing Office, under CPS Agreement 36863. This book chapter was authored in part by UT-Battelle LLC under contract DE-AC05-00OR22725 with DOE. The US government retains and the publisher, by accepting the article for publication, acknowledges that the US government retains a nonexclusive, paid-up, irrevocable, worldwide license to publish or reproduce the published form of this book chapter, or allow others to do so, for US government purposes. DOE will provide public access to these results of federally sponsored research in accordance with the DOE Public Access Plan (http://energy.gov/downloads/

*DOI: http://dx.doi.org/10.5772/intechopen.96157*

The authors declare no conflict of interest.

**Appendices and nomenclature**

PP Polypropylene PC Polycarbonate PE Polyethylene

MSW Municipal solid waste HDPE High density polyethylene

HHV Higher heating value LHV Lower heating value S/C Steam to carbon ratio ER Equivalence air ratio TC1 Thermocouple 1 TC2 Thermocouple 2 RDF Refuse derived fuel TR Tar reformer

DES Desulfurization reactor

SPA Solid phase adsorption

CHP Combined heat and power

WGS Water gas shift

GS Gasifier

doe-public-access-plan).

**Conflict of interest**

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors DOI: http://dx.doi.org/10.5772/intechopen.96157*

Manufacturing Office, under CPS Agreement 36863. This book chapter was authored in part by UT-Battelle LLC under contract DE-AC05-00OR22725 with DOE. The US government retains and the publisher, by accepting the article for publication, acknowledges that the US government retains a nonexclusive, paid-up, irrevocable, worldwide license to publish or reproduce the published form of this book chapter, or allow others to do so, for US government purposes. DOE will provide public access to these results of federally sponsored research in accordance with the DOE Public Access Plan (http://energy.gov/downloads/ doe-public-access-plan).

## **Conflict of interest**

*Gasification*

**3. Conclusion**

is mainly in the range of 0.7–3.0 Nm3

was a much higher value than that of the raw poplar wood residues (18 MJ/kg) [70]. Nhuchhen et al. [71] studied the torrefaction of yellow poplar in a two-staged reactor system at an angular speed of 4 rpm. Three different torrefaction temperatures (260, 290, and 320 °C) were investigated. An increase in the torrefaction temperature resulted in a decrease in solid mass yield from 93 wt% to 81 wt%. The HHV of the torrefied poplar increased from 20 to 23 MJ/kg with an increase in the torrefaction temperature from 260 to 320 °C [71]. However, further torrefaction studies on

Solid waste, including MSW, biomass residue, plastic waste, and their mixtures, has accumulated fast in recent years, leading to solid waste gasification gaining great attention. However, no systematic study has been performed to compare single-staged and multi-staged reactors. This book chapter systematically reviewed state-of-the-art research for both single- and multi-staged reactors. Discussion included analysis of the reactor dimensions, operating factors and performance, advantages, and disadvantages of these reactors. The yield of syngas generated from solid waste gasification

approach to investigate the specific effect of parameters at different stages, and the reactions can be optimized individually under appropriate conditions. Additionally, a multi-staged reactor can be helpful to improve gasification performance, but is more

Solid waste gasification is affected by several factors including temperature, reaction time, feed composition, and catalyst activity. An appropriate temperature (e.g., 800–900 °C) can be selected for solid waste gasification based on the elevated gasification performance and low energy consumption. A suitable feedstock concentration and reaction time should be selected to balance gasification efficiency and industrial application. Higher feedstock concentration can cause the reactor to plug and subsequent catalyst deactivation, while a longer reaction time may cause greater energy consumption. The use of a steam and O2 mixture as the gasification agent is helpful for gasification efficiency because it produces steam reforming reactions and has a lack of N2 dilution. Waste sorting is helpful to improve the gasification efficiency compared to unsorted waste. Moreover, an appropriate waste feed size should be selected because larger feed size can cause a loose bed and smaller feed size can lead to reactor blockage. The co-gasification of waste mixtures over Ni based catalysts is a promising technology due to the improved gasification

Additionally, multi-staged reactors have many unique advantages, which make

them useful in other applications such as pyrolysis and torrefaction. However, reducing the processing cost of converting solid waste to syngas remains a major technical challenge. Pretreating solid waste, such as MSW, to remove the impurities, high energy consumption at elevated temperatures, and the use of catalysts remain the most expensive aspects of this process. In the future, a better understanding of the gasification reactions, reactor design, and catalyst development needs to be

The authors acknowledge the support from the US Department of Energy

(DOE), Office of Energy Efficiency and Renewable Energy, Advanced

complex and has higher capital cost, compared to a single-staged reactor.

efficiency derived from the synergistic effect of the feed mixture.

investigated to improve syngas yield and avoid tar formation.

/kg. Multi-staged reactors are a convenient

the comparison of single- and multi-staged reactors will be needed.

**136**

**Acknowledgements**

The authors declare no conflict of interest.

## **Appendices and nomenclature**


## **Author details**

Xianhui Zhao1 \*, Kai Li2 , Meghan E. Lamm1 , Serdar Celik<sup>3</sup> , Lin Wei4 and Soydan Ozcan1 \*

1 Manufacturing Science Division, Oak Ridge National Laboratory, Knoxville, Tennessee, United States

2 Chemical Sciences Division, Oak Ridge National Laboratory, Oak Ridge, Tennessee, United States

3 Department of Mechanical and Mechatronics Engineering, Southern Illinois University, Edwardsville, Illinois, United States

4 Agricultural and Biosystems Engineering Department, South Dakota State University, Brookings, South Dakota, United States

\*Address all correspondence to: zhaox@ornl.gov and ozcans@ornl.gov

© 2021 The Author(s). Licensee IntechOpen. This chapter is distributed under the terms of the Creative Commons Attribution License (http://creativecommons.org/licenses/ by/3.0), which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.

