**3.1.1 Anaerobic digestion**

Anaerobic digestion is the treatment of biomass with naturally occurring microorganisms in the absence of air (oxygen) to produce a combustible gaseous fuel comprising primarily of methane (CH4) and carbon dioxide (CO2) and traces of other gases such as nitrogen (N2) and hydrogen sulphide (H2S). The gaseous mixtures is commonly termed "biogas". Virtually all nitrogen (N), phosphorus (P) and potassium (K) remain in the digested biomass.

The entire process takes place in three basic steps as shown in Figure 2. The first step is the conversion of complex organic solids into soluble compounds by enzymatic hydrolysis. The soluble organic material formed is then converted into mainly short-chain acids and alcohols during the acidogenesis step. In the methanogenesis step, the products of the second step are converted into gases by different species of strictly anaerobic bacteria. The percentage of methane in the final mixture has been reported to vary between 50 to 80%. A

the level of technology is beyond their manpower as well as their manufacturing and technological capability. Added to this is the unavailability of local materials and parts for the fabrication of these conversion units. Figure 1 shows the different methods for converting biomass into convenient fuel. Biomass conversion into heat energy is still the most efficient process but not all of energy requirement is in the form of heat. Biomass resources need to be converted into chemical, electrical or mechanical energy in order to have widespread use. These take the form of solid fuel like charcoal, liquid fuel like ethanol or gaseous fuel like methane. These fuels can be used in a wide range of energy conversion devices to satisfy the diverse energy needs. In general, conversion technologies for biomass utilization may either be based on bio-chemical or thermo-chemical conversion processes.

The two most important biochemical conversion processes are the anaerobic digestion and

Anaerobic digestion is the treatment of biomass with naturally occurring microorganisms in the absence of air (oxygen) to produce a combustible gaseous fuel comprising primarily of methane (CH4) and carbon dioxide (CO2) and traces of other gases such as nitrogen (N2) and hydrogen sulphide (H2S). The gaseous mixtures is commonly termed "biogas". Virtually all

The entire process takes place in three basic steps as shown in Figure 2. The first step is the conversion of complex organic solids into soluble compounds by enzymatic hydrolysis. The soluble organic material formed is then converted into mainly short-chain acids and alcohols during the acidogenesis step. In the methanogenesis step, the products of the second step are converted into gases by different species of strictly anaerobic bacteria. The percentage of methane in the final mixture has been reported to vary between 50 to 80%. A

nitrogen (N), phosphorus (P) and potassium (K) remain in the digested biomass.

Each process will be described separately.

Fig. 1. Methods of using biomass for energy.

**3.1 Bio-chemical conversion processes** 

fermentation processes.

**3.1.1 Anaerobic digestion** 

typical mixture consists of 65% methane and 35% CO2 with traces of other gases. The methane producing bacteria (called methanogenic bacteria) generally require a pH range for growth of 6.4 to 7.2. The acid producing bacteria can withstand low pH. In doing their work, the acid producing bacteria lower the pH and accumulate acids and salts of organic acids. If the methane-forming organisms do not rapidly convert these products, the conditions become adverse to methane formers. This is why the first type of reactors developed for conversion of biomass wastes into methane have long retention times seeking equilibrium between acid and methane formers.

Municipal wastes and livestock manures are the most suitable materials for anaerobic digestion. In the US, numerous landfill facilities now recover methane and use it for power generation. Aquatic biomass such as water hyacinth or micro-algae can be digested and may become valuable sources of energy in the future. Anaerobic digestion of organic wastes may constitute an effective device for pollution control with simultaneous energy generation and nutrient conservation. A major advantage of anaerobic digestion is that it utilizes biomass with high water contents of as high as 99%. Another advantage is the availability of conversion systems in smaller units. Also the residue has fertilizer value and can be used in crop production. The primary disadvantage of anaerobic digestion of diluted wastes is the large quantity of sludge that must be disposed of after the digestion process including the wastewater and the cost of biogas storage. In cold climates, a significant fraction of the gas produced may be used to maintain the reactor operating temperature. Otherwise, microorganisms that thrive on lower or moderate temperatures should be used.

