CN103304479A - Promoter for CO2 hydrate and application of promoter - Google Patents
Promoter for CO2 hydrate and application of promoter Download PDFInfo
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- CN103304479A CN103304479A CN2013102049770A CN201310204977A CN103304479A CN 103304479 A CN103304479 A CN 103304479A CN 2013102049770 A CN2013102049770 A CN 2013102049770A CN 201310204977 A CN201310204977 A CN 201310204977A CN 103304479 A CN103304479 A CN 103304479A
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Abstract
The invention relates to a promoter for generating a CO2 hydrate. The promoter is a low-concentration solution obtained by dissolving surface-active ion liquid into water, and the application concentration is 100-900 ppm; the surface-active ion liquid is respectively composed of 1-(3-sulfonic group) propyl hexamethyleneimine cations and dodecylbenzene sulfonic acid radical anions or 1-(3-sulfonic group) propyl pyrrolidine cations and the dodecylbenzene sulfonic acid radical anions. The promoter disclosed by the invention has a specific anion-cation structure and can be used for promoting the nucleation, growth and agglomeration of the CO2 hydrate, effectively lowering the phase equilibria point of the CO2 hydrate and shortening the generation induction time. Compared with the common promoter, the promoter disclosed by the invention has the advantages of more obvious promotion action, recycling capability, no pollution in a separation process, economy, environmental friendliness and high efficiency.
Description
Technical field
The invention belongs to chemical, environmental protection technical field, relate in particular to a kind of CO
2Storage technology.
Background technology
Gas hydrate is a kind of nonstoichiometry cage compound that is similar to ice that micro-molecular gas and water generate under cryogenic high pressure.In gas hydrate, form lattice structure by stronger hydrogen bonded between the water molecules, the Van der Waals force between gas molecule utilization and the water molecules is filled in interlattice cage, and does not have stoichiometric relation between gas and the water.In numerous gas hydrate species, because CO
2The special property of gas and effect, CO
2Hydrate receives the fervent concern in the whole world.
The world today, CO
2The a large amount of dischargings of gas cause global warming, and environmental problem has become the important topic that the whole world needs to be resolved hurrily.China is a country take coal as main energy sources, and wherein most coal is mainly used in thermal power generation, CO in power generation process
2Quantity discharged is very large, causes China CO
2The discharging situation is very severe, and suffered environment and international pressure are increasing.Present stage, CO
2Control mainly comprises three aspects: reclaim and separate, store transportation, trans-utilization, wherein reclaim the isolation technique energy consumption, cost is the highest, is restriction CO
2The key factor of emission control also is CO
2The first step of recycling.
Reclaim to separate and contain CO
2The main method of gaseous mixture has physical absorption, chemical absorption, pressure-variable adsorption and membrane sepn etc.Physical absorption is introduced absorption liquid with waste gas and is purified, and treats that absorption liquid is saturated to reclaim by heating, parsing, condensation, is applicable to the waste gas of atm number, low temperature, lower concentration, resolves retrieving arrangement but need to be equipped with heating, and equipment volume is large, investment is higher.The chemical absorption range of application is narrow, and it is large that absorption agent reclaims energy consumption.The pressure swing adsorption process Main Problems is that energy consumption is high, facility investment is large, the absorption utilization ratio is low etc.And now widely used membrane sepn rule has chemistry and poor heat stability, selectivity and flux are not high, processing power is limited, product purity is low etc. shortcoming.In the last few years, hydrate reclaimed, separates, seals up for safekeeping CO
2Technology is subject to international scholar's extensive concern.Utilize hydrate to reclaim separation of C O
2Technology has the following advantages:
(1) gas storage density is large.Under standard state, 1m
3Hydrate can be stored 150m
3Above gas.
(2) generate CO
2The hydrate condition comparatively easily realizes.CO
2Hydrate just can generate under pressure 1～5Mpa, 0 ℃～10 ℃ conditions of temperature.
(3) storage security.CO
2The thermophysical property of hydrate is more stable, at 10 ℃, and under the condition of normal pressure, CO
2Hydrate discharges gas fully to be needed more than 2 hours, than liquid CO
2Storage method safety a lot.
(4) gas hydrate decomposes or can absorb or emit a large amount of heat when generating.Therefore can be as the cold storage agent in the Cool Storage Technology, be than with the more effective a kind of Cool Storage Technology of other medium cold-storages.