**139**

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors*

[9] E.R. Widjaya, G.N. Chen, L. Bowtell, C. Hills, Gasification of non-woody biomass: A literature review, Renewable & Sustainable Energy Reviews, 89

[10] J.H. Park, H.-W. Park, S. Choi, D.-W. Park, Effects of blend ratio between high density polyethylene and biomass on co-gasification behavior in a twostage gasification system, International Journal of Hydrogen Energy, 41 (2016)

[11] T.K. Patra, P.N. Sheth, Biomass gasification models for downdraft gasifier: A state-of-the-art review, Renewable and Sustainable Energy

Reviews, 50 (2015) 583-593.

[12] A. Anukam, S. Mamphweli, P. Reddy, E. Meyer, O. Okoh, Preprocessing of sugarcane bagasse for gasification in a downdraft biomass gasifier system: A comprehensive review, Renewable and Sustainable Energy Reviews, 66 (2016) 775-801.

[13] D.T. Pio, L.A.C. Tarelho, M.A.A. Matos, Characteristics of the gas produced during biomass direct gasification in an autothermal pilotscale bubbling fluidized bed reactor,

[14] S.L. Yang, H. Wang, Y.G. Wei, J.H. Hu, J.W. Chew, Eulerian-Lagrangian simulation of air-steam biomass gasification in a three-dimensional bubbling fluidized gasifier, Energy, 181

Energy, 120 (2017) 915-928.

[15] J. Schneider, C. Grube, A. Herrmann, S. Rönsch, Atmospheric entrained-flow gasification of biomass and lignite for decentralized

applications, Fuel Processing Technology, 152 (2016) 72-82.

[16] X. Gao, Y. Zhang, B. Li, X. Yu, Model development for biomass

(2019) 1075-1093.

(2018) 184-193.

16813-16822.

*DOI: http://dx.doi.org/10.5772/intechopen.96157*

[1] S. Kaza, L. Yao, P. Bhada-Tata, F. Van Woerden, What a waste 2.0: a global snapshot of solid waste management to

2050, The World Bank2018.

[2] L.F. Pearse, J.P. Hettiaratchi, S. Kumar, Towards developing a representative biochemical methane potential (BMP) assay for landfilled municipal solid waste–A review, Bioresource technology, 254 (2018)

[3] S.S.A. Syed-Hassan, Y. Wang, S. Hu, S. Su, J. Xiang, Thermochemical processing of sewage sludge to energy and fuel: Fundamentals, challenges and considerations, Renewable and Sustainable Energy Reviews, 80 (2017)

[4] U. Arena, Process and technological aspects of municipal solid waste gasification. A review, Waste management, 32 (2012) 625-639.

[5] A. Bosmans, I. Vanderreydt, D. Geysen, L. Helsen, The crucial role of Waste-to-Energy technologies in enhanced landfill mining: a technology review, Journal of Cleaner Production,

[6] X. Zhao, A. Naqi, D.M. Walker, T. Roberge, M. Kastelic, B. Joseph, J.N. Kuhn, Conversion of landfill gas to liquid fuels through a TriFTS (tri-reforming and Fischer–Tropsch synthesis) process: a feasibility study, Sustain Energ Fuels, 3 (2019) 539-549.

[7] X. Zhao, B. Joseph, J. Kuhn, S. Ozcan, Biogas Reforming to Syngas: A Review,

[8] S. Sansaniwal, K. Pal, M. Rosen, S. Tyagi, Recent advances in the development of biomass gasification technology: A comprehensive review, Renewable and sustainable energy reviews, 72 (2017) 363-384.

iScience, 23 (2020) 101082.

**References**

312-324.

888-913.

55 (2013) 10-23.

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors DOI: http://dx.doi.org/10.5772/intechopen.96157*

## **References**

*Gasification*

**Author details**

and Soydan Ozcan1

\*, Kai Li2

Knoxville, Tennessee, United States

Oak Ridge, Tennessee, United States

University, Edwardsville, Illinois, United States

provided the original work is properly cited.

University, Brookings, South Dakota, United States

\*

, Meghan E. Lamm1

1 Manufacturing Science Division, Oak Ridge National Laboratory,

3 Department of Mechanical and Mechatronics Engineering, Southern Illinois

4 Agricultural and Biosystems Engineering Department, South Dakota State

© 2021 The Author(s). Licensee IntechOpen. This chapter is distributed under the terms of the Creative Commons Attribution License (http://creativecommons.org/licenses/ by/3.0), which permits unrestricted use, distribution, and reproduction in any medium,

\*Address all correspondence to: zhaox@ornl.gov and ozcans@ornl.gov

2 Chemical Sciences Division, Oak Ridge National Laboratory,

, Serdar Celik<sup>3</sup>

, Lin Wei4

Xianhui Zhao1

**138**

[1] S. Kaza, L. Yao, P. Bhada-Tata, F. Van Woerden, What a waste 2.0: a global snapshot of solid waste management to 2050, The World Bank2018.

[2] L.F. Pearse, J.P. Hettiaratchi, S. Kumar, Towards developing a representative biochemical methane potential (BMP) assay for landfilled municipal solid waste–A review, Bioresource technology, 254 (2018) 312-324.

