**The Expanded Electrodeionization Method for Sewage Reclamation**

Yansheng Li, Zhigang Liu, Ying Wang and Yunze Hui

Additional information is available at the end of the chapter

http://dx.doi.org/10.5772/60981

#### **Abstract**

The aim of the chapter is to introduce a new technology using the flow-divided electrodes for sewage reclamation based on redox and concentrating ions. This creative system can be used directly for sewage treatment without the need for costly ion-exchange membranes and other chemical reagents. Under experimental condi‐ tions, the removal percentage of TDS (total dissolved salts) is 83 %and the removal percentage of COD (chemical oxygen demand) is 92 %.

**Keywords:** Flow-divided electrodes, expanded electrodeionization, sewage recla‐ mation, ion-exchange

### **1. Introduction**

In general, urban sewage discharge accounts for 75\_85% of the consumption and the industrial sewage discharge accounts for 80\_90% of its consumption. Sewage, that is actually utilized in a biological or chemical way and disappears in the form of vaporization loss is less than 25%. Because of the low rate of sewage treatment in China, the majority of the surface water resources and the underground water resources are polluted to different extents, resulting in extra pressure, caused by the shortage of water resource, on the sound and sustainable development of economy and society. Sewage reclamation is not only favorable for enterprises to increase income and decrease expenditure as well as reduce consumption and improve efficiency, but is also an inevitable option for enhancing the supply capacity of urban water.

© 2015 The Author(s). Licensee InTech. 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.

It is more important to improve the revitalization environment of aquatic ecosystems, benefiting not only the present generation, but also future generations. Advanced sewage treatment means that, in order to cause urban sewage or industrial wastewater, which has been subjected to routine treatment, to reach a certain standard of recycled water and to be reused for production or living, treatment units are added in order to further remove the pollutants that cannot be removed by routine treatment, such as heavy metals, COD (chemical oxygen demand), TN (total nitrogen), TP (total phosphorus), TDS (total dissolved salt) and the like.

The electrochemical process has the prominent characteristics of wide adaptability, good cleaning property and easy control in removing the pollutants in sewage water, and its course is mainly mass transfer control. Firstly, it is necessary to eliminate the ohmic resistance between electrodes with a supporting electrolyte such as sodium chloride. However, the wide appli‐ cation of this method is limited by water recycling. Secondly, the reaction products (especially gases such as hydrogen from cathode and oxygen and carbon dioxide from anode as shown in Figs.1and 2) inhibit the reactants at the reaction zone and increase the ohmic resistance markedly. Thirdly, the scaling on cathode accumulates over the reaction zone and decreases current efficiency.

**Figure 1.** A schematic illustration of a sewage electrolysis system

**Figure 2.** Electrical circuit analogy of resistances in a sewage electrolysis system

It is more important to improve the revitalization environment of aquatic ecosystems, benefiting not only the present generation, but also future generations. Advanced sewage treatment means that, in order to cause urban sewage or industrial wastewater, which has been subjected to routine treatment, to reach a certain standard of recycled water and to be reused for production or living, treatment units are added in order to further remove the pollutants that cannot be removed by routine treatment, such as heavy metals, COD (chemical oxygen demand), TN (total nitrogen), TP (total phosphorus), TDS (total dissolved salt) and the like.

The electrochemical process has the prominent characteristics of wide adaptability, good cleaning property and easy control in removing the pollutants in sewage water, and its course is mainly mass transfer control. Firstly, it is necessary to eliminate the ohmic resistance between electrodes with a supporting electrolyte such as sodium chloride. However, the wide appli‐ cation of this method is limited by water recycling. Secondly, the reaction products (especially gases such as hydrogen from cathode and oxygen and carbon dioxide from anode as shown in Figs.1and 2) inhibit the reactants at the reaction zone and increase the ohmic resistance markedly. Thirdly, the scaling on cathode accumulates over the reaction zone and decreases

current efficiency.

258 Desalination Updates

**Figure 1.** A schematic illustration of a sewage electrolysis system

As shown in Fig.2, electrochemical resistance consists of the electrical resistance (R1 R2) reaction resistance (Ranode Rcathode) and transfer resistance (R anode bubble Relectrolyte Rdissolved gases R cathode bubble). Transfer resistance in a sewage electrolysis system is negatively related to the reaction resistance. Decreasing energy consumption of the electrochemical process is a challenge.

