CN104174275A - Compound type ionic liquid and preparation method and application of compound type ionic liquid as trapping agent - Google Patents
Compound type ionic liquid and preparation method and application of compound type ionic liquid as trapping agent Download PDFInfo
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- CN104174275A CN104174275A CN201410405562.4A CN201410405562A CN104174275A CN 104174275 A CN104174275 A CN 104174275A CN 201410405562 A CN201410405562 A CN 201410405562A CN 104174275 A CN104174275 A CN 104174275A
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Abstract
The invention relates to the field of ionic liquid and gas-liquid separation, particularly relates to the field of ionic liquid structures and flue gas desulfurization and decarburization, and particularly relates to a compound type ionic liquid and a preparation method and an application of the compound type ionic liquid as a trapping agent. The compound type ionic liquid is an amino acid-lactic acid alkyl diamine compound ionic liquid, the structure of the compound type ionic liquid is described in the specification, wherein R1 is alkyl containing 2-4 carbon atoms, and R2 is H or alkyl containing 1-2 carbon atoms. The compound type ionic liquid disclosed by the invention is applied to removing of SO2 and CO2 and is capable of greatly increasing the absorption amount of an absorbing agent and the removing efficiency; the raw materials are abundant, easy to purchase, low in price; the synthesis method is simple and easy to operate. The compound type ionic liquid is suitable for flue gas desulfurization and decarburization.
Description
Technical field
The present invention relates to ionic liquid and gas-liquid separation field, particularly relate to ionic liquid structure and flue gas desulfurization decarburization field, more specifically relate to a kind of compound ionic liquid and remove SO
2and CO
2.
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Background technology
In the flue gas such as coal-burning power plant, metallurgy industry, contain CO
2and SO
2deng sour gas, SO
2being one of Air Pollutant Discharge, is the formation source of acid rain, CO
2being main greenhouse gas, is one of main cause causing at present climate change.Along with the raising day by day that environmental protection requires Air Pollutant Emission, in gas cleaning process, how to select effectively and rationally decarbonization, desulfuration technique, with lower investment and operating cost, reach the purification object of flue gas decarbonization desulfurization, both made SO in flue gas
2discharge meets the regulation of discharging standards, can reduce CO again
2discharge capacity is the key issue that current coal-burning power plant, metallurgy industry etc. develop in a healthy way.Therefore, various high-performance CO
2and SO
2the exploitation of trapping agent is one of theme of this area research, and in recent years, ionic liquid was as the novel green medium of a class, due to its unique performance heat subject that is this area research and development always.
For same flue gas, decarburization and desulfurization are carried out respectively, and having realized at present industrialized flue gas decarbonization is mainly amine method (being MEA washing method), belongs to wet method.Flue gas desulfurization has by the common method of the kind of desulfurizing agent: 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.More than 90% commercialization flue gas desulfurization adopts calcium method desulfur technology in the world, and 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 smoke treatment contain absorbent, and this method has that desulphurization reaction speed is fast, equipment simple, removal efficiency advantages of higher, but ubiquity seriously corroded, operation and maintenance cost is high and cause secondary pollution problems.Desulfurization by dry method 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.In addition, also have that semi-dry desulphurization technology refers to desulfurizing agent desulfurization under drying regime, regeneration under wet condition (as washing regenerating active carbon flow process), or desulfurization under wet condition, under dry state, process the flue gas desulfurization technique of desulfurization product (as spray drying process).Particularly desulfurization under wet condition, under dry state, process the semidry method of desulfurization product, with its advantage that existing wet desulphurization reaction speed is fast, desulfuration efficiency is high, have again dry method without sewage spent acid discharge, the easy-to-handle advantage of desulfurization afterproduct and be subject to people and pay close attention to widely.At the desulfurizing agent of commercial Application (as calcium base etc.) tool, have great advantage, it can realize sulphur trapping, has arresting efficiency high, and energy-conservation, cost of material is cheap, and adsorbent cost is low, economy advantages of higher.But desulfurizing agent is in adsorption process, and trapping ability tends to decay gradually, adsorbent causes sintering when higher temperature, and adsorption capacity worsens, and adsorbent, in microstructure, as surface area, pore volume and structural form, all can impact response characteristic.The initial reaction activity of trapping agent is even more important, and in trapping flue gas carbon oxysulfide process, collector performance has fundamentally determined CO
2and SO
2the efficiency of trapping operation, thereby collector performance is had to very high requirement, and collector performance depends primarily on trapping agent chemical constitution.