(5) Application Areas is extensive.CO
2Hydrate can be used for food fresh keeping, sea water desaltination, gas delivery, solution concentrate, the fields such as sewage disposal.
CO
2The generation of hydrate is a slowly crystallisation process, is accompanied by gas-solid-liquid three-phase mass-and heat-transfer process, and induction time is long, the speed of growth is slow, the hydrate that generates at first can be gathered in liquid-gas interface, stops gas to enter liquid phase, hinders the further generation of hydrate.
Chinese patent CN102603674A discloses class gas hydrate accelerant [HMIPS] OTs and [HMIPS] Ss, proposes to utilize ionic liquid N
+With strong positive charge, strengthen the hydrogen bond action in the water, reduced CO
2Balancing each other a little of hydrate.But because [HMIPS] Ss and [HMIPS] Ots be under the concentration of 100ppm～900ppm, it is to measure with the full-automatic surface tension instrument of QBZY_1 type that the auspicious Instr Ltd. in Shanghai side produces that surface tension reaches 73.3～74.8mN/m(surface tension), cause CO
2Gas enters into relatively difficulty of liquid phase, fails to solve the long problem of induction time.
Summary of the invention
Technical problem to be solved by this invention is: in the prior art, there is the long problem of induction time in the generation of carbon dioxide hydrate.
For solving this technical problem, the technical solution used in the present invention is: the invention provides a kind of CO
2Hydrate accelerant, this CO
2Hydrate accelerant is a kind of surface-active ion liquid, and wherein, the positively charged ion of ionic liquid is selected from, 1-(3-sulfonic group) propyl group U-4527 positively charged ion or 1-(3-sulfonic group) propyl pyrrole alkane positively charged ion; Negatively charged ion is Witco 1298 Soft Acid root negatively charged ion.This surface-active ion liquid accelerator has following chemical structure:
In the ionic liquid, the N in nitrogenous organic ring-type positively charged ion
+Can strengthen the intensity of hydrogen bond in the water, reduce CO
2The nucleus that balancing each other a little of hydrate, its ring are conducive to hydrate generates;
Have surface-active negatively charged ion, can effectively reduce the surface tension of the aqueous solution, and have the effect of foaming, solubilising, and with ionic liquid in, nitrogenous organic ring-type positively charged ion forms synergistic effect, shortens induction time.
Above-mentioned CO
2Hydrate accelerant, when concrete the application, be operating as: first the surface-active ion liquid-mixing is made the certain density aqueous solution, concentration range is 100ppm～900ppm,
(1) injects the aqueous solution of above-mentioned surface-active ion liquid in the autoclave, open pumped vacuum systems, extract the gas in reactor and the pipeline, pumpdown time 30min;
(2) control bath temperature keeps temperature in the kettle stable, passes into CO with topping-up pump and air compressor machine in reactor
2Gas stops air inlet after reaching specified pressure, when treating that drop in temperature is to design temperature in the autoclave, opens magnetic stirring apparatus in the still, and the beginning timing, at this moment, and CO
2Hydrate generates fast, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was CO
2The induction time of hydrate,
Wherein, temperature in the kettle is 2 ℃～10 ℃, and specified pressure is 3～5Mpa, and when the magnetic stirring apparatus in the still was worked, rotating speed was 500 rev/mins;
(3) after temperature, pressure remains unchanged in the autoclave, can think CO
2Hydrate generates fully, opens vent valve, and control exhaust velocity (5～7 second pressure drop 0.01Mpa) keeps temperature in the kettle constant, by pressure transmitter with the temperature, pressure data transmission to computer, record CO
2The temperature, pressure of hydrate in decomposition course by the sight glass visor, finds CO
2Balancing each other a little of hydrate,
After opening vent valve, hydrate begins to decompose, and when obvious speck occurring in the glass visor, records the equilibrium of this moment, i.e. CO
2Balancing each other a little of hydrate.
The invention has the beneficial effects as follows: the present invention will have first surface-active ionic liquid and be used for CO
2Hydrate formation promoter under the zwitterion synergy, is conducive to CO
2Gas enters liquid phase, promotes CO
2The nucleation of hydrate, growth, agglomeration effectively reduce CO
2The hydrate induction time has reduced CO
2Balancing each other a little of hydrate, the effect of its promotor are better than simple ionic liquid and simple tensio-active agent.Surface-active ion liquid accelerator of the present invention is at CO
2Hydrate discharges CO after heating up and reducing pressure
2After can recycling, environmental protection, efficient.Can be applied in fields such as hydrate storage and transportation gas technology, hydrate separation technology.