Combination of ion exchange and electrochemical technology research from the beginning that the ion exchange membrane i.e. the electrodialysis technology. Ion exchangers and selective ion exchange membranes having ion conduction capability are simultaneously used in, electrodeionization (EDI) and to overcome the defects that electrolyte addition causes in the process of electrolytic reaction and chemical regeneration in the process of ion exchange. However, the particularity of hydrogen ion and hydroxyl ions (migration behavior in the electric field and selectivity of hydrogen ion to strongly acidic cation exchange resin and hydroxyl ions to strongly basic anion exchange resin) limits the efficiency of the electrical energy. Polarization caused by the verticality of membrane surface and flow field to electric field, as well as their impacts still exist as key factors that restrict the improvement of operation efficiency and the widening of applicable scope, their practical applications still require improvement.

The aim of this chapter is to provide a new technology using flow-divided electrodes for sewage reclamation based on redox and concentrating ions. This creative system can be used directly for sewage treatment without use of costly ion-exchange membranes and other chemical reagents. Under experimental conditions, the removal percentage of TDS (total dissolved salts) is 83 %and the removal percentage of COD (chemical oxygen demand) is 92 %.

#### **2. Technological process**

Fig 3 is a schematic diagram of the super advanced sewage treatment process. We proposed a novel EEDI system by introducing porous flow-divided electrodes (FDE) as the electroos‐ motic unit. During operation process, the flow of wastewater and gases from electrodes is controlled so as to penetrate into the internal part of FDE, which we call as the flow-divided model (Fig 3). The flow field is parallel to the electric by means of the porous FDE,thus avoiding mutual interference between the cathode reaction and the anode reaction, and reducing the ohmic resistance and mass transfer resistance (R anode bubble R cathode bubble), and realizing separation of the anolyte (containing oxygen and carbon dioxide) and catholyte (containing hydrogen) without any diaphragm(Fig 4).

2. Technological process

between the cathode reaction and the anode reaction, and reducing the ohmic resistance and mass

oxygen and carbon dioxide)and catholyte(containing hydrogen)without any diaphragm( Fig 4).

**Figure 3.** Schematic diagram of the Super Advanced Sewage Treatment process transfer resistance(R anode bubble R cathode bubble), and realizing separation of the anolyte(containing

**Figure 4.** Mechanisms of ion migration to the electroosmotic section

Furthermore, polarity of the electrodes can be flexibly switched, thus eliminating cathode scaling during extended operation. The EEDI utilizes electrochemical redox and ion-exchange simultaneously to produce the concentrated electrolyzed oxidizing water (EOW), desalted water (DW) and hydrogen as by-product. Furthermore, polarity of the electrodes can be flexibly switched, thus eliminating cathode scaling during extended operation. The EEDI utilizes electrochemical redox and ion-exchange simultaneously to produce the concentrated electrolyzed oxidizing water (EOW), desalted water (DW) and hydrogen as by-product.

Fig 4 Mechanisms of ion migration to the electroosmotic section

Since the anodes and cathodes in the EEDI are completely uniform and no ion-exchange membranes are used, it can be operated by switching anodes and cathodes flexibly for eliminating the scaling on the surface of cathodes. The strongly basic anion exchange resin grains placed among the anode and cathode act as supporting electrolyte, enapabling the treatment of wastewater with low salt. The concentrated and neutralized anolyte containing active chlorine is effective for disinfection and contaminant removal.

## **3. Materials and methods**

### **3.1. Titanic porous FDE and electroosmotic unit**

The electroosmotic unit was constructed with three hexagonal anodes and cathodes (area 0.0113 m2 ) within a insulated polymethyl methacrylate shell(Fig 5). The distance of between anode and cathode is 25 mm and they are packed with strong basic anion exchange resin grains (201×7, properties shown in Table 2). The electrolyzed oxidizing water (containing gases) and electrolyzed reducing water were pressed to flow out of the anode and cathode, respectively (see Fig 3).


**Table 1.** Properties of the porous FDE

**Figure 3.** Schematic diagram of the Super Advanced Sewage Treatment process

(DW) and hydrogen as by-product.

water (DW) and hydrogen as by-product.

