WO2017217708A1 - 용매 회수 장치 및 용매 회수 방법 - Google Patents
용매 회수 장치 및 용매 회수 방법 Download PDFInfo
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- WO2017217708A1 WO2017217708A1 PCT/KR2017/006056 KR2017006056W WO2017217708A1 WO 2017217708 A1 WO2017217708 A1 WO 2017217708A1 KR 2017006056 W KR2017006056 W KR 2017006056W WO 2017217708 A1 WO2017217708 A1 WO 2017217708A1
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- distillation column
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- reboiler
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- heat exchange
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J11/00—Recovery or working-up of waste materials
- C08J11/02—Recovery or working-up of waste materials of solvents, plasticisers or unreacted monomers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/343—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas
- B01D3/346—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas the gas being used for removing vapours, e.g. transport gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/38—Steam distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4205—Reflux ratio control splitter
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
- B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
- B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
- B01D5/0063—Reflux condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
- B01D5/0075—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with heat exchanging
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F6/00—Post-polymerisation treatments
- C08F6/06—Treatment of polymer solutions
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F6/00—Post-polymerisation treatments
- C08F6/06—Treatment of polymer solutions
- C08F6/10—Removal of volatile materials, e.g. solvents
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J11/00—Recovery or working-up of waste materials
- C08J11/04—Recovery or working-up of waste materials of polymers
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J11/00—Recovery or working-up of waste materials
- C08J11/04—Recovery or working-up of waste materials of polymers
- C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
- C08J11/14—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by treatment with steam or water
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Definitions
- the present application relates to a solvent recovery apparatus and a solvent recovery method in the synthetic rubber production process.
- Synthetic rubber is one of the most useful materials today and has elastic properties. However, natural rubber produced from rubber trees has limited production, and synthetic rubber is used in various fields to replace them. Synthetic rubber refers to a polymer material having the same or similar physical properties as natural rubber. Synthetic rubbers include butadiene rubber, styrene-butadiene rubber, acrylonitrile butadiene rubber and butyl rubber.
- the initiator (catalyst) is dissolved in the monomer, the monomer is dispersed in water and then the dispersant is incorporated to stabilize the formed suspension.
- surfactants are used to disperse the monomer particles so that the polymers do not fuse and agglomerate during the reaction, and various dispersants such as water-insoluble fine inorganic materials and organic materials are used depending on the monomers to be polymerized. There is a disadvantage that is lowered.
- An object of the present application is to provide a solvent recovery apparatus and a solvent recovery method.
- FIG. 1 is a schematic diagram illustrating a solvent recovery process performed in the production of a general synthetic rubber.
- a conventional synthetic rubber production process water and steam supplied from a water supply source 10 are mixed with a mixture of a polymerized polymer and a solvent and supplied to a stripping apparatus 20.
- the solvent recovered in the stripping device 20 is condensed and supplied to the distillation column 30 through the solvent inlet line 200.
- the solvent purified in the first distillation column 30 and the second distillation column 40 is recovered.
- first distillation column 30 and the second distillation column 40 use middle pressure steam (MP) as a heat source, and a large amount of energy is consumed in this process.
- MP middle pressure steam
- the present application relates to a solvent recovery apparatus and a solvent recovery method.
- waste heat of oil vapor discharged from the upper condenser of the distillation column for purifying the solvent used in the reaction in the production process of the synthetic rubber is recovered.
- this By using this to heat the water supplied to the stripping device or to use in the reboiler of the distillation column, it is possible to recover the waste heat to be discarded to save energy.
- the solvent recovery apparatus and the solvent recovery method of the present application recovers the solvent separated from the stripping apparatus after the reaction in the synthetic rubber production process, and then in the process of repurifying and reused in the distillation column, the water for supplying the stripping apparatus to the upper portion of the distillation column It can be heated by heat exchange with the effluent stream and fed to the stripper.
- "stripping" means separating and removing a gas dissolved in a liquid, and for example, may be performed by a method such as direct contact with steam, an inert gas or air, heating, and pressurization. In this specification, the stripping may be used in the same sense as stripping, dissipation or separation.
- piping system may refer to a structure including a pipe or a line connecting the devices, "line” may substantially mean the same pipe, “flow” is a fluid through the line or pipe It can mean the movement of, the lines, piping and flow herein may share the same reference numerals.
- Synthetic rubber production process of the present application includes a process for producing butadiene rubber (BR), styrene butadiene rubber (SBR), solution styrene butadiene rubber (Solution Styrene-Butadiene Rubber (SSBR), etc. .
- the adhesive material solution which is a mixture of a polymer and a solvent after the polymerization reaction, separates the solvent and the polymer by stripping using steam.
- the polymer produced after the polymerization reaction unreacted monomer and the solvent are separated by stripping after stripping, respectively.
- BR butadiene rubber
- SBR styrene butadiene rubber
- SSBR solution styrene butadiene rubber
- the amount of steam used in the stripping apparatus can be reduced by recovering and heating the waste heat from the upper condenser of the distillation column used for the solvent purification in order to supply water for the stripping apparatus used in the production process by the method of (Emulsion Polymerization).
- the amount of steam used in the distillation column may be reduced by recovering waste heat from the upper condenser of the distillation column and supplying the waste heat to the reboiler of the distillation column.
- the solvent recovery apparatus includes a solvent separation unit, a purification unit, and a piping system.