[3] S.S.A. Syed-Hassan, Y. Wang, S. Hu, S. Su, J. Xiang, Thermochemical processing of sewage sludge to energy and fuel: Fundamentals, challenges and considerations, Renewable and Sustainable Energy Reviews, 80 (2017) 888-913.

[4] U. Arena, Process and technological aspects of municipal solid waste gasification. A review, Waste management, 32 (2012) 625-639.

[5] A. Bosmans, I. Vanderreydt, D. Geysen, L. Helsen, The crucial role of Waste-to-Energy technologies in enhanced landfill mining: a technology review, Journal of Cleaner Production, 55 (2013) 10-23.

[6] X. Zhao, A. Naqi, D.M. Walker, T. Roberge, M. Kastelic, B. Joseph, J.N. Kuhn, Conversion of landfill gas to liquid fuels through a TriFTS (tri-reforming and Fischer–Tropsch synthesis) process: a feasibility study, Sustain Energ Fuels, 3 (2019) 539-549.

[7] X. Zhao, B. Joseph, J. Kuhn, S. Ozcan, Biogas Reforming to Syngas: A Review, iScience, 23 (2020) 101082.

[8] S. Sansaniwal, K. Pal, M. Rosen, S. Tyagi, Recent advances in the development of biomass gasification technology: A comprehensive review, Renewable and sustainable energy reviews, 72 (2017) 363-384.

[9] E.R. Widjaya, G.N. Chen, L. Bowtell, C. Hills, Gasification of non-woody biomass: A literature review, Renewable & Sustainable Energy Reviews, 89 (2018) 184-193.

[10] J.H. Park, H.-W. Park, S. Choi, D.-W. Park, Effects of blend ratio between high density polyethylene and biomass on co-gasification behavior in a twostage gasification system, International Journal of Hydrogen Energy, 41 (2016) 16813-16822.

[11] T.K. Patra, P.N. Sheth, Biomass gasification models for downdraft gasifier: A state-of-the-art review, Renewable and Sustainable Energy Reviews, 50 (2015) 583-593.

[12] A. Anukam, S. Mamphweli, P. Reddy, E. Meyer, O. Okoh, Preprocessing of sugarcane bagasse for gasification in a downdraft biomass gasifier system: A comprehensive review, Renewable and Sustainable Energy Reviews, 66 (2016) 775-801.

[13] D.T. Pio, L.A.C. Tarelho, M.A.A. Matos, Characteristics of the gas produced during biomass direct gasification in an autothermal pilotscale bubbling fluidized bed reactor, Energy, 120 (2017) 915-928.

[14] S.L. Yang, H. Wang, Y.G. Wei, J.H. Hu, J.W. Chew, Eulerian-Lagrangian simulation of air-steam biomass gasification in a three-dimensional bubbling fluidized gasifier, Energy, 181 (2019) 1075-1093.

[15] J. Schneider, C. Grube, A. Herrmann, S. Rönsch, Atmospheric entrained-flow gasification of biomass and lignite for decentralized applications, Fuel Processing Technology, 152 (2016) 72-82.

[16] X. Gao, Y. Zhang, B. Li, X. Yu, Model development for biomass

gasification in an entrained flow gasifier using intrinsic reaction rate submodel, Energy Conversion and Management, 108 (2016) 120-131.

[17] A. Mednikov, A Review of Technologies for Multistage Wood Biomass Gasification, Thermal Engineering, 65 (2018) 531-546.

[18] W.P. Chan, A. Veksha, J. Lei, W.-D. Oh, X. Dou, A. Giannis, G. Lisak, T.-T. Lim, A hot syngas purification system integrated with downdraft gasification of municipal solid waste, Appl Energ, 237 (2019) 227-240.

[19] P.R. Bhoi, R.L. Huhnke, A. Kumar, N. Indrawan, S. Thapa, Co-gasification of municipal solid waste and biomass in a commercial scale downdraft gasifier, Energy, 163 (2018) 513-518.

[20] R. Khonde, A. Chaurasia, Rice husk gasification in a two-stage fixed-bed gasifier: Production of hydrogen rich syngas and kinetics, Int J Hydrogen Energ, 41 (2016) 8793-8802.

[21] A. Gómez-Barea, B. Leckner, A.V. Perales, S. Nilsson, D.F. Cano, Improving the performance of fluidized bed biomass/waste gasifiers for distributed electricity: a new threestage gasification system, Applied Thermal Engineering, 50 (2013) 1453-1462.

[22] M. Irfan, A. Li, L. Zhang, M. Wang, C. Chen, S. Khushk, Production of hydrogen enriched syngas from municipal solid waste gasification with waste marble powder as a catalyst, Int J Hydrogen Energ, 44 (2019) 8051-8061.

[23] I.N. Zaini, Y. Gomez-Rueda, C. García López, D.K. Ratnasari, L. Helsen, T. Pretz, P.G. Jönsson, W. Yang, Production of H2-rich syngas from excavated landfill waste through steam co-gasification with biochar, Energy, 207 (2020) 118208.

[24] C. Bian, R. Zhang, L. Dong, B. Bai, W. Li, H. Jin, C. Cao, Hydrogen/ Methane Production from Supercritical Water Gasification of Lignite Coal with Plastic Waste Blends, Energ Fuel, 34 (2020) 11165-11174.

[25] D. Selvi Gökkaya, T. Çokkuvvetli, M. Sağlam, M. Yüksel, L. Ballice, Hydrothermal gasification of poplar wood chips with alkali, mineral, and metal impregnated activated carbon catalysts, The Journal of Supercritical Fluids, 152 (2019) 104542.