**Figure 4.** Mechanisms of ion migration to the electroosmotic section

active chlorine is effective for disinfection and contaminant removal.

Fig 3 Schematic diagram of the Super Advanced Sewage Treatment process

 Fig 3 is a schematic diagram of the super advanced sewage treatment process. We proposed a novel EEDI system by introducing porous flow-divided electrodes (FDE) as the electroosmotic unit. During operation process, the flow of wastewater and gases from electrodes is controlled so as to penetrate into the internal part of FDE, which we call as the flow-divided model (Fig 3). The flow field is parallel to the electric by means of the porous FDE ,thus avoiding mutual interference between the cathode reaction and the anode reaction, and reducing the ohmic resistance and mass transfer resistance(R anode bubble R cathode bubble), and realizing separation of the anolyte(containing oxygen and carbon dioxide)and catholyte(containing hydrogen)without any diaphragm( Fig 4).

+ -

Fig 4 Mechanisms of ion migration to the electroosmotic section Furthermore, polarity of the electrodes can be flexibly switched, thus eliminating cathode scaling during extended operation. The EEDI utilizes electrochemical redox and ion-exchange simultaneously to produce the concentrated electrolyzed oxidizing water (EOW), desalted water

Furthermore, polarity of the electrodes can be flexibly switched, thus eliminating cathode scaling during extended operation. The EEDI utilizes electrochemical redox and ion-exchange simultaneously to produce the concentrated electrolyzed oxidizing water (EOW), desalted

Since the anodes and cathodes in the EEDI are completely uniform and no ion-exchange membranes are used, it can be operated by switching anodes and cathodes flexibly for eliminating the scaling on the surface of cathodes. The strongly basic anion exchange resin grains placed among the anode and cathode act as supporting electrolyte, enapabling the treatment of wastewater with low salt. The concentrated and neutralized anolyte containing

2. Technological process

260 Desalination Updates

**Figure 5.** a structural schematic diagram of the electro-osmotic unit 1—anode, 2—cathode, 3—organic glass shell, 4 sewage inlet.


**Table 2.** Properties of 201×7type strong basicity anion exchange resin

#### **3.2. Ion exchange treatment and regeneration**

The electrolyzed oxidizing water out of anode was pumped into Na-form D113 column (regeneration), whose properties are shown in Table 3. The electrolyzed reducing water out of cathode was pumped into H-form D113 column (treatment).


**Table 3.** Properties of D113 weak acid cation exchanger

#### **3.3. Sewage treatment**

The flux of the simulated wastewater (properties shown in Table 4) is 7.5 L/h. The voltage of the electroosmotic unit is controlled at 25 V. The ratio of electrolyzed oxidizing water and electrolyzed reducing water is 1. The COD was determined by bichromate method. Concen‐ tration of Cl was determined by titration with silver nitrate solution. A power supply (LW10J10) was used to maintain constant DC voltage. Conductivities were measured by a conductometer (DDS-IIA). The pH of water was measured by an acidimeter (DELTA320). Temperature was held at room temperature during all experiments.

#### **3.4. Cooling water treatment**

The flux of the cooling water (properties shown in Table 5) is 3.0L/h. The voltage of the electroosmotic unit is controlled at 15 V. The ratio of electrolyzed oxidizing water and electrolyzed reducing water is 0.5. Apparent current density was between 88 and 90 Am - 2.

### **4. Results and discussion**

#### **4.1. Treatment of the simulated wastewater**

The properties of water samples, including the feed, electrolyzed oxidizing water, electrolyzed reducing water and the desalted water are shown in Table 4. The removal percentage of TDS and the removal percentage of COD for the desalted water are 83 % and 92 %, respectively.

