CN106084283A - Production of PVC is with reclaiming monomer processing means and Production of PVC with reclaiming monomer processing method - Google Patents

Production of PVC is with reclaiming monomer processing means and Production of PVC with reclaiming monomer processing method Download PDF

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Publication number
CN106084283A
CN106084283A CN201610495582.4A CN201610495582A CN106084283A CN 106084283 A CN106084283 A CN 106084283A CN 201610495582 A CN201610495582 A CN 201610495582A CN 106084283 A CN106084283 A CN 106084283A
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China
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monomer
tower
recovery
reclaim
reclaiming
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CN201610495582.4A
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CN106084283B (en
Inventor
王世刚
冯亮
刘枫
张宝华
杨振波
王志军
赵爱民
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Xinjiang Zhongtai Chemical Co Ltd
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Xinjiang Zhongtai Chemical Co Ltd
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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
    • 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
    • C08F14/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen
    • C08F14/02—Monomers containing chlorine
    • C08F14/04—Monomers containing two carbon atoms
    • C08F14/06—Vinyl chloride
    • 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
    • C08J2327/00—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers
    • C08J2327/02—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers not modified by chemical after-treatment
    • C08J2327/04—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers not modified by chemical after-treatment containing chlorine atoms
    • C08J2327/06—Homopolymers or copolymers of vinyl chloride
    • 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
    • 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

Abstract

The present invention relates to Production of PVC and reclaim monomer technical field, be that a kind of Production of PVC reclaims monomer processing means and Production of PVC reclaims monomer processing method.Including caustic wash tower, reclaim first-stage condenser, recovery secondary condenser, liquid seal trough, recovery monomer rectifying tower, recovery monomer delivery pump and polymerization inhibitor storage tank；It is installed with gas phase in the tower body bottom of caustic wash tower and reclaims monomer house steward, be installed with alkali liquor on the tower body top of caustic wash tower and enter tower tube line, go out tower tube line being installed with alkali liquor at the bottom of the tower of caustic wash tower.The present invention can the most effectively remove high-boiling components impurity and the auxiliary agent of residual in recovery monomer, thus improve recovery monomer mass, make to reclaim monomer mass stable, initiator amount keeps balance, resin whiteness effectively improves, while solving subsequent technique pipeline, equipment autohemagglutination problem, it is achieved that the saving and the product quality that produce auxiliary agent raw material promote.

Description

Production of PVC is single with reclaiming with reclaiming monomer processing means and Production of PVC Body processing method
Technical field
The present invention relates to Production of PVC and reclaim monomer technical field, be that a kind of Production of PVC reclaims monomer Processing means and Production of PVC are with reclaiming monomer processing method.
Background technology
Domestic PVC industry dog-eat-dog at present, for adapting to market environment, is promoted by technological transformation and optimization and produces Quality, packaging process units stable operation to reduce production cost significant.The quality reclaiming monomer is to affect PVC product The key that in quality whiteness index, process unit, in line equipment generation autohemagglutination and polymerization production process, initiator amount is big because of Element, and reclaim monomer mass can effectively control residual initiator therein, initiator free radical, high-boiling components and other residual Auxiliary agent content is attached most importance to influence factor.China PVC industry does not carries out spy to the above influence factor reclaiming monomer for many years Fixed process, the recovery monomer decrement jump that resin whiteness control indexes aspect will remain in after being polymerized produces to upstream vinyl chloride Operation, increase in polymerization production process on the consumption of heat stabilizer, and to recovery process assembling device pipeline and equipment autohemagglutination then Controlled by polymerization inhibitor consumption in annual periodic inspection or increase pipeline system.Also can realize on these method surfaces promoting PVC product whiteness index, the purpose that system autohemagglutination affects that reduces, but the PVC thereby resulted in produces auxiliary agent cost and raises, in PVC Under quality, degradation problem still annoyings PVC manufacturing enterprise.
Summary of the invention
The invention provides a kind of Production of PVC and reclaim monomer processing means and Production of PVC recovery list Body processing method, overcomes the deficiency of above-mentioned prior art, and it can effectively solve China's PVC industry the most not to reclaiming monomer The problem that the influence factors such as residual initiator, initiator free radical, high-boiling components and other residual auxiliary agent content carry out particular procedure.