[26] Y.L. Xiang, Q. Lin, L. Cai, Y. Guan, J. Lu, W. Liu, Study of the effect mechanism of municipal solid waste gasification conditions on the production of H2 and CO using modelling technique, J Environ Manage, 230 (2019) 301-310.

[27] W.C. Ng, S. You, R. Ling, K.Y.-H. Gin, Y. Dai, C.-H. Wang, Co-gasification of woody biomass and chicken manure: Syngas production, biochar reutilization, and cost-benefit analysis, Energy, 139 (2017) 732-742.

[28] M. Lei, J. Hai, J. Cheng, J. Lu, J. Zhang, T. You, Variation of toxic pollutants emission during a feeding cycle from an updraft fixed bed gasifier for disposing rural solid waste, Chinese Journal of Chemical Engineering, 26 (2018) 608-613.

[29] D. Antolini, S.S. Ail, F. Patuzzi, M. Grigiante, M. Baratieri, Experimental investigations of air-CO2 biomass gasification in reversed downdraft gasifier, Fuel, 253 (2019) 1473-1481.

[30] F. Pinto, R. André, M. Miranda, D. Neves, F. Varela, J. Santos, Effect of gasification agent on co-gasification of rice production wastes mixtures, Fuel, 180 (2016) 407-416.

[31] Y. Tian, X. Zhou, S. Lin, X. Ji, J. Bai, M. Xu, Syngas production from air-steam gasification of biomass with

**141**

(2018) 271-291.

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors*

shell and polystyrene plastic: Effect of different operating conditions, J Energy

[40] S. Rudra, Y.K. Tesfagaber, Future district heating plant integrated with municipal solid waste (MSW) gasification for hydrogen production,

L. Sapegno, E. Volponi, P. Venturini, F. Rispoli, E. Paris, M. Carnevale,

A. Colantoni, Influence of oxidant agent on syngas composition: Gasification of hazelnut shells through an updraft reactor, Energies, 13 (2020) 102.

[42] S.A. Salaudeen, B. Acharya, M. Heidari, S.M. Al-Salem, A. Dutta, Hydrogen-Rich Gas Stream from Steam Gasification of Biomass: Eggshell as a CO2 Sorbent, Energ Fuel, 34 (2020)

[43] B. Bai, Y. Liu, H. Zhang, F. Zhou, X. Han, Q. Wang, H. Jin, Experimental

[44] W.X. Peng, L.S. Wang, M. Mirzaee, H. Ahmadi, M.J. Esfahani, S. Fremaux, Hydrogen and syngas production by catalytic biomass gasification, Energ Convers Manage, 135 (2017) 270-273.

[45] H. Su, D. Hantoko, M. Yan, Y. Cai, E. Kanchanatip, J. Liu, X. Zhou, S. Zhang, Evaluation of catalytic subcritical water gasification of food waste for hydrogen production: Effect of process conditions and different types of catalyst loading, Int J Hydrogen

Energ, 44 (2019) 21451-21463.

[46] H. Su, W. Liao, J. Wang, D.

Hantoko, Z. Zhou, H. Feng, J. Jiang, M. Yan, Assessment of supercritical water gasification of food waste under the background of waste sorting: Influences

investigation on gasification characteristics of polyethylene terephthalate (PET) microplastics in supercritical water, Fuel, 262

4828-4836.

(2020) 116630.

Inst, 93 (2020) 1045-1052.

Energy, 180 (2019) 881-892.

[41] F. Gallucci, R. Liberatore,

*DOI: http://dx.doi.org/10.5772/intechopen.96157*

natural catalysts, Sci Total Environ, 645

[32] N. Indrawan, S. Thapa, P.R. Bhoi, R.L. Huhnke, A. Kumar, Electricity power generation from co-gasification of municipal solid wastes and biomass: Generation and emission performance,

[33] H. Su, E. Kanchanatip, D. Wang, R. Zheng, Z. Huang, Y. Chen, I. Mubeen, M. Yan, Production of H2-rich syngas from gasification of unsorted food waste in supercritical water, Waste

Energy, 162 (2018) 764-775.

Manag, 102 (2020) 520-527.

[34] B. Bai, W. Wang, H. Jin, Experimental study on gasification performance of polypropylene (PP) plastics in supercritical water, Energy,

[35] X. Zheng, Z. Ying, B. Wang, C. Chen, Hydrogen and syngas production from municipal solid waste (MSW) gasification via reusing CO2, Appl Therm Eng, 144 (2018) 242-247.

[36] D.T. Pio, L.A.C. Tarelho, A.M.A. Tavares, M.A.A. Matos, V. Silva, Co-gasification of refused derived fuel and biomass in a pilot-scale bubbling fluidized bed reactor, Energ Convers

[37] F. Meng, Q. Ma, H. Wang, Y. Liu, D. Wang, Effect of gasifying agents on sawdust gasification in a novel pilot scale bubbling fluidized bed system,

Manage, 206 (2020) 112476.

Fuel, 249 (2019) 112-118.

[38] Q. Xiong, M.M. Yeganeh, E.

[39] M.H. Basha, S.A. Sulaiman, Y. Uemura, Co-gasification of palm kernel

Yaghoubi, A. Asadi, M.H. Doranehgard, K. Hong, Parametric investigation on biomass gasification in a fluidized bed gasifier and conceptual design of gasifier, Chemical Engineering and Processing - Process Intensification, 127

191 (2020) 116527.

(2018) 518-523.

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors DOI: http://dx.doi.org/10.5772/intechopen.96157*

natural catalysts, Sci Total Environ, 645 (2018) 518-523.

*Gasification*

108 (2016) 120-131.