(Source: American Chemical Society)

Fig. 2. Steps in anaerobic digestion process with energy flow represented as % chemical oxygen demand (COD).

#### **3.1.1.1 The first generation biogas reactors**

Three main types of biogas facilities have been successfully developed in Asia for widespread biogas production in households and industrial use. These are the "Chinese Digester" of fixed dome type, the "Indian Gobar Gas Plant" of floating gas holder type and the rectangular commercial size biogas digesters developed in Taiwan. These are what we may call the first generation biogas reactors. Shown in Figure 3 is the common Chinese digester design. These

Biomass Energy Conversion 215

Figure 5 is an example of a rectangular biogas digester used in commercial swine facilities in Taiwan. Similar reactors have been built and used in the Philippines for commercial swine

While the above designs have been operated successfully, the reactors are still considered World War II technologies. The main disadvantage is the long retention times of between 30 to 60 days. Thus, for large scale units, they require larger reactor volumes which make the initial cost and area requirements quite high. Their main advantage is the fact that these units have less maintenance and operational costs and they are less prone to breakdowns due to variations in the quantity and quality of feed. They are resistant to shock loadings and minimal process parameters are monitored for efficient operation. The only operating

There are now new technologies which we may call the second generation biogas digesters. These high rate bio-reactors were originally designed for low strength liquid wastes but the progress has been remarkable and most units can now be used for even the high strength

Callander, et al., (1983), have made an extensive review of the development of the high rate digester technology. The improvements of such digesters can be largely attributed to better understanding of the microbiology of the methane production process. The most popular high rate anaerobic digesters originated from many conventional wastewater treatment plants that utilizes the anaerobic contact process (Figure 6) followed by the anaerobic clarigester. Perhaps the design that has caused widespread attention is the development of the upflow anaerobic sludge blanket (UASB) developed in Netherlands (Letingga, et al., 1980). Many commercial high rate digesters are now based on this design. Other reactors include the anaerobic filters (Young, et. al., 1969), the expanded bed fixed film reactor, and

As researchers began to understand the microbiology of the processes, they began to realize the varied nature and characteristics of the microorganisms used in the conversion. Thus recent designs call for the separation of two types of microorganisms in the reactors. Some new reactors are designed whereby acid forming bacteria are separated from the methane producing bacteria. With this design, the acid formers are now independent from the methane formers and therefore each group of microorganisms can do its job without

The retention times have been reduced for most of the high rate biogas digesters and thus reducing the size of the digesters. However, there are corresponding need for a modest

wastes with high quantities of suspended solids like those of livestock manure.

harming the population of the other types of microorganisms.

facilities (Maramba, 1978). The gas holder is designed and constructed separately.

Fig. 5. The Taiwan rectangular digester design with a separate gas holder.

procedure made is the daily mixing of the slurry. **3.1.1.2 The second generation biogas digesters** 

the stationary fixed film reactor.

designs have eliminated the use of a floating gas holder and incorporated local materials for construction (brick or concrete). Biogas is pressurized in the dome and can be easily used for cooking and lighting. Figure 4 shows the "Indian Gobar Gas Plant" with floating gas holder.

Fig. 3. The "Chinese Digester" of the dome type.

Fig. 4. The "Indian Gobar Gas Plant" schematic showing cross-sectional design.

The Indian design uses concrete inlet and outlet tanks and reactor. The steel cover acts as the floating gasholder. These digesters have no pumps, motors, mixing devices or other moving parts and digestion takes place at ambient temperature. As fresh material is added each day, digested slurry is displaced through an outlet pipe. The digesters contain a baffle in the center which ensures proper utilization of the entire digester volume and prevents short circuiting of fresh biomass material to the outlet pipe.

designs have eliminated the use of a floating gas holder and incorporated local materials for construction (brick or concrete). Biogas is pressurized in the dome and can be easily used for cooking and lighting. Figure 4 shows the "Indian Gobar Gas Plant" with floating gas holder.

