CN104324613A - Flue gas desulfurization method - Google Patents
Flue gas desulfurization method Download PDFInfo
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- CN104324613A CN104324613A CN201410472051.4A CN201410472051A CN104324613A CN 104324613 A CN104324613 A CN 104324613A CN 201410472051 A CN201410472051 A CN 201410472051A CN 104324613 A CN104324613 A CN 104324613A
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Abstract
The invention discloses a flue gas desulfurization method which is characterized in that the flue gas desulfurization method comprises the following steps: (a) flue gas and an adsorbent are contacted with each other in an absorption tower so as to obtain desulfurized flue gas and absorption liquid; (b) the absorption liquid passes through a dual-cell bipolar membrane electrodialyzer to carry out first electrodialysis so as to obtain first alkali lye and a first salt solution, or obtain a second salt solution and a first acid liquor; and (c) the first salt solution or the first acid liquor is introduced into a desorption tower to carry out desorption so as to obtain SO2 gas and a desorption solution; and the desorption solution is introduced into a three-cell bipolar membrane electrodialyzer (5) to carry out second electrodialysis so as to obtain a second acid liquor, a third salt solution and second alkali lye, wherein at least one of the second salt solution and the second alkali lye is recycled. Through the above technical scheme, the absorption liquid can effectively be recovered, effluents are no longer discharged, and power consumption is reduced.
Description
Technical field
The present invention relates to field of chemical engineering, particularly, relate to a kind of fume desulphurization method.
Background technology
The mixture of flue gas general reference gas and flue dust.The operation of the chemical industry equipments such as boiler, industrial furnace, thermal power plant, coke oven, cement plant, blast furnace, open hearth, converter, electric furnace and catalytic cracking (FCC) device all can produce a large amount of flue gases.The air pollutants such as a large amount of sulfur and nitrogen oxides contained in flue gas bring series of environmental problems.The discharge reduced containing air pollutants such as sulfur and nitrogen oxides is the task of top priority of protection of the environment.Such as standard GB/T 13271-91 " emission standard of air pollutants for boilers ", GB9078-1996 " industrial furnace atmosphere pollutants emission standards ", GB13223-1996 " fossil-fuel power plant atmospheric pollutant emission standard ", GB16171-1996 " coke oven atmosphere pollutants emission standards " and GB4915-1996 " Airborne Pollutants from Cement Plant discharge standard " define the discharge standard of pollutant in flue gas.Therefore, after desulphurization and denitration and dust removal process must being carried out to flue gas, just can discharge.
In the flue gas desulfurization technique of commercial Application, wet desulphurization is the most frequently used at present and one of comparatively ripe method.Conventional FCC regenerated flue gas absorption process has the WGS wet scrubbing of EXXON company, the THIOPAQ biotechnology of Uop Inc., the EDV wet scrubbing technology etc. of Belco company.Wherein the EDV Wet Flue Gas Desulfurization Technology of Belco company has become industrial gas purification and SO
2one of main method reclaimed.Started commercial Application from 1994, EDV Wet Flue Gas Desulfurization Technology just demonstrates excellent operability and reliability.So far, supporting more than 90 cover catalytic cracking units EDV facility, wherein maximum production capacity is 5Mt/a.But the greatest problem that EDV Wet Flue Gas Desulfurization Technology exists is that this technology can consume large water gaging and NaOH as absorbing liquid, and with the SO in flue gas
2after reaction, be a large amount of sodium sulfate salt solution through oxidation transformation, thus create the emission problem of a large amount of high-salt wastewater.Patent document CN102335553A utilizes bipolar membrane electrodialysis to be carried out by high-salt wastewater recycling the consumption that can reduce water and NaOH, but the method needs the sulfite ion of generation and sulfurous acid hydrogen radical ion to be oxidized to sulfate ion, then electrodialysis is carried out, make step complicated, cause power consumption high.
Summary of the invention
The object of this invention is to provide a kind of method, the method can be converted into the sodium hydroxide solution of reusable edible by the absorbing liquid that produces of wet desulfurizing and dust collecting system, and the sulfuric acid solution of recoverable and SO
2, substantially realize no effuent discharge, and power consumption can be reduced significantly.
The present inventor finds, by absorbing liquid is passed through two compartment bipolar membrane electrodialysis devices, desorber and three compartment bipolar membrane electrodialysis devices successively, can effectively reclaim absorbing liquid and reduce power consumption, resulting in the present invention.
To achieve these goals, the invention provides a kind of fume desulphurization method, this fume desulphurization method comprises the steps: that flue gas contacts in absorption tower with absorbent by (a), obtains the flue gas after desulfurization and absorbing liquid; Described absorbent is alkaline aqueous solution; B described absorbing liquid passes in two compartment bipolar membrane electrodialysis devices and carries out the first electrodialysis by (), obtain the first alkali lye and the first saline solution, or obtain the second saline solution and the first acid solution; C described first saline solution or the first acid solution pass in desorber and carry out desorb by (), obtain stripping liquid and SO
2rich gas; D described stripping liquid passes in three compartment bipolar membrane electrodialysis devices and carries out the second electrodialysis by (), obtain the second acid solution, the 3rd saline solution and the second alkali lye; Wherein, using described first alkali lye, described second saline solution and at least one reuse in the second alkali lye partly or entirely contacting with flue gas as absorbent to absorption tower.
By technique scheme, the present invention can realize no effuent discharge substantially, effectively reclaims absorbing liquid and reduces power consumption.
Other features and advantages of the present invention are described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and forms a part for description, is used from explanation the present invention, but is not construed as limiting the invention with detailed description of the invention one below.In the accompanying drawings:
Fig. 1 is flue gas desulfur device structural representation used in a kind of preferred embodiment of the present invention.
Fig. 2 is the structural representation of two compartment bipolar membrane electrodialysis devices used in a kind of preferred embodiment of the present invention.
Fig. 3 is flue gas desulfur device structural representation used in a kind of preferred embodiment of the present invention.
Fig. 4 is the structural representation of two compartment bipolar membrane electrodialysis devices used in a kind of preferred embodiment of the present invention.
Fig. 5 is the structural representation of three compartment bipolar membrane electrodialysis devices used in a kind of preferred embodiment of the present invention.