Description of drawings
Fig. 1 is 1-(3-sulfonic group) propyl group U-4527 Witco 1298 Soft Acid, the surface tension of different concns dilute solution under differing temps.
Fig. 2 is 1-(3-sulfonic group) propyl pyrrole alkane Witco 1298 Soft Acid, the surface tension of different concns dilute solution under differing temps.
From accompanying drawing, can find out: hydrate accelerant solution of the present invention, when concentration was 100ppm～900ppm, surface tension was 32.8～48.5mN/m, compared the surface tension 73.3～74.8mN/m of [HMIPS] Ss and [HMIPS] OTs solution, fall is 55.8% to the maximum, can promote CO
2Gas enters into liquid phase.
Above surface tension all is that the full-automatic surface tension instrument of QBZY_1 type of using the auspicious Instr Ltd. in Shanghai side to produce is measured.
Embodiment
Embodiment 1
Inject 100ppm1-(3-sulfonic group) the propyl group U-4527 dodecylbenzenesulfonic acid solution of 200mL in the autoclave, vacuumize 30min.
Open water bath with thermostatic control, the control bath temperature is 2.0 ℃, passes into 99.9% CO in reactor
2Gas stops air inlet after reaching 3.00Mpa, opens magnetic stirring apparatus (500 rev/mins) in the still, and the beginning timing, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was 70s, i.e. CO
2The hydrate induction time.
After temperature, pressure remains unchanged in the autoclave, can think CO
2Hydrate generates fully, at this moment, opens vent valve, control exhaust velocity (5～7 seconds pressure drop 0.01Mpa), decomposition of hydrate keeps temperature in the kettle constant, by pressure transmitter with the temperature, pressure data transmission to computer, record CO
2The temperature, pressure of hydrate in decomposition course when obvious speck occurring in the glass visor, recorded the equilibrium of this moment, at this moment CO
2The hydrate phase balance data are 2.0 ℃, 1.51Mpa.
Embodiment 2
Inject 300ppm1-(3-sulfonic group) the propyl group U-4527 dodecylbenzenesulfonic acid solution of 200mL in the autoclave, vacuumize 30min.
Open water bath with thermostatic control, the control bath temperature is 4.0 ℃, passes into 99.9% CO in reactor
2Gas stops air inlet after reaching 3.50Mpa, opens magnetic stirring apparatus (500 rev/mins) in the still, and the beginning timing, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was 110s, i.e. CO
2The hydrate induction time.
After temperature, pressure remains unchanged in the autoclave, can think CO
2Hydrate generates fully, at this moment, opens vent valve, control exhaust velocity (5～7 seconds pressure drop 0.01Mpa), decomposition of hydrate keeps temperature in the kettle constant, by pressure transmitter with the temperature, pressure data transmission to computer, record CO
2The temperature, pressure of hydrate in decomposition course when obvious speck occurring in the glass visor, recorded the equilibrium of this moment, at this moment CO
2The hydrate phase balance data are 4.0 ℃, 1.87Mpa.
Embodiment 3
Inject 700ppm1-(3-sulfonic group) the propyl group U-4527 dodecylbenzenesulfonic acid solution of 200mL in the autoclave, vacuumize 30min.
Open water bath with thermostatic control, the control bath temperature is 6.0 ℃, passes into 99.9% CO in reactor
2Gas stops air inlet after reaching 4.00Mpa, opens magnetic stirring apparatus (500 rev/mins) in the still, and the beginning timing, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was 200s, i.e. CO
2The hydrate induction time.
After temperature, pressure remains unchanged in the autoclave, can think CO
2Hydrate generates fully, at this moment, opens vent valve, control exhaust velocity (5～7 seconds pressure drop 0.01Mpa), decomposition of hydrate keeps temperature in the kettle constant, by pressure transmitter with the temperature, pressure data transmission to computer, record CO
2The temperature, pressure of hydrate in decomposition course when obvious speck occurring in the glass visor, recorded the equilibrium of this moment, at this moment CO
2The hydrate phase balance data are 6.0 ℃, 2.42Mpa.
Embodiment 4
Inject 900ppm1-(3-sulfonic group) the propyl group U-4527 dodecylbenzenesulfonic acid solution of 200mL in the autoclave, vacuumize 30min.
