WO2012037736A1 - 离子液体溶剂和气体净化方法 - Google Patents
离子液体溶剂和气体净化方法 Download PDFInfo
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- WO2012037736A1 WO2012037736A1 PCT/CN2010/077326 CN2010077326W WO2012037736A1 WO 2012037736 A1 WO2012037736 A1 WO 2012037736A1 CN 2010077326 W CN2010077326 W CN 2010077326W WO 2012037736 A1 WO2012037736 A1 WO 2012037736A1
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- ion
- ionic liquid
- gas
- absorption
- absorbent
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20436—Cyclic amines
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20478—Alkanolamines
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/30—Ionic liquids and zwitter-ions
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/60—Additives
- B01D2252/602—Activators, promoting agents, catalytic agents or enzymes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/206—Organic halogen compounds
- B01D2257/2064—Chlorine
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/304—Hydrogen sulfide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Definitions
- the wood invention mainly relates to an ionic liquid solvent gas purification process, which is: 1 body, involving a novel ionic liquid solvent and a gas cleaning method using the ionic liquid hydrazine solvent.
- ionic liquid As a new type of green solvent, ionic liquid has the advantages of good recycling, low volatility, low pollution tt, low energy consumption, adjustable structure and performance, good physical and chemical stability and environmental friendliness. It is widely used in the fields of separation, catalysis, gas absorption, etc., and is an ideal solvent for gas purification.
- the absorbent for purifying carbon dioxide and the like is mainly an alcohol amine compound or a mixture thereof, but the energy consumption is too high, and the loss of volatilization of the absorbent is too large.
- a conventional ionic liquid is used to purify a gas such as carbon dioxide, there may be problems such as high solvent viscosity and poor transfer efficiency. Therefore, it is particularly desirable to purify a gas having a low viscosity, suitable for carbon dioxide, sulfur dioxide, hydrogen chloride, hydrogen sulfide, etc., which has a large absorption capacity and is easy to desorb after absorption of gas, has low energy consumption, good stability, and high recyclability. Liquid solvent.
- the present invention - aspects relate to a novel ionic liquid solvent for gas purification and separation.
- the ionic liquid solvent main absorbent of the invention the main absorbent adjusting agent, the auxiliary absorbent, the activator, the antioxidant and the water, wherein the alcoholic amine functionalized ionic liquid containing 2-95% by mass is used as the main absorption 0-30% by mass of heterocyclic ionic liquid or amino acid ionic liquid as main absorbent regulator; 0.1-30% by mass of alcohol amine organic solvent as auxiliary absorbent; 0-5% mass concentration Activator, 0.1-1% by mass of antioxidants and
- Another aspect of the invention relates to a method based on ionic liquid solvent gasification, which adopts the above-mentioned wood invention ionic liquid solvent, wherein the liquid solvent can have a force of 0.1 MPa-10 MPa and a temperature of 1 "C -98 °"
- the gas is absorbed under C, and the gas is desorbed at a pressure of i 0.1 MPa to 5 MPa and a temperature of 40 to 300 °C.
- the novel ionic liquid solvent in the invention adopts a low temperature absorption and heating regeneration process in practical applications, and the ionic liquid used in the invention has low synthesis cost, low viscosity, high absorption capacity, and is easy to regenerate and recycle.
- the use of this solvent uses a conventional absorption regeneration process to purify the gas, which has the advantages of large absorption capacity, low energy consumption, and low operating cost compared with the conventional process.
- DRAWINGS Ml is the multi-stage absorption tower gas purification method used in the ionic liquid solvent gas purification method of the present invention
- the cabinet 2 is a process flow of the ionic liquid solvent method gas purification of the present invention.