Description of reference numerals
1 absorption tower 2 solid-liquid separator
3 two compartment bipolar membrane electrodialysis device 4 desorbers
5 three compartment bipolar membrane electrodialysis device 6 absorbing liquid circulating pumps
7 filter 8 liquid drop separators
11 smoke inlet 12 exhanst gas outlets
31 first salt room, alkali rooms 32 first
33 second sour room, salt rooms 34 first
51 second salt room, sour rooms 52 the 3rd
53 second alkali rooms
101 first negative electrode 102 first Bipolar Membrane
103 first cation-exchange membrane 104 second Bipolar Membrane
105 first anode 106 first salt room outlets
107 first salt chamber inlet 108 first alkali chamber inlets
109 first alkali rooms export 113 cation-exchange membranes
114 Bipolar Membrane 130 first pole films
131 second pole film 136 first sour room outlets
137 first sour chamber inlet 138 second salt chamber inlets
139 second salt room outlet 140 first anion-exchange membranes
201 second negative electrode 202 the 3rd Bipolar Membrane
203 second cation-exchange membrane 204 second anion-exchange membranes
205 the 4th Bipolar Membrane 206 second plates
207 second alkali room outlet 208 second sour room outlets
209 the 3rd salt room outlet 210 the 3rd salt chamber inlets
211 second sour chamber inlet 212 second alkali chamber inlets
223 cation-exchange membrane 224 anion-exchange membranes
225 Bipolar Membrane 230 the 3rd pole film
231 the 4th pole films
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.Should be understood that, detailed description of the invention described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
With reference to figure 1, Fig. 2, Fig. 3, Fig. 4 and Fig. 5, the invention provides a kind of fume desulphurization method, the method may be used for the desulfurization process of various sulfur-containing smoke gas in chemical field, and described flue gas includes but not limited to the flue gas produced by chemical industry equipments such as boiler, industrial furnace, thermal power plant, coke oven, cement plant, blast furnace, open hearth, converter, electric furnace and catalytic cracking (FCC) devices.In described flue gas, by volume, the content of sulfur dioxide can be 500-3000ppm.
According to fume desulphurization method provided by the invention, this fume desulphurization method comprises the steps: that flue gas contacts in absorption tower 1 with absorbent by (a), obtains the flue gas after desulfurization and absorbing liquid; Described absorbent is alkaline aqueous solution; B described absorbing liquid passes in two compartment bipolar membrane electrodialysis devices 3 and carries out the first electrodialysis by (), obtain the first alkali lye and the first saline solution, or obtain the second saline solution and the first acid solution; C described first saline solution or the first acid solution pass in desorber 4 and carry out desorb by (), obtain stripping liquid and SO
2rich gas; D described stripping liquid passes in three compartment bipolar membrane electrodialysis devices 5 and carries out the second electrodialysis by (), obtain the second acid solution, the 3rd saline solution and the second alkali lye; Wherein, using partly or entirely contacting with flue gas as absorbent in described first alkali lye, described second saline solution and at least one reuse in the second alkali lye to absorption tower 1.
Wherein, flue gas can enter absorption tower 1 through the smoke inlet 11 on absorption tower 1, contacts in absorption tower 1 with absorbent, to obtain desulfurization process, then discharges absorption tower 1 through exhanst gas outlet 12.Wherein, described desulfurization process can be carried out separately in absorption tower 1, also can carry out with the process of denitration and/or dedusting simultaneously.
Wherein, the not special requirement of type on described absorption tower 1, as long as the contact of flue gas and absorbent can be completed, include but not limited at least one in plate column, bubble absorbing tower, stirring bubble absorbing tower, injector, Venturi tube, spray tower, packed absorber and film-falling absorption tower.Wherein, preferably, desorber 4 can be vacuum column.
Wherein, described absorbent is pH value is the alkaline aqueous solution, and its pH value can be more than 8.Described absorbent can carry out dissolved sulfur dioxide by water, and described absorbent can also by the uptake of alkaline active ingredient increase to sulfur dioxide.Described alkaline active ingredient includes but not limited to NaOH, Na
2sO
3, at least one in ammoniacal liquor and water-soluble organic amine.
Wherein, described absorbent can for the NaOH aqueous solution contained; Or described absorbent can also for containing Na
2sO
3the aqueous solution; Or described absorbent can be not only containing NaOH but also containing Na
2sO
3the aqueous solution.Described absorbent is entering behind absorption tower 1 and smoke contacts, and the oxysulfide in flue gas is absorbed by absorbent, and the absorbent after contact is converted into absorbing liquid and discharges through absorbing liquid outlet.Containing NaHSO in the absorbing liquid of discharging
3, Na
2sO
3and Na
2sO
4, by the recycling of absorbing liquid recovery system, be converted into absorbent and recycled.Wherein, two compartment bipolar membrane electrodialysis devices 3 may be used for the NaHSO in the absorbing liquid of discharge
3and Na
2sO
3be separated into NaOH and H
2sO
3.Two compartment bipolar membrane electrodialysis devices 3 also may be used for the NaHSO in the absorbing liquid of discharge
3be separated into NaOH and Na
2sO
3mixture and H
2sO
3.Desorber 4 may be used for the H discharged by two compartment bipolar membrane electrodialysis devices 3
2sO
3with SO
2formal solution suction go out.Desorber 4 can also be used for the H discharged by two compartment bipolar membrane electrodialysis devices 3
2sO
3with SO
2formal solution suction go out, and to discharge containing Na simultaneously
2sO
4material.Three compartment bipolar membrane electrodialysis devices 5 may be used for desorber 4 to discharge containing Na
2sO
4material electrolytic separation be NaOH and H
2sO
4.The outlet of the NaOH of two compartment bipolar membrane electrodialysis device 3 electrolytic separation can be connected with the absorbent entrance on absorption tower 1 with the outlet of NaOH of three compartment bipolar membrane electrodialysis device 5 electrolytic separation, the NaOH of electrolytic separation recovery to be used for the desulfurization process in absorption tower 1 as absorbent.
Preferably, described two compartment bipolar membrane electrodialysis devices 3 have at least one group of two compartment bipolar membrane electrodialysis films pair be arranged between the first negative electrode 101 and the first anode 105, described two compartment bipolar membrane electrodialysis films are to comprising the first Bipolar Membrane 102, first cation-exchange membrane 103 and the second Bipolar Membrane 104, formed between first Bipolar Membrane 102 and the first cation-exchange membrane 103 between first alkali room 31, second Bipolar Membrane 104 and the first cation-exchange membrane 103 and form the first salt room 32; The first electrodialysis is carried out in the first salt room 32 passed into by described absorbing liquid in two compartment bipolar membrane electrodialysis devices 3, obtains the first alkali lye, in described first salt room 32, obtain the first saline solution in the first alkali room 31.
