WO2015160018A1 - 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템 - Google Patents
통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템 Download PDFInfo
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- WO2015160018A1 WO2015160018A1 PCT/KR2014/003655 KR2014003655W WO2015160018A1 WO 2015160018 A1 WO2015160018 A1 WO 2015160018A1 KR 2014003655 W KR2014003655 W KR 2014003655W WO 2015160018 A1 WO2015160018 A1 WO 2015160018A1
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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
- B01D3/14—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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
-
- 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
-
- 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
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
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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
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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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- 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 invention is a distillation system using a multi-stage stripper capable of integrated operation and reduced steam consumption, and more particularly, in a distillation system that separates the mixture by boiling point difference, condensing the upper steam discharged from the module with a stripper to condense water. After evaporation, the evaporated water vapor is compressed in multiple stages and supplied to at least two strippers, thereby increasing the heat recovery rate of the upper steam of the stripper and reducing the time and cost of the distillation process.
- a distillation system using a multistage stripper is a distillation system using a multistage stripper.
- the distillation system is for evaporating separation of the mixture present in the feedstock by boiling point difference.
- high volatile components are evaporated and separated in the form of overhead vapor, and at the bottom of the distillation system, the low volatile components are separated in undistilled form.
- the low boiling point material and the high boiling point material may each be a single component, or may be a mixture of two or more components, respectively.
- This distillation system essentially includes an evaporator that separates materials according to the boiling point difference.
- the evaporator includes a distillation column, a rectification column, a stripping column, a stripping vessel, stripper).
- the extraction tower is used to extract the low boiling point material from the evaporator as the target product, and the extraction tower or stripping tank is used to extract the high boiling point material to the target product.
- the stripping column is mainly used to extract high viscosity materials of low viscosity and the stripping tank is used to extract high viscosity materials of high viscosity.
- a conventional distillation system 10 having a stripping tank includes a stripping tank 110 in which a feedstock is separated into a high boiling point material and a low boiling point material, and a condenser 120 in which the upper steam of the low boiling point material is condensed. It is configured to include).
- the stripping tank 110 removes and refines low boiling point material, and recovers it as a raw material.
- the high viscosity material of high viscosity is dried to obtain a final product.
- FIG. 2 is a schematic illustration of a distillation system using two or more conventional stripping baths.
- the distillation system 20 having two stripping tanks may include a first stripping tank 111 to which feedstock is supplied, and a second stripping material supplied from the first stripping tank 111.
- Two compression modules 141, 142 Two compression modules 141, 142.
- the feedstock is first supplied to the first stripping tank 111.
- the low boiling point material of the feedstock is discharged to the upper steam and the high boiling point material is separated into the undistilled form at the bottom.
- the first stripping tank 111 only the low boiling point material having a boiling point below a predetermined temperature is discharged to the upper steam, and the material having a boiling point above a predetermined temperature is not discharged to the upper steam. For this reason, in the first stripping tank 111, all feedstocks are not separated into a low boiling point material and a high boiling point material, which are supplied to the second stripping tank 112 to be further separated.
- the upper steam discharged from the first stripping tank 111 generates saturated steam by heat-exchanging with water in the condensation evaporator 120, and then passes through the first compression module 141 to be resupplied to the first stripping tank 111. . This is used to separate the feedstock in the first stripping tank 111.
- the upper steam not condensed in the condensation evaporator 120 is supplied to the condenser 130 and finally condensed.
- the condensate generated in the condenser 130 is separated from the water by specific gravity and then supplied to the distillation tower 180.
- the reboiler 190 supplies steam to the distillation column, and the steam condensed water generated in the reboiler 190 is flashed under low pressure, compressed in the second compression module 142, and then supplied to the second stripping tank 112. It is used for the final stripping by direct heat exchange with the feedstock discharged from the first stripping tank 111
- the second stripping tank 112 is condensed and separated from the condenser is supplied to the distillation tower 180 for purification, the reboiler 190 expands and evaporates the hot steam condensed water in the second compression module 142 It must be supplied compressed.
- the reboiler 190 expands and evaporates the hot steam condensed water in the second compression module 142 It must be supplied compressed.