One of technical scheme is realized by following measures: a kind of Production of PVC reclaims monomer Processing means, including caustic wash tower, reclaims first-stage condenser, recovery secondary condenser, liquid seal trough, recovery monomer rectifying tower, recovery Monomer delivery pump and polymerization inhibitor storage tank；It is installed with gas phase in the tower body bottom of caustic wash tower and reclaims monomer house steward, at caustic wash tower Tower body top be installed with alkali liquor and enter tower tube line, go out tower tube line, in alkali cleaning being installed with alkali liquor at the bottom of the tower of caustic wash tower It is installed with recovery monomer between tower top and the thermal medium charging aperture reclaiming first-stage condenser of tower and goes out tower tube line, reclaim one-level It is installed with condenser between the gas outlet of condenser overhead with the thermal medium charging aperture reclaiming secondary condenser and is connected pipeline, Reclaim and on the gas outlet at secondary condenser top, be installed with exhaust line, reclaim the thermal medium discharging bottom first-stage condenser Lower liquid pipe it is installed with respectively between thermal medium discharging opening and the charging aperture of liquid seal trough bottom mouth and recovery secondary condenser Line, is installed with condensation water conveying pipe, the feed opening of liquid seal trough bottom and the charging reclaiming monomer rectifying tower bottom liquid seal trough It is installed with rectifying column feed line between Kou, rectifying column feed line is installed with recovery monomer delivery pump, returns The tower top receiving monomer rectifying tower is installed with rectification gas phase discharge pipe, reclaims and fixedly mounts on the discharging opening of monomer rectifying tower There is recovery monomer finished product feed-stock pipeline, reclaim and be installed with reboiler discharge line on the reboiler of monomer rectifying tower, inhibition Being installed with polymerization inhibitor charge pipe between agent storage tank and the close rectifying column feed line reclaiming monomer rectifying tower, polymerization inhibitor adds It is installed with polymerization inhibitor charge pump on material pipe.
Further optimization and/or improvements to foregoing invention technical scheme one of are presented herein below:
Above-mentioned Production of PVC reclaims monomer processing means and also includes Alkali liquid compounding tank and caustic wash tower circulating pump；Alkali liquor The discharge end of the other end and Alkali liquid compounding tank that enter tower tube line is fixedly installed togather, and enters at alkali liquor and is installed with on tower tube line Caustic wash tower circulating pump, the alkali liquor between caustic wash tower circulating pump and caustic wash tower enters to be installed with alkaline stream gauge on tower tube line respectively With alkaline stream adjustable valve, the alkali liquor between Alkali liquid compounding tank and caustic wash tower circulating pump enters tower tube line and goes out the another of tower tube line with alkali liquor One end is fixedly installed togather；The upper end of Alkali liquid compounding tank is installed with Alkali liquid compounding tank exhaust line.
Above-mentioned alkali liquor after alkaline stream gauge and alkaline stream adjustable valve enters that to be installed with alkali liquor on tower tube line pre- Hot device, alkali liquor enters the cold medium of tower tube line and alkali liquor preheater and imports and exports and be fixedly installed togather；Or/and, Alkali liquid compounding tank is arranged Internally piloted valve it is installed with on gas pipeline；Or/and, the other end of Alkali liquid compounding tank exhaust line is positioned at alkali liquor security personnel and accepts cylinder In.
Above-mentioned Production of PVC reclaims monomer processing means and also includes that recovery monomer finished product condenser, recovery monomer return Stream tank and recovery monomer finished product delivery pump, the other end of rectification gas phase discharge pipe and the thermal medium reclaiming monomer finished product condenser Feed end is fixedly installed togather, and reclaims and is installed with condenser exhaust gas pipeline on monomer finished product condenser, reclaims monomer and becomes It is installed with overhead condenser blanking pipeline between thermal medium discharge end and the recovery monomers flow back tank of product condenser, reclaims single It is installed with return tank discharging pipeline, on return tank discharging pipeline between body return tank and recovery monomer finished product feed-stock pipeline It is installed with recovery monomer finished product delivery pump, the polymerization inhibitor charge pipe after polymerization inhibitor charge pump and rectification gas phase discharge pipe And between overhead condenser blanking pipeline, it is installed with rectifying tower top polymerization inhibitor charge pipe and finished product cold blanking polymerization inhibitor respectively Charge pipe, fixes peace on the recovery monomer finished product feed-stock pipeline reclaimed between monomer rectifying tower and return tank discharging pipeline respectively Equipped with return flow control valve and return flow meter, near reclaiming the polymerization inhibitor charge pipe of monomer rectifying tower, rectifying tower top resistance Control valve it is installed with respectively on poly-agent charge pipe and finished product cold blanking polymerization inhibitor charge pipe.