Ionic liquid has unique chemical constitution, and as a kind of green solvent, its uniqueness is embodied in the designability of ionic liquid and multiple dimensioned structure-activity relationship.
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Summary of the invention
The object of the present invention is to provide a kind of compound ionic liquid, this compound ionic liquid can be used for removing CO in flue gas
2and SO
2, there is high absorptive capacity and removal efficiency.
Another object of the present invention is to provide the synthetic method of above-mentioned compound ionic liquid.
The present invention or object are to provide the application as trapping agent of above-mentioned compound ionic liquid.
Concrete technical scheme of the present invention is as follows:
A compound ionic liquid, this compound ionic liquid is the compound ionic liquid of amino acid lactic acid alkyl diamine, the structure of this compound ionic liquid is as follows:
R in formula
1for the alkyl containing 2-4 carbon, R
2for H or containing the alkyl of 1-2 carbon.
Further design of the present invention is:
The compound ionic liquid of amino acid lactic acid alkyl diamine is preferably: glycine lactic acid ethylenediamine, glycine lactic acid propane diamine, glycine lactic acid butanediamine, alanine lactic acid ethylenediamine, alanine lactic acid propane diamine, alanine lactic acid butanediamine, glycine lactic acid methyl-prop diamines or aminobutyric acid lactic acid ethylenediamine.
The present invention also provides above-mentioned compound ionic liquid preparation method, and the concrete steps of the method are as follows:
1) quantitative alkyl diamine is added to water and form solution, be placed in three mouthfuls of containers, a side interface of three mouthfuls of containers is installed dropping funel, and intermediary interface is installed agitator, and opposite side is as solid feed inlet;
2) quantitative lactic acid is placed in to dropping funel;
3) three mouthfuls of containers are placed in to water bath with thermostatic control, bath temperature is controlled at 30-60 ℃, starts agitator;
4) start dropping funel switch, lactic acid is dropwise splashed in alkyl diamine solution, drip off rear continuation reaction 1-3h;
5) quantitative amino acid is added in upper step reaction solution by spoon by solid material mouth, add rear continuation reaction 1-3h, cessation reaction; In reaction system, the mol ratio of lactic acid, amino acid and alkyl diamine is 1:1:1,
6) solution after having reacted is the compound ionic liquid solution of product amino acid lactic acid alkyl diamine.
In step 1), the mass ratio of alkyl diamine and water is 1:(5.5 ~ 53.0).
Alkyl diamine described in step 1) is selected ethylenediamine, propane diamine, butanediamine or methyl-prop diamines.
In step 3), react mixing speed 800-1200r/min.
In step 4), react drip/min of drop rate 80-120.
The compound ionic liquid concentration 0.2-1.8mol/kg of product amino acid lactic acid alkyl diamine preparing in step 6).
The present invention also provides above-mentioned compound ionic liquid as CO
2and SO
2the application of trapping agent.
the present invention compared to existing technology tool has the following advantages:
Present inventor is doing great many of experiments and research work aspect ionic liquid structural design and structure-activity relationship, proposed a kind of compound ionic liquid and removed SO
2and CO
2, the method is simple, and this ionic liquid can trap CO in flue gas efficiently
2and SO
2, there is high absorptive capacity and removal efficiency, at present at gas cleaning CO
2and SO
2field has no uses and reports.
The compound ionic liquid that the present invention proposes, structurally be different from other ionic liquid, other ionic liquid only has a cation and an anion to form conventionally, and the structure of compound ionic liquid is comprised of a cation and two anion, the chemical constitution of this uniqueness has multiple dimensioned structure effect effect, embody the functional of uniqueness, to CO
2and SO
2show multiple physical and chemical reaction mechanism, research is found, there is both sexes mechanism in compound ionic liquid simultaneously, affine mechanism, the mechanism of shuttling back and forth and acid-base neutralization mechanism etc., these mechanism can greatly improve ionic liquid reaction rate, and after tested, compound ionic liquid reaction rate is other ionic liquid ([apmim] [BF for example
4]) 2-3 doubly.