Wherein, the first salt room 32 can have at least one first salt chamber inlet 107 and at least one the first salt room outlet 106.First salt chamber inlet 107 can export with the absorbing liquid on absorption tower 1 and be connected.The absorbing liquid of discharging on absorption tower 1 can be imported through the first salt chamber inlet 107.First alkali room 31 can have at least one first alkali chamber inlet 108 and at least one the first alkali room outlet 109.Drive to import water through the first alkali chamber inlet 108 when enabling at device.Under the effect of the electric field formed at the first negative electrode 101 and the first anode 105, OH in the first alkali room 31
-ion enrichment, H in the first salt room 32
+ion enrichment, the Na in the first salt room 32
+ion enters the first alkali room 31 and and OH through the first cation-exchange membrane 103
-ion forms the NaOH aqueous solution, and the NaOH aqueous solution of formation is derived through the first alkali room outlet 109.First alkali room outlet 109 can be connected with the absorbent entrance on absorption tower 1.The NaOH aqueous solution that first alkali room outlet 109 is derived can be used for the desulfurization process in absorption tower 1 as absorbent.HSO in first salt room 32
3 -and SO
3 2-with H
+ion forms H
2sO
3, can with Na
2sO
4together, discharged by the first salt room outlet 106.First salt room outlet 106 can be connected with the stripping liquid entrance of desorber 4.That is discharged by the first salt room outlet 106 contains H
2sO
3and Na
2sO
4material obtain desorb at desorber 4, release SO
2.Desorber 4 have gas vent and liquid outlet.The SO discharged after desorb
2discharge through gas vent.The SO discharged
2may be used for preparing sulphur.The SO of release
2the liquid outlet of rear remaining material on desorber 4 is discharged.Release SO
2rear remaining material main component is Na
2sO
4the aqueous solution.
Wherein, described two compartment bipolar membrane electrodialysis devices 3 can have the many groups of two compartment bipolar membrane electrodialysis films pair be arranged between the first negative electrode 101 and the first anode 105; And adjacent two group of two compartment bipolar membrane electrodialysis film centering, right the second Bipolar Membrane of last group of two compartment bipolar membrane electrodialysis film is as right the first Bipolar Membrane of rear one group of two compartment bipolar membrane electrodialysis film.Such as, two bipolar membrane electrodialysis films pair as shown in Figure 2, bipolar membrane electrodialysis film on the left of Fig. 2 is to comprising the first Bipolar Membrane 102, first cation-exchange membrane 103 and the second Bipolar Membrane 104, formed between first Bipolar Membrane 102 and the first cation-exchange membrane 103 between first alkali room 31, second Bipolar Membrane 104 and the first cation-exchange membrane 103 and form the first salt room 32; Bipolar membrane electrodialysis film on the right side of Fig. 2 is to comprising the second Bipolar Membrane 104, cation-exchange membrane 113 and Bipolar Membrane 114, form another the first alkali room 31 between second Bipolar Membrane 104 and cation-exchange membrane 113, between Bipolar Membrane 114 and cation-exchange membrane 113, form another the first salt room 32.
Wherein, room, pole can be formed between the first negative electrode 101 and the first pole film 130, between the first anode 105 and the second pole film 131, also can form room, pole.Containing pole liquid in room, pole.Such as pole liquid can for containing Na
2sO
4the aqueous solution (concentration can be 2-3 about % by weight).Wherein, the first pole film 130 and two compartment bipolar membrane electrodialysis films between (such as between the first pole film 130 and the first Bipolar Membrane 102) another the first salt room 32 can be formed.Wherein, the second pole film 131 and two compartment bipolar membrane electrodialysis films between (such as between the second pole film 131 and Bipolar Membrane 114) another one first alkali room 31 can be formed.
Preferably, with reference to figure 3 and Fig. 4, described two compartment bipolar membrane electrodialysis devices 3 have at least one group of two compartment bipolar membrane electrodialysis films pair be arranged between the first negative electrode 101 and the first anode 105, described two compartment bipolar membrane electrodialysis films are to comprising the first Bipolar Membrane 102, first anion-exchange membrane 140 and the second Bipolar Membrane 104, formed between first Bipolar Membrane 102 and the first anion-exchange membrane 140 between second salt room 33, second Bipolar Membrane 104 and the first anion-exchange membrane 140 and form the first sour room 34; The first electrodialysis is carried out in the second salt room 33 passed into by described absorbing liquid in two compartment bipolar membrane electrodialysis devices 3, in described second salt room 33, obtain the second saline solution, in described first sour room 34, obtain the first acid solution.
Wherein, the second salt chamber inlet 138 can export with the absorbing liquid on absorption tower 1 and be connected.The absorbing liquid of discharging on absorption tower 1 can be imported through the second salt chamber inlet 138.Second salt room 33 is provided with at least one second saline solution outlet, the second saline solution outlet can be the second salt room outlet 139.When electric dialyzator starts, Na can be imported through the first sour chamber inlet 137
2sO
4the aqueous solution, also can import water through the first sour chamber inlet 137.Under the effect of the electric field formed at the first negative electrode 101 and the first anode 105, OH in the second salt room 33
-ion enrichment, H in the first sour room 34
+, HSO
3 -and SO
3 2-ion enrichment, the NaHSO in the second salt room 33
3and OH
-ion forms Na
2sO
3the aqueous solution, the Na of formation
2sO
3the aqueous solution and NaOH solution export 139 through the second salt room to be derived.Second salt room outlet 139 can be connected with the absorbent entrance on absorption tower 1.What the second salt room outlet 139 was derived contains Na
2sO
3the desulfurization process in absorption tower 1 can be back to the aqueous solution of NaOH.HSO in first sour room 34
3 -and SO
3 2-with H
+ion forms H
2sO
3, with Na
2sO
4together, discharged by the first sour room outlet 136.First sour room outlet 136 can be connected with the stripping liquid entrance of desorber 4.That is discharged by the first sour room outlet 136 contains H
2sO
3material obtain desorb at desorber 4, release SO
2.Desorber 4 have gas vent and liquid outlet.The SO discharged after desorb
2discharge through gas vent.The SO discharged
2may be used for preparing sulphur.The SO of release
2the liquid outlet of rear remaining material on desorber 4 is discharged.Release SO
2rear remaining material main component is for containing Na
2sO
4and H
2sO
4the aqueous solution.