Fig. 3. The "Chinese Digester" of the dome type.

Fig. 4. The "Indian Gobar Gas Plant" schematic showing cross-sectional design.

circuiting of fresh biomass material to the outlet pipe.

The Indian design uses concrete inlet and outlet tanks and reactor. The steel cover acts as the floating gasholder. These digesters have no pumps, motors, mixing devices or other moving parts and digestion takes place at ambient temperature. As fresh material is added each day, digested slurry is displaced through an outlet pipe. The digesters contain a baffle in the center which ensures proper utilization of the entire digester volume and prevents short Figure 5 is an example of a rectangular biogas digester used in commercial swine facilities in Taiwan. Similar reactors have been built and used in the Philippines for commercial swine facilities (Maramba, 1978). The gas holder is designed and constructed separately.

Fig. 5. The Taiwan rectangular digester design with a separate gas holder.

While the above designs have been operated successfully, the reactors are still considered World War II technologies. The main disadvantage is the long retention times of between 30 to 60 days. Thus, for large scale units, they require larger reactor volumes which make the initial cost and area requirements quite high. Their main advantage is the fact that these units have less maintenance and operational costs and they are less prone to breakdowns due to variations in the quantity and quality of feed. They are resistant to shock loadings and minimal process parameters are monitored for efficient operation. The only operating procedure made is the daily mixing of the slurry.

### **3.1.1.2 The second generation biogas digesters**

There are now new technologies which we may call the second generation biogas digesters. These high rate bio-reactors were originally designed for low strength liquid wastes but the progress has been remarkable and most units can now be used for even the high strength wastes with high quantities of suspended solids like those of livestock manure.

Callander, et al., (1983), have made an extensive review of the development of the high rate digester technology. The improvements of such digesters can be largely attributed to better understanding of the microbiology of the methane production process. The most popular high rate anaerobic digesters originated from many conventional wastewater treatment plants that utilizes the anaerobic contact process (Figure 6) followed by the anaerobic clarigester. Perhaps the design that has caused widespread attention is the development of the upflow anaerobic sludge blanket (UASB) developed in Netherlands (Letingga, et al., 1980). Many commercial high rate digesters are now based on this design. Other reactors include the anaerobic filters (Young, et. al., 1969), the expanded bed fixed film reactor, and the stationary fixed film reactor.

As researchers began to understand the microbiology of the processes, they began to realize the varied nature and characteristics of the microorganisms used in the conversion. Thus recent designs call for the separation of two types of microorganisms in the reactors. Some new reactors are designed whereby acid forming bacteria are separated from the methane producing bacteria. With this design, the acid formers are now independent from the methane formers and therefore each group of microorganisms can do its job without harming the population of the other types of microorganisms.

The retention times have been reduced for most of the high rate biogas digesters and thus reducing the size of the digesters. However, there are corresponding need for a modest

Biomass Energy Conversion 217

decomposition of large organic molecules requires the catalytic action of certain enzymes

Crops mentioned as potential substrate for the production of alcohol include sugarcane, sorghum, cassava, and sugar beets. The two main by-products of then fermentation are CO2 and the spent materials, which will contain the non-fermentable fraction of the substrate, the non-fermented sugars and the yeast cells. The two most important reasons for the high costs for ethanol production are: the batch nature of the process and the end-product (ethanol)

Continuous fermentation has been found successful on a laboratory scale. One way of avoiding end product inhibition is operation under vacuum so that ethanol is removed as it is formed. More researches are underway. Figure 7 shows a schematic diagram for the

If the feedstock is high in cellulosic components, these must be hydrolyzed also by a different sets of enzymes to break down the long chain cellulose structure into shorter chain compounds. In our laboratory facilities, we made use of enzymes produced by *Trichoderma reesi*. Commercially, genetically modified *T. reesi* may be sourced from Genencor

Biomass wastes can be easily converted into other forms of energy at high temperatures, They break down to form smaller and less complex molecules both liquid and gaseous including some solid products. Combustion represents a complete oxidation to carbon dioxide (CO2) and water (H2O). By controlling the process using a combination of temperature, pressures and various catalysts, and through limiting the oxygen supply, partial breakdown can be achieved to yield a variety of useful fuels. The main thermochemical conversion approaches are as follows: pyrolysis/charcoal production, gasification

also produced by microorganisms. The most popular microbe is the *Aspegillus niger*.

production of high percent ethanol from cassava (NRC, 1983).