- the solvent separator may include a water supply tank 10, a stripping device 22, and a pipe connecting the water supply tank 10 and the stripping device 22.
- the pipe may include a water supply line 121 through which water is supplied, a steam supply line 131, a polymer inflow line 101 through which a polymer and a solvent are introduced.
- the said "removal apparatus” is an apparatus which can separate the multicomponent substance contained in a raw material by each boiling point difference, or a stripping apparatus for separating the substance to isolate
- a stripping device 22 a stripping device having various forms may be used in the present application in consideration of boiling points such as components of incoming raw materials or components to be separated.
- Exemplary stripping apparatus of the present application may be introduced into the high temperature water of the polymer solution and by using a steam to volatilize the solvent with water vapor to separate the solvent and the polymer.
- the stripping device may be configured such that a polymer solution containing a solvent to be recovered in the flow direction of the fluid and a stream of steam providing heat required for recovery flow in counter currents.
- the stripping apparatus may include water in the stripping apparatus to maintain a constant S / C (slurry content, mass of the rubber-like polymer in the stripping apparatus / gross mass of the contents of the stripping apparatus) in a stripping process to recover the polymer. It may be filled.
- a stripping device that can be used as the stripping device or stripper may be, for example, a distillation column or a device having a general structure, and preferably, a stripping device having two stripping devices connected to each other. Can be.
- the stripping device 22 includes a raw material supply portion to which raw materials are supplied, a first outlet for flowing out the bottom product of the stripping device 22, and a second outlet for flowing out the top product of the stripping device 22. It may include wealth.
- the first outlet may be located at the bottom of the stripping device 22 and / or at the bottom of the stripping device, and the second outlet may be located at the top of the stripping device 22 and / or on the top of the stripping device.
- the "upper” means a relatively upper portion in the stripping device, and more specifically, when the stripping device is divided into two vertically, for example, perpendicularly to the length or height direction of the stripping device. This may mean the upper part of the two divided regions.
- “lower” in the above means a relatively lower portion within the stripping device, more specifically, the stripping device is divided into two in the vertical direction, for example, perpendicular to the length or height direction of the stripping device.
- the "top" of the stripping device means the top of the stripping device, and may be located above the stripping device, and the "top” of the stripping device is the bottom of the top of the stripping device. It means, it can be located under the above-mentioned stripping device.
- the stripping device when the stripping device is divided into three equal parts in the longitudinal direction, the stripping device may be divided into upper, middle and lower regions, in which case the stripping may occur in all of the upper, middle and lower regions, or in the middle. It can only happen in the subdomain.
- the purification unit is a distillation tower (31, 41) and the distillation column (distillation tower (31, 41) for distilling the mixture of the solvent and water introduced from the solvent inlet line 201 for introducing a mixture of the solvent and water discharged from the stripping device 22 ( It may include a condenser 51 to condense the overhead stream 401 flowing out of the overhead region of the 31, 41, and to return a portion of the overhead stream 401 to the distillation tower (31, 41).
- the distillation column may be selected from distillation columns used in distillation processes in the general industrial field. At this time, the operating conditions of the distillation column, for example, the number and diameter of each column, the pressure and temperature, and the ratio of the reflux of the upper and lower discharge is not particularly limited, these are to perform the separation process continuously in a stabilized state I wish I could.
- each of the distillation column may be provided with a condenser and / or heat exchanger (or reboiler).
- the condenser and / or heat exchanger may be selectively installed or not installed according to each distillation column.
- the condenser and the heat exchanger may be a component that may be omitted even if shown in the drawings, unless specifically mentioned.
- the “top” of the distillation tower (31, 41) means the top of the column of the distillation tower (31, 41), can be included in the upper region of the above-described distillation tower (31, 32), the distillation tower (31, 41 means the bottom portion of the tower of the distillation towers 31 and 41 and may be included in the lower region of the distillation towers 31 and 41 described above.
- the "condenser” is a device installed separately from the distillation column, and may mean an apparatus for cooling the material flowing out of the distillation column in such a manner as to contact the cooling water introduced from the outside.
- the condenser 51 may be a device for condensing the overhead stream 401 flowing out of the overhead regions of the distillation columns 31 and 41.
- the "reboiler” is a heating device installed on the outside of the distillation column, it may mean a device for heating and evaporating again the high boiling point flow.
- the reboiler 411 of the distillation apparatus may be a device for heating the bottom stream flowing out from the bottom region of the distillation columns 31 and 41.
- the solvent separation unit and the purification unit may be connected through a heat exchanger.
- the water supply line 121 is connected to the heat exchanger 61 through the water inlet line 611, and the heat exchanger 61 is connected to the water supply line 121 through the water outlet line 601.
- the top stream 401 flowing out of the top of the distillation column 41 may be introduced into the heat exchanger 61, and may pass through the heat exchanger 61 through the reflux line 501. 41).
- the "heat exchanger” is a device that is separately installed outside the distillation column, and performs heat exchange so that heat transfer occurs smoothly between two fluid flows having different temperatures.
- the heat exchanger 61 is the distillation column 41. It may be a device for heat-exchanging the overhead flow 401 and the water inflow flow 611 flowing out from the top of the area.
- the overhead stream 401 and the water inflow stream 611 which flow out from the overhead region of the distillation column 41 are heat-exchanged with each other in the heat exchanger 61, and this is the water outlet line 601.
- the purification unit may include a first distillation column 31 and a second distillation column 41.