Recovery monomer rectifying feed it is installed with on above-mentioned rectifying column feed line after reclaiming monomer delivery pump Groove, is installed with recovery single on the rectifying column feed line reclaimed between monomer rectifying feeder channel and recovery monomer rectifying tower Body rectifying column feed pump；Or/and, the other end condensing water conveying pipe is installed with condensate water collecting tank, condensate water collecting tank Tank base be installed with condensation water drainage pipeline, condensation water drainage pipeline is provided with automatic valve, condense water receive It is installed with liquidometer on collection tank；Or/and, the other end reclaiming monomer finished product feed-stock pipeline is installed with recovery monomer one-tenth Product groove.
The two of technical scheme are realized by following measures: the above-mentioned Production of PVC of a kind of employing is used Reclaim the Production of PVC recovery monomer processing method that monomer processing means is carried out, carry out in the steps below: the first step, gas Reclaim monomer mutually to reclaim monomer house steward by gas phase and enter into caustic wash tower bottom, gas phase recovery monomer in caustic wash tower from bottom to top Flowing, meanwhile, is entered, by alkali liquor, the top that tower tube line is delivered in caustic wash tower by the alkali liquor that concentration is 15% to 20%, and alkali liquor exists In caustic wash tower, flowing from top to bottom is reclaimed monomer and is inversely contacted and wash gas phase recovery monomer with gas phase, and wherein, gas phase reclaims single It is 700m3/h to 15000m3/h at 0.15Mpa to 0.25Mpa, flow that body enters the Stress control of caustic wash tower, each layer in caustic wash tower The temperature of tower tray is 40 DEG C to 50 DEG C, and the pressure reduction at the bottom of caustic wash tower tower top and tower is less than 0.01Mpa；Second step, washes through caustic wash tower Gas phase after washing reclaims monomer and goes out tower tube line and sequentially enter recovery first-stage condenser and reclaim secondary condenser and enter by reclaiming monomer Row cooling liquid, wherein, controls by reclaiming first-stage condenser and reclaiming the temperature of secondary condenser liquid phase recovery monomer out It it is 15 DEG C to 25 DEG C；3rd step, liquid phase reclaims monomer and removes the water reclaimed in monomer in lower liquid pipeline enters liquid seal trough, its In, the liquid phase controlling liquid seal trough reclaims the water content of monomer less than 0.04%；4th step, reclaims monomer by rectifying column by liquid phase Feed line and reclaim monomer delivery pump and be delivered to reclaim in monomer rectifying tower and carry out rectification process, by polymerization inhibitor charge pipe to Enter and reclaim the liquid phase of monomer rectifying tower and reclaim monomer adds polymerization inhibitor, the gas phase after reclaiming monomer rectifying tower and processing by Rectification gas phase discharge pipe is discharged, and the recovery monomer after reclaiming monomer rectifying tower and processing is by reclaiming monomer finished product feed-stock pipeline Discharging, wherein, the flow controlling to enter the liquid phase recovery monomer reclaiming monomer rectifying tower is 10m3/h to 35m3/h, controls to reclaim The pressure of monomer rectifying column overhead is 0.25Mpa to 0.30Mpa, temperature is 21 DEG C to 23 DEG C, by reclaiming monomer rectifying tower again Boiling device control recovery pressure at the bottom of monomer rectifying tower tower is 0.30Mpa to 0.35Mpa, temperature is 30 DEG C to 40 DEG C, reclaims monomer The discharge capacity of rectifying column high-boiling components is 5kg/h to 35kg/h, and the addition of polymerization inhibitor is that liquid phase per ton reclaims monomer addition 3g extremely 6g polymerization inhibitor.