237 (2019) 227-240.

Energy, 163 (2018) 513-518.

[17] A. Mednikov, A Review of Technologies for Multistage Wood Biomass Gasification, Thermal Engineering, 65 (2018) 531-546.

gasification in an entrained flow gasifier using intrinsic reaction rate submodel, Energy Conversion and Management,

[24] C. Bian, R. Zhang, L. Dong, B. Bai, W. Li, H. Jin, C. Cao, Hydrogen/ Methane Production from Supercritical Water Gasification of Lignite Coal with Plastic Waste Blends, Energ Fuel, 34

[25] D. Selvi Gökkaya, T. Çokkuvvetli, M. Sağlam, M. Yüksel, L. Ballice, Hydrothermal gasification of poplar wood chips with alkali, mineral, and metal impregnated activated carbon catalysts, The Journal of Supercritical

(2020) 11165-11174.

Fluids, 152 (2019) 104542.

[26] Y.L. Xiang, Q. Lin, L. Cai, Y. Guan, J. Lu, W. Liu, Study of the effect mechanism of municipal solid waste gasification conditions on the production of H2 and CO using modelling technique, J Environ Manage, 230 (2019) 301-310.

[27] W.C. Ng, S. You, R. Ling, K.Y.-H. Gin, Y. Dai, C.-H. Wang, Co-gasification

of woody biomass and chicken manure: Syngas production, biochar reutilization, and cost-benefit analysis,

[28] M. Lei, J. Hai, J. Cheng, J. Lu, J. Zhang, T. You, Variation of toxic pollutants emission during a feeding cycle from an updraft fixed bed gasifier for disposing rural solid waste, Chinese Journal of Chemical Engineering, 26

[29] D. Antolini, S.S. Ail, F. Patuzzi, M. Grigiante, M. Baratieri, Experimental investigations of air-CO2 biomass gasification in reversed downdraft gasifier, Fuel, 253 (2019) 1473-1481.

[30] F. Pinto, R. André, M. Miranda, D. Neves, F. Varela, J. Santos, Effect of gasification agent on co-gasification of rice production wastes mixtures, Fuel,

[31] Y. Tian, X. Zhou, S. Lin, X. Ji, J. Bai, M. Xu, Syngas production from air-steam gasification of biomass with

Energy, 139 (2017) 732-742.

(2018) 608-613.

180 (2016) 407-416.

[18] W.P. Chan, A. Veksha, J. Lei, W.-D. Oh, X. Dou, A. Giannis, G. Lisak, T.-T. Lim, A hot syngas purification system integrated with downdraft gasification of municipal solid waste, Appl Energ,

[19] P.R. Bhoi, R.L. Huhnke, A. Kumar, N. Indrawan, S. Thapa, Co-gasification of municipal solid waste and biomass in a commercial scale downdraft gasifier,

[20] R. Khonde, A. Chaurasia, Rice husk gasification in a two-stage fixed-bed gasifier: Production of hydrogen rich syngas and kinetics, Int J Hydrogen Energ, 41 (2016) 8793-8802.

[21] A. Gómez-Barea, B. Leckner, A.V. Perales, S. Nilsson, D.F. Cano, Improving the performance of fluidized

bed biomass/waste gasifiers for distributed electricity: a new threestage gasification system, Applied Thermal Engineering, 50 (2013)

[22] M. Irfan, A. Li, L. Zhang, M. Wang, C. Chen, S. Khushk, Production of hydrogen enriched syngas from municipal solid waste gasification with waste marble powder as a catalyst, Int J Hydrogen Energ, 44 (2019) 8051-8061.

[23] I.N. Zaini, Y. Gomez-Rueda, C. García López, D.K. Ratnasari, L. Helsen, T. Pretz, P.G. Jönsson, W. Yang, Production of H2-rich syngas from excavated landfill waste through steam co-gasification with biochar, Energy,

1453-1462.

**140**

207 (2020) 118208.

[32] N. Indrawan, S. Thapa, P.R. Bhoi, R.L. Huhnke, A. Kumar, Electricity power generation from co-gasification of municipal solid wastes and biomass: Generation and emission performance, Energy, 162 (2018) 764-775.

[33] H. Su, E. Kanchanatip, D. Wang, R. Zheng, Z. Huang, Y. Chen, I. Mubeen, M. Yan, Production of H2-rich syngas from gasification of unsorted food waste in supercritical water, Waste Manag, 102 (2020) 520-527.

[34] B. Bai, W. Wang, H. Jin, Experimental study on gasification performance of polypropylene (PP) plastics in supercritical water, Energy, 191 (2020) 116527.

[35] X. Zheng, Z. Ying, B. Wang, C. Chen, Hydrogen and syngas production from municipal solid waste (MSW) gasification via reusing CO2, Appl Therm Eng, 144 (2018) 242-247.

[36] D.T. Pio, L.A.C. Tarelho, A.M.A. Tavares, M.A.A. Matos, V. Silva, Co-gasification of refused derived fuel and biomass in a pilot-scale bubbling fluidized bed reactor, Energ Convers Manage, 206 (2020) 112476.

[37] F. Meng, Q. Ma, H. Wang, Y. Liu, D. Wang, Effect of gasifying agents on sawdust gasification in a novel pilot scale bubbling fluidized bed system, Fuel, 249 (2019) 112-118.

[38] Q. Xiong, M.M. Yeganeh, E. Yaghoubi, A. Asadi, M.H. Doranehgard, K. Hong, Parametric investigation on biomass gasification in a fluidized bed gasifier and conceptual design of gasifier, Chemical Engineering and Processing - Process Intensification, 127 (2018) 271-291.