COD(mg/L)


This result demonstrates that the novel flow-divided EEDI can remove contaminants effec‐ tively without chemical reagents. (mg/L) pH Conductance(μs/cm)

Simulated wastewater 689 7.28 2100 426

The properties of water samples, including the feed, electrolyzed oxidizing water, electrolyzed reducing water and the desalted water are shown in Table 4. The removal percentage of TDS and the removal percentage of COD for the desalted water are 83 % and 92 %, respectively. This result demonstrates that the novel flow-divided EEDI can remove contaminants

**Table 4.** Properties of the feed and the electrolyzed oxidizing and electrolyzed reducing water Desalted water 4.16 350 32.6

Fig 6 The pH of NEOW and DW versus time Fig 6 shows pH variation for EOW and DW from flow-divided EEDI versus time. It can be **Figure 6.** The pH of NEOW and DW versus time

**4. Results and discussion** 

effectively without chemical reagents.

Cl-

concentration

**4.1 Treatment of the simulated wastewater**

**Group Exchange capacity**

**Group Exchange capacity**

**3.3. Sewage treatment**

**3.4. Cooling water treatment**

**4. Results and discussion**

**4.1. Treatment of the simulated wastewater**

tration of Cl-

**(mmol/ml)**

**Table 3.** Properties of D113 weak acid cation exchanger


262 Desalination Updates

**(mmol/ml)**

**Diameter (mm)**

**Table 2.** Properties of 201×7type strong basicity anion exchange resin

cathode was pumped into H-form D113 column (treatment).

**Diameter (mm)**


Temperature was held at room temperature during all experiments.

**3.2. Ion exchange treatment and regeneration**

**Water content (%)**

(CH3)3 ≥1.4 0.6\_1.4 42\_48 1.06\_1.11 Cl → OH:18\_22 100 1\_14

The electrolyzed oxidizing water out of anode was pumped into Na-form D113 column (regeneration), whose properties are shown in Table 3. The electrolyzed reducing water out of

The flux of the simulated wastewater (properties shown in Table 4) is 7.5 L/h. The voltage of the electroosmotic unit is controlled at 25 V. The ratio of electrolyzed oxidizing water and electrolyzed reducing water is 1. The COD was determined by bichromate method. Concen‐

(LW10J10) was used to maintain constant DC voltage. Conductivities were measured by a conductometer (DDS-IIA). The pH of water was measured by an acidimeter (DELTA320).

The flux of the cooling water (properties shown in Table 5) is 3.0L/h. The voltage of the electroosmotic unit is controlled at 15 V. The ratio of electrolyzed oxidizing water and electrolyzed reducing water is 0.5. Apparent current density was between 88 and 90 Am - 2.

The properties of water samples, including the feed, electrolyzed oxidizing water, electrolyzed reducing water and the desalted water are shown in Table 4. The removal percentage of TDS and the removal percentage of COD for the desalted water are 83 % and 92 %, respectively.

**Density (g/ml)**

was determined by titration with silver nitrate solution. A power supply

**Water content (%)**

**Density**

**(g/ml) Expansibility (%)**

**Expansibility (%)**

20\_30

**Upper limit temperature (°C)**

**Upper limit temperature (°C) pH range**

100 5\_14

**pH range**

seen that pH of EOW gradually decreased, while pH of DW gradually increased with time. The change of pH can periodically provide information about the transforming degree of the ion exchanger for the polarity reversal operation. Fig 6 shows pH variation for EOW and DW from flow-divided EEDI versus time. It can be seen that pH of EOW gradually decreased, while pH of DW gradually increased with time. The change of pH can periodically provide information about the transforming degree of the ion exchanger for the polarity reversal operation.

#### **4.2. Mechanism of ion migration and COD removal**

The strong base anion exchange resins placed between anode and cathode play an important role in gathering anions, in adjusting ion migration and acting as the supporting electrolyte. There are three routes for anion migration: (1) ions migrate alternatively through solution or ion-exchange resins, (2) ions migrate through ion-exchange resin grains and (3) ions migrate in solution. However, there is only one route for cation migration, that is, through solution (Fig 7). Furthermore, the diffusion coefficient for ion migration in ion-exchange resins is much higher than that in solution. As a result, the amount of anions in anode affinity is much higher than the cations in cathode affinity. Chlorine ions thus gathered in anode around and formed concentrated chlorine water. The relevant reactions are shown as follows:

$$\text{2Cl} \quad \text{2e} \quad \text{2e} \quad \text{ \to Cl}\_2 \tag{1}$$

$$\text{CH}\_2\text{O} \quad \text{Cl}\_2 \rightarrow \text{H}^+ + \text{Cl}^- + \text{HClO} \tag{2}$$

$$\text{H}\_2\text{O} \quad 2\text{e} \quad \rightarrow \text{H}^+ \ 1/2\text{ O}\_2 \tag{3}$$

$$\text{Organic substances} \quad \text{ne} \quad \rightarrow \text{intermediate} \text{+ CO}\_2 \tag{4}$$

