# US 5,350,519 A · Pervaporation process and use in treating waste stream from glycol dehydrator > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 5,350,519 A - Document ID: US5350519A - Status: Granted - Kind: A - Application number: 08/093,819 - Filed: 1993-07-19 - Granted: 1994-09-27 - Earliest claimed: 1993-07-19 - Assignees: Membrane Technology and Research, Inc. - Inventors: Jurgen Kaschemekat; Richard W. Baker - Web page: https://patentgrep.com/patent/US5350519A ## CPC - B01D 61/362: {Pervaporation} - C02F 1/44: by dialysis, osmosis or reverse osmosis {(general membrane separation processes B01D61/00, membrane modules B01D63/00, electrodialysis C02F1/4693, combination of membrane modules and bioreactors C02F3/1268)} - C02F 1/448: {by pervaporation} - B01D: SEPARATION (separating solids from solids by wet methods B03B, B03D; by pneumatic jigs or tables B03B; by other dry methods B07; magnetic or electrostatic separation of solid materials from solid materials or fluids, separation by high-voltage electric fields B03C; centrifuges, vortex apparatus B04; presses per se for squeezing-out liquid from liquid-containing material B30B9/02; treatment of water C02F, e.g. softening by ion-exchange C02F1/42; {arrangements of air intake cleaners in gas turbine plants F02C7/05} ; arrangements or mounting of filters in air-conditioning, air-humidification or ventilation F24F13/28) - C02F: TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE (separation in general B01D; special arrangements on waterborne vessels of installations for treating water, waste water or sewage, e.g. for producing fresh water, B63J; adding materials to water to prevent corrosion C23F; treating radioactively-contaminated liquids G21F9/04; regeneration of reactants for recirculation into processes, see the relevant places for the processes) ## Abstract Pervaporation processes and apparatus with few moving parts. Ideally, only one pump is used to provide essentially all of the motive power and driving force needed. The process is particularly useful for handling small streams with flow rates less than about 700 gpd. Specifically, the process can be used to treat waste streams from glycol dehydrator regeneration units. ## Claims ### Claim 1 A process for treating a waste stream from a glycol dehydrator regeneration process, comprising the steps of: (i) withdrawing from said regeneration process an incoming waste stream comprising steam and an organic compound; (ii) condensing at least a portion of said waste stream; (iii) passing at least a portion of the resulting at-least-partially condensed waste stream through a liquid-ring pump and thence to a separator wherein an over-pressure can be maintained by said liquid-ring pump; (iv) using said over-pressure at least as part of a motive force to pass an aqueous liquid stream from said separator across the feed side of a pervaporation unit having a feed side and a permeate side, on which permeate side a reduced pressure is maintained by connecting said liquid-ring pump on its suction side to said permeate side; (v) withdrawing from said feed side a water stream depleted in organic compound compared with said aqueous liquid stream; (vi) withdrawing from said permeate side a permeate stream enriched in organic compound compared with said aqueous liquid stream, passing said permeate stream through said liquid-ring pump and returning it on the high-pressure side to said separator; (vii) using said over-pressure at least as part of a motive force to withdraw uncondensed gas from said separator; (viii) using said over-pressure at least as part of a motive force to withdraw an organic liquid phase from said separator. ### Claim 2 (depends on 1) The process of claim 1, wherein said incoming waste stream contains an organic compound chosen from the group consisting of benzene, toluene, ethylbenzene and xylene. ### Claim 3 (depends on 1) The process of claim 1, further comprising drawing said permeate stream through an integrated gas ejector upstream of said liquid-ring pump. ### Claim 4 (depends on 1) The process of claim 1, wherein said step (iv) comprises: (iv) using said over-pressure at least as part of a motive force to pass an aqueous liquid stream from said separator through a heater and thence across the feed side of a pervaporation unit having a feed side and a permeate side, on which permeate side a reduced pressure is maintained by connecting said liquid-ring pump on its suction side to said permeate side. ### Claim 5 (depends on 4) The process of claim 4, wherein said heater comprises a heat exchanger wherein said aqueous liquid stream passes in heat-exchanging relationship with said incoming waste stream. ### Claim 6 (depends on 1) The process of claim 1, wherein said step (vi) comprises: (vi) withdrawing from said permeate side a permeate stream enriched in organic compound compared with said aqueous liquid stream, condensing at least a portion of said permeate stream and passing the resulting