The compound ionic liquid that the present invention proposes, in chemical constitution, hydroxyl, many carboxyls and polyamino form new covalency and ion combination state in course of reaction, form in molecule and intermolecular hydrogen bonding simultaneously, these chemistry and physical aspect promote material diffusion, transmission and process widely, have improved compound ionic liquid absorptive capacity.After tested, compound ionic liquid absorptive capacity is other ionic liquid ([apmim] [BF for example
4]) more than 2.8 times.
Accompanying drawing explanation
Fig. 1 is provided by the invention a kind of for evaluating compound ionic liquid trapping CO
2and SO
2performance devices figure (bubbling column reactor).
Wherein: 1-gas cylinder, 2-gas flowmeter, 3-bubbling reactor, 4-constant temperature jacket, P-pressure gauge, A-sample point.
The specific embodiment
Below in conjunction with accompanying drawing, the present invention is described in further detail.
embodiment 1
In a constant temperature stirring reaction system, 108g ethylenediamine and 595g water add in three mouthfuls of containers; 162g lactic acid is placed in to dropping funel, by warming-in-water to 60 ℃ of reaction temperatures, and constant temperature; Start agitator, control mixing speed 1000r/min; Start dropping funel switch, lactic acid dropwise splashes in ethylenediamine solution, and 120/min of drop rate drips off rear continuation reaction 1h.135g glycine is added in upper step solution by spoon, in 30min, add, add rear continuation reaction 1h, cessation reaction.Solution after having reacted is the compound ionic liquid solution of product glycine lactic acid ethylenediamine, and concentration is 1.8mol/kg, and product is without dehydration and purification, directly as CO
2and SO
2trapping agent.
Pack synthetic product into bubbling column reactor, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency.
Get same concentration MEA(monoethanolamine) pack bubbling column reactor (adopting Fig. 1 device, as follows) into, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency, measured value is data as a comparison.
Compound ionic liquid trapping CO
2and SO
2performance and common absorbent MEA compare, evaluation result is shown in Table 1.
embodiment 2
In a constant temperature stirring reaction system, 104g propane diamine and 665g water add in three mouthfuls of containers; 126g lactic acid is placed in to dropping funel, by warming-in-water to 50 ℃ of reaction temperatures, and constant temperature; Start agitator, control mixing speed 800r/min; Start dropping funel switch, lactic acid dropwise splashes in propane diamine solution, and 110/min of drop rate drips off rear continuation reaction 2h.105g glycine is added in upper step solution by spoon, in 30min, add, add rear continuation reaction 2h, cessation reaction.Solution after having reacted is the compound ionic liquid solution of product glycine lactic acid propane diamine, and concentration is 1.4mol/kg, and product is without dehydration and purification, directly as CO
2and SO
2trapping agent.
Pack synthetic product into bubbling column reactor, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency.
Get same concentration MEA and pack bubbling column reactor into, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency, measured value is data as a comparison.
Compound ionic liquid trapping CO
2and SO
2performance and common absorbent MEA compare, evaluation result is shown in Table 1.
embodiment 3
In a constant temperature stirring reaction system, 88g butanediamine and 747g water add in three mouthfuls of containers; 90g lactic acid is placed in to dropping funel, by warming-in-water to 45 ℃ of reaction temperatures, and constant temperature; Start agitator, control mixing speed 1200r/min; Start dropping funel switch, lactic acid dropwise splashes in butanediamine solution, and 120/min of drop rate drips off rear continuation reaction 3h.75g glycine is added in upper step solution by spoon, in 30min, add, add rear continuation reaction 2h, cessation reaction.Solution after having reacted is the compound ionic liquid solution of product glycine lactic acid butanediamine, and concentration is 1.0mol/kg, and product is without dehydration and purification, directly as CO
2and SO
2trapping agent.
Pack synthetic product into bubbling column reactor, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency.