- one or more of the main absorbents, the alkanolamine ionic liquid, which is separated from the liquid solvent, has the following structural formula: AB, wherein A has the following structural formula:
- the B is an ⁇ F anion: chloride ion (CD, bromide (Bf), iodide ion ( ⁇ :), tetrafluoroborate ion (131 ⁇ ), hexafluoro Phosphate ion (PF 6 _), hydroxide ion (OH-), carbonate ion (C0 3 2 — ), hydrogencarbonate ion (H: C0 3 _), acetate ion (C3 ⁇ 4COO carboxylate (RCOO - ), alkoxide (RO-), phenate (PhO-), trimethylsulfonamide ion (Tf 2 N -), tri-gas methylsulfon
- the main absorbent When the concentration range is 2-95%, the effect of purifying the gas is better. In addition, the desorption energy consumption is lower when the concentration of the main absorbent is in the range of 2-95%.
- the more preferable concentration range of the main absorbent is 25-80% by mass.
- the ring-type ionic liquid and the base acid ionic liquid can be used as a regulator of the main absorbent.
- the heterocyclic ionic liquid cation mainly includes: spiropyrans, furans, pyridines, phenothiazines, and imidazoles, pyrrole, Pyrazoles, azoles, thiazoles, anthraquinones, pyridoxines, pyridazines, quinolines, morpholines, quinazolines, piperazines, piperidines, azoles, 1 oxazoline,
- the heterocyclic species are separated from the liquid anion mainly include: chloride ion (cr), bismuth (Bf), iodide ion ( ⁇ ), tetrafluoroborate ion ( BF 4 "), hexafluorophosphate ion (PF 6 _), hydroxide ion (OH -), carbonate ion (CO -), bicarbonate ion (HC (V), acetate ion (C
- the inducing agent of the invention may be adapted to adjust the physicochemical properties of the main absorbent, such as viscosity, density, acidity and alkalinity, corrosivity, etc., and the concentration range thereof is adapted according to the physical and chemical properties of the ionic liquid solvent after the addition of the regulator:
- the ground is selected in the range of 0-30% by mass, more preferably 0.1 10% by mass, most preferably 0.5-5% by mass.
- the auxiliary absorbent alcohol amine organic solvent in the present invention is composed of one or more substances having the following structures, such as ethanolamine, diethanolamine, triethanolamine, hydrazine-methyldiethanolamine, and diglycolamine:
- the auxiliary absorbent can effectively increase the amount of the main absorbent purification gas per unit mass, but the excessive amount of the auxiliary absorbent may affect the effect of the ionic liquid solvent purifying gas. Therefore, the concentration of the auxiliary absorbent preferably ranges from 0.5 to 30% by mass. More preferably, it is 0.5-20% by mass.
- the activator in the present invention is one or more of aminoacetic acid, imidazole, methylimidazole, sulfolane, piperazine, hydroxyethyldiamine, ethylenediamine, tetramethylpropanediamine and derivatives thereof.
- the activator can effectively increase the rate of purifying the gas per unit mass of the main absorbent, and the concentration thereof preferably ranges from 0 to 5% by mass.
- the antioxidant is composed of one or two of hydroquinone, tannin, and bismuth. It is used to improve the stability of the ionic liquid solvent, and its concentration range does not affect the ionic liquid solvent. The performance is appropriate: ⁇ 0. Bu 1% mass concentration.
- the ionic liquid solvent composed of the components of the present invention in the present invention may have a pressure of 0.1 MPa to 10 MPa and a temperature of 1. C-98.
- the C-F absorbing gas desorbs the gas at a pressure of 0.1 MPa to 5 MPa and a temperature of 40 Torr to 300 Torr. Therefore, the ionic liquid solvent of the present invention can provide a method for purifying a gas based on an ionic liquid solvent.
- the gas involved in the gas purification method of the present invention includes: carbon dioxide, sulfur dioxide, hydrogen chloride, hydrogen sulfide, nitrogen oxides (N(:V), sulfur oxides (SO,), ammonia, hydrogen, carbon monoxide, helium, acetonitrile, One or more of propylene glycol, ether, diethyl ether, ethylene, propylene, acetylene, formaldehyde, stabilizing, monohydric, dichloromethane, gas, and oxygen.