at-least-partially condensed permeate stream through said liquid-ring pump and returning it on the high-pressure side to said separator. ### Claim 7 (depends on 1) The process of claim 1, wherein said liquid-ring pump provides essentially all of the motive force required to move fluids into, out of, and through said separator and said pervaporation unit. ### Claim 8 (depends on 1) The process of claim 1, further comprising providing additional pumping capacity to withdraw said uncondensed gas from said separator. ### Claim 9 (depends on 1) The process of claim 1, further comprising providing additional pumping capacity to withdraw said organic liquid phase from said separator. ### Claim 10 (depends on 1) The process of claim 1, wherein said water stream depleted in organic compound contains less than 100 ppmw total organic compound. ### Claim 11 (depends on 1) The process of claim 1, wherein said water stream depleted in organic compound contains less than 50 ppmw total organic compound. ### Claim 12 (depends on 1) The process of claim 1, wherein said water stream depleted in organic compound contains less than 10 ppmw total organic compound. ### Claim 13 (depends on 1) The process of claim 1, further comprising diverting a portion of said aqueous liquid stream to recirculate directly into said liquid-ring pump. ### Claim 14 Liquid-treating apparatus, comprising a feed conduit, a separator having an inlet and three outlets, a pervaporation unit having a feed side and a permeate side, and a liquid-ring pump having a high-pressure side and a suction side, wherein; (i) an over-pressure can be maintained in said separator by connecting said liquid-ring pump on its high-pressure side to said inlet of said separator; (ii) one of said outlets of said separator is in liquid-transmitting connection with said feed side of said pervaporation unit; (iii) said permeate side of said pervaporation unit is maintained at reduced pressure by connecting said liquid-ring pump on its suction side to said permeate side; (iv) said feed conduit is connected to said liquid-ring pump so that fluid flowing in said feed conduit can pass into said liquid-ring pump; (v) said over-pressure is sufficient at least to provide part of a motive force to drive a liquid stream from one of said outlets of said separator across said feed side of said pervaporation unit and is sufficient at least to provide part of a motive force to drive withdrawal of a second liquid stream from the second outlet of said separator and withdrawal of a gaseous stream from the third outlet of said separator; (vi) said reduced pressure is sufficient to drive transmembrane permeation in said pervaporation unit. ### Claim 15 (depends on 14) The apparatus of claim 14, further comprising a condenser positioned between said permeate side of said pervaporation unit and said suction side of said liquid-ring pump. ### Claim 16 (depends on 14) The apparatus of claim 14, further comprising a condenser positioned in said feed conduit upstream of said liquid-ring pump to create a liquid or partially liquid stream to be treated by said apparatus. ### Claim 17 (depends on 14) The apparatus of claim 14, further comprising a heater positioned so as to heat liquid passing from said separator to said pervaporation unit. ### Claim 18 (depends on 17) The apparatus of claim 17, wherein said heater comprises a heat exchanger wherein said liquid passing from said separator to said pervaporation unit is heated by passing in heat-exchanging relationship with an incoming fluid flowing in said feed conduit. ### Claim 19 (depends on 14) The apparatus of claim 14, wherein said liquid-ring pump provides essentially all of the motive force required to move fluids into, out of and through said apparatus. ### Claim 20 (depends on 14) The apparatus of claim 14, further comprising an additional pump positioned in liquid-transmitting connection between said separator and said pervaporation unit. ### Claim 21 (depends on 14) The apparatus of claim 14, further comprising an additional pump for pumping a gas phase out of said separator. ### Claim 22 (depends on 14) The apparatus of claim 14, further comprising an additional pump for pumping a second liquid stream out of said separator. ### Claim 23 (depends on 14) The apparatus of claim 14, further comprising an integrated gas ejector positioned between said permeate side and said suction side of said liquid-ring pump. ### Claim 24 (depends on 14) The apparatus of claim 14, further comprising a connecting line to divert a portion of liquid that would otherwise pass to said pervaporation unit to recirculate directly into said liquid-ring pump. ### Claim 25 A pervaporation process, comprising the steps of: (i) passing a stream for treatment by pervaporation through a liquid-ring pump and thence to a separator wherein an over-pressure can be maintained by said liquid-ring pump; (ii) using said over-pressure at least as part of a motive force to pass a first liquid phase from said