The organic substances (or HCO3 – ) around the anode are oxidized directly or indirectly into carbon dioxide or intermediates. The hydroxide ions are concentrated and passed through the filter cylinder cathode. Hydrogen formed by water electrolysis penetrates into the inner part of FDE by the force of electric fields and flow fields. In this case, concentration and ohm resistance can be reduced remarkably. Hydrogen evolution from water electrolysis is shown as follows:

$$2\text{H}\_2\text{O} \quad \text{Na}^+\text{ }2\text{e}^- \rightarrow \text{H}\_2 \quad \text{Na}^+ + 2\text{OH} \tag{5}$$

$$\text{H}^+\text{ 2e}^- \rightarrow \text{H}\_2\tag{6}$$

**Figure 7.** Schematic representation of the three paths that the current can take

**Figure 8.** Distribution of the species between anode and cathode

#### **4.3. Reaction of ion exchange**

higher than that in solution. As a result, the amount of anions in anode affinity is much higher than the cations in cathode affinity. Chlorine ions thus gathered in anode around and formed

> H O Cl H + Cl + HClO 2 2 +

carbon dioxide or intermediates. The hydroxide ions are concentrated and passed through the filter cylinder cathode. Hydrogen formed by water electrolysis penetrates into the inner part of FDE by the force of electric fields and flow fields. In this case, concentration and ohm resistance can be reduced remarkably. Hydrogen evolution from water electrolysis is shown

® <sup>2</sup> 2 Cl 2e Cl (1)

® <sup>+</sup> H O 2e H 1/2 O 2 2 (3)

) around the anode are oxidized directly or indirectly into

H 2e H <sup>+</sup> ® <sup>2</sup> (6)

Organic substances ne intermediate+ CO ® <sup>2</sup> (4)

2H O Na 2e H Na + 2OH 2 2 + + ® (5)

® (2)

concentrated chlorine water. The relevant reactions are shown as follows:

–

**Figure 7.** Schematic representation of the three paths that the current can take

The organic substances (or HCO3

as follows:

264 Desalination Updates

The neutralization reaction between the electrolyzed reducing water and the H-form D113 resin is as follows:

$$\text{R-COOH} \quad \text{Na}^+ \quad \text{OH} \quad \rightarrow \text{R-COONa} \quad \text{H}\_2\text{O} \tag{7}$$

Na+ Ions are adsorbed on ion-exchange resin, thereby desalting the feeds. The Na-form D113 ion-exchange resin was regenerated into H-form D113 with electrolyzed oxidizing water for reuse. The reaction is shown as follows:

$$\text{R-COONa} + \text{H}^+ \rightarrow \text{R-COOH} + \text{Na}^+ \tag{8}$$

Since the cathodes and anodes in EEDI are completely uniform and no ion-exchange mem‐ brance are used in this system, this flow-divided EEDI can be operated by switching anodes and cathodes flexibly, eliminating the scaling on the surface of cathodes.

#### **4.4. Mass balance**

The mass balance of this novel flow-divided EEDI was calculated according to the ratio of electrolyzed oxidizing water and electrolyzed reducing water as shown in Fig 5. As mentioned in Section 3.2, NaCl was concentrated in anode around up to 83 %(mass ratio) with the help of strong base ion-exchange resin. Organic contaminants were oxidized in anode with COD removal percentage of 92 %.

is as follows:

Na<sup>+</sup>

strong base ion‐exchange resin. Organic contaminants were oxidized in anode with COD removal

Fig 8 Distribution of the species between anode and cathode

The neutralization reaction between the electrolyzed reducing water and the H-form D113 resin

ion-exchange resin was regenerated into H-form D113 with electrolyzed oxidizing water for reuse.