The three of technical scheme are realized by following measures: the above-mentioned Production of PVC of a kind of employing is used Reclaim the Production of PVC recovery monomer processing method that monomer processing means is carried out, carry out in the steps below: the first step, beat Open internally piloted valve, Alkali liquid compounding tank is prepared the alkali liquor of 15% to 20%；Second step, gas phase is reclaimed monomer and is reclaimed by gas phase single Body house steward enters into caustic wash tower bottom, and gas phase reclaims monomer and flows from bottom to top in caustic wash tower, meanwhile, will be joined by alkali liquor The alkali liquor that tank processed prepares is entered, by alkali liquor, the top that tower tube line is delivered in caustic wash tower, alkali liquor in caustic wash tower from top to bottom flowing with Gas phase reclaims monomer and inversely contacts and wash gas phase recovery monomer, and washed gas phase reclaims the alkali liquor of monomer and goes out tower tube through alkali liquor Line is gone out tower tube line by alkali liquor and discharges, and is delivered to caustic wash tower top by caustic wash tower circulating pump and is circulated utilization, and wherein, gas phase is returned Receive monomer entering the Stress control of caustic wash tower is 700m3/h to 15000m3/h at 0.15Mpa to 0.25Mpa, flow, in caustic wash tower The temperature of each layer tower tray is 40 DEG C to 50 DEG C, and the pressure reduction at the bottom of caustic wash tower tower top and tower is less than 0.01Mpa, by alkaline stream gauge and The circular flow of flux of alkaline liquor governor valve control alkali liquor is 40m3/h to 50m3/h；3rd step, the gas after caustic wash tower washs Mutually reclaim monomer by reclaim monomer go out tower tube line sequentially enter recovery first-stage condenser and reclaim secondary condenser carry out coolant Change, wherein, control by reclaim first-stage condenser and reclaim secondary condenser liquid phase out reclaim the temperature of monomer be 15 DEG C extremely 25℃；4th step, liquid phase reclaims monomer and removes the water reclaimed in monomer in lower liquid pipeline enters liquid seal trough, wherein, controls The liquid phase of liquid seal trough reclaims the water content of monomer less than 0.04%；5th step, reclaims monomer by rectifying column feed line by liquid phase Rectification process is carried out, by polymerization inhibitor charge pipe to entering recovery with reclaiming in monomer delivery pump is delivered to reclaim monomer rectifying tower The liquid phase of monomer rectifying tower reclaims and adds polymerization inhibitor in monomer, and the gas phase after reclaiming monomer rectifying tower and processing is by rectification gas phase Discharge pipe is discharged, and the recovery monomer after reclaiming monomer rectifying tower and processing is discharged by reclaiming monomer finished product feed-stock pipeline, its In, the flow controlling to enter the liquid phase recovery monomer reclaiming monomer rectifying tower is 10m3/h to 35m3/h, controls to reclaim monomer essence The pressure evaporating column overhead is 0.25Mpa to 0.30Mpa, temperature is 21 DEG C to 23 DEG C, reclaim the discharge of monomer rectifying tower high-boiling components Amount is 5kg/h to 35kg/h, and the pressure controlled at the bottom of recovery monomer rectifying tower tower by reclaiming monomer rectifying tower reboiler is 0.30Mpa to 0.35Mpa, temperature are 30 DEG C to 40 DEG C, and the addition of polymerization inhibitor is that liquid phase per ton reclaims monomer addition 3g to 6g Polymerization inhibitor.
The four of technical scheme are realized by following measures: the above-mentioned Production of PVC of a kind of employing is used Reclaim the Production of PVC recovery monomer processing method that monomer processing means is carried out, carry out in the steps below: the first step, gas Reclaim monomer mutually to reclaim monomer house steward by gas phase and enter into caustic wash tower bottom, gas phase recovery monomer in caustic wash tower from bottom to top Flowing, meanwhile, is entered, by alkali liquor, the top that tower tube line is delivered in caustic wash tower by alkali liquor, and alkali liquor flows in caustic wash tower from top to bottom The dynamic monomer that reclaims with gas phase inversely contacts and washs gas phase recovery monomer, and washed gas phase reclaims the alkali liquor of monomer and goes out through alkali liquor Tower tube line is gone out tower tube line by alkali liquor and discharges, and is delivered to caustic wash tower top by caustic wash tower circulating pump and is