- steam is supplied from the steam supply unit 160 according to the temperature required by the first stripping tank 111, and the upper steam discharged from the first stripping tank 111 Even though the water vapor generated by the heat exchange through the first compression module 141 is supplied to the first stripping tank 111 and used again, the steam supply unit 160 is not sufficient to operate the first stripping tank 111. Steam must be supplied continuously.
- the amount of steam to be supplied from the outside until the second stripping tank 112 is driven to supply the upper steam of the second stripping tank 112 to the first stripping tank 111 is excessively expensive. do.
- the first compression module 141 and the second compression module 142 should be driven separately. There is a problem.
- an object of the present invention is to solve such a conventional problem, in the distillation system for separating the mixture by the difference in boiling point, after evaporating the water using the upper steam discharged from the stripper module, the evaporation
- the evaporation By multi-stage compression of compressed water vapor and supplying it to at least two strippers, it is possible to increase the heat recovery rate of the upper steam of the stripper and to reduce the cost and time required for the distillation process. In providing a system.
- the distillation system for separating a mixture existing in the feedstock into a low boiling point material and a high boiling point material by boiling point difference, it is provided with a plurality of strippers, the feedstock is supplied to the low boiling point
- a stripper module in which a material is evaporated and discharged into an upper steam and the high boiling point material is undistilled from the bottom, and the gas-liquid equilibrium pressure and temperature of the low boiling point material evaporated from each stripper are different from each other;
- a condensation evaporator in which water supplied from a water source exchanges heat with the upper steam passing through the stripper module to condense and evaporate the upper steam and water, respectively;
- a Mechanical Vapor Recompression (MVR) module for compressing water vapor evaporated from the condensation evaporator in multiple stages;
- the compressed water vapor in the mechanical vapor recompression module is achieved by a distillation system using an integrated operation supplied to at least two or more strippers and a multistage stripper capable of reducing steam consumption.
- the stripper module may include: a first stripper supplied with the feedstock, the low boiling point material is evaporated and discharged into the upper steam, and the high boiling point material is not distilled off from the bottom; A second stripper driven at a higher temperature than the first stripper and receiving a material that is not evaporated from the first stripper, the low boiling point material is removed and discharged into the upper steam, and the high boiling point material is not distilled off from the bottom; Preferably, some of the water vapor compressed in the mechanical vapor recompression module is first supplied to the second stripper, and the other is supplied to the first stripper.
- the temperature and pressure of the water vapor passing through the mechanical vapor recompression module is the temperature and pressure required to separate the feedstock from the first stripper, and a portion of the water vapor passing through the mechanical vapor recompression module is the first temperature.
- a thermal vapor recompression module (TVR) which directs the feed to the stripper side and increases the temperature and pressure of the water vapor supplied to the second stripper to the temperature and pressure required to separate the feedstock from the second stripper. Recompression) is preferably further included.
- the upper steam of the second stripper is supplied to the first stripper, it is preferably used as a heat source for separating the feedstock from the first stripper.
- the steam supply unit for supplying steam to the first stripper and the second stripper;
- a first valve provided to open and close to control whether the steam is supplied to the first stripper;
- a second valve is provided to open and close to control whether the steam is supplied to the second stripper.
- a third valve which is provided to be opened and closed, and guides a part of the steam supplied from the steam supply part to the thermal steam recompression module side.
- the mechanical vapor recompression module comprises a first module provided with a plurality of mechanical vapor recompression devices; A second module provided with a plurality of mechanical vapor recompression devices, and further compressing water vapor passing through the first module; It is preferable to include a; laminator for lowering the speed of the compressed water vapor passed through the first module to supply to the second module.
- a condenser for condensing the upper steam is not condensed in the evaporator; It is preferable to further include a distillation column for receiving the condensate condensed in the condenser.
- it further comprises a reboiler for supplying steam to the distillation column, the steam condensate of the reboiler is preferably evaporated and supplied to the laminator.
- the laminator preferably equalizes the temperature of the vapor from which the compressed steam passed through the first module and the steam condensed water supplied from the reboiler are evaporated.
- the flow rate control unit is preferably installed at the inlet end of the first module.