Open water bath with thermostatic control, the control bath temperature is 10.0 ℃, passes into 99.9% CO in reactor
2Gas stops air inlet after reaching 5.00Mpa, opens magnetic stirring apparatus (500 rev/mins) in the still, and the beginning timing, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was 500s, i.e. CO
2The hydrate induction time.
After temperature, pressure remains unchanged in the autoclave, can think CO
2Hydrate generates fully, at this moment, opens vent valve, control exhaust velocity (5～7 seconds pressure drop 0.01Mpa), decomposition of hydrate keeps temperature in the kettle constant, by pressure transmitter with the temperature, pressure data transmission to computer, record CO
2The temperature, pressure of hydrate in decomposition course when obvious speck occurring in the glass visor, recorded the equilibrium of this moment, at this moment CO
2The hydrate phase balance data are 10.0 ℃, 4.27Mpa.
Embodiment 5
Inject 100ppm1-(3-sulfonic group) the propyl pyrrole alkane dodecylbenzenesulfonic acid solution of 200mL in the autoclave, vacuumize 30min.
Open water bath with thermostatic control, the control bath temperature is 2.0 ℃, passes into 99.9% CO in reactor
2Gas stops air inlet after reaching 3.00Mpa, opens magnetic stirring apparatus (500 rev/mins) in the still, and the beginning timing, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was 60s, i.e. CO
2The hydrate induction time.
After temperature, pressure remains unchanged in the autoclave, can think CO
2Hydrate generates fully, at this moment, opens vent valve, control exhaust velocity (5～7 seconds pressure drop 0.01Mpa), decomposition of hydrate keeps temperature in the kettle constant, by pressure transmitter with the temperature, pressure data transmission to computer, record CO
2The temperature, pressure of hydrate in decomposition course when obvious speck occurring in the glass visor, recorded the equilibrium of this moment, at this moment CO
2The hydrate phase balance data are 2.0 ℃, 1.46Mpa.
Embodiment 6
Inject 300ppm1-(3-sulfonic group) the propyl pyrrole alkane dodecylbenzenesulfonic acid solution of 200mL in the autoclave, vacuumize 30min.
Open water bath with thermostatic control, the control bath temperature is 4.0 ℃, passes into 99.9% CO in reactor
2Gas stops air inlet after reaching 3.50Mpa, opens magnetic stirring apparatus (500 rev/mins) in the still, and the beginning timing, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was 95s, i.e. CO
2The hydrate induction time.
After temperature, pressure remains unchanged in the autoclave, can think CO
2Hydrate generates fully, at this moment, opens vent valve, control exhaust velocity (5～7 seconds pressure drop 0.01Mpa), decomposition of hydrate keeps temperature in the kettle constant, by pressure transmitter with the temperature, pressure data transmission to computer, record CO
2The temperature, pressure of hydrate in decomposition course when obvious speck occurring in the glass visor, recorded the equilibrium of this moment, at this moment CO
2The hydrate phase balance data are 4.0 ℃, 1.82Mpa.
Embodiment 7
Inject 500ppm1-(3-sulfonic group) the propyl pyrrole alkane dodecylbenzenesulfonic acid solution of 200mL in the autoclave, vacuumize 30min.
Open water bath with thermostatic control, the control bath temperature is 8.0 ℃, passes into 99.9% CO in reactor
2Gas stops air inlet after reaching 4.50Mpa, opens magnetic stirring apparatus (500 rev/mins) in the still, and the beginning timing, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was 300s, i.e. CO
2The hydrate induction time.
After temperature, pressure remains unchanged in the autoclave, can think CO
2Hydrate generates fully, at this moment, opens vent valve, control exhaust velocity (5～7 seconds pressure drop 0.01Mpa), decomposition of hydrate keeps temperature in the kettle constant, by pressure transmitter with the temperature, pressure data transmission to computer, record CO
2The temperature, pressure of hydrate in decomposition course when obvious speck occurring in the glass visor, recorded the equilibrium of this moment, at this moment CO
2The hydrate phase balance data are 8.0 ℃, 3.02Mpa.
Embodiment 8
Inject 700ppm1-(3-sulfonic group) the propyl pyrrole alkane dodecylbenzenesulfonic acid solution of 200mL in the autoclave, vacuumize 30min.