- the ionic liquid solvent of the present invention is particularly useful for removing acid gases such as carbon dioxide. Effective, but also used for gases other than acid gases, including the neutral gases mentioned above or some weakly aggressive gases. F and the liquid solvent process gasification process of the present invention are described with reference to the accompanying drawings.
- the purification process of the present invention uses a multi-stage column to purify the gas, which reduces the energy consumption during gas absorption.
- the patented multi-stage absorption tower has good operational flexibility, that is, it can perform single-stage absorption, two-stage absorption, and can also perform multi-stage absorption.
- the two-stage absorption tower is composed of the main mountain k and the lower two towers (the primary tower and the secondary tower). It is equipped with temperature and force display, control and display; the inlet and outlet are equipped with temperature, £1 force and material control device. Transitions can be provided between different tower sections.
- Multistage absorption towers nf are bubble towers, packed towers and towers.
- the tower body material is alloy steel, and the inside of the tower body is coated with anti-corrosive materials, and the main body includes zinc silicate paint, alkyd red dan antirust primer, iron red iron antirust primer, alkyd cloud iron antirust primer or Intermediate paint, alkyd enamel, epoxy red enamel, epoxy zinc-rich paint, epoxy iron red paint, epoxy phosphoric acid paint epoxy iron paint, fluorocarbon paint, silicone paint.
- the feeding method of the two-stage absorption tower is shown in Figure I.
- the process flow of the present invention will be described by taking a two-stage absorption/desorption process as an example.
- the mountain multi-stage absorption tower Il enters, the semi-lean liquid enters from the tower, and the two feeds are absorbed in countercurrent contact with the feed gas feed at the bottom of the tower, and the purified gas is taken from the tower.
- the top discharge enters the purifier separator to remove the entrained liquid; the absorption gas enters the liquid phase to form a rich liquid stream, the bottom of the mountain tower discharges, and enters the rich liquid flash tank to remove the entrained other gas, and then
- the mountain solvent heat exchanger enters the upper part of the desorption tower, it is desorbed by heat, and the top of the gas phase mountain tower is discharged.
- the mountain regeneration cooler After passing through the mountain regeneration cooler, it enters the regeneration gas separator to obtain high-purity regeneration gas.
- the liquid discharge at the bottom of the separator enters the gas stripping regeneration. At the bottom of the tower, it is further desorbed by heat, and the whole lean liquid is obtained, and is discharged from the bottom of the tower.
- the multi-stage absorption tower and the desorption tower have high temperature and high pressure resistant materials, the high temperature resistant high pressure material is ceramic material or butyl rubber; the multistage absorption tower has high temperature resistant high pressure spray pipe; the multistage absorption tower and the desorption tower have stirring S 1 ; multi-stage absorption tower, desorption tower, regenerative cooler, regeneration gas separation tank, purification gas separator with heat exchange device, can also have 3 ⁇ 41 fog sprayer, demister material is high temperature resistant high 1 glass or ceramic .
- the multistage absorption tower can be a scrubber and a sedimentation tank; the desorption tower can have a sedimentation tank.
- the multistage absorption tower and the desorption column have a continuously distributed scaly structure; the scaly structure has a trapezoidal or circular cross section.
- Example 1 The experimental setup consisted of a four-necked flask, a reflux condenser, a mechanical stirrer, and a mercury thermometer. Accurate weighing
- the experimental setup is as above. Accurately weigh 61.08 g of ethanolamine and 219.613 g of tetrafluoroboric acid.
- Ethanol The amine was dissolved in 12.9 ml of ethanol and added to a four-IJ flask, and then tetra-boric acid was mixed with 56.3 ml of the drunken funnel and placed in a dropping funnel. )) ⁇ mechanical stirrer, slowly drip the tetrafluoroboric acid solution into the dip-amine solution with a dropping funnel under stirring, and drip in 30 minutes. The reaction was carried out under normal temperature and normal pressure for 24 hours. Finally, the obtained liquid was dried in a vacuum oven at 50 Torr for 40 hours to obtain 148.830 g of N (CH 2 C 3 ⁇ 4 OH) BF 4 ionic liquid, and the yield was 99.94%.
