CN103432882A - Absorbent for separating sulfur dioxide in gas mixture - Google Patents
Absorbent for separating sulfur dioxide in gas mixture Download PDFInfo
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- CN103432882A CN103432882A CN2013102845559A CN201310284555A CN103432882A CN 103432882 A CN103432882 A CN 103432882A CN 2013102845559 A CN2013102845559 A CN 2013102845559A CN 201310284555 A CN201310284555 A CN 201310284555A CN 103432882 A CN103432882 A CN 103432882A
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- absorbent
- sulfur dioxide
- gas
- malate
- mixed gas
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- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 title claims abstract description 58
- 239000002250 absorbent Substances 0.000 title claims abstract description 42
- 230000002745 absorbent Effects 0.000 title claims abstract description 42
- 239000000203 mixture Substances 0.000 title abstract description 3
- 239000007864 aqueous solution Substances 0.000 claims abstract description 23
- 150000001412 amines Chemical class 0.000 claims abstract description 17
- 229940049920 malate Drugs 0.000 claims abstract description 12
- BJEPYKJPYRNKOW-UHFFFAOYSA-N malic acid Chemical compound OC(=O)C(O)CC(O)=O BJEPYKJPYRNKOW-UHFFFAOYSA-N 0.000 claims abstract description 12
- KEAYESYHFKHZAL-UHFFFAOYSA-N Sodium Chemical group [Na] KEAYESYHFKHZAL-UHFFFAOYSA-N 0.000 claims description 25
- SVICABYXKQIXBM-UHFFFAOYSA-L potassium malate Chemical compound [K+].[K+].[O-]C(=O)C(O)CC([O-])=O SVICABYXKQIXBM-UHFFFAOYSA-L 0.000 claims description 25
- 235000011033 potassium malate Nutrition 0.000 claims description 25
- 239000001415 potassium malate Substances 0.000 claims description 25
- ASUDFOJKTJLAIK-UHFFFAOYSA-N 2-methoxyethanamine Chemical compound COCCN ASUDFOJKTJLAIK-UHFFFAOYSA-N 0.000 claims description 11
- PIICEJLVQHRZGT-UHFFFAOYSA-N Ethylenediamine Chemical compound NCCN PIICEJLVQHRZGT-UHFFFAOYSA-N 0.000 claims description 11
- 238000002156 mixing Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 39
- 238000000034 method Methods 0.000 abstract description 38
- 238000006477 desulfuration reaction Methods 0.000 abstract description 23
- 239000012528 membrane Substances 0.000 abstract description 23
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 19
- 239000003546 flue gas Substances 0.000 abstract description 19
- 230000023556 desulfurization Effects 0.000 abstract description 17
- 239000007788 liquid Substances 0.000 abstract description 14
- 238000012546 transfer Methods 0.000 abstract description 11
- 238000010521 absorption reaction Methods 0.000 abstract description 9
- 239000002131 composite material Substances 0.000 abstract description 9
- 238000000926 separation method Methods 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 abstract description 2
- 239000003795 chemical substances by application Substances 0.000 description 16
- 230000003009 desulfurizing effect Effects 0.000 description 15
- 239000000243 solution Substances 0.000 description 12
- 238000011156 evaluation Methods 0.000 description 11
- QUSNBJAOOMFDIB-UHFFFAOYSA-N Ethylamine Chemical compound CCN QUSNBJAOOMFDIB-UHFFFAOYSA-N 0.000 description 8
- 239000008246 gaseous mixture Substances 0.000 description 8
- BPGIOCZAQDIBPI-UHFFFAOYSA-N 2-ethoxyethanamine Chemical compound CCOCCN BPGIOCZAQDIBPI-UHFFFAOYSA-N 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- -1 propoxyl group Chemical group 0.000 description 7
- 239000006096 absorbing agent Substances 0.000 description 6
- 238000003860 storage Methods 0.000 description 5
- 150000001875 compounds Chemical class 0.000 description 4
- 239000003517 fume Substances 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 230000036632 reaction speed Effects 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000000809 air pollutant Substances 0.000 description 2
- 231100001243 air pollutant Toxicity 0.000 description 2
- 230000004888 barrier function Effects 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000005272 metallurgy Methods 0.000 description 2
- 238000003908 quality control method Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003086 colorant Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000004567 concrete Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 150000007530 organic bases Chemical class 0.000 description 1
- 230000002572 peristaltic effect Effects 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000002798 spectrophotometry method Methods 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Images
Abstract
