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Separation using ionic liquid solvents

An ionic liquid solvent and ion technology, applied in the separation of dispersed particles, separation methods, gas treatment, etc., can solve the problems of high reflux ratio cost limitation, low efficiency, poor diffusion rate of ionic liquid membrane, large capital expenditure, etc.

Active Publication Date: 2020-11-20
CHEVRON PHILLIPS CHEMICAL CO LP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Distillation requires many stages and / or high reflux ratios and can be cost prohibitive when fluid components have close boiling points
Ionic liquid membranes are limited by membrane diffusion rate and can have poor flux or require considerable capital expenditure for commercial applications
Water in an aqueous metal salt solution has a considerable vapor pressure, which makes recovery of the separated components from the aqueous solution inefficient (for example, after the components are separated from the aqueous solution, the water usually carries the components with it, which requires dehydration)

Method used

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  • Separation using ionic liquid solvents
  • Separation using ionic liquid solvents
  • Separation using ionic liquid solvents

Examples

Experimental program
Comparison scheme
Effect test

example 1

[0112] Example 1 uses figure 1 system 100 . figure 1 Process stream 111 is fed to the bottom of separator 110. The composition and conditions of process stream 111 for Example 1 are given in Table 1 below:

[0113] Table 1

[0114]

[0115] A solvent stream 122 comprising an ionic liquid solvent is fed to the top of separator 110 . The pressure of separator 110 is about 186 psia, and the temperature is about 30°C. The ionic liquid solvent is bis(trifluoromethanesulfonyl)amide silver(I)([Ag(I)][Tf 2 N]) in ethylmethylimidazolium bis(trifluoromethanesulfonyl)amide ([emim][Tf 2 N]) in solution, expressed as [emim][Tf 2 N]-Ag, and the concentration of Ag(I) in the ionic liquid solvent is about 1.8N.

[0116] In separator 110, gaseous hydrogen, nitrogen, ethane, ethylene, and isobutane rise through the ionic liquid solvent, and ethylene is captured (via absorption and complexation as described herein) into [emim][Tf 2 N]-Ag, while isobutane is physically adsorbed. with ...

example 2

[0120] Example 2 uses figure 1 system 100 . Contains gaseous hydrogen, nitrogen, ethane, ethylene, and isobutane figure 1 Process stream 111 is fed to the bottom of separator 110. The composition and conditions of process stream 111 for Example 2 are given in Table 1 above. A solvent stream 122 comprising an ionic liquid solvent is fed to the top of separator 110 .

[0121] The pressure of separator 110 is about 186 psia, and the temperature is about 30°C. The ionic liquid solvent is [emim][Tf 2 N]-Ag, and the concentration of Ag(I) in the ionic liquid solvent is about 1.8N.

[0122] In separator 110, gaseous ethane, ethylene, and isobutane rise through the ionic liquid solvent, and ethylene is captured (via absorption and complexation as described herein) into [emim][Tf 2 N]-Ag. with [emim][Tf 2 N]-Ag complexed ethylene exits separator 110 and flows to regenerator 120 via captured stream 113 . In regenerator 120 where the pressure is about 16 psia and the temperatu...

example 3

[0126] Example 3 uses figure 2 system 200. Contains gaseous hydrogen, nitrogen, ethane, ethylene, and isobutane figure 1 Process stream 111 is fed to the bottom of separator 110. The composition and conditions of process stream 111 for Example 3 are shown in Table 2 below:

[0127] Table 2

[0128]

[0129] A solvent stream 122 comprising an ionic liquid solvent is fed to the top of separator 110 . The pressure of separator 110 is about 186 psia, and the temperature is about 30°C. The ionic liquid solvent is [emim][Tf 2 N]-Ag, and the concentration of Ag(I) in the ionic liquid solvent is about 1.8N.

[0130] In separator 110, gaseous ethane, ethylene, and isobutane rise through the ionic liquid solvent, and ethylene is absorbed (via complexation as described herein) into [emim][Tf 2 N]-Ag. with [emim][Tf 2 The N]-Ag complexed ethylene exits separator 110 and flows to regenerator 120 via captured stream 113 . In regenerator 120 where the pressure is 16 psia and t...

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Abstract

Disclosed are systems and methods that provide a process stream comprising a gaseous component from which an ionic liquid solvent passing through a separator captures the gaseous component and extracts the gaseous component from all The captured gas components were recovered in the ionic liquid solvent described above. A second gas component from the process stream can be captured by the ionic liquid solvent in the separator, and the second gas component can be recovered from the ionic liquid solvent in the regenerator. Alternatively, the second gas component from the process stream may not be captured by the ionic liquid solvent, and the non-captured second gas component may be recovered from the membrane unit.

Description

[0001] Cross References to Related Applications [0002] As a continuation-in-part, this application claims priority to U.S. Application Serial No. 13 / 948,861, filed July 23, 2013, and entitled "Separations with Ionic Liquid Solvents," cited in its It is incorporated herein by reference in its entirety. technical field [0003] The present invention relates to the separation of one or more gaseous components from process streams using ionic liquid solvents. Background technique [0004] In commercial processing facilities (including those in the chemical industry, petrochemical industry, polymer industry, oil and gas industry) there are many process streams that contain two or more fluid components. Examples of process streams containing two or more fluid components include: polymerization process streams, ethane cracking process streams, natural gas process streams, synthesis gas process streams, biomass gasification process streams, Fischer-Tropsch process streams, alka...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): B01D53/14
CPCB01D53/1487B01D53/1493B01D2252/30B01D2256/16B01D2256/20B01D2256/24B01D2256/245B01D2257/304B01D2257/504B01D2257/7022B01D2258/05
Inventor L·姬章艾茀M·S·迪瑞沃H-K·C·蒂姆肯
Owner CHEVRON PHILLIPS CHEMICAL CO LP