Get same concentration MEA and pack bubbling column reactor into, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency, measured value is data as a comparison.
Compound ionic liquid trapping CO
2and SO
2performance and common absorbent MEA compare, evaluation result is shown in Table 1.
embodiment 4
In a constant temperature stirring reaction system, 72g ethylenediamine and 713g water add in three mouthfuls of containers; 108g lactic acid is placed in to dropping funel, by warming-in-water to 55 ℃ of reaction temperatures, and constant temperature; Start agitator, control mixing speed 1100r/min; Start dropping funel switch, lactic acid dropwise splashes in ethylenediamine solution, and 90/min of drop rate drips off rear continuation reaction 2h.107g alanine is added in upper step solution by spoon, in 30min, add, add rear continuation reaction 2h, cessation reaction.Solution after having reacted is the compound ionic liquid solution of product alanine lactic acid ethylenediamine, and concentration is 1.2mol/kg, and product is without dehydration and purification, directly as CO
2and SO
2trapping agent.
Pack synthetic product into bubbling column reactor, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency.
Get same concentration MEA and pack bubbling column reactor into, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency, measured value is data as a comparison.
Compound ionic liquid trapping CO
2and SO
2performance and common absorbent MEA compare, evaluation result is shown in Table 1.
embodiment 5
In a constant temperature stirring reaction system, 59g propane diamine and 798g water add in three mouthfuls of containers; 72g lactic acid is placed in to dropping funel, by warming-in-water to 30 ℃ of reaction temperatures, and constant temperature; Start agitator, control mixing speed 1200r/min; Start dropping funel switch, lactic acid dropwise splashes in propane diamine solution, and 100/min of drop rate drips off rear continuation reaction 2h.71g alanine is added in upper step solution by spoon, in 30min, add, add rear continuation reaction 2h, cessation reaction.Solution after having reacted is the compound ionic liquid solution of product alanine lactic acid propane diamine, and concentration is 0.8mol/kg, and product is without dehydration and purification, directly as CO
2and SO
2trapping agent.
Pack synthetic product into bubbling column reactor, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency.
Get same concentration MEA(monoethanolamine) pack bubbling column reactor into, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency, measured value is data as a comparison.
Compound ionic liquid trapping CO
2and SO
2performance and common absorbent MEA compare, evaluation result is shown in Table 1.
embodiment 6
In a constant temperature stirring reaction system, 35g butanediamine and 893g water add in three mouthfuls of containers; 36g lactic acid is placed in to dropping funel, by warming-in-water to 40 ℃ of reaction temperatures, and constant temperature; Start agitator, control mixing speed 850r/min; Start dropping funel switch, lactic acid dropwise splashes in butanediamine solution, and 80/min of drop rate drips off rear continuation reaction 1h.36g alanine is added in upper step solution by spoon, in 30min, add, add rear continuation reaction 1h, cessation reaction.Solution after having reacted is the compound ionic liquid solution of product alanine lactic acid butanediamine, and concentration is 0.4mol/kg, and product is without dehydration and purification, directly as CO
2and SO
2trapping agent.
Pack synthetic product into bubbling column reactor, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency.
Get same concentration MEA and pack bubbling column reactor into, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency, measured value is data as a comparison.
Compound ionic liquid trapping CO
2and SO
2performance and common absorbent MEA compare, evaluation result is shown in Table 1.
example 7
In a constant temperature stirring reaction system, 18g methyl-prop diamines and 949g water add in three mouthfuls of containers; 18g lactic acid is placed in to dropping funel, by warming-in-water to 30 ℃ of reaction temperatures, and constant temperature; Start agitator, control mixing speed 1000r/min; Start dropping funel switch, lactic acid dropwise splashes in methyl-prop two amine aqueous solutions, and 90/min of drop rate drips off rear continuation reaction 2h.15g glycine is added in upper step solution by spoon, in 30min, add, add rear continuation reaction 2h, cessation reaction.Solution after having reacted is the compound ionic liquid solution of product glycine lactic acid methyl-prop diamines, and concentration is 0.2mol/kg, and product is without dehydration and purification, directly as CO
2and SO
2trapping agent.