circulated utilization, wherein, and gas Reclaim monomer mutually entering the Stress control of caustic wash tower is 700m3/h to 15000m3/h at 0.15Mpa to 0.25Mpa, flow, alkali cleaning In tower, the temperature of each layer tower tray is 40 DEG C to 50 DEG C, and the pressure reduction at the bottom of caustic wash tower tower top and tower is less than 0.01Mpa；Second step, passes through Caustic wash tower washing after gas phase reclaim monomer by reclaim monomer go out tower tube line sequentially enter recovery first-stage condenser and reclaim two grades Condenser carries out cooling liquid, wherein, controls the liquid phase recovery by reclaiming first-stage condenser with reclaim secondary condenser out single The temperature of body is 15 DEG C to 25 DEG C；3rd step, liquid phase reclaims monomer and removes in lower liquid pipeline enters liquid seal trough in recovery monomer Water, wherein, the liquid phase controlling liquid seal trough reclaims the water content of monomer less than 0.04%；4th step, reclaims monomer by liquid phase Carry out rectification process in being delivered to reclaim monomer rectifying tower by rectifying column feed line and recovery monomer delivery pump, pass through polymerization inhibitor Charge pipe, rectifying tower top polymerization inhibitor charge pipe and finished product cold blanking polymerization inhibitor charge pipe are respectively to rectifying column feed line, rectification In gas phase discharge pipe and overhead condenser blanking pipeline add polymerization inhibitor, through recovery monomer rectifying tower process after gas phase by Rectification gas phase discharge pipe drains into and reclaims recovery monomer remaining in monomer finished product condenser condensation gas phase, becomes through reclaiming monomer Gas after product condenser processes is discharged by condenser exhaust gas pipeline, through reclaiming the recovery that monomer finished product condenser condenses out Monomer is delivered to reclaim monomers flow back tank by overhead condenser blanking pipeline, then through return tank discharging pipeline and recovery monomer finished product The recovery monomer part reclaimed in monomers flow back tank is back to reclaim monomer rectifying tower, a part and pass through recovery by delivery pump Recovery monomer after monomer rectifying tower processes is discharged by recovery monomer finished product feed-stock pipeline together, wherein, controls to enter and reclaims list It is 10m3/h to 35m3/h that the liquid phase of body rectifying column reclaims the flow of monomer, and the pressure controlling to reclaim monomer rectifying column overhead is 0.25Mpa to 0.30Mpa, temperature are 21 DEG C to 23 DEG C, control to reclaim monomer rectifying tower by reclaiming monomer rectifying tower reboiler The discharge capacity that pressure at the bottom of tower is 0.30Mpa to 0.35Mpa, temperature is 30 DEG C to 40 DEG C, reclaim monomer rectifying tower high-boiling components is 5kg/h to 35kg/h, the addition of polymerization inhibitor is that liquid phase per ton reclaims monomer addition 3g to 6g polymerization inhibitor everywhere, is back to reclaim The flow reclaiming monomer of monomer rectifying tower is 20m3/h to 25m3/h, reclaims the inlet water temperature control of monomer finished product condenser System, at 15 DEG C to 30 DEG C, is recovery monomer in 1m3/h to 2m3/h, gas by the flow of condenser exhaust gas pipeline expellant gas Content be 10% to 35%.
The five of technical scheme are realized by following measures: the above-mentioned Production of PVC of a kind of employing is used Reclaim the Production of PVC recovery monomer processing method that monomer processing means is carried out, carry out in the steps below: the first step, beat Open internally piloted valve, Alkali liquid compounding tank is prepared the alkali liquor of 15% to 20%；Second step, gas phase is reclaimed monomer and is reclaimed by gas phase single Body house steward enters into caustic wash tower bottom, and gas phase reclaims monomer and flows from bottom to top in caustic wash tower, meanwhile, will be joined by alkali liquor The alkali liquor that tank processed prepares is entered, by alkali liquor, the top that tower tube line is delivered in caustic wash tower, alkali liquor in caustic wash tower from top to bottom flowing with Gas phase reclaims monomer and inversely contacts and wash gas phase recovery monomer, and washed gas phase reclaims the alkali liquor of monomer and goes out tower tube through alkali liquor Line is gone out tower tube line by alkali liquor and discharges, and is delivered to caustic wash tower top by caustic wash tower circulating pump and is circulated