- 3 ⁇ 4 inspection S is as above. Accurately weigh the amount of the substance] 19.202 g of N-methyldiethanolamine and 95.947 g of hydrochloric acid. After dissolving N-methyldiisopropylamine in 25.2 ml of ethanol, it was added to a four 1 1 flask, and then hydrochloric acid was mixed with 56.3 ml of a drunken funnel into a dropping funnel. The mechanical stirrer was smashed, and the hydrochloric acid solution was slowly dropped into the N-methyldiethanolamine solution with a dropping funnel while stirring, and the dropwise addition was completed in 30 minutes.
- the experimental setup is as above.
- the amount of the substance such as 19.202 g of N-methyldiethanolamine and 145.972 g of hexafluorophosphoric acid were accurately weighed.
- the mechanical stirrer was turned on, and the hexafluorophosphoric acid solution was slowly dropped into the N-methyldiethanolamine solution by stirring in a dropping funnel, and the mixture was dropped in 30 minutes.
- the absorption temperature is 30 ° C and the pressure is 1.6 MPa.
- the absorption of C0 2 is detected by on-line gas chromatography until the absorption equilibrium of C0 2 is ⁇ , and the equilibrium time is about 8-10 ⁇ .
- the absorption capacity of 0.0530 g CO 2 /g of absorbent can be calculated from the data recorded by gas chromatography.
- the absorption experiment device is mainly composed of an absorption reaction kettle and a gas chromatograph. Weigh a certain amount of triethanolamine and water
- Absorption temperature 3 (TC, Hill 1.6MPa, the absorption of C0 2 is detected by the on-line gas color during absorption, straightening 3 ⁇ 4 [0 2 absorption equilibrium, I'nJ is about 8-10 hours at equilibrium. According to gas chromatography The recorded data can be calculated to have an absorption capacity of 0.125 gC0 2 /g of absorbent.
- the synthesized ionic liquid, diisopropylamine fluoroborate NH 2 (CH 2 CH 2 OH) 2 BF 4 is placed in a vacuum T-drying T to remove moisture, accurately weighed a certain amount: .
- the gas mass flow ffiil was used: a mixed gas of nitrogen and carbon dioxide was introduced, wherein the flow rate of N 2 was 300 ml/min, and the flow rate of C 2 2 was 100 ml/min.
- the absorption capacity of 0.137 gC0 2 /g of absorbent can be calculated from the data recorded by gas chromatography.
- the ionic liquid triethanolamine bromide salt NH(CH 2 CH 2 OH) 3 Br was synthesized in a similar manner to the synthesis example described in the following, and placed in a vacuum drying oven to remove moisture, accurately weighing a certain amount.
- a gas mass flow meter is used to quantitatively introduce a mixed gas of nitrogen and carbon dioxide, wherein N 2 flow I: 300 ml/min, and C0 2 flow is 100 ml/min.
- I'nj is about 8-10 hours.
- the absorption capacity of 0.134 gC0 2 /g of absorbent can be calculated from the data recorded by gas chromatography.
- the synthesized ionic liquid diethanolamine hydrochloride NH 2 (CH 2 CH 2 0H) 2 C1 was placed in a vacuum drying bath to remove water, and about 600 ml was poured into an absorption reactor. Nitrogen and carbon dioxide are set by using a gas-filled flow meter A mixed gas in which N 2 flow is 300 ml/min, and C0 2 flow is 100 ml/min.
- the absorption temperature is 40 °C
- the ffi force is 1.6MPa
- the absorption of co 2 is detected by the on-line gas chromatograph during absorption.