[39] M.H. Basha, S.A. Sulaiman, Y. Uemura, Co-gasification of palm kernel shell and polystyrene plastic: Effect of different operating conditions, J Energy Inst, 93 (2020) 1045-1052.

[40] S. Rudra, Y.K. Tesfagaber, Future district heating plant integrated with municipal solid waste (MSW) gasification for hydrogen production, Energy, 180 (2019) 881-892.

[41] F. Gallucci, R. Liberatore, L. Sapegno, E. Volponi, P. Venturini, F. Rispoli, E. Paris, M. Carnevale, A. Colantoni, Influence of oxidant agent on syngas composition: Gasification of hazelnut shells through an updraft reactor, Energies, 13 (2020) 102.

[42] S.A. Salaudeen, B. Acharya, M. Heidari, S.M. Al-Salem, A. Dutta, Hydrogen-Rich Gas Stream from Steam Gasification of Biomass: Eggshell as a CO2 Sorbent, Energ Fuel, 34 (2020) 4828-4836.

[43] B. Bai, Y. Liu, H. Zhang, F. Zhou, X. Han, Q. Wang, H. Jin, Experimental investigation on gasification characteristics of polyethylene terephthalate (PET) microplastics in supercritical water, Fuel, 262 (2020) 116630.

[44] W.X. Peng, L.S. Wang, M. Mirzaee, H. Ahmadi, M.J. Esfahani, S. Fremaux, Hydrogen and syngas production by catalytic biomass gasification, Energ Convers Manage, 135 (2017) 270-273.

[45] H. Su, D. Hantoko, M. Yan, Y. Cai, E. Kanchanatip, J. Liu, X. Zhou, S. Zhang, Evaluation of catalytic subcritical water gasification of food waste for hydrogen production: Effect of process conditions and different types of catalyst loading, Int J Hydrogen Energ, 44 (2019) 21451-21463.

[46] H. Su, W. Liao, J. Wang, D. Hantoko, Z. Zhou, H. Feng, J. Jiang, M. Yan, Assessment of supercritical water gasification of food waste under the background of waste sorting: Influences of plastic waste contents, Int J Hydrogen Energ, 45 (2020) 21138-21147.

[47] C. Cao, C. Bian, G. Wang, B. Bai, Y. Xie, H. Jin, Co-gasification of plastic wastes and soda lignin in supercritical water, Chem Eng J, 388 (2020) 124277.

[48] X. Zheng, Z. Ying, B. Wang, C. Chen, CO2 Gasification of Municipal Solid Waste in a Drop-Tube Reactor: Experimental Study and Thermodynamic Analysis of Syngas, Energ Fuel, 32 (2018) 5302-5312.

[49] Z. Wang, X. Liu, K.G. Burra, J. Li, M. Zhang, T. Lei, A.K. Gupta, Towards enhanced catalytic reactivity in CO2 assisted gasification of polypropylene, Fuel, 284 (2021) 119076.

[50] M. Niu, Y. Huang, B. Jin, S. Liang, Q. Dong, H. Gu, R. Sun, A novel twostage enriched air biomass gasification for producing low-tar high heating value fuel gas: Pilot verification and performance analysis, Energy, 173 (2019) 511-522.

[51] Z. Wan, S. Yang, Y. Sun, Y. Wei, J. Hu, H. Wang, Distribution and particle-scale thermochemical property of biomass in the gasifier of a dual fluidized bed, Energ Convers Manage, 209 (2020) 112672.

[52] B. Bai, Y. Liu, X. Meng, C. Liu, H. Zhang, W. Zhang, H. Jin, Experimental investigation on gasification characteristics of polycarbonate (PC) microplastics in supercritical water, J Energy Inst, 93 (2020) 624-633.

[53] A. Abedi, A.K. Dalai, Steam gasification of oat hull pellets over Ni-based catalysts: Syngas yield and tar reduction, Fuel, 254 (2019) 115585.

[54] Y. Xiao, S. Xu, Y. Song, Y. Shan, C. Wang, G. Wang, Biomass steam gasification for hydrogen-rich gas production in a decoupled dual loop gasification system, Fuel Process Technol, 165 (2017) 54-61.

[55] M. Lajili, C. Guizani, F.J. Escudero Sanz, M. Jeguirim, Fast pyrolysis and steam gasification of pellets prepared from olive oil mill residues, Energy, 150 (2018) 61-68.

[56] P. Prasertcharoensuk, S.J. Bull, A.N. Phan, Gasification of waste biomass for hydrogen production: Effects of pyrolysis parameters, Renew Energ, 143 (2019) 112-120.

[57] A.S. Al-Rahbi, P.T. Williams, Hydrogen-rich syngas production and tar removal from biomass gasification using sacrificial tyre pyrolysis char, Appl Energ, 190 (2017) 501-509.

[58] D. Xu, Y. Xiong, J. Ye, Y. Su, Q. Dong, S. Zhang, Performances of syngas production and deposited coke regulation during co-gasification of biomass and plastic wastes over Ni/γ-Al2O3 catalyst: Role of biomass to plastic ratio in feedstock, Chem Eng J, 392 (2020) 123728.

[59] L. Liu, Y. Huang, J. Cao, C. Liu, L. Dong, L. Xu, J. Zha, Experimental study of biomass gasification with oxygenenriched air in fluidized bed gasifier, Science of The Total Environment, 626 (2018) 423-433.