The invention relates to the field of liquid-gas separation, especially to the field of flue gas desulphurization, specifically to an absorbent for separating sulfur dioxide in a gas mixture. The objective of the invention is to provide a sulfur dioxide absorbent used for absorption of a membrane contactor. The absorbent is composed of malate and an aqueous solution of organic amine mixed according to a mol ratio of 1: 0.5-3. The absorbent, i.e., a composite desulfurizer, has the advantages of good chemical stability, small foamability, small viscosity and a wide source, easy purchasing and a low price of raw materials. A desulphurization process using the composite desulfurizer has the advantages of a high mass transfer coefficient, no disturbance during flowing of gas and liquid, small mass transfer resistance, a high desulfurization rate, convenience in operation, great operational flexibility, no secondary pollution and stable running in the membrane contactor.
Description
Technical field
The present invention relates to liquid gas separation field, particularly relate to the desulfuration field of flue gas, more specifically relate to the absorbent of sulfur dioxide in a kind of separating mixed gas.
Background technology
SO in the flue gas such as coal-burning power plant, metallurgy industry
2being one of Air Pollutant Discharge, is the formation source of acid rain.The raising day by day Air Pollutant Emission required along with environmental protection, in flue gas desulfurization purifies, reasonable selection sulfur removal technology how, reach SO after flue gas desulfurization with low investment and operating cost
2discharge capacity meets the regulation of discharging standards, is the key issue that the flue gas desulfurizations such as coal-burning power plant, metallurgy industry develop in a healthy way.Therefore, various high-performance SO
2the exploitation of absorbent is one of theme of this area research, and in recent years, composite absorber was because its unique performance has become the heat subject of acid gas absorbent research and development.
In flue gas desulfurization (Flue gas desulfurization is called for short FGD) technology, the method common by the kind of desulfurizing agent has: with CaCO
3(lime stone) is basic calcium method, take MgO as basic magnesium method, with Na
2sO
3for basic sodium method, with NH
3for basic ammonia process, take organic base as basic organic alkaline process.Commercialization flue gas desulfurization more than 90% adopts calcium method desulfur technology in the world, and the calcium method is divided into wet method, dry method and half-dried (half is wet) method.Wet technique is to adopt solution or the slurries contain absorbent to process sulfur-containing smoke gas, and this method has that desulphurization reaction speed is fast, equipment simple, the desulfuration efficiency advantages of higher, but the ubiquity seriously corroded, operation and maintenance cost is high and cause secondary pollution problems.Dry technique is that the processing of absorption process and product is all carried out under anhydrous state, this method have without spent acid sewage discharge, equipment corrosion is lighter, the problems such as flue-gas temperature is without the advantage such as obviously reducing, secondary pollution is few, but exists desulfuration efficiency low, and reaction speed is slow, equipment is huge.Semi-dry process refers to desulfurizing agent desulfurization under drying regime, regeneration under wet condition (as washing regenerating active carbon flow process), or desulfurization under wet condition, processes the flue gas desulfurization technique of desulfurization product (as spray drying process) under dry state.Particularly desulfurization under wet condition, process the semidry method of desulfurization product under dry state, with its advantage that existing wet desulphurization reaction speed is fast, desulfuration efficiency is high, have again dry method without the sewage spent acid discharge, the easy-to-handle advantage of desulfurization afterproduct and be subject to people and pay close attention to widely.In chemical absorbing flue gas desulfurization, the performance of absorbent has fundamentally determined SO
2the efficiency of absorption operation, thereby the performance of absorbent is had to very high requirement.Carry out chemical absorbing SO for flue gas
2process, in order to strengthen mass transport process, improve desulfuration efficiency, reduce investment and the operating cost of equipment, also must possess certain requirement to desulfurizer and operation.