Open water bath with thermostatic control, the control bath temperature is 6.0 ℃, passes into 99.9% CO in reactor
2Gas stops air inlet after reaching 4.00Mpa, opens magnetic stirring apparatus (500 rev/mins) in the still, and the beginning timing, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was 180s, i.e. CO
2The hydrate induction time.
After temperature, pressure remains unchanged in the autoclave, can think CO
2Hydrate generates fully, at this moment, opens vent valve, control exhaust velocity (5～7 seconds pressure drop 0.01Mpa), decomposition of hydrate keeps temperature in the kettle constant, by pressure transmitter with the temperature, pressure data transmission to computer, record CO
2The temperature, pressure of hydrate in decomposition course when obvious speck occurring in the glass visor, recorded the equilibrium of this moment, at this moment CO
2The hydrate phase balance data are 6.0 ℃, 2.44Mpa.
Comparative example 1
Other experiment conditions are identical with embodiment 3, only change the kind of hydrate accelerant:
Inject 700ppm1-(3-sulfonic group) propyl group U-4527 hydrosulfate ([HMIPS] Ss) solution of 200mL in the autoclave, vacuumize 30min.
Open water bath with thermostatic control, the control bath temperature is 6.0 ℃, passes into 99.9% CO in reactor
2Gas stops air inlet after reaching 4.00Mpa, opens magnetic stirring apparatus (500 rev/mins) in the still, and the beginning timing, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was 550s, i.e. CO
2The hydrate induction time.
Comparative Examples 2
Other experiment conditions are identical with embodiment 3, only change the kind of hydrate accelerant:
Inject the 700ppm Sodium dodecylbenzene sulfonate solution of 200mL in the autoclave, vacuumize 30min.
Open water bath with thermostatic control, the control bath temperature is 6.0 ℃, passes into 99.9% CO in reactor
2Gas stops air inlet after reaching 4.00Mpa, opens magnetic stirring apparatus (500 rev/mins) in the still, and the beginning timing, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was 450s, i.e. CO
2The hydrate induction time.
In the time of 6 ℃, under the original pressure 4.0MPa condition, the induction time 610s of pure aquatic system, from Comparative Examples 1,2, can find out, used other hydrate accelerant, the amplitude that induction time descends is limited, and uses surface-active ion liquid of the present invention as hydrate accelerant, and the amplitude that induction time descends is fairly obvious.
Comparative example 3
Other experiment conditions are identical with embodiment 6, only change the kind of hydrate accelerant:
Inject 300ppm1-(3-sulfonic group) the propyl group U-4527 p-methyl benzenesulfonic acid solution of 200mL in the autoclave, vacuumize 30min.
Open water bath with thermostatic control, the control bath temperature is 4.0 ℃, passes into 99.9% CO in reactor
2Gas stops air inlet after reaching 3.50Mpa, opens magnetic stirring apparatus (500 rev/mins) in the still, and the beginning timing, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was 510s, i.e. CO
2The hydrate induction time.
Comparative example 4
Other experiment conditions are identical with embodiment 6, only change the kind of hydrate accelerant:
Inject the 300ppm Sodium dodecylbenzene sulfonate solution of 200mL in the autoclave, vacuumize 30min.
Open water bath with thermostatic control, the control bath temperature is 4.0 ℃, passes into 99.9% CO in reactor
2Gas stops air inlet after reaching 3.50Mpa, opens magnetic stirring apparatus (500 rev/mins) in the still, and the beginning timing, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was 400s, i.e. CO
2The hydrate induction time.
In the time of 4 ℃, under the original pressure 3.50MPa condition, the induction time 550s of pure aquatic system, from Comparative Examples 3,4, can find out, used other hydrate accelerant, the amplitude that induction time descends is limited, and uses surface-active ion liquid of the present invention as hydrate accelerant, and the amplitude that induction time descends is fairly obvious.
Claims (5)
1. CO
2Hydrate accelerant is characterized in that: described CO
2Hydrate accelerant is a kind of surface-active ion liquid, and wherein, the positively charged ion of ionic liquid is selected from, 1-(3-sulfonic group) propyl group U-4527 positively charged ion or 1-(3-sulfonic group) propyl pyrrole alkane positively charged ion; Negatively charged ion is Witco 1298 Soft Acid root negatively charged ion.