Fig. 7. Schematic of ethanol production from cassava.

International (Palo Alto, California, USA).

**3.2 Thermo-chemical conversion processes** 

inhibition of the yeast.

laboratory for microbial analysis, system pH control and monitoring of other parameters such as buffering capacity, solids retention times, alkalinity and the like.

Fig. 6. Some examples of second generation biogas digesters.

### **3.1.2 Ethanol fermentation**

Ethyl alcohol can be produced from a variety of sugar containing materials by fermentation with yeasts. Strains of *Saccharomyces cerevisiae* are usually selected to carry on the fermentation that converts glucose (C6H12O6) into ethyl alcohol (C2H5OH) and carbon dioxide (CO2). In the batch process the substrate is diluted to a sugar content of about 20% by weight, acidified to ph 4-5, 8-10%, the liquid is distilled, fractionated and rectified. One gallon of alcohol (3.79 liters, 21257 kcal) is obtained from 2.5 gallons of cane molasses or the equivalent of 5.85 kg of sugar (21,842 kcal). So there is almost no energy loss in the fermentation process.

When a starchy material, such a corn, grain sorghum or barley, is used as substrate, the starch must be converted into fermentable sugars before yeast fermentation. The

laboratory for microbial analysis, system pH control and monitoring of other parameters

such as buffering capacity, solids retention times, alkalinity and the like.

Fig. 6. Some examples of second generation biogas digesters.

Ethyl alcohol can be produced from a variety of sugar containing materials by fermentation with yeasts. Strains of *Saccharomyces cerevisiae* are usually selected to carry on the fermentation that converts glucose (C6H12O6) into ethyl alcohol (C2H5OH) and carbon dioxide (CO2). In the batch process the substrate is diluted to a sugar content of about 20% by weight, acidified to ph 4-5, 8-10%, the liquid is distilled, fractionated and rectified. One gallon of alcohol (3.79 liters, 21257 kcal) is obtained from 2.5 gallons of cane molasses or the equivalent of 5.85 kg of sugar (21,842 kcal). So there is almost no energy loss in the

When a starchy material, such a corn, grain sorghum or barley, is used as substrate, the starch must be converted into fermentable sugars before yeast fermentation. The

**3.1.2 Ethanol fermentation** 

fermentation process.

decomposition of large organic molecules requires the catalytic action of certain enzymes also produced by microorganisms. The most popular microbe is the *Aspegillus niger*.

Crops mentioned as potential substrate for the production of alcohol include sugarcane, sorghum, cassava, and sugar beets. The two main by-products of then fermentation are CO2 and the spent materials, which will contain the non-fermentable fraction of the substrate, the non-fermented sugars and the yeast cells. The two most important reasons for the high costs for ethanol production are: the batch nature of the process and the end-product (ethanol) inhibition of the yeast.

Continuous fermentation has been found successful on a laboratory scale. One way of avoiding end product inhibition is operation under vacuum so that ethanol is removed as it is formed. More researches are underway. Figure 7 shows a schematic diagram for the production of high percent ethanol from cassava (NRC, 1983).

Fig. 7. Schematic of ethanol production from cassava.

If the feedstock is high in cellulosic components, these must be hydrolyzed also by a different sets of enzymes to break down the long chain cellulose structure into shorter chain compounds. In our laboratory facilities, we made use of enzymes produced by *Trichoderma reesi*. Commercially, genetically modified *T. reesi* may be sourced from Genencor International (Palo Alto, California, USA).