The composite absorber compatibility premium properties of single absorbent, higher mass transfer force, higher absorptive capacity, higher absorption rate and regeneration rate can be provided in absorption process.Therefore composite absorber has higher premium properties, in the flue gas desulfurization field, has obtained paying close attention to widely and applying.
Membrane gas absorption technology (being called for short film absorbs) is separated the new gas separation process combined with the solvent absorption gas technology as film, adopt membrane contactor as desulfurizer, it has stable mass transfer interface, high-specific surface area, high mass transfer efficiency, energy consumption is low, the advantages such as device volume is little, and stable operation and elasticity are large; Microporous barrier in membrane contactor is only the barrier between gas-liquid two-phase, and to the separation non-selectivity of gas, absorbent provides high selectivity and high drive in separation process.Therefore exploitation and membrane material mutually the high-performance absorbent of compatibility there is the meaning of particular importance.At present, absorb SO for membrane contactor
2composite absorber is less, and absorbent properties also need to improve.We absorb SO at film
2lot of experiments work has been done in the composite absorber aspect, has proposed the composite absorber of novel and high-efficiency, at present at gas cleaning SO
2field has no uses and reports.
Summary of the invention
The object of the present invention is to provide a kind of sulfur dioxide absorbent that can absorb for membrane contactor.
Concrete scheme is as follows:
1, in the separating mixed gas the invention discloses, the absorbent of sulfur dioxide is comprised of the aqueous solution of malate and organic amine, and described malate is 1:(0.5 ~ 3 with the mol ratio of mixing of organic amine).
2, preferably, organic amine is selected from arbitrary in following structural formula:
；
R wherein
1be selected from-NH
2,-OCH
3,-OC
2h
5,-OC
3h
7.
3, particularly preferably, R
1be selected from-NH
2perhaps-OCH
3.
4, preferably, the total concentration of malate and organic amine is 0.1 ~ 4.0mol/L.
5, preferably, described malate is natrium malicum or potassium malate.
6, preferably, the aqueous solution that in separating mixed gas, the absorbent of sulfur dioxide is natrium malicum and methoxyethyl amine, be perhaps the aqueous solution of potassium malate and methoxyethyl amine, or be the aqueous solution of natrium malicum and ethylenediamine, or be the aqueous solution of potassium malate and ethylenediamine.
7, preferably, the more typical value of laminated desulfurizer total concentration of malate and organic amine is 0.5～2.5mol/L.
8, preferably, malate and organic amine mol ratio more representative value be 1:(1～2.0).
The laminated desulfurizer chemical stability that the present invention proposes is good, and foaminess is little, and viscosity is little, and raw material sources are abundant, easily buys low price.The sulfur removal technology of applying laminated desulfurizer disclosed by the invention has high mass tranfer coefficient, the Liquid Flow undisturbed, and resistance to mass tranfer is little, and desulfurization degree is high, easy to operate, and operating flexibility is large, can stable operation in membrane contactor.The desulfuration solution non-scaling, do not stop up simultaneously, corrosion-free.The laminated desulfurizer that the present invention proposes can be used in membrane contactor, can certainly in tower class reactor (as bubble tower, packed tower, plate column etc.), use.
The absorbent of sulfur dioxide, have identical implication with Compositional type absorbent and Compositional type reclaiming agent etc. in the present invention, all mean can sulfur dioxide absorption organic solution.