- the distillation unit of the present application heats a first distillation column 31 for distilling a mixture of solvent and water introduced into the solvent inlet line 201, and a first column bottom stream 301 flowing out of the bottom region of the first distillation column 31. It may include a first reboiler 311 for refluxing a portion of the first distillation column 31 and the first outflow line 321 for transferring the substance flowing out of the first distillation column (31).
- the refining unit heats the second distillation column 41 for distilling the material introduced through the first outlet line 321 and the second column bottom stream 421 flowing out from the bottom region of the second distillation column 41.
- a piping system comprising: a first line configured to introduce water from the water supply tank into the stripping apparatus after mixing with the mixture; A second line formed to introduce the solvent recovered from the solvent separation unit into the first distillation column; And a third line formed to introduce the solvent purified in the first distillation column into the second distillation column.
- the first line may include a water supply line 121, a steam supply line 131, and a polymer inflow line 101.
- the water supply line 121 supplied from the water supply tank 10 may be connected to each other through a pipe with the steam supply line 131, the polymer inflow line 101, and the stripping device 22.
- the water supplied from the water supply line 10 and the steam supply line 131 are mixed in the steam mixer 71, mixed with the mixture of the polymer and the solvent, and then removed through the polymer inlet line 101. It may be fluidically connected to be able to enter the device 22.
- the second line may include a solvent inlet line 201 for introducing a mixture of solvent and water discharged from the stripping device 22, and the third line sends the solvent flowing out of the first distillation column to the second distillation column.
- the first outlet line 321 may be introduced.
- the piping system may include a first heat exchange line.
- the first heat exchange line may include a water supply line 121, a water inflow line 611, a water outlet line 601, a heat exchanger 61, and a condenser 51.
- the water supply line 121 may be connected to the heat exchanger 61 through a water inlet line 611, and the heat exchanger 61 may be connected to the water supply line 121 through a water outlet line 601. .
- the top line 401 flowing out of the top of the distillation column 41 flows into the heat exchanger 61, passes through the heat exchanger 61, and is connected to the condenser 51, and a reflux line 501 is provided. Through the distillation column (31, 41) can be connected.
- FIG 3 is a view showing an exemplary solvent purification apparatus according to another embodiment of the present application.
- the solvent recovery apparatus flows out of the top region of the first column bottom stream 302 and the second distillation column 42 which flow out from the bottom region of the first distillation column 32.
- At least a portion 442 of the overhead stream 402 may be heat exchanged in the first reboiler 312.
- a portion 442 of the overhead stream 402 is used to heat the first column bottom stream 302 in a first reboiler and feed it to the first distillation column 32 to save energy to be used for heating the column bottom stream. Can be.
- the top stream flowing out of the top region of the second distillation column 42 heat exchanged with the first bottom stream 302 flowing out of the bottom region of the first distillation column 32 in the first reboiler 312 ( 402 may be supplied between the condenser 52 and the heat exchanger 62.
- the piping system can include a second heat exchange line.
- the second heat exchange line may include a first reboiler 312 and a condenser 52 of the first distillation column.
- the second heat exchange line introduces a portion 442 of the overhead stream 402 of the second distillation column 42 into the reboiler 312 of the first distillation column 32 and reboilers 312 of the first distillation column. After the heat exchange in the) may be refluxed to the first distillation column 32 or the second distillation column 42 through the condenser (52).
- the present application also relates to a solvent recovery method.
- the solvent recovery method may be performed by the solvent recovery apparatus described above.
- An exemplary method includes a solvent recovery step comprising introducing a mixture comprising a polymer component and a solvent with water from a water supply tank and then introducing the mixture into a stripping apparatus; And a solvent purification step of purifying the solvent recovered in the solvent recovery step in the first and second distillation columns, wherein the top product of the second distillation column is mixed with water or the first distillation column before the top product of the second distillation column is mixed with the mixture through a piping system. And heat exchange with the reboiler.
- the water supply stream 121 and the steam supply stream 131 are introduced into the steam mixer 71 to be mixed, and the steam flowing out of the steam mixer 71 is mixed.
- the difference between the temperature of the top product (Ti) before heat exchange with water or reboiler and the temperature (Ta) of the outflow flow of water or reboiler after heat exchange with top product is shown by the following general formula 1 Can be controlled to satisfy.
- the difference between the temperature (Ti) of the top product before heat exchange with the water or reboiler and the temperature (Ta) of the outflow flow of water or reboiler after heat exchange with the top product (Ti-Ta) is in the above range.
- the difference (Ti-Ta) of the temperature of the top product (Ti) before heat exchange with the water or reboiler and the temperature (Ta) of the outflow flow of water or reboiler after heat exchange with the top product is particularly limited, as long as it is within the above-mentioned range.
- the temperature may be 60 ° C or less, 50 ° C or less, 40 ° C or less, preferably 30 ° C or less, and the lower limit is not particularly limited.
- the temperature Ti of the columnar product before heat exchange with the water or reboiler is not particularly limited as long as the general formula 1 is satisfied, but may be 110 ° C. to 160 ° C., for example, 110 ° C. to 150 ° C.
- the temperature Ta of the outflow flow of water or reboiler after heat exchange with the column product is not particularly limited as long as the general formula 1 is satisfied, but is 90 ° C. to 140 ° C., for example, 95 ° C. to 135 ° C. , 100 ° C to 130 ° C.