#### **3.2 Thermo-chemical conversion processes**

Biomass wastes can be easily converted into other forms of energy at high temperatures, They break down to form smaller and less complex molecules both liquid and gaseous including some solid products. Combustion represents a complete oxidation to carbon dioxide (CO2) and water (H2O). By controlling the process using a combination of temperature, pressures and various catalysts, and through limiting the oxygen supply, partial breakdown can be achieved to yield a variety of useful fuels. The main thermochemical conversion approaches are as follows: pyrolysis/charcoal production, gasification

Biomass Energy Conversion 219

Gasification is the thermo-chemical process of converting biomass waste into a low medium energy gas utilizing sub-stoichiometric amounts of oxidant (Coovattanachai, 1991). The simplest form of gasification is air gasification in which biomass is subjected to partial combustion with a limited supply of air. Air gasifiers are simple, cheap and reliable. Their chief drawback is that the gas produced is diluted with nitrogen and hence has low calorific value. The gas produced is uneconomical to distribute; it must be used on-site for process heat. In oxygen gasification, pure oxygen is used so that the gas produced is of high energy content. The chief disadvantage of oxygen gasification is that it requires an oxygen plant and thus increases the total cost of gasification. The schematic diagram of the processes occurring is a gasifier is shown in Figure 9 including the

Fig. 9. Schematic diagram of processes occurring in a gasifier and the temperature profile. The simplest air gasifier is the updraft gasifier shown in Figure 10. Air is introduced at the bottom of the bed of biomass near the hearth zone. The gas produced is usually at a low temperature. The sensible heat of the gas is used to dry and preheat the biomass before it reaches the reduction zone. Products from the distillation and drying zones consist mainly of water vapor, tar and oil vapors and are not passed through the hot bed. They therefore leave the reactor uncracked and will later condense at temperatures

Because the tar vapors leaving an updraft gas producer seriously interfere with the operation of internal combustion engines, the downdraft gasifiers (Barret, et. al., 1985) are more extensively used. The air is introduced into a downward flowing bed of solid fuel and the gas outlet is at the bottom as shown in Figure 11. The tarry oils and vapors given off in

temperature profile at each important step in the process.

**3.2.2 Gasification** 

between 125oC – 400oC.

and combustion. The advantages of thermo-chemical conversion processes include the following:


### **3.2.1 Pyrolysis**

Pyrolysis or destructive distillation is an irreversible chemical change caused by the action of heat in the absence of oxygen. Pyrolysis of biomass leads to gases, liquids and solid residues. The important components of pyrolysis gas in most cases are hydrogen, carbon monoxide, carbon dioxide, methane and lesser quantities of other hydrocarbons (C2H4, C2H6, etc.). The liquid consists of methanol, acetic acid, acetone, water and tar. The solid residue consists of carbon and ash. Thus pyrolysis can be used to convert biomass into valuable chemicals and industrial feedstock.

In a typical pyrolysis process the feed material goes through the following operations: (a) primary shredding (b) drying the shredded material (c) removal of organics (d) further shredding to fine size (e) pyrolysis (f) cooling of the products to condense the liquids and (g) storage of the products.

Different types of pyrolytic reactors include vertical shaft reactors, horizontal beds. Among these, the simplest and generally cheapest is the vertical shaft type. Fluidized bed reactors are relatively a recent development. Figure 8 shows a rotary kiln pyrolysis reactor. The unit is cylindrical, slightly inclined and rotates slowly which causes the biomass to move through the kiln to the discharge end.

Numerous technologies have now been developed for the production of bio-oil and char using the pyrolysis process, Many of the reactors developed are improvements on the traditional reactors used in rural areas of developing countries that include simple pit kilns or drum type reactors. The energy efficiency of charcoal production using these methods is only the order of 17-29% while theoretically, efficiencies as high as 40% could be achieved.

Fig. 8. Schematic of the rotary kiln pyrolysis reactor.