separator across the feed side of a pervaporation unit having a feed side and a permeate side, on which permeate side a reduced pressure is maintained by connecting said liquid-ring pump on its suction side to said permeate side; (iii) withdrawing from said feed side a liquid stream depleted in one component compared with said first liquid phase; (iv) withdrawing from said permeate side a permeate stream enriched in said one component compared with said first liquid phase; passing said permeate stream through said liquid-ring pump and returning it on the high-pressure side to said separator; (v) using said over-pressure at least as part of a motive force to withdraw a gaseous phase from said separator; (vi) using said over-pressure at least as part of a motive force to withdraw a second liquid phase from said separator. ### Claim 26 (depends on 25) The process of claim 25, wherein said stream for treatment by pervaporation comprises water. ### Claim 27 (depends on 25) The process of claim 25, wherein said stream for treatment by pervaporation comprises an organic compound. ### Claim 28 (depends on 25) The process of claim 25, wherein said stream for treatment by pervaporation comprises at least two organic compounds. ### Claim 29 (depends on 25) The process of claim 25, wherein said first liquid phase comprises water. ### Claim 30 (depends on 25) The process of claim 25, wherein said first liquid phase comprises an organic liquid. ### Claim 31 (depends on 25) The process of claim 25, wherein said second liquid phase comprises an organic liquid. ### Claim 32 (depends on 25) The process of claim 25, wherein said second liquid phase comprises water. ### Claim 33 (depends on 25) The process of claim 25, wherein said gaseous phase comprises organic vapor. ### Claim 34 (depends on 25) The process of claim 25, wherein said gaseous phase comprises air. ### Claim 35 (depends on 25) The process of claim 25, further comprising drawing said permeate stream through an integrated gas ejector upstream of said liquid-ring pump. ### Claim 36 (depends on 25) The process of claim 25, wherein said step (ii) comprises: (ii) using said over-pressure at least as part of a motive force to pass a first liquid phase from said separator through a heater and thence across the feed side of a pervaporation unit having a feed side and a permeate side, on which permeate side a reduced pressure is maintained by connecting said liquid-ring pump on its suction side to said permeate side. ### Claim 37 (depends on 36) The process of claim 36, wherein said heater comprises a heat exchanger wherein said first liquid phase passes in heat-exchanging relationship with said stream for treatment by pervaporation. ### Claim 38 (depends on 25) The process of claim 25, wherein said step (iv) comprises: (iv) withdrawing from said permeate side a permeate stream enriched in said one component compared with said first liquid phase, condensing at least a portion of said permeate stream and passing the resulting at-least-partially condensed permeate stream through said liquid-ring pump and returning it on the high-pressure side to said separator. ### Claim 39 (depends on 25) The process of claim 25, further comprising condensing at least a portion of said stream for treatment by pervaporation prior to step (i). ### Claim 40 (depends on 25) The process of claim 25, wherein said stream for treatment by pervaporation has a flow rate less than about 1,500 gpd. ### Claim 41 (depends on 25) The process of claim 25, wherein said stream for treatment by pervaporation has a flow rate less than about 700 gpd. ### Claim 42 (depends on 25) The process of claim 25, wherein said stream for treatment by pervaporation has a flow rate less than about 300 gpd. ### Claim 43 (depends on 25) The process of claim 25, wherein said liquid-ring pump provides essentially all of the motive force required to move fluids into, out of and through said separator and said pervaporation unit. ### Claim 44 (depends on 25) The process of claim 25, further comprising providing additional pumping capacity to withdraw said gaseous phase from said separator. ### Claim 45 (depends on 25) The process of claim 25, further comprising providing additional pumping capacity to withdraw said second liquid phase from said separator. ### Claim 46 (depends on 25) The process of claim 25, further comprising providing additional pumping capacity to pass said first liquid phase from said separator to said pervaporation unit. ### Claim 47 (depends on 25) The process of claim 25, wherein said liquid stream is depleted by at least 90% in said one component compared with said first liquid phase. ### Claim 48 (depends on 25) The process of claim 25, wherein said liquid stream is depleted by at least 95% in said one component compared with said first liquid phase. ### Claim 49 (depends on 25) The process of claim 25, wherein said liquid stream is depleted by at least 99% in said one component compared with said first liquid phase.