The accompanying drawing explanation
Fig. 1 is that film absorbs SO
2the device for evaluating performance of sulfur dioxide absorbent in application.
Wherein:
1-1-N
2gas bomb, 1-2-SO
2gas bomb, 2-gas Quality Control instrument, 3-mixing steady-flow tank, 4-membrane contactor, 5-peristaltic meatering pump, 6-the first solution storage trough, 7-the second solution storage trough, 8-infrared gas analyser, P-pressure gauge, A-sample point.
Fig. 2 and 3 is SO
2the block diagram of absorbent properties and one pack system sulfur dioxide absorbent properties comparing data.
Wherein the different colours of color lump means different absorbent selection modes, and in Fig. 2, the height of color lump means SO
2mass tranfer coefficient, in Fig. 3, the height of color lump means SO
2removal efficiency;
Wherein,
In I group data, organic amine be ethylenediamine, compound be potassium malate/natrium malicum and ethylenediamine solution; In II group data, organic amine be methoxyethyl amine, compound be potassium malate/natrium malicum and the methoxyethyl amine aqueous solution; In III group data, organic amine be ethoxy ethyl amine, compound be potassium malate/natrium malicum and the ethoxy ethyl amine aqueous solution; In IV group data, organic amine be propoxyl group ethamine, compound be potassium malate/natrium malicum and propoxyl group ethylamine solution.
The specific embodiment
Below in conjunction with accompanying drawing, the present invention is described in further detail.
Embodiment 1
The method of evaluating performance that in separating mixed gas, the absorbent of sulfur dioxide is applied in membrane contactor.
Operating condition: room temperature (19-22 ℃), mixture pressure 0.11MPa, membrane mass transfer area 1.5 m
2, gas flow rate 0.5-2 L/min, flow rate of liquid 200-500mL/min.
As shown in Figure 1, respectively from N
2gas bomb 1-1 and SO
2the gas of gas bomb 1-2, after gas Quality Control instrument 2 metering, enters and mixes steady-flow tank 3 and form containing the 0.1%-0.6%(percentage by volume) SO
2gaseous mixture, the gaseous mixture after the air-flow current stabilization enters in membrane contactor 4, SO in gaseous mixture
2diffuse to the film opposite side by fenestra, absorbed by laminated desulfurizer, enter liquid phase, the gas phase after absorption is emitted from membrane contactor other end gas vent, and the desulfurizing agent in membrane contactor is from the first solution storage trough 6.Desulfurizing agent is extracted out by peristaltic meatering pump 5, and the laminated desulfurizer in the first solution storage trough 6 is sent in membrane contactor 4, thus the SO that the trapping diffusion is come
2.Desulfurizing agent after use is discharged from membrane contactor 4, and is stored by the second solution storage trough 7.
Gas phase is imported and exported to be comprised of infrared gas analyser 8 and is measured.Solution component through the sampling after, by hplc determination, liquid phase SO
2content adopts spectrophotometry.
Evaluation criterion:
The cumulative volume mass tranfer coefficient
k g a:
SO
2removal efficiency
η:
In formula
g,
awith
lbe respectively gaseous phase volume flow velocity, film cross-sectional area and film length,
c g, inwith
c g, outbe respectively gas phase and import and export SO
2concentration.
The aqueous solution that in separating mixed gas, the absorbent of sulfur dioxide is potassium malate/natrium malicum and ethylenediamine, potassium malate/natrium malicum and the ethylenediamine total concentration in the aqueous solution is 0.1 ~ 4mol/L, and the mol ratio of potassium malate/natrium malicum and ethylenediamine is 1:(0.5 ~ 3).
Adopt the method for evaluating performance in embodiment 1 to be detected.
Process condition: room temperature, gaseous pressure 0.11MPa, gaseous mixture SO
2content 0.1%-0.6%(percentage by volume), membrane mass transfer area 1.5m
2, gas speed: 0.5-2L/min, liquid speed: 200-500mL/min.