- the 1 benzyl tributyl hydrazine amino acid salt is a hydrazine absorber modifier.
- ⁇ Use the body 3 ⁇ 4 stream M: ⁇ quantitatively pass a mixture of nitrogen and carbon dioxide, the ⁇ N:; flow rate 300ml / min, C0 2 flow: 100ml / rain.
- the absorption temperature is 30'C and the pressure is 1.6MPa.
- the absorption of C0 2 is detected by on-line gas chromatography until the absorption of C0 2 is balanced.
- the equilibrium time is about 5-6 hours.
- the equilibrium time is better than the addition of the main absorbent.
- the absorption capacity of 0.162 gC0 2 /g of absorbent can be calculated, and the absorption amount is better than before the addition of the main absorbent modifier.
- the rich gas ionic liquid solvent is at a pressure of 0.1 MPa, 0.3 MPa, temperature 70 ⁇ ⁇ 120 Desorption in the range of V.
- the decomposed liquid solvent is circulated into the multistage absorption tower.
- the new process of low energy consumption, the purity of C0 2 captured by the new work ⁇ capture system is 99.5%.
- the liquid C0 2 purity is 3 ⁇ 4 99.997%, which meets the national food grade standard.
- the energy saving effect is >30%, reaching the world advanced level.
- the total cost of absorbing carbon dioxide is 13% lower than the total cost of the existing carbon dioxide absorption process.
- the amount of carbon dioxide absorbed by the new solvent in the bismuth quality is 10% higher than that of the existing carbon dioxide absorbing process.
- the new solvent has low volatility. Carbon dioxide absorption and desorption in each process The amount of agent loss is ⁇ 0.5%. The desorption efficiency is >99%, and the desorption time is 30% shorter than the existing carbon dioxide absorption process.
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US13/823,707 US9358497B2 (en) | 2010-09-26 | 2010-09-26 | Ionic liquid solvent and gas purification method using the same |
JP2013529524A JP5717112B2 (ja) | 2010-09-26 | 2010-09-26 | イオン液体溶媒とガス浄化方法 |
PCT/CN2010/077326 WO2012037736A1 (zh) | 2010-09-26 | 2010-09-26 | 离子液体溶剂和气体净化方法 |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
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PCT/CN2010/077326 WO2012037736A1 (zh) | 2010-09-26 | 2010-09-26 | 离子液体溶剂和气体净化方法 |
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WO2012037736A1 true WO2012037736A1 (zh) | 2012-03-29 |
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PCT/CN2010/077326 WO2012037736A1 (zh) | 2010-09-26 | 2010-09-26 | 离子液体溶剂和气体净化方法 |
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US (1) | US9358497B2 (zh) |
JP (1) | JP5717112B2 (zh) |
WO (1) | WO2012037736A1 (zh) |
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WO2015047712A1 (en) * | 2013-09-30 | 2015-04-02 | Uop Llc | Ionic liquid and solvent mixtures for hydrogen sulfide removal |
CN105408003A (zh) * | 2013-07-23 | 2016-03-16 | 切弗朗菲利浦化学公司 | 使用离子液体溶剂进行的分离 |
CN110105228A (zh) * | 2019-06-05 | 2019-08-09 | 中国科学院兰州化学物理研究所 | 一种质子型离子液体及其制备方法和作为水基润滑添加剂的应用 |
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WO2015047712A1 (en) * | 2013-09-30 | 2015-04-02 | Uop Llc | Ionic liquid and solvent mixtures for hydrogen sulfide removal |
EA034098B1 (ru) * | 2013-09-30 | 2019-12-26 | Юоп Ллк | Смеси из ионной жидкости и растворителя для удаления сероводорода |
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CN110105228A (zh) * | 2019-06-05 | 2019-08-09 | 中国科学院兰州化学物理研究所 | 一种质子型离子液体及其制备方法和作为水基润滑添加剂的应用 |
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US9358497B2 (en) | 2016-06-07 |
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