- water is evaporated using the upper steam discharged from the module as a stripper, and then the vaporized steam is multistage compressed and supplied to at least two or more strippers, thereby increasing the heat recovery rate of the discharge steam of the stripper and distilling it.
- a distillation system is provided that utilizes integrated operation to reduce the cost of the process and a multi-stage stripper capable of reducing steam consumption.
- the second stripper and the first stripper can be driven almost simultaneously.
- the first module and the second module can be controlled at the same time.
- the temperature of the steam supplied from the reboiler and the saturated steam discharged from the first module can be equalized and supplied to the second module.
- thermal vapor recompression module saturated steam discharged from the second module can be easily supplied to the second stripper side.
- the temperature and pressure of the saturated steam discharged from the second module can be easily set to the temperature and pressure required for the stripping process in the second stripper.
- 1 is a view schematically showing a conventional distillation system having a stripping tank.
- FIG. 2 is a schematic illustration of a distillation system using two or more conventional stripping baths.
- Figure 3 is a schematic diagram of a distillation system using a multi-stage stripper capable of integrated operation and reduced steam consumption according to an embodiment of the present invention.
- FIG. 4 is a view schematically showing the operation before the condensate generated in the condenser of the distillation system using the multi-stage stripper capable of integrated operation and reducing steam consumption of FIG. 3 is supplied to the distillation column.
- FIG. 5 is a view schematically showing the operation after the condensate generated in the condenser of the distillation system using the integrated operation of FIG. 3 and the multi-stage stripper capable of reducing steam consumption is supplied to the distillation column.
- the present invention relates to a multistage stripping tank, ie a distillation system using a multistage stripper.
- Distillation system using a multi-stage stripper capable of integrated operation and reduced steam consumption according to an embodiment of the present invention is evaporated water using the upper steam discharged from the module as a stripper, and then the vaporized steam is multi-stage compressed to at least 2
- the present invention relates to a distillation system using a multi-stage stripper capable of integrated operation and reducing steam consumption by increasing the heat recovery rate of the upper steam of the stripper module and supplying more than two strippers.
- FIG. 3 is a schematic diagram of a distillation system using a multi-stage stripper capable of integrated operation and reduced steam consumption according to an embodiment of the present invention.
- a distillation system 100 using a multi-stage stripper capable of integrated operation and reduced steam consumption according to an embodiment of the present invention includes a stripper module 110 and a stripper module 110 to which a feedstock is supplied.
- the valve 170 to control the supply of steam from, and the distillation column 180 and the reboiler 190.
- the stripper module 110 refers to a stripping tank module for removing a low boiling point monomer from a feedstock and obtaining a high viscosity high boiling point polymer.
- the stripper module 110 includes a first stripper 111 and a second stripper 112.
- the feedstock may be, for example, a mixture produced after the polymerization of synthetic rubber.
- the first stripper 111 is a device for separating a low boiling point material and a high boiling point material by receiving a feedstock having a mixture or the like. Steam is supplied to the first stripper 111 from the steam supply unit 160 through a first valve 171 controlled according to a condition such as a temperature required by the first stripper 111. In addition, the upper steam is supplied from the second stripper 112, the saturated steam discharged from the second module 142 is supplied. The steam and saturated steam described above are the same material. The steam supplied from the steam supply unit 160 is in direct contact with the high boiling point material of the lower portion of the first stripper 111 to transfer heat. The low boiling point material in the mixture is evaporated and discharged into the upper steam together with water vapor.
- the first stripper 111 does not evaporate all of the low boiling point material present in the feedstock.
- Each of the low boiling point material and the high boiling point material may be a mixture of two or more components.
- the cost may be excessive because the temperature of steam required for evaporating all the low boiling point materials is high. Therefore, only the low boiling point material having a boiling point below a predetermined temperature is evaporated in the first stripper 111.
- the second stripper 112 is a device that receives and separates the low boiling point material and the high boiling point material which are not separated from the first stripper 111.
- the first stripper 111 only the low boiling point material having a boiling point below a predetermined temperature is evaporated, and the low boiling point material having a boiling point above a predetermined temperature is evaporated from the second stripper 112, so that the second stripper 112 may include a first stripper ( Compared to 111).