Pack synthetic product into bubbling column reactor, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency.
Get same concentration MEA and pack bubbling column reactor into, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency, measured value is data as a comparison.
Compound ionic liquid trapping CO
2and SO
2performance and common absorbent MEA compare, evaluation result is shown in Table 1.
example 8
In a constant temperature stirring reaction system, 30g ethylenediamine and 873g water add in three mouthfuls of containers; 45g lactic acid is placed in to dropping funel, by warming-in-water to 35 ℃ of reaction temperatures, and constant temperature; Start agitator, control mixing speed 1000r/min; Start dropping funel switch, lactic acid dropwise splashes in ethylenediamine solution, and 100/min of drop rate drips off rear continuation reaction 1h.52g aminobutyric acid is added in upper step solution by spoon, in 30min, add, add rear continuation reaction 1h, cessation reaction.Solution after having reacted is the compound ionic liquid solution of product aminobutyric acid lactic acid ethylenediamine, and concentration is 0.5mol/kg, and product is without dehydration and purification, directly as CO
2and SO
2trapping agent.
Pack synthetic product into bubbling column reactor, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency.
Get same concentration MEA and pack bubbling column reactor into, pass into simulated flue gas and carry out performance evaluation.Flue gas pressures 0.12MPa, simulated flue gas forms (percent by volume) 12%CO
2, 0.1%SO
2, 3%O
2, all the other are N
2; Absorb 40 ℃ of temperature, flue gas flow 50-500 mL/min.Measure absorptive capacity and removal efficiency, measured value is data as a comparison.
Compound ionic liquid trapping CO
2and SO
2performance and common absorbent MEA compare, evaluation result is shown in Table 1.
The compound ionic liquid trapping of table 1 CO
2and SO
2performance evaluation
Result shows: compound ionic liquid trapping CO
2and SO
2performance be better than common absorbent MEA, absorptive capacity and removal efficiency be all higher than common absorbent MEA, the 1.8-1.86 that compound ionic liquid absorptive capacity is common absorbent MEA doubly, SO
2removal efficiency is approximately 1.45-1.69 times of common absorbent MEA, CO
2removal efficiency is a little more than MEA, and the compound ionic liquid physical efficiency of the present invention removes SO in flue gas efficiently
2and CO
2, and have SO
2high selectivity.
Claims (10)
1. a compound ionic liquid, is characterized in that: this compound ionic liquid is the compound ionic liquid of amino acid lactic acid alkyl diamine, and the structure of this compound ionic liquid is as follows:
R in formula
1for the alkyl containing 2-4 carbon, R
2for H or containing the alkyl of 1-2 carbon.
2. compound ionic liquid according to claim 1, is characterized in that: the compound ionic liquid of amino acid lactic acid alkyl diamine is preferably: glycine lactic acid ethylenediamine, glycine lactic acid propane diamine, glycine lactic acid butanediamine, alanine lactic acid ethylenediamine, alanine lactic acid propane diamine, alanine lactic acid butanediamine, glycine lactic acid methyl-prop diamines or aminobutyric acid lactic acid ethylenediamine.
3. compound ionic liquid preparation method according to claim 1, is characterized in that: the concrete steps of the method are as follows:
1) quantitative alkyl diamine is added to water and form solution, be placed in three mouthfuls of containers, a side interface of three mouthfuls of containers is installed dropping funel, and intermediary interface is installed agitator, and opposite side is as solid feed inlet;
2) quantitative lactic acid is placed in to dropping funel;
3) three mouthfuls of containers are placed in to water bath with thermostatic control, bath temperature is controlled at 30-60 ℃, starts agitator;
4) start dropping funel switch, lactic acid is dropwise splashed in alkyl diamine solution, drip off rear continuation reaction 1-3h;
5) quantitative amino acid is added in upper step reaction solution by spoon by solid material mouth, add rear continuation reaction 1-3h, cessation reaction; In reaction system, the mol ratio of lactic acid, amino acid and alkyl diamine is 1:1:1,
6) solution after having reacted is the compound ionic liquid solution of product amino acid lactic acid alkyl diamine.