[60] D. Schweitzer, A. Gredinger, M. Schmid, G. Waizmann, M. Beirow, R. Spörl, G. Scheffknecht, Steam gasification of wood pellets, sewage sludge and manure: Gasification performance and concentration of impurities, Biomass Bioenerg, 111 (2018) 308-319.

[61] Y.-S. Jeong, K.-B. Park, J.-S. Kim, Hydrogen production from steam gasification of polyethylene using a twostage gasifier and active carbon, Appl Energ, 262 (2020) 114495.

**143**

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors*

[70] D.A. Granados, P. Basu, F. Chejne,

Biomass Torrefaction in a Two-Stage Rotary Reactor: Modeling and Experimental Validation, Energ Fuel, 31

[71] D.R. Nhuchhen, P. Basu, B. Acharya, Torrefaction of Poplar in a Continuous Two-Stage, Indirectly Heated Rotary Torrefier, Energ Fuel, 30

(2017) 5701-5709.

(2016) 1027-1038.

*DOI: http://dx.doi.org/10.5772/intechopen.96157*

[62] M. Kuba, H. Hofbauer,

(2018) 35-44.

241-248.

225 (2020) 113407.

(2016) 2939-2977.

200 (2020) 117536.

Experimental parametric study on product gas and tar composition in dual fluid bed gasification of woody biomass, Biomass Bioenerg, 115

[63] Y. Chai, N. Gao, M. Wang, C. Wu, H2 production from co-pyrolysis/ gasification of waste plastics and biomass under novel catalyst Ni-CaO-C,

Chem Eng J, 382 (2020) 122947.

[64] Y. Tursun, S. Xu, A. Abulikemu, T. Dilinuer, Biomass gasification for hydrogen rich gas in a decoupled triple bed gasifier with olivine and NiO/ olivine, Bioresour Technol, 272 (2019)

[65] W. Ma, C. Chu, P. Wang, Z. Guo, B. Liu, G. Chen, Characterization of tar evolution during DC thermal plasma steam gasification from biomass and plastic mixtures: Parametric optimization via response surface methodology, Energ Convers Manage,

[66] L. Zhang, W. Wu, Y. Zhang, X. Zhou, Clean synthesis gas production from municipal solid waste via catalytic gasification and reforming technology,

[67] V.S. Sikarwar, M. Zhao, P. Clough, J. Yao, X. Zhong, M.Z. Memon, N. Shah, E.J. Anthony, P.S. Fennell, An overview of advances in biomass gasification, Energy & Environmental Science, 9

[68] S. Cheng, L. Wei, X. Zhao, J. Julson, E. Kadis, Converting alkali lignin to biofuels over NiO/HZSM-5 catalysts using a two-stage reactor, Chem Eng Technol, 40 (2017) 1069-1077.

[69] B. Guzelciftci, K.-B. Park, J.-S. Kim, Production of phenol-rich bio-oil via a two-stage pyrolysis of wood, Energy,

Catal Today, 318 (2018) 39-45.

*Solid Waste Gasification: Comparison of Single- and Multi-Staged Reactors DOI: http://dx.doi.org/10.5772/intechopen.96157*

[62] M. Kuba, H. Hofbauer, Experimental parametric study on product gas and tar composition in dual fluid bed gasification of woody biomass, Biomass Bioenerg, 115 (2018) 35-44.

*Gasification*

of plastic waste contents, Int J Hydrogen

gasification system, Fuel Process Technol, 165 (2017) 54-61.

(2018) 61-68.

(2019) 112-120.

501-509.

(2020) 123728.

(2018) 423-433.

308-319.

[55] M. Lajili, C. Guizani, F.J. Escudero Sanz, M. Jeguirim, Fast pyrolysis and steam gasification of pellets prepared from olive oil mill residues, Energy, 150

[56] P. Prasertcharoensuk, S.J. Bull, A.N. Phan, Gasification of waste biomass for hydrogen production: Effects of pyrolysis parameters, Renew Energ, 143

[57] A.S. Al-Rahbi, P.T. Williams, Hydrogen-rich syngas production and tar removal from biomass gasification using sacrificial tyre pyrolysis char, Appl Energ, 190 (2017)

[58] D. Xu, Y. Xiong, J. Ye, Y. Su, Q. Dong, S. Zhang, Performances of syngas production and deposited coke regulation during co-gasification of biomass and plastic wastes over Ni/γ-Al2O3 catalyst: Role of biomass to plastic ratio in feedstock, Chem Eng J, 392

[59] L. Liu, Y. Huang, J. Cao, C. Liu, L. Dong, L. Xu, J. Zha, Experimental study of biomass gasification with oxygenenriched air in fluidized bed gasifier, Science of The Total Environment, 626

[60] D. Schweitzer, A. Gredinger, M. Schmid, G. Waizmann, M. Beirow, R. Spörl, G. Scheffknecht, Steam gasification of wood pellets, sewage sludge and manure: Gasification performance and concentration of impurities, Biomass Bioenerg, 111 (2018)

[61] Y.-S. Jeong, K.-B. Park, J.-S. Kim, Hydrogen production from steam gasification of polyethylene using a twostage gasifier and active carbon, Appl

Energ, 262 (2020) 114495.

[47] C. Cao, C. Bian, G. Wang, B. Bai, Y. Xie, H. Jin, Co-gasification of plastic wastes and soda lignin in supercritical water, Chem Eng J, 388 (2020) 124277.

[48] X. Zheng, Z. Ying, B. Wang, C. Chen, CO2 Gasification of

Municipal Solid Waste in a Drop-Tube Reactor: Experimental Study and Thermodynamic Analysis of Syngas, Energ Fuel, 32 (2018) 5302-5312.