- the second stripper 112 is provided to receive steam from the steam supply unit 160 and the thermal steam recompression module 150. Specifically, steam is supplied from the steam supply unit 160 through the second valve 172 controlled according to a condition such as the temperature required by the second stripper 112. In addition, the thermal steam recompression module 150 receives steam passed through the third valve 173 and the second module 142 controlled according to conditions such as the temperature required by the second stripper 112.
- the second stripper 112 is driven at a higher temperature than the first stripper 111. Therefore, the upper steam discharged from the second stripper 112 is provided to be supplied to the first stripper 111, which is used as a heat source for separating the feedstock from the first stripper 111.
- the condensation evaporator 120 condenses upper steam of two or more components having different single or saturated steam pressures supplied from the first stripper 111, and delivers the maximum amount of heat to water, thereby generating heat amount of steam corresponding to the amount of heat delivered.
- Configuration. the condensation evaporator 120 is supplied with water from a separate water source, so that the saturated steam can be compressed in the mechanical vapor recompression module 140 to the temperature and pressure required by the first stripper 111, condensation Condensation of the upper steam as necessary in the evaporator 120 to deliver the heat to the water.
- the remaining upper steam that is not condensed is supplied to the condenser 130, and the heat transferred from the upper steam is saturated steam and is supplied to the mechanical vapor recompression module 140.
- the condenser 130 is configured to condense the upper steam not condensed in the condensation evaporator 120.
- the upper steam not condensed in the condensation evaporator 120 is supplied to the condenser 130, and finally condensed in the condenser 130.
- the condensate generated in the condenser 130 is separated by specific gravity and then supplied to the distillation tower 180.
- the mechanical steam recompression module 140 is a component for compressing the saturated steam generated in the condensation evaporator 120 to the temperature and pressure required by the first stripper 111, and the first module 141 and the second module. 142, a laminator 143, and a flow control unit 144.
- the first module 141 is configured to compress the saturated steam generated by the condensation evaporator 130.
- the first module 141 is provided with a plurality of mechanical vapor recompression device.
- the mechanical vapor recompression apparatus may be used a high speed compressor, a low speed blow centrifugal compressor and the like.
- the blow centrifugal compressor is a low-cost blow centrifugal compressor with a low speed of less than 10000 rpm, and has a merit that it can be stably operated without damaging the compressor even during long time operation because of low speed.
- the blower centrifugal compressor is a low speed compressor of 10000 rpm or less, preferably 4000 to 7000 rpm, and has a lower compression ratio than the high speed multi-stage turbo compressor.
- a plurality of blower centrifugal compressors are provided to compensate for the low compression ratio.
- the saturated water vapor saturated in the condensation evaporator 120 is multi-stage compressed in the plurality of air centrifugal compressors according to a predetermined compression ratio.
- the mechanical vapor recompression apparatus has been described using a low-speed blow centrifugal compressor as an example, but the temperature and pressure required for the temperature and pressure of the saturated steam generated in the condensation evaporator 120 are required by the first stripper 111. If it can be compressed to, but not necessarily limited thereto.
- the flow rate controller 144 may be installed at the inlet end of the first module 141.
- the flow controller 144 includes an inlet guide vane (IGV) or inverter motor control.
- the second module 142 is a component that finally compresses the saturated water vapor compressed by the first module 141 to have the temperature and pressure required by the first stripper 111.
- the second module 142 is provided with a plurality of mechanical vapor recompression device. Meanwhile, the mechanical vapor recompression apparatus of the second module 142 may be provided as a low speed air centrifugal compressor like the first module 141.
- the laminator 143 is installed between the first module 141 and the second module 142 to lower the speed of saturated steam discharged from the first module 141 and to control the temperature.
- the first module 141 is composed of a plurality of air centrifugal compressors, and compresses the saturated steam generated in the condensation evaporator 120 in multiple stages.
- the saturated water vapor passing through the plurality of air centrifugal compressors has a very high velocity and strong vortices are formed by the rotary motion of the impeller.
- the distribution of the inlet vapor density into the second module 142 is not uniform, so that excessive stress is generated in the cross section of the impeller of the blow centrifugal compressor of the second module 141 due to the high velocity pressure, thereby causing vibration and damage. This may be a concern.