Wherein, described two compartment bipolar membrane electrodialysis devices 3 can have the many groups of two compartment bipolar membrane electrodialysis films pair be arranged between the first negative electrode 101 and the first anode 105; And adjacent two group of two compartment bipolar membrane electrodialysis film centering, right the second Bipolar Membrane of last group of two compartment bipolar membrane electrodialysis film is as right the first Bipolar Membrane of rear one group of two compartment bipolar membrane electrodialysis film.Such as, two bipolar membrane electrodialysis films pair as shown in Figure 4, bipolar membrane electrodialysis film on the left of Fig. 4 is to comprising the first Bipolar Membrane 102, first anion-exchange membrane 140 and the second Bipolar Membrane 104, formed between first Bipolar Membrane 102 and the first anion-exchange membrane 140 between second salt room 33, second Bipolar Membrane 104 and the first anion-exchange membrane 140 and form the first sour room 34; Bipolar membrane electrodialysis film on the right side of Fig. 4 is to comprising the second Bipolar Membrane 104, anion-exchange membrane 141 and Bipolar Membrane 114, form another the second salt room 33 between second Bipolar Membrane 104 and anion-exchange membrane 141, between Bipolar Membrane 114 and anion-exchange membrane 141, form another the first sour room 34.
Wherein, room, pole can be formed between the first negative electrode 101 and the first pole film 130, between the first anode 105 and the second pole film 131, also can form room, pole.Containing pole liquid in room, pole.The effect of polar region provides direct current to bipolar membrane electrodialysis device exactly.Such as pole liquid can for containing Na
2sO
4the aqueous solution.Wherein, the first pole film 130 and two compartment bipolar membrane electrodialysis films between (such as between the first pole film 130 and the first Bipolar Membrane 102) another the first sour room 34 can be formed.Wherein, the second pole film 131 and two compartment bipolar membrane electrodialysis films between (such as between the second pole film 131 and Bipolar Membrane 114) another one second salt room 33 can be formed.
Preferably, with reference to figure 5, described three compartment bipolar membrane electrodialysis devices (5) have at least one group of three compartment bipolar membrane electrodialysis films pair be arranged between the second negative electrode (201) and second plate (206), described three compartment bipolar membrane electrodialysis films are to comprising the 3rd Bipolar Membrane (202), second cation-exchange membrane (203), second anion-exchange membrane (204) and the 4th Bipolar Membrane (205), the second alkali room (53) is formed between 3rd Bipolar Membrane and the second cation-exchange membrane (203), the 3rd salt room (52) is formed between second cation-exchange membrane (203) and anion-exchange membrane (204), the second sour room (51) is formed between second anion-exchange membrane (204) and the 4th Bipolar Membrane (205), the second electrodialysis is carried out in the 3rd salt room (52) passed into by described stripping liquid in three compartment bipolar membrane electrodialysis devices (5), the second acid solution is obtained in the second sour room (51), in the 3rd salt room (52), obtain the 3rd saline solution, in the second alkali room (53), obtain the second alkali lye.
Wherein, the 3rd salt chamber inlet 210 can be connected with the liquid outlet of desorber 4.The main component importing desorber 4 discharge through the 3rd salt chamber inlet 210 is Na
2sO
4the material of the aqueous solution.When device is driven, water can be imported through the second alkali chamber inlet 212 and the second sour chamber inlet 211.Under the effect of the electric field formed at the second negative electrode 201 and second plate 206, OH in the second alkali room 53
-ion enrichment, H in the second sour room 51
+ion enrichment, the Na in the 3rd salt room 52
+ion enters the second alkali room 53 and and OH
-ion forms the NaOH aqueous solution, and the NaOH aqueous solution of formation is derived through the second alkali room outlet 207.Second alkali room outlet 207 can be connected with the absorbent entrance on absorption tower 1.The NaOH aqueous solution that second alkali room outlet 207 is derived can be used for the desulfurization process in absorption tower 1 as absorbent.SO in 3rd salt room 52
4 2-enter the second sour room 51 and and H
+ion forms H
2sO
4, discharged by the second sour room outlet 208.3rd salt room 52 has the second salt room outlet 209, can be used for discharge the 3rd saline solution.
Wherein, described three compartment bipolar membrane electrodialysis devices 5 can have the many groups of three compartment bipolar membrane electrodialysis films pair be arranged between the second negative electrode 201 and second plate 206; And adjacent two group of three compartment bipolar membrane electrodialysis film centering, right the 4th Bipolar Membrane of last group of three compartment bipolar membrane electrodialysis film is as right the 3rd Bipolar Membrane of rear one group of three compartment bipolar membrane electrodialysis film.Such as, two bipolar membrane electrodialysis films pair as shown in Figure 5, bipolar membrane electrodialysis film on the left of Fig. 5 is to comprising the 3rd Bipolar Membrane 202, second cation-exchange membrane 203, second anion-exchange membrane 204 and the 4th Bipolar Membrane 205, the second alkali room 53 is formed between 3rd Bipolar Membrane and the second cation-exchange membrane 203, formed between second cation-exchange membrane 203 and anion-exchange membrane 204 between the 3rd salt room 52, second anion-exchange membrane 204 and the 4th Bipolar Membrane 205 and form the second sour room 51; Bipolar membrane electrodialysis film on the right side of Fig. 5 is to comprising the 4th Bipolar Membrane 205, cation-exchange membrane 223, anion-exchange membrane 224 and Bipolar Membrane 225, the second alkali room 53 is formed between 4th Bipolar Membrane 205 and cation-exchange membrane 223, form the 3rd salt room 52 between cation-exchange membrane 223 and anion-exchange membrane 224, between anion-exchange membrane 224 and Bipolar Membrane 225, form the second sour room 51.
Wherein, described second alkali room 53 can be provided with at least one second alkali lye outlet; Described second sour room 51 can be provided with at least one second acid solution outlet; Described second alkali lye outlet is connected with the absorbent entrance on absorption tower 1.As shown in Figure 5, the second alkali lye outlet can be the second alkali room outlet 207, second acid solution outlet can be the second sour room outlet 208.