- the difference between the temperature (Ti) of the top product of the second distillation column before heat exchange with the reboiler of the first distillation column and the temperature (Tb) of the effluent flow of the reboiler after heat exchange with the top product of the second distillation column (Ti-Tb) can be controlled to satisfy the following general formula (2).
- the difference between the temperature (Ti) of the top product before heat exchange with the reboiler and the temperature (Tb) of the outflow stream (Tb) of the effluent flow after the heat exchange with the top product of the second distillation column (Ti-Tb) By adjusting within the range, the amount of steam used in the reboiler can be reduced.
- the difference (Ti-Tb) of the temperature (Ti) of the overhead product before heat exchange with the reboiler and the temperature (Tb) of the effluent flow of the reboiler after heat exchange with the overhead product of the second distillation column is described above.
- the temperature Ti of the columnar product before heat exchange with the reboiler is not particularly limited as long as the general formula 2 is satisfied, but may be 130 ° C. to 160 ° C., for example, 130 ° C. to 150 ° C.
- the temperature (Tb) of the outflow stream of the reboiler after being heat-exchanged with the column top product of the second distillation column is not particularly limited as long as it satisfies the general formula (2), 120 °C to 140 °C, for example, 125 °C To 135 ° C.
- the top operating temperature of the first distillation column is in the range of 95 to 105 °C
- the bottom operating temperature may be in the range of 125 to 140 °C
- the top operating temperature of the second distillation column is in the range of 110 to 160 °C
- the bottom operating temperature may be in the range of 120 to 165 °C.
- the operating pressure P2 of the second distillation column 41 of the present application may be controlled to be higher than the operating pressure P1 of the first distillation column 31.
- the operating pressure of the distillation column is not particularly limited in the case of exchanging the top product of the second distillation column with water, but in the case of exchanging the top product of the second distillation column with the reboiler, the operating pressure (P2) of the second distillation column is changed to the first distillation column. It can be controlled higher than the operating pressure (P1) of.
- the pressure difference P2-P1 between the operating pressure P2 of the second distillation column and the operating pressure P1 of the first distillation column is 0.6 to 2.5 barg, 0.6 to 2.2 barg, 0.6 to 1.9 barg, or 0.7 to May be 1.6 barg.
- the operating pressure of the second distillation column may be 2.5 to 7.5 barg, 3.0 to 7.0 barg, 3.5 to 6.5 barg, or 4.0 to 6.0 barg.
- the operating pressure of the first distillation column may be 3.5 to 5.0 barg, 3.5 to 4.5 barg, 3.5 to 4.0 barg.
- the solvent recovery method of the present application may satisfy the following general formula (3).
- P2 is the pressure of the second distillation column and P1 is the pressure of the first distillation column.
- the temperature of the overhead stream 401 flowing out of the top of the second distillation column 41 and the outlet of the heat exchanger 61 can be controlled as in Formula 1, thereby effectively recovering waste heat.
- Column top 402 which heat-exchanges at least a portion 442 in the first reboiler 312 and exits at least a portion 612 of the water feed stream 122 and the top region of the second distillation column 42.
- the remaining part 452 of) may be heat exchanged.
- a portion 442 of the overhead stream 402 is used to heat the first column bottom stream 302 in a first reboiler and feed it to the first distillation column 32 to save energy to be used for heating the column bottom stream. Can be.
- the top stream flowing out of the top region of the second distillation column 42 heat exchanged with the first bottom stream 302 flowing out of the bottom region of the first distillation column 32 in the first reboiler 312 ( 402 may be supplied between the condenser 52 and the heat exchanger 62.
- the difference between the temperature of the top product (Ti) before heat exchange with water and reboiler and the temperature (Ta) of the outflow flow of water and reboiler after heat exchange with the top product (Ta-Ti) is Can be controlled to satisfy.
- the condenser by adjusting the temperature (Ti) of the top product before heat exchange with the water and reboiler and the temperature (Ti-Ta) of the outflow flow of water and reboiler after heat exchange with the top product (Ti-Ta) within the above range, The amount of coolant used can be reduced.
- the difference (Ti-Ta) between the temperature (Ti) of the overhead product before heat exchange with the water and reboiler and the temperature (Ta) of the outflow flow of water and reboiler after heat exchange with the overhead product (Ti-Ta) is particularly limited,
- the temperature may be 60 ° C or less, 50 ° C or less, 40 ° C or less, preferably 30 ° C or less, and the lower limit is not particularly limited.
- the temperature Ti of the columnar product before heat exchange with the water and the reboiler is not particularly limited as long as the general formula 1 is satisfied, but may be 130 ° C. to 160 ° C., for example, 130 ° C. to 140 ° C.
- the temperature Ta of the outflow flow of water and reboiler after heat-exchanging with the column top product is not particularly limited as long as it satisfies Formula 1, but is 90 ° C to 140 ° C, for example, 95 ° C to 135 ° C. , 100 ° C to 130 ° C, or 101 ° C to 127 ° C.
- the temperature (Ti) of the top product of the second distillation column prior to heat exchange with water and the reboiler of the first distillation column and the temperature (Tb) of the effluent stream of the reboiler after heat exchange with the top product of the second distillation column ) can be controlled to satisfy the following general formula (2).