- the laminator 143 is installed between the first module 141 and the second module 141, thereby lowering the speed of saturated steam discharged from the first module 141, and increasing the high speed pressure of 50 to 90 kPa of the saturated steam. Is converted to a constant pressure to gradually flow into the second module 142 at a uniform vapor density without vortex saturation of saturated steam.
- the laminator 143 adjusts the temperature of the saturated steam discharged from the first module 141.
- the laminator 143 is supplied with steam vaporized by expansion and evaporation of steam condensate generated in the reboiler 190 as well as saturated steam discharged from the first module 141.
- the laminator 143 equilibrates the temperature of the saturated steam with the steam and then supplies it to the second module 142. That is, after the steam condensate generated in the reboiler 190 expands and evaporates the same temperature as the saturated steam discharged from the first module 141, the steam condensed water is supplied to the second module 142 to supply the first stripper ( To the required temperature and pressure.
- the thermal vapor recompression module 150 is configured to compress the saturated water vapor passed through the mechanical vapor recompression module 140 to the temperature and pressure required by the second stripper 111. Some of the saturated steam passing through the mechanical steam recompression module 140 is supplied to the second stripper 111 to separate the feedstock, and the remainder is supplied to the first stripper 111 to separate the feedstock. do. At this time, the water vapor passed through the mechanical vapor recompression module 140 is first compressed to the temperature and pressure required by the first stripper 111. Since the second stripper 112 is driven at a higher temperature than the first stripper 111, additional compression of water vapor passing through the mechanical vapor recompression module 140 is required.
- Saturated water vapor is compressed while passing through the thermal steam recompression module 150 to have the temperature and pressure required by the second stripper 112, and the third valve 173 configured in the thermal steam recompression module 150 automatically.
- the amount of steam required for the second stripper 112 is supplied by this.
- the saturated water vapor passing through the second module 142 is preferentially introduced into the second stripper 112. Therefore, the thermal vapor recompression module 150 sucks saturated water vapor passed through the second module 142 to induce the inflow to the second stripper 112 side.
- the thermal vapor recompression module 150 sucks the saturated water vapor passed through the second module 142 to induce the inflow to the second stripper 112 side first.
- the steam supply unit 160 is configured to supply steam to the stripper module 110, that is, the first stripper 111 and the second stripper 112 and the thermal steam recompression module 150.
- steam supplied from the steam supply unit 160 is supplied to the first stripper 111, heat is directly contacted with the high boiling point material in the lower portion, and the low boiling point material in the mixture is evaporated by this heat and discharged into the upper steam together with water vapor. .
- the valve 170 is configured to control whether steam is supplied to the stripper module 110, and includes a first valve 171, a second valve 172, and a third valve 173.
- the first valve 171 is a component for controlling the supply of steam supplied from the steam supply unit 160 to the first stripper 111.
- the first valve 171 controls the amount of steam supplied to the first stripper 111 according to the temperature conditions required to separate the feedstock from the first stripper 111.
- the first valve 171 is opened at the beginning of driving of the distillation system 100 to allow steam to be supplied into the first stripper 111.
- the steam condensed water of the reboiler 190 is compressed in the second module 142 via the first module 141 until the vapor condensed water is supplied to the laminator 143 and preferentially in the thermal vapor recompression module 150.
- the recompressed steam is supplied to the second stripper 142.
- the shortage of the second valve 173 of the thermal vapor recompression module 150 is supplied by the second valve 172.
- the second valve 172 is a component for controlling whether the steam supplied from the steam supply unit 160 to the second stripper 112 is supplied. Unlike the first valve 171, the second valve 172 is not opened at the initial stage of driving of the apparatus, and after driving the third valve 173, steam supplied from the third valve 173 as described below. The amount of is opened when the steam supply amount for gas-liquid pressure equilibrium with the first stripper 111 is insufficient to replenish steam so that the feedstock is separated from the second stripper 112.
- the third valve 173 is a component for controlling whether the steam supplied from the steam supply unit 160 to the second stripper 112 is supplied.