utilization, and wherein, gas phase is returned Receive monomer entering the Stress control of caustic wash tower is 700m3/h to 15000m3/h at 0.15Mpa to 0.25Mpa, flow, in caustic wash tower The temperature of each layer tower tray is 40 DEG C to 50 DEG C, and the pressure reduction at the bottom of caustic wash tower tower top and tower is less than 0.01Mpa, by alkaline stream gauge and The circular flow of flux of alkaline liquor governor valve control alkali liquor is 40m3/h to 50m3/h；3rd step, the gas after caustic wash tower washs Mutually reclaim monomer by reclaim monomer go out tower tube line sequentially enter recovery first-stage condenser and reclaim secondary condenser carry out coolant Change, wherein, control by reclaim first-stage condenser and reclaim secondary condenser liquid phase out reclaim the temperature of monomer be 15 DEG C extremely 25℃；4th step, liquid phase reclaims monomer and removes the water reclaimed in monomer in lower liquid pipeline enters liquid seal trough, wherein, controls The liquid phase of liquid seal trough reclaims the water content of monomer less than 0.04%；5th step, reclaims monomer by rectifying column feed line by liquid phase Rectification process is carried out, by polymerization inhibitor charge pipe, rectifying tower top with reclaiming in monomer delivery pump is delivered to reclaim monomer rectifying tower Polymerization inhibitor charge pipe and finished product cold blanking polymerization inhibitor charge pipe are respectively to rectifying column feed line, rectification gas phase discharge pipe and tower Adding polymerization inhibitor in the condenser blanking pipeline of top, the gas phase after reclaiming monomer rectifying tower and processing is by rectification gas phase discharge pipe Drain into and reclaim recovery monomer remaining in monomer finished product condenser condensation gas phase, after reclaiming monomer finished product condenser and processing Gas is discharged by condenser exhaust gas pipeline, through reclaiming the recovery monomer that condenses out of monomer finished product condenser by overhead condenser Blanking pipeline is delivered to reclaim monomers flow back tank, then will reclaim monomer through return tank discharging pipeline and recovery monomer finished product delivery pump A recovery monomer part in return tank be back to reclaim monomer rectifying tower, a part and through recovery monomer rectifying tower process after Recovery monomer together by reclaim monomer finished product feed-stock pipeline discharge, wherein, control enter reclaim monomer rectifying tower liquid phase return Receive monomer flow be 10m3/h to 35m3/h, control reclaim monomer rectifying column overhead pressure be 0.25Mpa to 0.30Mpa, Temperature is 21 DEG C to 23 DEG C, and the pressure controlled at the bottom of recovery monomer rectifying tower tower by reclaiming monomer rectifying tower reboiler is The discharge capacity that 0.30Mpa to 0.35Mpa, temperature be 30 DEG C to 40 DEG C, reclaims monomer rectifying tower high-boiling components is 5kg/h to 35kg/ H, the addition of polymerization inhibitor is that liquid phase per ton reclaims monomer addition 3g to 6g polymerization inhibitor everywhere, is back to reclaim monomer rectifying tower The flow reclaiming monomer is 20m3/h to 25m3/h, and the inlet water temperature reclaiming monomer finished product condenser controls at 15 DEG C to 30 DEG C, the flow of condenser exhaust gas pipeline expellant gas it is that to reclaim the content of monomer in 1m3/h to 2m3/h, gas be 10% To 35%.
The present invention can the most effectively remove high-boiling components impurity and the auxiliary agent of residual in recovery monomer, thus it is single to improve recovery Weight so that reclaim monomer mass stable, initiator amount keeps balance, and resin whiteness effectively improves, and is solving While subsequent technique pipeline, the equipment autohemagglutination problem of having determined, it is achieved that the saving and the product quality that produce auxiliary agent raw material promote.
Accompanying drawing explanation
Fig. 1 is the process pipelines schematic flow sheet of embodiment in the present invention.
Fig. 2 is the initiator amount correlation curve before and after the A production line present invention comes into operation.
Fig. 3 is the initiator amount correlation curve before and after the B production line present invention comes into operation.
Fig. 4 is that in the present invention, acetaldehyde curve in monomer is reclaimed in caustic wash tower import and export.
Fig. 5 is that in the present invention, carbon dioxide content curve in monomer is reclaimed in caustic wash tower import and export.