- the difference (Ti-Tb) of the temperature (T) of the overhead product before heat-exchanging with the water and the reboiler and the temperature (Tb) of the effluent stream (Tb) of the effluent flow after the heat exchange with the overhead product of the second distillation column This can reduce the amount of coolant used in the condenser and reduce the amount of steam used in the reboiler.
- the difference (Ti-Tb) of the temperature (Ti) of the overhead product before heat exchange with the reboiler and the temperature (Tb) of the outflow stream of the reboiler after heat exchange with the overhead product of the second distillation column is described above.
- the temperature Ti of the columnar product before heat exchange with the water or reboiler is not particularly limited as long as the general formula 2 is satisfied, but may be 130 ° C. to 160 ° C., for example, 130 ° C. to 150 ° C.
- the temperature (Tb) of the outflow stream of the reboiler after being heat exchanged with the column top product of the second distillation column is not particularly limited as long as the general formula (2) is satisfied, 120 °C to 160 °C, for example, 125 °C To 150 ° C.
- the top operating temperature of the first distillation column is in the range of 95 to 105 °C
- the bottom operating temperature may be in the range of 125 to 140 °C.
- the top operating temperature of the second distillation column is in the range of 130 to 160 °C
- the bottom operating temperature may be in the range of 140 to 165 °C.
- the operating pressure P2 of the second distillation column 41 of the present application may be controlled to be higher than the operating pressure P1 of the first distillation column 31.
- the pressure difference between the operating pressure P2 of the second distillation column and the operating pressure P1 of the first distillation column may be 0.6 to 2.5 barg, 0.6 to 2.2 barg, 0.6 to 1.9 barg, or 0.7 to 1.6 barg. .
- the operating pressure of the second distillation column may be 4.0 to 7.5 barg, 4.1 to 7.0 barg, 4.1 to 6.5 barg, or 4.2 to 6.0 barg.
- the operating pressure of the first distillation column may be 3.0 to 5.0 barg, 3.2 to 4.5 barg, 3.5 to 4.0 barg.
- the solvent recovery method of the present application may satisfy the following general formula (3).
- P2 is the pressure of the second distillation column and P1 is the pressure of the first distillation column.
- the temperature of the overhead stream 402 flowing out of the top of the second distillation column 42 and the outlet of the heat exchanger 62 can be controlled as in Formula 1, thereby effectively recovering the waste heat.
- the ratio of the flow rate (A) of the top product of the second distillation column to be heat-exchanged with water and the flow rate (B) of the top product of the second distillation column to be heat-exchanged with the reboiler of the first distillation column may be 0.40 to 0.65.
- the waste heat from the distillation column upper condenser is recovered and supplied to the heat source of the stripping apparatus, which can significantly reduce energy as compared to the conventional synthetic rubber production process.
- 1 is a block diagram illustrating a solvent recovery process performed in the conventional synthetic rubber production.
- FIG. 2 is a configuration diagram of a synthetic rubber production process to which the process waste heat recovery method according to the first embodiment of the present application is applied.
- FIG. 3 is a configuration diagram of a synthetic rubber production process to which the process waste heat recovery method according to the second embodiment of the present application is applied.
- the water supplied from the water supply tank 10 through the water supply line 121 and the steam supplied through the steam supply line 131 are mixed in the steam mixer 71 to remove the removal device ( 22).
- the solvent separated from the polymer in the stripping device 22 is recovered and introduced into the first distillation column 31 through the solvent inlet line 201.
- the first bottom stream 301 flowing out of the bottom region of the first distillation column 31 was reheated through the first reboiler 311 to be refluxed to the first distillation column 31.
- the solvent flowing out of the first distillation column 31 was introduced into the second distillation column 41 through the first outlet line 321.
- the second bottom stream 421 flowing out of the bottom region of the second distillation column 41 was heated in the second reboiler 411 and refluxed to the second distillation column 41.
- a portion 611 of the water supply flow 121 is heat-exchanged with the overhead stream 401 flowing out of the overhead region of the second distillation column 41 in the heat exchanger 61 and then water is passed through the water outlet line 601. It was supplied to the supply line 121.
- the temperature of the overhead stream 401 flowing out from the overhead region of the second distillation column is 114 ° C, and the temperature of the water outlet stream 601 after heat exchange in the overhead stream 401 is 109 ° C.
- the operating pressure of the first distillation column was 3.8 barg, and the operating pressure of the second distillation column was 2.5 barg.
- a portion 612 of the water feed stream 122 is heat exchanged with a portion 452 of the overhead stream 402 exiting the overhead zone of the second distillation column 42 in the heat exchanger 62. After that, it is supplied to the water supply line 122 through the water outlet line 602, and a portion 442 of the overhead stream 402 is introduced into the first reboiler 312 to the The same apparatus as in Example 1 was used except that it was heat exchanged with the first bottom stream 302.
- the temperature of the overhead stream 402 flowing out from the overhead region of the second distillation column is 132 ° C., and the temperature of the water effluent stream 602 flowing out through the heat exchanger 62 is 101 ° C.
- the temperature of the outflow stream 332 flowing out of the first reboiler 312 after being heat exchanged with a portion 442 of the overhead stream 402 was 127 ° C.
- the ratio of the portion 452 of the overhead stream 402 heat exchanged with the heat exchanger 62 and the portion 442 of the overhead stream 402 heat exchanged with the first reboiler 312 is 0.55. .
- the operating pressure of the first distillation column was 3.5 barg, and the operating pressure of the second distillation column was 4.2 barg.