Since the cathodes and anodes in EEDI are completely uniform and no ion-exchange membrance are used in this system, this flow-divided EEDI can be operated by switching anodes

The mass balance of this novel flow‐divided EEDI was calculated according to the ratio of electrolyzed oxidizing water and electrolyzed reducing water as shown in Fig 5. As mentioned in

and cathodes flexibly, eliminating the scaling on the surface of cathodes.

Ions are adsorbed on ion-exchange resin, thereby desalting the feeds. The Na-form D113

→ R-COONa+H2O ( 7 )

→R-COOH + Na+ ( 8)

**Figure 9.** Schematic representation of mass balance

**4.3 Reaction of ion exchange** 

R-COOH+Na<sup>+</sup>+ OH-

The reaction is shown as follows: R-COONa + H+

**4.4 Mass balance** 

#### **4.5. Treatment of the cooling water 4.5.1 Material equilibrium of the cooling water treament**

#### *4.5.1. Material equilibrium of the cooling water treament*

The properties of the cooling water and the desalted water are shown in Table 5. The removal percentage of the hardness and the removal percentage of Cl for the desalted water are 98 %and 74 %, respectively. The removal percentage of dissolved oxygen is 36 %. conductance (μs/cm) DO(mg/L) pH Cl- (mg/L) Hardness (CaCO3mg/L)

Table 5 Properties of the feed and the desalted water

Cooling water 2100 7.5 7.55 479.85 750

Fig 9 Schematic representation of mass balance


→2H2O ( 9 )

The above reaction decreases the dissolved oxygen content of the cooling water and

The electrolyzed reducing water with the higher pH goes into the series type hydrogen D113.

 R-COOH+Na++OH→ R-COONa+H2O ( 10) 2R-COONa+Ca(Mg) 2+ →(R-COO)2Ca(Mg)+ 2Na+ ( 11)

 Fig 10 Mass balance of the cooling water treatment **Figure 10.** Mass balance of the cooling water treatment

contributes to corrosion control in the circulating system.

Neutralization and exchange reaction is shown as follows:

**4.5.3 The sterilization effect**

O2+4H<sup>+</sup>

+4e-

#### *4.5.2. Mechanism of DO and hardness ions removal*

**4.5.2 Mechanism of DO and hardness ions removal** The water passes through the cathode and the following reactions take place:

The water passes through the cathode and the following reactions take place:

$$\text{O}\_2 \text{+4H}^+ \text{+4e}^\cdot \rightarrow 2\text{H}\_2\text{O} \tag{9}$$

The above reaction decreases the dissolved oxygen content of the cooling water and contributes to corrosion control in the circulating system.

The electrolyzed reducing water with the higher pH goes into the series type hydrogen D113. Neutralization and exchange reaction is shown as follows:

$$\text{R-COOH} \quad \text{Na} \quad \text{OH} \rightarrow \text{R-COONa} \quad \text{H}\_2\text{O} \tag{10}$$

$$\text{2R-COONa} \quad \text{Ca} \left(\text{Mg}\right)^{\text{2+}} \rightarrow \text{(R-COO)}\_2\text{Ca} \left(\text{Mg}\right) \quad \text{2Na}^+ \tag{11}$$

#### *4.5.3. The sterilization effect*

Fig 8 Distribution of the species between anode and cathode

The neutralization reaction between the electrolyzed reducing water and the H-form D113 resin

ion-exchange resin was regenerated into H-form D113 with electrolyzed oxidizing water for reuse.

Since the cathodes and anodes in EEDI are completely uniform and no ion-exchange membrance are used in this system, this flow-divided EEDI can be operated by switching anodes

The mass balance of this novel flow‐divided EEDI was calculated according to the ratio of electrolyzed oxidizing water and electrolyzed reducing water as shown in Fig 5. As mentioned in Section 3.2, NaCl was concentrated in anode around up to 83 %(mass ratio) with the help of strong base ion‐exchange resin. Organic contaminants were oxidized in anode with COD removal

Fig 9 Schematic representation of mass balance

The properties of the cooling water and the desalted water are shown in Table 5. The removal

NEOW DW

50% H2O 50% H2O

The feeds

and cathodes flexibly, eliminating the scaling on the surface of cathodes.