Wherein, between the second negative electrode 201 and the 3rd pole film 230, room, pole can be formed, between second plate 206 and the 4th pole film 231, also can form room, pole.Pole liquid can be contained in room, pole.Such as pole liquid can contain Na
2sO
4the aqueous solution.Wherein, the 3rd pole film 230 and three compartment bipolar membrane electrodialysis films between (such as between the 3rd pole film 230 and the 3rd Bipolar Membrane 202) another the second sour room 51 can be formed.Wherein, the 4th pole film 231 and three compartment bipolar membrane electrodialysis films between (such as between the 4th pole film 231 and Bipolar Membrane 225) another one second alkali room 53 can be formed.
Preferably, the absorbing liquid on described absorption tower 1 exports and be also connected with absorbing liquid circulating pump 6 between the entrance of described absorbing liquid recovery system.The absorbing liquid that absorption tower 1 can be discharged by absorbing liquid circulating pump 6 absorbs liquid pump to absorption tower 1 and/or absorbing liquid recovery system.
Preferably, solid-liquid separator 2 is also connected with between the entrance of described absorbing liquid circulating pump 6 and described absorbing liquid recovery system, the absorbing liquid outlet on described absorption tower 1 is connected with the entrance of absorbing liquid circulating pump 6, and the outlet of described absorbing liquid circulating pump 6 is connected with the entrance of described solid-liquid separator 2 with the circulating absorption solution entrance on described absorption tower 1; The purified liquor outlet of described solid-liquid separator 2 is connected with the entrance of described absorbing liquid recovery system with the absorbing liquid entrance on described absorption tower 1.The solid constituent that described solid-liquid separator 2 comes in separate absorbent liquid can be used.Wherein, described solid-liquid separator 2 can be settling vessel and/or filter.
Preferably, the exhanst gas outlet on described absorption tower 1 is also provided with filter 7 and/or liquid drop separator 8.Described filter 7 can be used to the dust in the flue gas removing absorption tower 1 discharge.Described liquid drop separator 8 can be used to remove the drop carried secretly in the flue gas of absorption tower 1 discharge.
Wherein, under preferable case, described absorbent contains NaOH and/or Na
2sO
3; By controlling the flow of flue gas and the flow of absorbent, make NaHSO in absorbing liquid
3with Na
2sO
3mol ratio be (0.1-100): 1, be more preferably (1-30): 1.Wherein, in theory, the NaOH of 1 mole can absorb the SO of 1 mole
2obtain the NaHSO of 1 mole
3; The NaOH of 2 moles can absorb the SO of 1 mole
2obtain the Na of 1 mole
2sO
3; The Na of 1 mole
2sO
3the SO of 1 mole can be absorbed
2obtain the NaHSO of 2 moles
3.Such as, in FCC flue gas by volume the content of sulfur dioxide be the flue gas of 700-900ppm, when using the aqueous solution of NaOH of 8-12mol/L as absorbent, the flow controlling flue gas is (40-100) ten thousand m
3/ h, the flow of absorbent is 1-20m
3/ h, NaHSO in the absorbing liquid obtained
3with Na
2sO
3mol ratio be (7-9): 1.
Wherein, under preferable case, described absorbent contains NaOH and/or Na
2sO
3; In described absorbent, the content of sodium ion is 0.2-20mol/L, is preferably 5-15mol/L.Wherein, in described absorbent, the source of sodium ion can be NaOH and/or Na
2sO
3.In the present invention, the content of the sodium ion in described absorbent can keep relative constancy.
Wherein, under preferable case, described absorbent contains NaOH and/or Na
2sO
3; When two compartment bipolar membrane electrodialysis devices 3 have first cation-exchange membrane 103, by controlling voltage in two compartment bipolar membrane electrodialysis devices 3 and/or electrodialysis time, the pH value of the first alkali lye is made to be more than 8, preferably more than 10.Wherein, can voltage substantial constant in maintenance two compartment bipolar membrane electrodialysis device 3, by regulating the electrodialysis time, make the pH value of the first alkali lye be more than 8, preferably more than 10.Such as, in FCC flue gas by volume the content of sulfur dioxide be the flue gas of 700-900ppm, when using the aqueous solution of NaOH of 8-12mol/L as absorbent, the flow controlling flue gas is (40-60) ten thousand m
3/ h, the flow of absorbent is 3-10m
3/ h, NaHSO in the absorbing liquid obtained
3with Na
2sO
3mol ratio be (7-9): 1; Each organizes two compartment bipolar membrane electrodialysis films when being 2-3V to the voltage of upper applying, and the electrodialysis time is 5-60min, and the pH value of the first alkali lye is 10.0-13.5.
Wherein, under preferable case, described absorbent contains NaOH and/or Na
2sO
3; When two compartment bipolar membrane electrodialysis devices 3 comprise first anion-exchange membrane 140, by controlling voltage in two compartment bipolar membrane electrodialysis devices 3 and/or electrodialysis time, the pH value of the second saline solution is made to be more than 8, preferably more than 10.Wherein, can voltage substantial constant in maintenance two compartment bipolar membrane electrodialysis device 3, by regulating the electrodialysis time, make the pH value of the first alkali lye be more than 8, preferably more than 10.Such as, in FCC flue gas by volume the content of sulfur dioxide be the flue gas of 700-900ppm, when using the aqueous solution of NaOH of 8-12mol/L as absorbent, the flow controlling flue gas is (40-60) ten thousand m
3/ h, the flow of absorbent is 3-10m
3/ h, NaHSO in the absorbing liquid obtained
3with Na
2sO
3mol ratio be (7-9): 1; In two compartment bipolar membrane electrodialysis devices 3, each organizes two compartment bipolar membrane electrodialysis films when being 2-3V to the voltage of upper applying, and the electrodialysis time is 5-60min, and the pH value of the second saline solution is 10.0-13.5.
Wherein, under preferable case, described absorbent contains NaOH and/or Na
2sO
3; The condition of desorb makes the H in stripping liquid
2sO
3content be 0.01-0.4mol/L, SO
2sO in rich gas
2content is 95-99.9 volume %.Wherein, desorber can be vacuum column.Such as, when two compartment bipolar membrane electrodialysis devices 3 have first cation-exchange membrane 103, H in the first saline solution
2sO
3content be 0.5-1.25mol/L, the tower top temperature of desorb can be 0-100 DEG C, and column bottom temperature can be 0-100 DEG C, and feeding temperature can be 20-35 DEG C, the H in the stripping liquid obtained under this desorption condition
2sO
3content be 0.01-0.04mol/L, SO
2sO in rich gas
2content is 95-97 volume %.Such as, when two compartment bipolar membrane electrodialysis devices 3 have first anion-exchange membrane 140, H in the first acid solution
2sO
3content be 0.5-1.25mol/L, the tower top temperature of desorb can be 0-100 DEG C, and column bottom temperature can be 0-100 DEG C, and feeding temperature can be 20-35 DEG C, and the tower top pressure of vacuum stripper is 0.01-1Pa, the H in the stripping liquid obtained under this desorption condition
2sO
3content be 0.01-0.04mol/L, SO
2sO in rich gas
2content is 95-97 volume %.The SO that desorb obtains
2rich gas may be used for preparing sulphur or sulfuric acid.