- the overhead stream 400 flowing out of the overhead region of the second distillation column 40 is condensed through the condenser 55 and then introduced into the first distillation column 30 or the second distillation column 40.
- the same apparatus as in Example 1 was used except that the waste heat from the cooling water supplied to the condenser 50 was discarded.
- Example 2 First Distillation Column Upper Temperature 100 °C 100 °C 99 °C First distillation column bottom temperature 130 °C 130 °C 127 °C Second distillation column overhead temperature 74 °C 114 °C 132 °C Second distillation column bottom temperature 84 °C 123 °C 143 °C Ti-Ta - 5 °C 31 °C Ti-Tb - - 5 °C P2-P1 - - 0.7
- Table 1 is a table comparing the operating conditions of Examples and Comparative Examples.
- Example 2 First distillation column 2,752 2,752 0 2nd distillation column 3,648 5,694 6,708 Stripper supply 5,500 0 1,817 Total usage 11,900 8,446 8,524 Savings - 3,454 3,376 % Savings 29.0 28.4
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Abstract
Description
비교예 | 실시예1 | 실시예2 | |
제 1 증류탑 상부 온도 | 100℃ | 100℃ | 99℃ |
제 1 증류탑 하부 온도 | 130℃ | 130℃ | 127℃ |
제 2 증류탑 상부 온도 | 74℃ | 114℃ | 132℃ |
제 2 증류탑 하부 온도 | 84℃ | 123℃ | 143℃ |
Ti - Ta | - | 5℃ | 31℃ |
Ti - Tb | - | - | 5℃ |
P2 - P1 | - | - | 0.7 |
스팀사용량(Kg/hr) | 비교예(종래) | 실시예1 | 실시예2 |
제 1 증류탑 | 2,752 | 2,752 | 0 |
제 2 증류탑 | 3,648 | 5,694 | 6,708 |
탈거 장치 공급 | 5,500 | 0 | 1,817 |
총 사용량 | 11,900 | 8,446 | 8,524 |
절감량 | - | 3,454 | 3,376 |
절감율(%) | 29.0 | 28.4 |
Claims (16)
- 물 공급 탱크 및 고분자 성분과 용매를 포함하는 혼합물로부터 상기 고분자 성분과 상기 용매를 분리할 수 있는 탈거 장치를 포함하는 용매 분리부; 상기 용매 분리부에서 회수된 용매를 정제할 수 있는 정제부로서, 서로 연결되어 있어 있으며, 각각 재비기와 응축기를 가지는 제 1 증류탑과 제 2 증류탑을 포함하는 정제부; 및 배관 시스템을 포함하고,상기 배관 시스템은, 상기 물 공급 탱크로부터의 물을 상기 혼합물과 혼합한 후에 상기 탈거 장치로 도입할 수 있도록 형성된 제 1 라인;상기 용매 분리부로부터 회수된 용매를 상기 제 1 증류탑에 도입할 수 있도록 형성된 제 2 라인; 및상기 제 1 증류탑에서 정제된 용매를 상기 제 2 증류탑으로 도입할 수 있도록 형성된 제 3 라인을 포함하고,상기 배관 시스템은, 상기 혼합물과 혼합되기 전의 물과 상기 제 2 증류탑의 탑정 생성물을 열교환시킬 수 있도록 설치된 제 1 열교환 라인 또는 상기 제 1 증류탑의 재비기와 상기 제 2 증류탑의 탑정 생성물을 열교환시킬 수 있도록 설치된 제 2 열교환 라인을 추가로 포함하는 용매 회수 장치.
- 제 1 항에 있어서, 제 1 열교환 라인에는 열교환기 및 제 2 증류탑의 응축기가 설치되어 있고, 상기 열교환기 및 제 2 증류탑의 응축기는 제 2 증류탑의 탑정 생성물이 상기 열교환기에서 물과 열교환된 후에 상기 제 2 응축기로 도입될 수 있도록 상기 제 1 열교환 라인에 설치되어 있는 용매 회수 장치.
- 제 1 항에 있어서, 제 2 열교환 라인에는 제 1 증류탑의 재비기 및 제 2 증류탑의 응축기가 설치되어 있고, 상기 제 1 증류탑의 재비기 및 제 2 증류탑의 응축기는 제 2 증류탑의 탑정 생성물이 상기 제 1 증류탑의 재비기를 거친 후에 상기 제 2 응축기를 거칠 수 있도록 상기 제 2 열교환 라인에 설치되어 있는 용매 회수 장치.
- 제 1 항에 있어서, 제 1 라인에 스팀을 공급할 수 있도록 설치된 스팀 공급 라인을 추가로 포함하는 용매 회수 장치.
- 제 1 항에 있어서, 배관 시스템은 제 1 및 제 2 열교환 라인을 포함하고, 상기 제 1 및 제 2 열교환 라인은, 제 2 증류탑의 탑정 생성물의 일부가 용매 회수부의 물과 열교환된 후에 제 2 증류탑의 응축기를 거쳐 제 2 증류탑으로 환류되고, 상기 제 2 증류탑의 탑정 생성물의 다른 일부가 제 1 증류탑의 재비기 및 상기 제 2 증류탑의 응축기를 순차로 거친 후에 상기 제 2 증류탑으로 환류될 수 있도록 형성되어 있는 용매 회수 장치.