- the steam is not directly supplied to the second stripper 112 like the second valve 172, but is configured to be supplied to the thermal steam recompression module 150. That is, the amount of steam supplied to the thermal steam recompression module 150 is limited according to the temperature condition required by the second stripper 112, and the steam is compressed in the thermal steam recompression module 150 and then the second stripper. It is supplied to 111.
- the distillation tower 180 is for rectifying the condensed water generated by the condenser 120, and the reboiler 190 is a configuration for supplying steam from the distillation tower 180.
- the condensate of steam generated in the reboiler 190 is expanded and evaporated and then supplied to the laminator 143.
- the temperature of the vapor that is evaporated and supplied to the laminator 143 and the steam supplied to the laminator 143 from the first module 141 are different, but the same temperature in the laminator 143 becomes the second module. Supplied.
- FIG. 4 is a view schematically showing the operation of the condensate generated in the condenser of the distillation system using the multi-stage stripper of FIG. 3 before being supplied to the distillation column.
- the feedstock is supplied to the first stripper 111 from the supply portion.
- the first valve 171 controlled according to a condition such as the temperature required by the first stripper 111 is opened to supply steam to the first stripper 111 from the steam supply unit 160. Steam transfers heat by directly contacting the high boiling point material below the first stripper 111. By this heat, the low boiling point material having a boiling point below a predetermined temperature in the feedstock is evaporated and discharged into the upper steam together with water vapor, and the high boiling point material is undistilled and supplied to the second stripper 112.
- the upper steam discharged from the first stripper 111 is introduced into the condensation evaporator 120.
- the upper steam is partially condensed in the condensation evaporator 120, and transfers heat to the water supplied to the condensation evaporator 120 from a separate water source.
- the water transferred from the upper steam is saturated steam and is supplied to the mechanical vapor recompression module 140, and the uncondensed upper steam is supplied to the condenser 130.
- Saturated water vapor generated by the condensation evaporator 120 is supplied to the first module 141.
- a flow controller 144 may be installed to control the flow rate of the saturated steam supplied to the first module 141.
- Saturated water vapor is supplied to the laminator 143 after the multi-stage compression while passing through the first module (141). While passing through the first module 141, saturated steam increases in velocity and pressure, and vortices are formed by the rotation of the impeller. For this reason, the distribution of the inlet vapor density into the second module 142 is not uniform, which may cause damage to the second module 142. However, the laminator 143 lowers the velocity pressure of the saturated steam, prevents the formation of vortices, preferably moves linearly, and allows the saturated steam to flow into the second module 142 at a uniform vapor density.
- the static pressure is increased by lowering the speed pressure, but as a uniform vapor density flows into the second module 142 as compared with the case where the speed pressure is high, the damage of the device does not occur.
- the saturated water vapor introduced into the second module 142 through the laminator 142 is additionally compressed in multiple stages to be a temperature and pressure condition for separating the feedstock from the first stripper 111.
- a portion of the saturated steam discharged from the second module 142 is preferentially sucked by the thermal vapor recompression module 150. That is, some of the saturated steam discharged from the second module 142 is supplied to the thermal vapor recompression module 150, and the other is supplied to the first stripper 111. Saturated water vapor introduced into the thermal vapor recompression module 150 is further compressed to the temperature and pressure required by the second stripper 112, and then separates the feedstock from the second stripper 112. At this time, the amount of upper steam generated in the first stripper 111 is not sufficient at the initial stage of the driving of the distillation system 100, and some of them are transferred to the second stripper 112 by the thermal vapor recompression module 150. It is supplied but is insufficient during the initial operation, it is supplemented by the control by the second valve (172).
- the upper steam generated by the steam is supplied to the second stripper 112 to separate the feedstock is supplied to the first stripper 111. Since the temperature required by the second stripper 112 is higher than that of the first stripper 111, the upper steam of the second stripper 112 may be used as a heat source of the first stripper 111.
- the second valve 172 for supplying steam to the second stripper 112 is closed and the third valve 173 is closed. The first stripper 111 and the second stripper 112 enter a stable operation state by the control.
- the condensate generated and separated in the condenser in this process is supplied to the distillation tower 180, and the vapor condensed and expanded by the reboiler 190 flows into the laminator 143 to allow the first module 141 and the second module 142. Will enter stable operation.