Various desulfurizing agents Evaluation results under various conditions is shown in Table 1.
Table 1 laminated desulfurizer Evaluation results
Result shows: laminated desulfurizer adaptability is high, not only adapts to low-concentration flue gas, also adapts to high-concentration fume, the concentration of absorbing wide ranges of use, and gas-liquid speed operating flexibility is large, SO
2removal efficiency is high, is greater than 99%, and the film device mass tranfer coefficient is large, between 0.29-0.42.
The aqueous solution that in separating mixed gas, the absorbent of sulfur dioxide is potassium malate/natrium malicum and ethoxy ethyl amine, potassium malate/natrium malicum and the ethoxy ethyl amine total concentration in the aqueous solution is 0.1 ~ 4mol/L, and the mol ratio of potassium malate/natrium malicum and ethoxy ethyl amine is 1:(0.5 ~ 3).
Adopt the method for evaluating performance in embodiment 1 to be detected.
Process condition: room temperature, gaseous pressure 0.11MPa, gaseous mixture SO
2content 0.1%-0.6%(percentage by volume), membrane mass transfer area 1.5m
2, gas speed: 0.5-2L/min, liquid speed: 200-500mL/min.
Various desulfurizing agents Evaluation results under various conditions is shown in Table 2.
Table 2 laminated desulfurizer Evaluation results
Result shows: laminated desulfurizer adaptability is high, not only adapts to low-concentration flue gas, also adapts to high-concentration fume, the concentration of absorbing wide ranges of use, and gas-liquid speed operating flexibility is large, SO
2removal efficiency is high, is greater than 99%, and the film device mass tranfer coefficient is large, at 0.26-0.40.
Embodiment 4
The aqueous solution that in separating mixed gas, the absorbent of sulfur dioxide is potassium malate/natrium malicum and methoxyethyl amine, potassium malate/natrium malicum and the methoxyethyl amine total concentration in the aqueous solution is 0.1 ~ 4mol/L, and the mol ratio of potassium malate/natrium malicum and methoxyethyl amine is 1:(0.5 ~ 3).
Adopt the method for evaluating performance in embodiment 1 to be detected.
Process condition: room temperature, gaseous pressure 0.11MPa, gaseous mixture SO
2content 0.1%-0.6%(percentage by volume), membrane mass transfer area 1.5m
2, gas speed: 0.5-2L/min, liquid speed: 200-500mL/min.
Various desulfurizing agents Evaluation results under various conditions is shown in Table 3.
Table 3 laminated desulfurizer Evaluation results
Result shows: laminated desulfurizer adaptability is high, not only adapts to low-concentration flue gas, also adapts to high-concentration fume, the concentration of absorbing wide ranges of use, and gas-liquid speed operating flexibility is large, SO
2removal efficiency is high, is greater than 99%, and the film device mass tranfer coefficient is large, at 0.30-0.43.
The aqueous solution that in separating mixed gas, the absorbent of sulfur dioxide is potassium malate/natrium malicum and propoxyl group ethamine, potassium malate/natrium malicum and the total concentration of propoxyl group ethamine in the aqueous solution are 0.1 ~ 4mol/L, and the mol ratio of potassium malate/natrium malicum and propoxyl group ethamine is 1:(0.5 ~ 3).
Adopt the method for evaluating performance in embodiment 1 to be detected.
Process condition: room temperature, gaseous pressure 0.11MPa, gaseous mixture SO
2content 0.1%-0.6%(percentage by volume), membrane mass transfer area 1.5m
2, gas speed: 0.5-2L/min, liquid speed: 200-500mL/min.
Various desulfurizing agents Evaluation results under various conditions is shown in Table 4.