Preferably, by controlling voltage in three compartment bipolar membrane electrodialysis devices 5 and/or electrodialysis time, the pH value of the second alkali lye is made to be more than 8, preferably more than 10.Wherein, can voltage substantial constant in maintenance three compartment bipolar membrane electrodialysis device 5, by regulating the electrodialysis time, make the pH value of the second alkali lye be more than 8, preferably more than 10.
Preferably, fume desulphurization method of the present invention also comprise by the 3rd saline solution reclaim be used in two compartment bipolar membrane electrodialysis devices 3 and three compartment bipolar membrane electrodialysis devices 5.3rd saline solution can import the first alkali room 31 by the first alkali chamber inlet 108.3rd saline solution also can lead to the first sour chamber inlet 137 and import the first sour room 34.3rd saline solution also can lead to the first sour chamber inlet 137 and import the first sour room 34.3rd saline solution can also import the second alkali room 53 through the second alkali chamber inlet 212.3rd saline solution can also import the second sour room 51 through the second sour chamber inlet 211.Under this preferable case, the water consumption of fume desulphurization method can be reduced further.
In the present invention, described absorbent is the aqueous solution, and containing NaOH, Na
2sO
3, at least one in ammoniacal liquor and water-soluble organic amine.Preferably, described absorbent is the aqueous solution, and containing NaOH and/or Na
2sO
3.As another embodiment of the invention, described absorbent is the aqueous solution, and containing ammoniacal liquor; Wherein, the concentration of ammoniacal liquor can be 1-10 % by weight.As another embodiment of the invention, described absorbent is the aqueous solution, and containing water-soluble organic amine; Wherein, the concentration of water-soluble organic amine can be 1-50 % by weight.Wherein, water-soluble organic amine can include but not limited at least one in trimethylamine, triethylamine, ethylenediamine and dimethyl formamide.
In the present invention, two compartment bipolar membrane electrodialysis films all can obtain by buying commercial film product with the Bipolar Membrane of three compartment bipolar membrane electrodialysis film centerings, cation-exchange membrane and anion-exchange membrane.Such as can buy from Zhejiang Qianqiu Environmental Water Treatment Co., Ltd. and obtain.
Further describe the present invention by the following examples.In following examples, use the gaseous mixture of nitrogen and sulfur dioxide to test as the flue gas of simulation, in this gaseous mixture, by volume, the content of FCC sulfur dioxide in flue gas is 800ppm.
Embodiment 1
With reference to figure 1, Fig. 2 and Fig. 5, the smoke inlet 11 of flue gas through absorption tower 1 enters absorption tower 1,
Contact with absorbent in absorption tower 1, to obtain desulfurization process, then discharge absorption tower 1 through exhanst gas outlet 12.At the initial period of fume treatment, absorbent is the NaOH of 1mol/L.Wherein, the flow controlling flue gas is 500,000 m
3/ h, the flow of absorbent is 4m
3/ h, NaHSO in the absorbing liquid obtained
3with Na
2sO
3mol ratio be 8:1.
The absorbing liquid of discharging on absorption tower 1 is imported through the first salt chamber inlet 107.At the initial period of fume treatment, import water through the first alkali chamber inlet 108.Under the effect of the electric field formed at the first negative electrode 101 and the first anode 105, OH in the first alkali room 31
-ion enrichment, H in the first salt room 32
+ion enrichment, the Na in the first salt room 32
+ion enters the first alkali room 31 and and OH through the first cation-exchange membrane 103
-ion forms the NaOH aqueous solution, and first alkali lye containing the NaOH aqueous solution of formation is derived through the first alkali room outlet 109.First alkali room outlet 109 is connected with the absorbent entrance on absorption tower 1.The first alkali lye that first alkali room outlet 109 is derived is used for the desulfurization process in absorption tower 1 as absorbent.HSO in first salt room 32
3 -and SO
3 2-with H
+ion forms H
2sO
3, obtain containing H
2sO
3the first saline solution, the first saline solution by first salt room outlet 106 discharge.Each in two compartment bipolar membrane electrodialysis devices 3 organizes two compartment bipolar membrane electrodialysis films when being 2.5V to the voltage of upper applying, and the electrodialysis time is 30min, and the pH value of the first alkali lye is 12.
First salt room outlet 106 is connected with the stripping liquid entrance of desorber 4.First saline solution of being discharged by the first salt room outlet 106 obtains desorb at desorber 4, release SO
2rich gas.Desorber 4 have gas vent and liquid outlet.The SO discharged after desorb
2rich gas is discharged through gas vent.The SO discharged
2for the preparation of sulphur.The SO of release
2rear remaining material is discharged as the liquid outlet of stripping liquid on desorber 4.The tower top temperature of desorb is 4 DEG C, and column bottom temperature is 95 DEG C, and feeding temperature is 30 DEG C, and the tower top pressure of vacuum stripper is 0.5Pa, the H in the stripping liquid obtained
2sO
3content be 0.03mol/L, SO
2sO in rich gas
2content is 95 volume %.
The stripping liquid of desorber 4 discharge is imported through the 3rd salt chamber inlet 210.At the initial period of fume treatment, import water through the second alkali chamber inlet 212 and the second sour chamber inlet 211.Under the effect of the electric field formed at the second negative electrode 201 and second plate 206, OH in the second alkali room 53
-ion enrichment, H in the second sour room 51
+ion enrichment, the Na in the 3rd salt room 52
+ion enters the second alkali room 53 and and OH
-ion forms the NaOH aqueous solution, and the second alkali lye formed containing the NaOH aqueous solution is derived through the second alkali room outlet 207.Second alkali room outlet 207 is connected with the absorbent entrance on absorption tower 1.Second alkali lye is used for the desulfurization process in absorption tower 1 as absorbent.SO in 3rd salt room 52
3 2-enter the second sour room 51 and and H
+ion forms H
2sO
3, discharged by the second sour room outlet 208.3rd salt room 52 has the second salt room outlet 209, for discharging the 3rd saline solution in the 3rd salt room, the 3rd saline solution is the remaining water reaching pollution emission standard of electrodialysis.When voltage substantial constant in maintenance three compartment bipolar membrane electrodialysis device 5, by regulating the electrodialysis time, the pH value of the second alkali lye is made to be 12.