Ions are adsorbed on ion-exchange resin, thereby desalting the feeds. The Na-form D113

→ R-COONa+H2O ( 7 )

17%NaCl

8%COD

for the desalted water are 98

Hardness (CaCO3mg/L)

 **(mg/L) Hardness (CaCO3mg/L)**

26% Cl-

2% Ca2+

for the desalted water are 98 %and

→R-COOH + Na+ ( 8)

**4.3 Reaction of ion exchange** 

R-COOH+Na<sup>+</sup>+ OH-

The reaction is shown as follows: R-COONa + H+

**4.4 Mass balance** 

percentage of 92 %.

266 Desalination Updates

Desalted water (DW)

74 %Cl-

98%Ca2+

Desalted water

O2+4H<sup>+</sup>

+4e-

contributes to corrosion control in the circulating system.

Neutralization and exchange reaction is shown as follows:

**4.5.3 The sterilization effect**

83% NaCl

92% COD

conductance (μs/cm)

**Figure 9.** Schematic representation of mass balance

*4.5.1. Material equilibrium of the cooling water treament*

**Conductance**

**Table 5.** Properties of the feed and the desalted water

**Figure 10.** Mass balance of the cooling water treatment

*4.5.2. Mechanism of DO and hardness ions removal*

74 %, respectively. The removal percentage of dissolved oxygen is 36 %.

**4.5.2 Mechanism of DO and hardness ions removal**

The water passes through the cathode and the following reactions take place:

percentage of the hardness and the removal percentage of Cl-

percentage of the hardness and the removal percentage of Cl-

**4.5.1 Material equilibrium of the cooling water treament** 

%and 74 %, respectively. The removal percentage of dissolved oxygen is 36 %.

Cooling water 2100 7.5 7.55 479.85 750

(DW) 580 4.6 6.57 189.94 30

DO(mg/L) pH Cl-

Table 5 Properties of the feed and the desalted water

**(μs/cm) DO (mg/L) pH Cl-**

The properties of the cooling water and the desalted water are shown in Table 5. The removal

Fig 10 Mass balance of the cooling water treatment

The water passes through the cathode and the following reactions take place:

→2H2O ( 9 )

The above reaction decreases the dissolved oxygen content of the cooling water and

The electrolyzed reducing water with the higher pH goes into the series type hydrogen D113.

 R-COOH+Na++OH→ R-COONa+H2O ( 10) 2R-COONa+Ca(Mg) 2+ →(R-COO)2Ca(Mg)+ 2Na+ ( 11)

Cooling water 2100 7.5 7.55 479.85 750

The feeds

<sup>36</sup>% DO <sup>64</sup>%DO

34%H2O 66%H2O

NEOW DW

580 4.6 6.57 189.94 30

(mg/L)

**4.5. Treatment of the cooling water**

**4.5 Treatment of the cooling water**

is as follows:

Na<sup>+</sup>

Fig 11 shows bacterial concentration in the feed and DW samples. It can be observed that there are groups of bacteria in the feed sample. When water passes through the electrode, the bacteria are destroyed by directly touching the electrodes. As a result, no bacteria exist in the culture dish. The DW does not come in contact with the active chlorine, but the bacteria are destroyed by cathode and electric field.

Fig 11 Comparison of bacterial concentration in the feed and the DW **Figure 11.** Comparison of bacterial concentration in the feed and the DW

#### are destroyed by directly touching the electrodes. As a result, no bacteria exist in the culture dish. **5. Conclusion and expectation**

pollution is caused.

of sewage reclamation.

cathode and electric field. **5. Conclusion and expectation**  The electro-osmosis ion exchange method presented here has wide adaptability in the aspect of the super advanced purification of sewage, no chemical agent is needed and no secondary pollution is caused.

The DW does not come in contact with the active chlorine, but the bacteria are destroyed by

**5.1.** The electro-osmosis ion exchange method presented here has wide adaptability in the aspect of the super advanced purification of sewage, no chemical agent is needed and no secondary

cathode/anode-equivalent micropore titanium filter electrode array and the designadopted,such that the flow field is parallel to the electric field , avoids mutual interference between the cathode reaction and the anode reaction and reduces current reduction and mass transfer hindrance, which are caused by gas coverage generated in the process of electrolysis. Furthermore, the elimination of scaling of electrodes through electrode reverse operation and the regeneration and continuous

**5.3.** Filling resin between the electrodes results in an electrolyte supporting effect, so as to avoid the limitation on the electrical conductivity of influent. Electrolyte addition is not required when

**5.4.** The invention provides a new way for pollution control and resource recycling, has become

an extremely promising technology as the recycling of H2 is turned into another point for economic growth and will bring wide prospect to ion exchange application technology in the field

**5.2.** The electro-osmosis unit does not require the use of membranes, the

operation of subsequent ion exchange resin are facilitated.

sewage with low electrical conductivity is treated.