- 제 1 항의 용매 회수 장치를 사용하여 용매를 회수하는 방법으로서, 고분자 성분과 용매를 포함하는 혼합물을 물 공급 탱크로부터의 물과 혼합한 후에 탈거 장치로 도입하는 공정을 포함하는 용매 회수 단계; 및 용매 회수 단계에서 회수된 용매를 제 1 및 제 2 증류탑에서 정제하는 용매 정제 단계를 포함하되,배관 시스템을 통하여 상기 제 2 증류탑의 탑정 생성물을 상기 혼합물과 혼합되기 전의 물 또는 상기 제 1 증류탑의 재비기와 열교환시키는 단계를 수행하는 용매 회수 방법.
- 제 6 항에 있어서, 물 또는 재비기와 열교환되기 전의 탑정 생성물의 온도(Ti) 및 탑정 생성물과 열교환 된 후 물 또는 재비기의 유출 흐름의 온도(Ta)가 하기 일반식 1을 만족하도록 제어하는 용매 회수 방법:[일반식 1]│Ti - Ta│ ≤ 60℃
- 제 7 항에 있어서, 물 또는 재비기와 열교환되기 전의 탑정 생성물의 온도(Ti)가 110 내지 160℃ 의 범위 내에 있는 용매 회수 방법.
- 제 7 항에 있어서, 탑정 생성물과 열교환 된 후 물 또는 재비기의 유출 흐름의 온도(Ta)가 90 내지 140℃의 범위 내에 있는 용매 회수 방법.
- 제 6 항에 있어서, 제 1 증류탑의 재비기로 도입되기 전의 제 2 증류탑의 탑정 생성물의 온도(Ti) 및 상기 제 2 증류탑의 탑정 생성물과 열교환된 후의 상기 재비기의 유출 흐름의 온도(Tb)의 차이(Ti-Tb)가 하기 일반식 2를 만족하도록 제어하는 용매 회수 방법:[일반식 2]│Ti - Tb│ ≤ 25℃
- 제 10 항에 있어서, 제 1 증류탑의 재비기로 도입되기 전의 제 2 증류탑의 탑정 생성물의 온도(Ti)가 130 내지 160℃ 의 범위 내에 있는 용매 회수 방법.
- 제 10 항에 있어서, 제 1 증류탑 및 제 2 증류탑의 압력은 하기 일반식 3을 만족하는 용매 회수 방법:[일반식 3]0.6≤P2 - P1≤2.5 barg,3.5≤P1≤5.0 barg여기서 P2는 제 2 증류탑의 압력이고, P1은 제 1 증류탑의 압력이다.
- 제 6 항에 있어서, 배관 시스템을 통하여 상기 제 2 증류탑의 탑정 생성물의 일부를 상기 혼합물과 혼합되기 전의 물과 열교환시키고, 상기 제 2 증류탑의 탑정 생성물의 다른 일부를 상기 제 1 증류탑의 재비기와 열교환시키는 단계를 수행하는 용매 회수 방법.
- 제 12 항에 있어서, 물과 열교환되는 제 2 증류탑의 탑정 생성물의 유량(A)과 제 1 증류탑의 재비기와 열교환되는 제 2 증류탑의 탑정 생성물의 유량(B)의 비율이 0.40 내지 0.65인 용매 회수 방법.
- 제 6 항에 있어서, 제 1 증류탑의 탑정 운전 온도는 95 내지 105℃ 의 범위 내이고, 탑저 운전온도는 125 내지 140℃ 의 범위 내인 용매 회수 방법.
- 제 6 항에 있어서, 제 2 증류탑의 탑정 운전 온도는 110 내지 160℃의 범위 내이고, 탑저 운전온도는 120 내지 165℃의 범위 내인 용매 회수 방법.
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US15/779,304 US10703875B2 (en) | 2016-06-16 | 2017-06-12 | Solvent recovery apparatus and solvent recovery method |
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Cited By (5)
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CN108273282A (zh) * | 2018-02-28 | 2018-07-13 | 重庆云天化天聚新材料有限公司 | 三聚甲醛合成蒸馏塔汽相低位热回收系统及其回收方法 |
EP3572440A4 (en) * | 2018-02-09 | 2020-03-25 | Lg Chem, Ltd. | METHOD AND APPARATUS FOR PRODUCING CONJUGATED DENE POLYMER |
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Families Citing this family (5)
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US11970558B2 (en) | 2020-07-22 | 2024-04-30 | Lg Chem, Ltd. | Method of recovering solvent and solvent recovery apparatus |
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Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4406750A (en) * | 1981-09-29 | 1983-09-27 | Phillips Petroleum Company | Solvent removal from polymer solution utilizing flashed vapor as a heat source |
KR100811971B1 (ko) * | 2007-10-01 | 2008-03-10 | 이주선 | 증류시스템 및 그 증류방법 |
WO2009032143A1 (en) * | 2007-08-30 | 2009-03-12 | Environmental Protection Agency | Liquid separation by membrane assisted vapor process |
US20100101273A1 (en) * | 2008-10-27 | 2010-04-29 | Sechrist Paul A | Heat Pump for High Purity Bottom Product |
KR20160051665A (ko) * | 2014-10-31 | 2016-05-11 | 주식회사 엘지화학 | 증류 장치 |
Family Cites Families (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6010041B2 (ja) * | 1975-12-19 | 1985-03-14 | 旭化成株式会社 | ゴム状重合体の取得法 |
JPS6297601A (ja) * | 1985-10-21 | 1987-05-07 | Chisso Corp | スチ−ムストリツピングによる溶媒回収方法 |
US20050267288A1 (en) | 2002-07-03 | 2005-12-01 | Jsr Corporation | Method of removing solvent from polymer solution and solvent removing apparatus |
KR100495335B1 (ko) | 2002-11-15 | 2005-06-14 | 주식회사 엘지화학 | 스팀의 직접접촉을 이용한 고분자 회수방법 |