Table 4 laminated desulfurizer Evaluation results
Result shows: laminated desulfurizer adaptability is high, not only adapts to low-concentration flue gas, also adapts to high-concentration fume, the concentration of absorbing wide ranges of use, and gas-liquid speed operating flexibility is large, SO
2removal efficiency is high, except indivedual lower slightly, all be greater than 99%, the film device mass tranfer coefficient is large, at 0.25-0.38.
Select single group desulfurizing agent as a comparison: flue gas one pack system desulfurizing agent is potassium malate, or natrium malicum, or ethylenediamine, or methoxyethyl amine, or ethoxy ethyl amine, or the aqueous solution of propoxyl group ethamine; Potassium malate, or natrium malicum, or ethylenediamine, or methoxyethyl amine, or ethoxy ethyl amine, or propoxyl group ethamine, the concentration of one-component desulfurizing agent in the aqueous solution is 3.0mol/L.
The one pack system desulfurizing agent is estimated, and compared with laminated desulfurizer.
Process condition: room temperature, gaseous pressure 0.11MPa, gaseous mixture SO
2content 0.4%(percentage by volume), membrane mass transfer area 1.5m
2, gas speed: 1L/min, liquid speed: 500mL/min, total 3.0 mol/L of composite type solution concentration, mol ratio 1:2.0.
Process operation is with reference to the evaluation method in embodiment 1.
Various one pack system desulfurizing agent performances and laminated desulfurizer performance evaluation and comparative result are shown in shown in Fig. 2 and 3.
Result shows: the laminated desulfurizer mass tranfer coefficient
k g aand removal efficiency
ηvalue is higher than the one pack system organic amine desulfurizer, and also far above potassium malate or natrium malicum, the performance of laminated desulfurizer is better than the one pack system desulfurizing agent.
Claims (8)
1. the absorbent of sulfur dioxide in a separating mixed gas, the absorbent that it is characterized in that sulfur dioxide in described separating mixed gas is comprised of the aqueous solution of malate and organic amine, described malate is 1:(0.5 ~ 3 with the mol ratio of mixing of organic amine).
2. the absorbent of sulfur dioxide in separating mixed gas according to claim 1 is characterized in that: described organic amine is selected from arbitrary in following structural formula:
3. the absorbent of sulfur dioxide in separating mixed gas according to claim 2, is characterized in that: R
1be selected from-NH
2perhaps-OCH
3.
4. the absorbent of sulfur dioxide in separating mixed gas according to claim 1, it is characterized in that: described malate is natrium malicum or potassium malate.
5. the absorbent of sulfur dioxide in separating mixed gas according to claim 2, it is characterized in that: the aqueous solution that in described separating mixed gas, the absorbent of sulfur dioxide is natrium malicum and methoxyethyl amine, be perhaps the aqueous solution of potassium malate and methoxyethyl amine, be perhaps the aqueous solution of natrium malicum and ethylenediamine, or be the aqueous solution of potassium malate and ethylenediamine.
6. according to the absorbent of sulfur dioxide in the described separating mixed gas of any one in claim 1 to 5, it is characterized in that: in described separating mixed gas in the absorbent of sulfur dioxide the total concentration of malate and organic amine be 0.1 ~ 4.0mol/L.
7. the absorbent of sulfur dioxide in separating mixed gas according to claim 6, it is characterized in that: in described separating mixed gas, the absorbent total concentration of sulfur dioxide is 0.5～2.5mol/L.
8. the absorbent of sulfur dioxide in separating mixed gas according to claim 1, it is characterized in that: described malate and organic amine mol ratio are 1:(1～2.0).
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|---|---|---|---|
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Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012058558A2 (en) * | 2010-10-29 | 2012-05-03 | E. I. Du Pont De Nemours And Company | Regenerative recovery of sulfur dioxide from effluent gases |
-
2013
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012058558A2 (en) * | 2010-10-29 | 2012-05-03 | E. I. Du Pont De Nemours And Company | Regenerative recovery of sulfur dioxide from effluent gases |
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