4. the synthetic method of compound ionic liquid according to claim 3, is characterized in that: in step 1), the mass ratio of alkyl diamine and water is 1:(5.5 ~ 53.0).
5. the synthetic method of compound ionic liquid according to claim 3, is characterized in that: alkyl diamine described in step 1) is selected ethylenediamine, propane diamine, butanediamine or methyl-prop diamines.
6. the synthetic method of compound ionic liquid according to claim 3, is characterized in that: in step 3), react mixing speed 800-1200r/min.
7. the synthetic method of compound ionic liquid according to claim 3, is characterized in that: in step 4), react drip/min of drop rate 80-120.
8. the synthetic method of compound ionic liquid according to claim 3, is characterized in that: amino acid described in step 5) is selected glycine, alanine or aminobutyric acid.
9. the synthetic method of compound ionic liquid according to claim 3, is characterized in that: the compound ionic liquid concentration 0.2-1.8mol/kg of product amino acid lactic acid alkyl diamine preparing in step 6).
Described in claim 1 compound ionic liquid as CO
2and SO
2the application of trapping agent.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105194982A (en) * | 2015-10-14 | 2015-12-30 | 黄锐 | Ionic liquid capable of absorbing sulfur dioxide as well as preparation method and application of ionic liquid |
| CN105727694A (en) * | 2016-04-07 | 2016-07-06 | 浙江大学 | Method for improving amino functional carbon capture through spatial synergistic effect |
| US9802186B2 (en) | 2016-01-29 | 2017-10-31 | Chevron U.S.A. Inc. | Reactor for homogeneous regeneration of spent ionic liquid |
| US10005057B1 (en) | 2017-09-26 | 2018-06-26 | Chevron U.S.A. Inc. | Segmented reactor for homogeneous regeneration of spent ionic liquid |
| US11135575B2 (en) | 2016-01-29 | 2021-10-05 | Chevron U.S.A. Inc. | Apparatus for regeneration of acidic ionic liquid without addition of a hydrogenation catalyst |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20070119302A1 (en) * | 2005-11-14 | 2007-05-31 | Maciej Radosz | Polymers containing ionic groups for gas separation and storage |
| CN101215262A (en) * | 2007-01-05 | 2008-07-09 | 中国纺织科学研究院 | ionic liquid and its preparing process and use |
| CN101844090A (en) * | 2009-12-07 | 2010-09-29 | 中国科学院山西煤炭化学研究所 | Imidazole grafting-type ionic liquid catalyst and preparation method and application |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20070119302A1 (en) * | 2005-11-14 | 2007-05-31 | Maciej Radosz | Polymers containing ionic groups for gas separation and storage |
| CN101215262A (en) * | 2007-01-05 | 2008-07-09 | 中国纺织科学研究院 | ionic liquid and its preparing process and use |
| CN101844090A (en) * | 2009-12-07 | 2010-09-29 | 中国科学院山西煤炭化学研究所 | Imidazole grafting-type ionic liquid catalyst and preparation method and application |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105194982A (en) * | 2015-10-14 | 2015-12-30 | 黄锐 | Ionic liquid capable of absorbing sulfur dioxide as well as preparation method and application of ionic liquid |
| US9802186B2 (en) | 2016-01-29 | 2017-10-31 | Chevron U.S.A. Inc. | Reactor for homogeneous regeneration of spent ionic liquid |
| US11135575B2 (en) | 2016-01-29 | 2021-10-05 | Chevron U.S.A. Inc. | Apparatus for regeneration of acidic ionic liquid without addition of a hydrogenation catalyst |
| CN105727694A (en) * | 2016-04-07 | 2016-07-06 | 浙江大学 | Method for improving amino functional carbon capture through spatial synergistic effect |
| CN105727694B (en) * | 2016-04-07 | 2018-05-29 | 浙江大学 | A kind of method that the trapping of amino functional carbon is improved using spatial cooperation effect |
| US10005057B1 (en) | 2017-09-26 | 2018-06-26 | Chevron U.S.A. Inc. | Segmented reactor for homogeneous regeneration of spent ionic liquid |
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| CN104174275B (en) | 2016-02-03 |
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