2. CO as claimed in claim 1
2The application of hydrate accelerant is characterized in that: described application is specially, and first the surface-active ion liquid-mixing is made the certain density aqueous solution, and concentration range is 100ppm～900ppm,
(1) injects the aqueous solution of above-mentioned surface-active ion liquid in the autoclave, open pumped vacuum systems, extract the gas in reactor and the pipeline, pumpdown time 30min;
(2) control bath temperature keeps temperature in the kettle stable, passes into CO with topping-up pump and air compressor machine in reactor
2Gas stops air inlet after reaching specified pressure, when treating that drop in temperature is to design temperature in the autoclave, opens magnetic stirring apparatus in the still, and the beginning timing, at this moment, and CO
2Hydrate generates fast, and visible CO is arranged in the glass visor
2When the hydrate nucleus occurred, required time was CO
2The induction time of hydrate;
(3) after temperature, pressure remains unchanged in the autoclave, can think CO
2Hydrate generates fully, opens vent valve, the control exhaust velocity, 5～7 second pressure drop 0.01Mpa, keep temperature in the kettle constant, by pressure transmitter with the temperature, pressure data transmission to computer, record CO
2The temperature, pressure of hydrate in decomposition course by the sight glass visor, finds CO
2Balancing each other a little of hydrate.
3. CO as claimed in claim 2
2The application of hydrate accelerant is characterized in that: the temperature in the kettle described in the step (2) is 2 ℃～10 ℃.
4. CO as claimed in claim 2
2The application of hydrate accelerant is characterized in that: the specified pressure described in the step (2) is 3-5Mpa.
5. CO as claimed in claim 2
2The application of hydrate accelerant is characterized in that: pass through the sight glass visor described in the step (3), find CO
2Balancing each other a little of hydrate refers to record the equilibrium of this moment, i.e. CO when obvious speck occurring in the glass visor
2Balancing each other a little of hydrate.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310204977.0A CN103304479B (en) | 2013-05-28 | 2013-05-28 | Promoter for CO2 hydrate and application of promoter |
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|---|---|---|---|
| CN201310204977.0A CN103304479B (en) | 2013-05-28 | 2013-05-28 | Promoter for CO2 hydrate and application of promoter |
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| CN103304479B CN103304479B (en) | 2015-07-01 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109609226A (en) * | 2018-12-29 | 2019-04-12 | 郑州大学 | The new application of pyrrolidines |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2755790C1 (en) * | 2020-12-14 | 2021-09-21 | федеральное государственное автономное образовательное учреждение высшего образования "Казанский (Приволжский) федеральный университет" (ФГАОУ ВО КФУ) | Promoter of hydrate formation based on castor oil |
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| US6352576B1 (en) * | 2000-03-30 | 2002-03-05 | The Regents Of The University Of California | Methods of selectively separating CO2 from a multicomponent gaseous stream using CO2 hydrate promoters |
| CN102603674A (en) * | 2012-02-20 | 2012-07-25 | 常州大学 | Gas hydrate generation promoter and preparation method thereof |
| CN102887873A (en) * | 2012-09-12 | 2013-01-23 | 常州大学 | Ionic liquids with surface active function and preparation method for ionic liquids |
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2013
- 2013-05-28 CN CN201310204977.0A patent/CN103304479B/en active Active
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|---|---|---|---|---|
| US6352576B1 (en) * | 2000-03-30 | 2002-03-05 | The Regents Of The University Of California | Methods of selectively separating CO2 from a multicomponent gaseous stream using CO2 hydrate promoters |
| CN102603674A (en) * | 2012-02-20 | 2012-07-25 | 常州大学 | Gas hydrate generation promoter and preparation method thereof |
| CN102887873A (en) * | 2012-09-12 | 2013-01-23 | 常州大学 | Ionic liquids with surface active function and preparation method for ionic liquids |
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| Title |
|---|
| XIAO-SEN LI 等: "Tetra-n-butyl ammonium bromide semi-clathrate hydrate process for post-combustion capture of carbon dioxide in the presence of dodecyl trimethyl ammonium chloride", 《ENERGY》, vol. 35, no. 9, 30 September 2010 (2010-09-30) * |
| 周诗岽 等: "十六烷基三甲基溴化铵促进CO2水合物生成的实验研究", 《现代化工》, vol. 33, no. 2, 20 February 2013 (2013-02-20) * |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109609226A (en) * | 2018-12-29 | 2019-04-12 | 郑州大学 | The new application of pyrrolidines |
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