US8524972B1 (en) * | 2012-04-18 | 2013-09-03 | Exxonmobil Chemical Patents Inc. | Low temperature steam stripping for byproduct polymer and solvent recovery from an ethylene oligomerization process |
KR101640654B1 (ko) * | 2013-01-16 | 2016-07-18 | 주식회사 엘지화학 | 알칸올의 제조 장치 |
CA2809718C (en) * | 2013-03-15 | 2020-03-24 | Nova Chemicals Corporation | Improved energy utilization in a solution polymerization plant |
JP6194191B2 (ja) * | 2013-06-07 | 2017-09-06 | ソニー株式会社 | 情報処理システム |
CN103864602B (zh) * | 2014-04-03 | 2015-12-30 | 泰兴市裕廊化工有限公司 | 一种具有两套氧化一套精制的节能丙烯酸制备方法 |
-
2016
- 2016-06-16 KR KR1020160074837A patent/KR102089414B1/ko active IP Right Grant
-
2017
- 2017-06-12 WO PCT/KR2017/006056 patent/WO2017217708A1/ko active Application Filing
- 2017-06-12 EP EP17813532.3A patent/EP3473668B1/en active Active
- 2017-06-12 US US15/779,304 patent/US10703875B2/en active Active
- 2017-06-12 JP JP2018523811A patent/JP6615995B2/ja active Active
- 2017-06-12 CN CN201780004696.7A patent/CN108368288B/zh active Active
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4406750A (en) * | 1981-09-29 | 1983-09-27 | Phillips Petroleum Company | Solvent removal from polymer solution utilizing flashed vapor as a heat source |
WO2009032143A1 (en) * | 2007-08-30 | 2009-03-12 | Environmental Protection Agency | Liquid separation by membrane assisted vapor process |
KR100811971B1 (ko) * | 2007-10-01 | 2008-03-10 | 이주선 | 증류시스템 및 그 증류방법 |
US20100101273A1 (en) * | 2008-10-27 | 2010-04-29 | Sechrist Paul A | Heat Pump for High Purity Bottom Product |
KR20160051665A (ko) * | 2014-10-31 | 2016-05-11 | 주식회사 엘지화학 | 증류 장치 |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP3572440A4 (en) * | 2018-02-09 | 2020-03-25 | Lg Chem, Ltd. | METHOD AND APPARATUS FOR PRODUCING CONJUGATED DENE POLYMER |
US11299565B2 (en) | 2018-02-09 | 2022-04-12 | Lg Chem, Ltd. | Method of preparing conjugated diene-based polymer and apparatus for preparing conjugated diene-based polymer |
CN108273282A (zh) * | 2018-02-28 | 2018-07-13 | 重庆云天化天聚新材料有限公司 | 三聚甲醛合成蒸馏塔汽相低位热回收系统及其回收方法 |
CN108273282B (zh) * | 2018-02-28 | 2023-11-10 | 重庆云天化天聚新材料有限公司 | 三聚甲醛合成蒸馏塔汽相低位热回收系统及其回收方法 |
CN111886062A (zh) * | 2018-11-01 | 2020-11-03 | 株式会社Lg化学 | 从包含有机溶剂的混合溶液中分离有机溶剂的方法 |
EP3753618A4 (en) * | 2018-11-01 | 2021-03-17 | Lg Chem, Ltd. | PROCESS FOR SEPARATING ORGANIC SOLVENT FROM A MIXED SOLUTION CONTAINING AN ORGANIC SOLVENT |
US11541327B2 (en) | 2018-11-01 | 2023-01-03 | Lg Chem, Ltd. | Method of separating organic solvent from mixed solution containing the organic solvent |
JP2021526152A (ja) * | 2018-12-10 | 2021-09-30 | エルジー・ケム・リミテッド | エチレンオリゴマー化反応生成物の分離方法 |
JP7123179B2 (ja) | 2018-12-10 | 2022-08-22 | エルジー・ケム・リミテッド | エチレンオリゴマー化反応生成物の分離方法 |
CN111630093A (zh) * | 2018-12-18 | 2020-09-04 | 株式会社Lg化学 | 用于回收基于酰胺的化合物的方法 |
CN111630093B (zh) * | 2018-12-18 | 2022-08-12 | 株式会社Lg化学 | 用于回收基于酰胺的化合物的方法 |
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CN108368288B (zh) | 2021-03-26 |
KR20170141872A (ko) | 2017-12-27 |
JP2018533477A (ja) | 2018-11-15 |
JP6615995B2 (ja) | 2019-12-04 |
EP3473668A1 (en) | 2019-04-24 |
EP3473668B1 (en) | 2020-03-18 |
EP3473668A4 (en) | 2019-04-24 |
KR102089414B1 (ko) | 2020-03-16 |
US10703875B2 (en) | 2020-07-07 |
CN108368288A (zh) | 2018-08-03 |
US20180319949A1 (en) | 2018-11-08 |
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