In the present embodiment, process flue gas described in every kilostere, the electric energy that electrodialysis consumes is 5.7 kilowatt hours.
Embodiment 2
With reference to figure 3 Fig. 4 and Fig. 5, the smoke inlet 11 of flue gas through absorption tower 1 enters absorption tower 1, contacts in absorption tower 1 with absorbent, to obtain desulfurization process, then discharges absorption tower 1 through exhanst gas outlet 12.At the initial period of fume treatment, absorbent is the NaOH of 1mol/L.Wherein, the flow controlling flue gas is 500,000 m
3/ h, the flow of absorbent is 4m
3/ h, NaHSO in the absorbing liquid obtained
3with Na
2sO
3mol ratio be 8:1.
The absorbing liquid of discharging on absorption tower 1 is imported through the second salt chamber inlet 138.Second salt room 33 is provided with at least one second saline solution outlet, the second saline solution outlet is the second salt room outlet 139.When electrodialysis starts, import Na through the first sour chamber inlet 137
2sO
4the aqueous solution, also when electrodialysis starts, can import water through the first sour chamber inlet 137.Under the effect of the electric field formed at the first negative electrode 101 and the first anode 105, OH in the second salt room 33
-ion enrichment, H in the first sour room 34
+, HSO
3 -and SO
3 2-ion enrichment, forms the first acid solution, the NaHSO in the second salt room 33
3and OH
-ion forms Na
2sO
3the aqueous solution, is formed containing Na
2sO
3second saline solution of the aqueous solution and NaOH solution exports 139 through the second salt room is derived.Second salt room outlet 139 is connected with the absorbent entrance on absorption tower 1.The second saline solution that second salt room outlet 139 is derived is back to the desulfurization process in absorption tower 1.The first acid solution in first sour room 34, is discharged by the first sour room outlet 136.In two compartment bipolar membrane electrodialysis devices 3, each organizes two compartment bipolar membrane electrodialysis films when being 2.5V to the voltage of upper applying, and the electrodialysis time is 30min, and the pH value of the second saline solution is 12.5.
First sour room outlet 136 is connected with the stripping liquid entrance of desorber 4.First acid solution of being discharged by the first sour room outlet 136 obtains desorb at desorber 4, release SO
2rich gas.Desorber 4 have gas vent and liquid outlet.The SO discharged after desorb
2rich gas is discharged through gas vent.The SO discharged
2rich gas is for the preparation of sulphur.The SO of release
2rear remaining material is stripping liquid, and the liquid outlet on desorber 4 is discharged.The tower top temperature of desorb is 3 DEG C, and column bottom temperature is 97 DEG C, and feeding temperature is 30 DEG C, and the tower top pressure of vacuum stripper is 0.8Pa, the H in the stripping liquid obtained
2sO
3content be 0.03mol/L, SO
2sO in rich gas
2content is 95 volume %.
The stripping liquid of desorber 4 discharge is imported through the 3rd salt chamber inlet 210.At the initial period of fume treatment, import water through the second alkali chamber inlet 212 and the second sour chamber inlet 211.Under the effect of the electric field formed at the second negative electrode 201 and second plate 206, OH in the second alkali room 53
-ion enrichment, H in the second sour room 51
+ion enrichment, the Na in the 3rd salt room 52
+ion enters the second alkali room 53 and and OH
-ion forms the NaOH aqueous solution, and the second alkali lye formed containing the NaOH aqueous solution is derived through the second alkali room outlet 207.Second alkali room outlet 207 is connected with the absorbent entrance on absorption tower 1.Second alkali lye is used for the desulfurization process in absorption tower 1 as absorbent.SO in 3rd salt room 52
3 2-enter the second sour room 51 and and H
+ion forms H
2sO
3, discharged by the second sour room outlet 208.3rd salt room 52 has the second salt room outlet 209, for discharging the 3rd saline solution in the 3rd salt room, the 3rd saline solution is the remaining water reaching pollution emission standard of electrodialysis.3rd saline solution imports the first alkali room 31 by the first alkali chamber inlet 108.3rd saline solution also imports the second alkali room 53 through the second alkali chamber inlet 212.3rd saline solution also imports the second sour room 51 through the second sour chamber inlet 211.When voltage substantial constant in maintenance three compartment bipolar membrane electrodialysis device 5, by regulating the electrodialysis time, the pH value of the second alkali lye is made to be 12.5.
In the present embodiment, process every cubic metre of described flue gas, the electric energy that electrodialysis consumes is 4.6 kilowatt hours.
Comparative example 1
The smoke inlet 11 of flue gas through absorption tower 1 enters absorption tower 1, contacts in absorption tower 1 with absorbent, to obtain desulfurization process, then discharges absorption tower 1 through exhanst gas outlet 12.At the initial period of fume treatment, absorbent is the NaOH of 1mol/L.Wherein, the flow controlling flue gas is 500,000 m
3/ h, the flow of absorbent is 3m
3/ h, NaHSO in the absorbing liquid obtained
3with Na
2sO
3mol ratio be 8:1.
Air is passed into, to be oxidized Na in absorbing liquid
2sO
3for Na
2sO
4, obtain the absorbing liquid after being oxidized.
The absorbing liquid after oxidation is imported through the 3rd salt chamber inlet 210.At the initial period of fume treatment, import water through the second alkali chamber inlet 212 and the second sour chamber inlet 211.Under the effect of the electric field formed at the second negative electrode 201 and second plate 206, OH in the second alkali room 53
-ion enrichment, H in the second sour room 51
+ion enrichment, the Na in the 3rd salt room 52
+ion enters the second alkali room 53 and and OH
-ion forms the NaOH aqueous solution, and the second alkali lye formed containing the NaOH aqueous solution is derived through the second alkali room outlet 207.Second alkali room outlet 207 is connected with the absorbent entrance on absorption tower 1.Second alkali lye is used for the desulfurization process in absorption tower 1 as absorbent.SO in 3rd salt room 52
4 2-enter the second sour room 51 and and H
+ion forms H
2sO
4, discharged by the second sour room outlet 208.3rd salt room 52 has the second salt room outlet 209, for discharging the 3rd saline solution in the 3rd salt room, the 3rd saline solution is the remaining water reaching pollution emission standard of electrodialysis.