- FIG. 5 is a view schematically showing the operation after condensate generated in the condenser of the distillation system using the multi-stage stripper of FIG. 3 is supplied to the distillation column.
- the upper steam not condensed in the condensation evaporator 120 is supplied to the condenser 130 and finally condensed.
- the condensate generated and separated in the condenser 130 is supplied to the distillation tower 180 and rectified. At this time, steam is supplied from the reboiler 190 for rectification in the distillation column 180.
- the laminator 143 uniformly adjusts the temperature of saturated steam and steam and lowers the speed pressure to be supplied to the second module 142. That is, compared to before the condensate is supplied to the distillation column 180, the amount of saturated steam supplied to the second module 142 and compressed is increased.
- the saturated steam discharged from the second module 142 is supplied by the thermal vapor recompression module 150 to the second stripper 112 after being compressed by suction.
- the steam generated from the steam condensate discharged from the reboiler 190 is added, so that the amount of steam supplied to the second stripper 112 is enough to supply the third valve 173 to the thermal steam recompression module 150. Design it.
- the upper steam generated by the stripping reaction in the second stripper 112 is supplied to the first stripper 111. Since the amount of steam supplied to the second stripper 112 is sufficient, the amount of upper steam supplied to the first stripper 11 is increased, and the amount of saturated steam discharged from the second module 142 is increased. The amount of saturated steam supplied to the first stripper 111 increases. Therefore, the amount of steam required by the first stripper 111 is sufficient, and thus, whether or not the new supply steam can be shut off by closing the first valve 171 depends on the composition of the multi-stage stripper upper steam. It is usually expected that some supplemental steam will be required.
- the vaporized water vapor is compressed in multiple stages and supplied to at least two or more strippers, thereby increasing the heat recovery rate of the upper steam of the stripper.
- a distillation system using a multi-stage stripper that can reduce the cost of the distillation process.
- a distillation system that separates the mixture by boiling point difference, the water is evaporated using the upper steam discharged from the module by the stripper, and then the vaporized steam is multistage compressed and fed to at least two strippers,
- a distillation system using a multi-stage stripper with integrated operation and reduced steam consumption which increases the heat recovery of the upper steam and reduces the cost of the distillation process.
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Abstract
Description
Claims (12)
- 공급원료 중에 존재하는 혼합물질을 비점차에 의하여 저비점물질과 고비점물질로 분리하는 증류시스템에 있어서,복수 개의 스트리퍼로 마련되며, 상기 공급원료를 공급받아 상기 저비점물질이 증발되어 상부증기로 배출되며 상기 고비점물질이 하부에서 미증류 분리되되, 상기 각각의 스트리퍼에서 증발되는 저비점물질의 기액 평형 압력과 온도가 서로 상이한 스트리퍼 모듈;물 공급원으로부터 공급된 물이 상기 스트리퍼 모듈을 통과한 상기 상부증기와 열교환하여 상기 상부증기 및 물이 각각 응축 및 증발되는 응축증발기;상기 응축증발기에서 증발된 수증기를 다단으로 압축하는 기계적 증기 재압축(MVR:Mechanical Vapor Recompression) 모듈;상기 기계적 증기 재압축 모듈에서 압축된 수증기는 적어도 2개 이상의 스트리퍼에 공급되는 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템.
- 제1항에 있어서,상기 기계적 증기 재압축 모듈에서 압축된 수증기 중 일부는, 증발되는 저비점물질의 온도가 가장 높은 스트리퍼에 공급되는 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템.
- 제2항에 있어서,상기 스트리퍼 모듈은,상기 공급원료를 공급받아, 상기 저비점물질이 증발되어 상부증기로 배출되며 상기 고비점물질이 하부에서 미증류 분리되는 제1스트리퍼; 상기 제1스트리퍼 보다 높은 온도에서 구동하며, 상기 제1스트리퍼에서 증발되지 않은 물질을 공급받아, 저비점물질이 탈거되어 상부증기로 배출되며 고비점물질이 하부에서 미증류 분리되는 제2스트리퍼;를 포함하며,상기 기계적 증기 재압축 모듈에서 압축된 수증기 중 일부는 우선적으로 상기 제2스트리퍼로 공급되며, 나머지는 상기 제1스트리퍼로 공급되는 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템.