Fig 11 shows bacterial concentration in the feed and DW samples. It can be observed that there are groups of bacteria in the feed sample. When water passes through the electrode, the bacteria The electro-osmosis unit does not require the use of membranes, the cathode/anode-equivalent micropore titanium filter electrode array and the designadopted,such that the flow field is parallel to the electric field, avoids mutual interference between the cathode reaction and the anode reaction and reduces current reduction and mass transfer hindrance, which are caused by gas coverage generated in the process of electrolysis. Furthermore, the elimination of scaling of electrodes through electrode reverse operation and the regeneration and continuous operation of subsequent ion exchange resin are facilitated.

Filling resin between the electrodes results in an electrolyte supporting effect, so as to avoid the limitation on the electrical conductivity of influent. Electrolyte addition is not required when sewage with low electrical conductivity is treated.

The invention provides a new way for pollution control and resource recycling, has become an extremely promising technology as the recycling of H2 is turned into another point for economic growth and will bring wide prospect to ion exchange application technology in the field of sewage reclamation.

A wide space is provided for the application and development of the electro-osmosis ion exchange method due to diversified commercial ion exchangers.

### **Author details**

Yansheng Li1\*, Zhigang Liu1 , Ying Wang1 and Yunze Hui2

\*Address all correspondence to: hjx@djtu.edu.cn

1 College of Environmental and Chemical Engineering, Dalian Jiaotong University and Liaoning Key Laboratory for Environmental science and Technology, Dalian, China

2 Newcastle University, Australia

### **References**


[4] Yansheng Li, Yongbin Li, Zhigang Liu, et al. A novel electrochemical ion exchange system and its application in water treatment[J] Journal Of Environmental Sciences 2011,23Supplement:14-17

The electro-osmosis unit does not require the use of membranes, the cathode/anode-equivalent micropore titanium filter electrode array and the designadopted,such that the flow field is parallel to the electric field, avoids mutual interference between the cathode reaction and the anode reaction and reduces current reduction and mass transfer hindrance, which are caused by gas coverage generated in the process of electrolysis. Furthermore, the elimination of scaling of electrodes through electrode reverse operation and the regeneration and continuous

Filling resin between the electrodes results in an electrolyte supporting effect, so as to avoid the limitation on the electrical conductivity of influent. Electrolyte addition is not required

The invention provides a new way for pollution control and resource recycling, has become an extremely promising technology as the recycling of H2 is turned into another point for economic growth and will bring wide prospect to ion exchange application technology in the

A wide space is provided for the application and development of the electro-osmosis ion

and Yunze Hui2

1 College of Environmental and Chemical Engineering, Dalian Jiaotong University and

[1] Mark A. Shannon, Paul W. Bohn, Menachem Elimelech, et al. Science and technology for water purification in the coming decades Nature, 2008, 452 (20) :301-310.

[2] Konstantinos Dermentzisa, Konstantinos Ouzounis Continuous capacitive deioniza‐ tion–electrodialysis reversal through electrostatic shielding for desalination and dei‐

[3] ANDREW TURNER.Electrochemical ion exchange[J].Membane Technology, 1996,

onization of water Electrochimica Acta 53 (2008) 7123–7130

Liaoning Key Laboratory for Environmental science and Technology, Dalian, China

operation of subsequent ion exchange resin are facilitated.

when sewage with low electrical conductivity is treated.

exchange method due to diversified commercial ion exchangers.

, Ying Wang1

field of sewage reclamation.

Yansheng Li1\*, Zhigang Liu1

2 Newcastle University, Australia

\*Address all correspondence to: hjx@djtu.edu.cn

**Author details**

268 Desalination Updates

**References**

75: 6-9.


**Special Industrial Application**