In this comparative example, process every cubic metre of described flue gas, the electric energy that electrodialysis consumes is 8.5 kilowatt hours.
Below the preferred embodiment of the present invention is described in detail by reference to the accompanying drawings; but; the present invention is not limited to the detail in above-mentioned embodiment; within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each concrete technical characteristic described in above-mentioned detailed description of the invention, in reconcilable situation, can be combined by any suitable mode, in order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible combination.
In addition, also can be combined between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (10)
1. a fume desulphurization method, is characterized in that: this fume desulphurization method comprises the steps:
A flue gas contacts in absorption tower (1) with absorbent by (), obtain the flue gas after desulfurization and absorbing liquid; Described absorbent is alkaline aqueous solution;
B described absorbing liquid passes in two compartment bipolar membrane electrodialysis devices (3) and carries out the first electrodialysis by (), obtain the first alkali lye and the first saline solution, or obtain the second saline solution and the first acid solution;
C described first saline solution or the first acid solution pass in desorber (4) and carry out desorb by (), obtain stripping liquid and SO
2rich gas;
D described stripping liquid passes in three compartment bipolar membrane electrodialysis devices (5) and carries out the second electrodialysis by (), obtain the second acid solution, the 3rd saline solution and the second alkali lye;
Wherein, using partly or entirely contacting with flue gas as absorbent in described first alkali lye, described second saline solution and at least one reuse in the second alkali lye to absorption tower (1).
2. fume desulphurization method according to claim 1, it is characterized in that: described two compartment bipolar membrane electrodialysis devices (3) have at least one group of two compartment bipolar membrane electrodialysis films pair be arranged between the first negative electrode (101) and the first anode (105), described two compartment bipolar membrane electrodialysis films are to comprising the first Bipolar Membrane (102), first cation-exchange membrane (103) and the second Bipolar Membrane (104), the first alkali room (31) is formed between first Bipolar Membrane (102) and the first cation-exchange membrane (103), the first salt room (32) is formed between second Bipolar Membrane (104) and the first cation-exchange membrane (103),
The first electrodialysis is carried out in the first salt room (32) passed into by described absorbing liquid in two compartment bipolar membrane electrodialysis devices (3), in the first alkali room (31), obtain the first alkali lye, in described first salt room (32), obtain the first saline solution.
3. fume desulphurization method according to claim 1, it is characterized in that: described two compartment bipolar membrane electrodialysis devices (3) have at least one group of two compartment bipolar membrane electrodialysis films pair be arranged between the first negative electrode (101) and the first anode (105), described two compartment bipolar membrane electrodialysis films are to comprising the first Bipolar Membrane (102), first anion-exchange membrane (140) and the second Bipolar Membrane (104), the second salt room (33) is formed between first Bipolar Membrane (102) and the first anion-exchange membrane (140), the first sour room (34) is formed between second Bipolar Membrane (104) and the first anion-exchange membrane (140),
The first electrodialysis is carried out in the second salt room (33) passed into by described absorbing liquid in two compartment bipolar membrane electrodialysis devices (3), in described second salt room (33), obtain the second saline solution, in described first sour room (34), obtain the first acid solution.
4. fume desulphurization method according to claim 1, it is characterized in that: described three compartment bipolar membrane electrodialysis devices (5) have at least one group of three compartment bipolar membrane electrodialysis films pair be arranged between the second negative electrode (201) and second plate (206), described three compartment bipolar membrane electrodialysis films are to comprising the 3rd Bipolar Membrane (202), second cation-exchange membrane (203), second anion-exchange membrane (204) and the 4th Bipolar Membrane (205), the second alkali room (53) is formed between 3rd Bipolar Membrane and the second cation-exchange membrane (203), the 3rd salt room (52) is formed between second cation-exchange membrane (203) and anion-exchange membrane (204), the second sour room (51) is formed between second anion-exchange membrane (204) and the 4th Bipolar Membrane (205),
The second electrodialysis is carried out in the 3rd salt room (52) passed into by described stripping liquid in three compartment bipolar membrane electrodialysis devices (5), the second acid solution is obtained in the second sour room (51), in the 3rd salt room (52), obtain the 3rd saline solution, in the second alkali room (53), obtain the second alkali lye.
5. according to the fume desulphurization method in claim 1-4 described in any one, it is characterized in that: described absorbent contains NaOH and/or Na
2sO
3; By controlling the flow of flue gas and the flow of absorbent, make NaHSO in absorbing liquid
3with Na
2sO
3mol ratio be (0.1-100): 1.
6. fume desulphurization method according to claim 5, is characterized in that: in described absorbent, the content of sodium ion is 0.2-20mol/L.
7. fume desulphurization method according to claim 2, is characterized in that: described absorbent contains NaOH and/or Na
2sO
3; By controlling voltage in two compartment bipolar membrane electrodialysis devices (3) and/or electrodialysis time, make the pH value of the first alkali lye higher than 8.
8. fume desulphurization method according to claim 3, is characterized in that: described absorbent contains NaOH and/or Na
2sO
3; By controlling voltage in two compartment bipolar membrane electrodialysis devices (3) and/or electrodialysis time, make the pH value of the second saline solution higher than 8.
9. fume desulphurization method according to claim 3, is characterized in that: described absorbent contains NaOH and/or Na
2sO
3; The condition of desorb makes the H in stripping liquid
2sO
3content be 0.01-0.04mol/L, SO
2sO in rich gas
2content is 95-99.9 volume %.
10. fume desulphurization method according to claim 1, is characterized in that: described absorbent contains NaOH and/or Na
2sO
3; By controlling voltage in three compartment bipolar membrane electrodialysis devices (5) and/or electrodialysis time, make the pH value of the second alkali lye higher than 8.
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| CN114788997A (en) * | 2022-04-14 | 2022-07-26 | 中国石油大学(北京) | Flue gas CO by chemical absorption method 2 Trapping system |
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Effective date of registration: 20170527 Address after: 414500 Hunan Province, Yueyang high tech Industrial Park Pingjiang County Innovation Park Kunyu Road No. 3 Patentee after: Hunan China Tianyuan Environmental Engineering Co., Ltd. Address before: 101407 Beijing city Huairou District Yan Xi Zhen Yan Xi Island 50 meters West Patentee before: Beijing Zhongtianyuan Environmental Engineering Co., Ltd. |