### **3.2.2 Gasification**

218 Sustainable Growth and Applications in Renewable Energy Sources

and combustion. The advantages of thermo-chemical conversion processes include the

Pyrolysis or destructive distillation is an irreversible chemical change caused by the action of heat in the absence of oxygen. Pyrolysis of biomass leads to gases, liquids and solid residues. The important components of pyrolysis gas in most cases are hydrogen, carbon monoxide, carbon dioxide, methane and lesser quantities of other hydrocarbons (C2H4, C2H6, etc.). The liquid consists of methanol, acetic acid, acetone, water and tar. The solid residue consists of carbon and ash. Thus pyrolysis can be used to convert biomass into

In a typical pyrolysis process the feed material goes through the following operations: (a) primary shredding (b) drying the shredded material (c) removal of organics (d) further shredding to fine size (e) pyrolysis (f) cooling of the products to condense the liquids and (g)

Different types of pyrolytic reactors include vertical shaft reactors, horizontal beds. Among these, the simplest and generally cheapest is the vertical shaft type. Fluidized bed reactors are relatively a recent development. Figure 8 shows a rotary kiln pyrolysis reactor. The unit is cylindrical, slightly inclined and rotates slowly which causes the biomass to move

Numerous technologies have now been developed for the production of bio-oil and char using the pyrolysis process, Many of the reactors developed are improvements on the traditional reactors used in rural areas of developing countries that include simple pit kilns or drum type reactors. The energy efficiency of charcoal production using these methods is only the order of 17-29% while theoretically, efficiencies as high as 40% could be achieved.

following:

**3.2.1 Pyrolysis** 

storage of the products.

a. Rapid completion of reactions b. Large volume reduction of biomass

valuable chemicals and industrial feedstock.

through the kiln to the discharge end.

Fig. 8. Schematic of the rotary kiln pyrolysis reactor.

c. Range of liquid, solid and gaseous products are produced

d. Some processes do not require additional heat to complete the process

Gasification is the thermo-chemical process of converting biomass waste into a low medium energy gas utilizing sub-stoichiometric amounts of oxidant (Coovattanachai, 1991). The simplest form of gasification is air gasification in which biomass is subjected to partial combustion with a limited supply of air. Air gasifiers are simple, cheap and reliable. Their chief drawback is that the gas produced is diluted with nitrogen and hence has low calorific value. The gas produced is uneconomical to distribute; it must be used on-site for process heat. In oxygen gasification, pure oxygen is used so that the gas produced is of high energy content. The chief disadvantage of oxygen gasification is that it requires an oxygen plant and thus increases the total cost of gasification. The schematic diagram of the processes occurring is a gasifier is shown in Figure 9 including the temperature profile at each important step in the process.

Fig. 9. Schematic diagram of processes occurring in a gasifier and the temperature profile.

The simplest air gasifier is the updraft gasifier shown in Figure 10. Air is introduced at the bottom of the bed of biomass near the hearth zone. The gas produced is usually at a low temperature. The sensible heat of the gas is used to dry and preheat the biomass before it reaches the reduction zone. Products from the distillation and drying zones consist mainly of water vapor, tar and oil vapors and are not passed through the hot bed. They therefore leave the reactor uncracked and will later condense at temperatures between 125oC – 400oC.

Because the tar vapors leaving an updraft gas producer seriously interfere with the operation of internal combustion engines, the downdraft gasifiers (Barret, et. al., 1985) are more extensively used. The air is introduced into a downward flowing bed of solid fuel and the gas outlet is at the bottom as shown in Figure 11. The tarry oils and vapors given off in

Biomass Energy Conversion 221

Fig. 11. Schematic diagram of a downdraft draft gasifier.

Fig. 12. Schematic diagram of a fluidized bed gasifier.

the distillation zone are cracked and reduced to non-condensible gaseous products while passing through the oxidation (hearth) zone. Downdraft gasifiers have a reduced crosssectional area above which the air is introduced. The throat ensures a homogeneous layer of hot carbon through which the distillation gases must pass.

Fig. 10. Schematic diagram of an updraft gasifier.