[49] Z. Wang, X. Liu, K.G. Burra, J. Li, M. Zhang, T. Lei, A.K. Gupta, Towards enhanced catalytic reactivity in CO2 assisted gasification of polypropylene,

[50] M. Niu, Y. Huang, B. Jin, S. Liang, Q. Dong, H. Gu, R. Sun, A novel twostage enriched air biomass gasification for producing low-tar high heating value fuel gas: Pilot verification and performance analysis, Energy, 173

[51] Z. Wan, S. Yang, Y. Sun, Y. Wei, J. Hu, H. Wang, Distribution and particle-scale thermochemical property of biomass in the gasifier of a dual fluidized bed, Energ Convers Manage,

[52] B. Bai, Y. Liu, X. Meng, C. Liu, H. Zhang, W. Zhang, H. Jin, Experimental

characteristics of polycarbonate (PC) microplastics in supercritical water, J Energy Inst, 93 (2020) 624-633.

investigation on gasification

[53] A. Abedi, A.K. Dalai, Steam gasification of oat hull pellets over Ni-based catalysts: Syngas yield and tar reduction, Fuel, 254 (2019) 115585.

[54] Y. Xiao, S. Xu, Y. Song, Y. Shan, C. Wang, G. Wang, Biomass steam gasification for hydrogen-rich gas production in a decoupled dual loop

Fuel, 284 (2021) 119076.

(2019) 511-522.

209 (2020) 112672.

Energ, 45 (2020) 21138-21147.

**142**

[63] Y. Chai, N. Gao, M. Wang, C. Wu, H2 production from co-pyrolysis/ gasification of waste plastics and biomass under novel catalyst Ni-CaO-C, Chem Eng J, 382 (2020) 122947.

[64] Y. Tursun, S. Xu, A. Abulikemu, T. Dilinuer, Biomass gasification for hydrogen rich gas in a decoupled triple bed gasifier with olivine and NiO/ olivine, Bioresour Technol, 272 (2019) 241-248.

[65] W. Ma, C. Chu, P. Wang, Z. Guo, B. Liu, G. Chen, Characterization of tar evolution during DC thermal plasma steam gasification from biomass and plastic mixtures: Parametric optimization via response surface methodology, Energ Convers Manage, 225 (2020) 113407.

[66] L. Zhang, W. Wu, Y. Zhang, X. Zhou, Clean synthesis gas production from municipal solid waste via catalytic gasification and reforming technology, Catal Today, 318 (2018) 39-45.

[67] V.S. Sikarwar, M. Zhao, P. Clough, J. Yao, X. Zhong, M.Z. Memon, N. Shah, E.J. Anthony, P.S. Fennell, An overview of advances in biomass gasification, Energy & Environmental Science, 9 (2016) 2939-2977.

[68] S. Cheng, L. Wei, X. Zhao, J. Julson, E. Kadis, Converting alkali lignin to biofuels over NiO/HZSM-5 catalysts using a two-stage reactor, Chem Eng Technol, 40 (2017) 1069-1077.

[69] B. Guzelciftci, K.-B. Park, J.-S. Kim, Production of phenol-rich bio-oil via a two-stage pyrolysis of wood, Energy, 200 (2020) 117536.

[70] D.A. Granados, P. Basu, F. Chejne, Biomass Torrefaction in a Two-Stage Rotary Reactor: Modeling and Experimental Validation, Energ Fuel, 31 (2017) 5701-5709.

[71] D.R. Nhuchhen, P. Basu, B. Acharya, Torrefaction of Poplar in a Continuous Two-Stage, Indirectly Heated Rotary Torrefier, Energ Fuel, 30 (2016) 1027-1038.

**145**

**Chapter 7**

**Abstract**

material, and sawdust.

**1. Introduction**

**1.1 Global energy status**

future energy for 2035.

sawdust

Gasification Process Using

for Different Feedstock

*Md. Emdadul Hoque and Fazlur Rashid*

Downdraft Fixed-Bed Gasifier

The use of conventional fuels is decreasing globally due to its limited reserves and negative impact on the environment. The associated cost of conventional fuels is increasing owing to the higher demand for conventional fuels. Hence, utilization methods of biomass to generate energy are of growing interest. Among different biomass feedstocks, rice husks, waste plastics, and sawdust are significantly available in the global environment. The annual generation amount of rice husk is approximately 120 million tons worldwide, with an annual energy generation potential of 109 GJ with a heating value of 15 MJ/kg. The gasification process is assumed to be the most effective biomass conversion method that can generate synthetic gas to operate IC engines, fuel cells, and boilers. Synthetic gas production from biomass using a gasification process is a significant source of future energy. Downdraft fixed-bed gasifiers are considered as a feasible option of biomass conversion in the gasification process. By optimizing the operating conditions of downdraft fixed-bed gasifier, such as reaction zone temperature, combustion zone temperature, intake air temperature, airflow rate, the humidity of intake air, a significant amount of synthetic gas can be produced from rice husks, waste plastic

**Keywords:** gasification, downdraft fixed-bed gasifier, rice husk, waste plastic,

Human civilization and development have significantly increased world energy demand over the past years [1]. Consumption of world energy includes all energy sources consumed by humans in their economy and industrial purposes [2, 3]. Major factors that influence energy consumption are the high growth rate of population and per capita energy consumption. The globalization of international trade is another factor that affects the global energy profile [4]. **Figure 1** shows the global energy consumption from 2000 to 2020 and the forecast of

However, the world's population is the main global energy consumer [2–4]. According to the United Nations forecast data, the global population will reach

## **Chapter 7**