- 제3항에 있어서,상기 기계적 증기 재압축 모듈을 통과하는 수증기의 온도 및 압력은 상기 제1스트리퍼에서 상기 공급원료를 분리하는데 요구되는 온도 및 압력이며,상기 기계적 증기 재압축 모듈을 통과하는 수증기의 일부가 상기 제2스트리퍼 측으로 공급되도록 유도하며, 상기 제2스트리퍼로 공급되는 수증기의 온도 및 압력을 상기 제2스트리퍼에서 상기 공급원료를 분리하는데 요구되는 온도 및 압력으로 증가시키는 열적 증기 재압축 모듈(TVR:Thermal Vapor Recompression)을 더 포함하는 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템.
- 제4항에 있어서,상기 제2스트리퍼의 상부증기는 상기 제1스트리퍼에 공급되어, 상기 제1스트리퍼에서 상기 공급원료를 분리하는데 필요한 열원으로 사용되는 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템.
- 제5항에 있어서,상기 제1스트리퍼 및 상기 제2스트리퍼에 스팀을 공급하는 스팀 공급부; 개폐가능하게 마련되어 상기 제1스트리퍼로의 상기 스팀 공급 여부를 제어하는 제1밸브; 개폐가능하게 마련되어 상기 제2스트리퍼로의 상기 스팀 공급 여부를 제어하는 제2밸브;를 더 포함하는 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템.
- 제6항에 있어서,개폐가능하게 마련되며, 상기 스팀 공급부로부터 공급되는 상기 스팀의 일부를 상기 열적 증기 재압축 모듈 측으로 유도하는 제3밸브를 더 포함하는 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템.
- 제7항에 있어서,상기 기계적 증기 재압축 모듈은 복수 개의 기계적 증기 재압축 장치로 마련되는 제1모듈; 복수 개의 기계적 증기 재압축 장치로 마련되며, 상기 제1모듈을 통과한 수증기를 추가적으로 압축하는 제2모듈; 상기 제1모듈을 통과한 압축된 수증기의 속도를 낮추어 상기 제2모듈로 공급시키는 라미네이터;를 포함하는 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템.
- 제8항에 있어서,상기 증발기에서 응축되지 않은 상부증기를 공급받아 응축하는 응축기;상기 응축기에서 응축된 응축액을 공급받는 증류탑을 더 포함하는 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템.
- 제9항에 있어서,상기 증류탑에 스팀을 공급하는 재비기를 더 포함하며,상기 재비기의 스팀 응축수는 증발되어 상기 라미네이터로 공급되는 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템.
- 제10항에 있어서,상기 라미네이터는 상기 제1모듈을 통과한 압축된 수증기와 상기 재비기로부터 공급된 스팀 응축수가 증발된 증기의 온도를 동일하게 하는 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템.
- 제7항에 있어서,상기 제1모듈의 유입단에는, 유량 제어부가 설치되는 통합 운전과 소모 스팀 감량화가 가능한 다단 스트리퍼를 이용하는 증류 시스템.
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US15/303,910 US10486081B2 (en) | 2014-04-14 | 2014-04-25 | Distillation system using multi stage stripper capable of integrated operation and steam consumption reduction |
CN201480000344.0A CN105188870B (zh) | 2014-04-14 | 2014-04-25 | 利用可一体化操作并能降低蒸汽消耗量的多级汽提器的蒸馏系统 |
ES14889267T ES2702189T3 (es) | 2014-04-14 | 2014-04-25 | Sistema de destilación que utiliza una columna de extracción de múltiples etapas que puede realizar una operación integrada y una reducción del consumo de vapor |
EP14889267.2A EP3132836B1 (en) | 2014-04-14 | 2014-04-25 | Distillation system using multistage stripper capable of integrated operation and steam consumption reduction |
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CN111170389A (zh) * | 2020-01-09 | 2020-05-19 | 长沙矿冶研究院有限责任公司 | 一种氨氮废水汽提蒸氨系统和方法 |
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CN105188870B (zh) | 2017-02-22 |
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US10486081B2 (en) | 2019-11-26 |
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