The crossdraft gasifier is also a fixed bed gasifier where the feed material could be moved by gravity while the flow of air is at an angle against the feed flow. The usual flow of air is perpendicular to the flow of biomass. They have almost the same performance as the updraft and downdraft gasifiers.

A fluidized bed gasifier (LePori and Soltes, 1985) consists of a fluidized bed of inert particles in which biomass is fed. The gas stream generally carries with it the char particles out of the bed. These particles are separated from the gas by means of cyclones. Fluidized beds can gasify much higher amounts of biomass area per unit of time compared to the other types of gasifiers. The precise composition of the gas from the gasifiers depends on the type of biomass used, the temperature and rate of reaction. Typically, if wood is used as the feed, the gas composition is shown in Table 3. The heat content is about 5500 kJ/m3. The synthesis gas quality for the Texas A&M University fluidized bed gasifier is shown in Table 4 (Lepori, 1985). A schematic of a fluidized bed gasifier is shown in Figure 12.

the distillation zone are cracked and reduced to non-condensible gaseous products while passing through the oxidation (hearth) zone. Downdraft gasifiers have a reduced crosssectional area above which the air is introduced. The throat ensures a homogeneous layer of

The crossdraft gasifier is also a fixed bed gasifier where the feed material could be moved by gravity while the flow of air is at an angle against the feed flow. The usual flow of air is perpendicular to the flow of biomass. They have almost the same performance as the

A fluidized bed gasifier (LePori and Soltes, 1985) consists of a fluidized bed of inert particles in which biomass is fed. The gas stream generally carries with it the char particles out of the bed. These particles are separated from the gas by means of cyclones. Fluidized beds can gasify much higher amounts of biomass area per unit of time compared to the other types of gasifiers. The precise composition of the gas from the gasifiers depends on the type of biomass used, the temperature and rate of reaction. Typically, if wood is used as the feed, the gas composition is shown in Table 3. The heat content is about 5500 kJ/m3. The synthesis gas quality for the Texas A&M University fluidized bed gasifier is shown in Table 4 (Lepori, 1985). A schematic of a fluidized bed

hot carbon through which the distillation gases must pass.

Fig. 10. Schematic diagram of an updraft gasifier.

updraft and downdraft gasifiers.

gasifier is shown in Figure 12.

Fig. 11. Schematic diagram of a downdraft draft gasifier.

Fig. 12. Schematic diagram of a fluidized bed gasifier.

Biomass Energy Conversion 223

absence of fouling and deposits on heat transfer surfaces. The schematic diagram of a fluidized bed combustor is similar to that of a fluidized bed gasifier. The only difference is the use of

So far FBC has been used mostly for coals. A number of wastes, e.g. wastes from coal mining and municipal wastes, are also sometimes incinerated in fluidized beds. It has been suggested that certain quick-maturing varieties of wood could be combusted in fluidized beds for generation of steam. There is indeed a global search for suitable varieties of wood for this purpose and FBC is likely to play an important role in supplying energy

excess air for combustion processes and starved air for gasification processes.

Fig. 13. Schematic diagram of a reciprocating grate combustor (Courtesy of Detroit

Kg/hr-m2 have been achieved in fluidized bed combustors using biomass fuels.

Granular biomass fuels, e.g. paddy husk and chips of wood up to 2cm x 2cm x 2cm in size have been successfully combusted in fluidized beds of sand particles. Conventional combustion of paddy husk is slow and inefficient. Nearly complete combustion and high combustion intensities of paddy husk can be achieved in a fluidized bed combustor. The same combustor can also be used for burning wood. Combustion intensities up to about 500

A number of thermo-chemical conversion processes exist for converting biomass into liquid fuels. These can be crudely divided into direct liquefaction and indirect liquefaction (in which the biomass is gasified as a preliminary step) processes. While all these techniques are relatively sophisticated and will generally be suitable for large scale conversion facilities,

requirements in certain countries in the future.

Reciprogate Stocker).


Table 3. Typical gas composition of a fluidized bed gasifier using wood as feedstock.


Table 4. Typical gas composition of the TAMU fluidized bed gasifier.