It is caustic wash tower that coding in accompanying drawing is respectively as follows: 1, and 2 is that gas phase reclaims monomer house steward, and 3 go out tower tube line for alkali liquor, and 4 are Reclaiming first-stage condenser, 5 go out tower tube line for reclaiming monomer, and 6 for reclaiming secondary condenser, and 7 connect pipeline for condenser, and 8 is row Gas pipeline, 9 is liquid seal trough, and 10 is lower liquid pipeline, and 11 for condensing water conveying pipe, and 12 for reclaiming monomer rectifying tower, and 13 is rectifying column Feed line, 14 for reclaiming monomer delivery pump, and 15 is rectification gas phase discharge pipe, and 16 for reclaiming monomer finished product feed-stock pipeline, and 17 For reboiler discharge line, 18 is polymerization inhibitor storage tank, and 19 is polymerization inhibitor charge pipe, and 20 is polymerization inhibitor charge pump, and 21 enter for alkali liquor Tower tube line, 22 is Alkali liquid compounding tank, and 23 is caustic wash tower circulating pump, and 24 is alkaline stream gauge, and 25 is alkaline stream adjustable valve, and 26 are Alkali liquid compounding tank exhaust line, 27 is alkali liquor preheater, and 28 is internally piloted valve, and 29 accept cylinder for alkali liquor security personnel, and 30 for reclaiming monomer Finished product condenser, 31 is condenser exhaust gas pipeline, and 32 for reclaiming monomers flow back tank, and 33 is overhead condenser blanking pipeline, and 34 are Return tank discharging pipeline, 35 for reclaiming monomer finished product delivery pump, and 36 is rectifying tower top polymerization inhibitor charge pipe, and 37 is the cold blanking of finished product Polymerization inhibitor charge pipe, 38 is return flow control valve, and 39 is return flow meter, and 40 is control valve, and 41 supply for reclaiming monomer rectifying Hopper, 42 for reclaiming monomer rectifying tower feed pump, and 43 is condensate water collecting tank, and 44 is condensation water drainage pipeline, and 45 is automatic valve Door, 46 is liquidometer, and 47 for reclaiming monomer pan tank.
Detailed description of the invention
The present invention is not limited by following embodiment, can determine specifically according to technical scheme and practical situation Embodiment.In the present invention, all of percent is mass percent, and alkali liquor is sodium hydrate aqueous solution.
In the present invention, for the ease of describing, the description of the relative position relation of each parts is all according to Figure of description 1 Butut mode be described, such as: the position relationship of upper and lower, left and right etc. is based on the Butut direction of Figure of description to be come Determine.
Below in conjunction with embodiment and accompanying drawing, the invention will be further described:
Embodiment 1, as shown in Figure 1, this Production of PVC reclaims monomer processing means and includes caustic wash tower 1, reclaims First-stage condenser 4, recovery secondary condenser 6, liquid seal trough 9, recovery monomer rectifying tower 12, recovery monomer delivery pump 14 and polymerization inhibitor Storage tank 18；It is installed with gas phase in the tower body bottom of caustic wash tower 1 and reclaims monomer house steward 2, fix on the tower body top of caustic wash tower 1 Alkali liquor is installed and enters tower tube line 21, go out tower tube line 3 being installed with alkali liquor at the bottom of the tower of caustic wash tower 1, caustic wash tower 1 tower top with It is installed with recovery monomer between the thermal medium charging aperture of recovery first-stage condenser 4 and goes out tower tube line 5, reclaim first-stage condenser 4 It is installed with condenser between the gas outlet at top with the thermal medium charging aperture reclaiming secondary condenser 6 and is connected pipeline 7, reclaim It is installed with exhaust line 8 on the gas outlet at secondary condenser 6 top, reclaims the thermal medium discharging bottom first-stage condenser 4 Lower liquid it is installed with respectively between thermal medium discharging opening and the charging aperture of liquid seal trough 9 bottom mouth and recovery secondary condenser 6 Pipeline 10, is installed with condensation water conveying pipe 11, the feed opening of liquid seal trough 9 bottom and recovery monomer rectifying bottom liquid seal trough 9 It is installed with rectifying column feed line 13 between the charging aperture of tower 12, rectifying column feed line 13 is installed with recovery Monomer delivery pump 14, the tower top reclaiming monomer rectifying tower 12 is installed with rectification gas phase discharge pipe 15, reclaims monomer rectifying It is installed with recovery monomer finished product feed-stock pipeline 16 on the discharging opening of tower 12, reclaims on the reboiler of monomer rectifying tower 12 fixing Reboiler discharge line 17 is installed, polymerization inhibitor storage tank 18 with near reclaim monomer rectifying tower 12 rectifying column feed line 13 it Between be installed with polymerization inhibitor charge pipe 19, polymerization inhibitor charge pipe 19 is installed with polymerization inhibitor charge pump 20.Alkali liquor is defeated The top delivering to caustic wash tower 1 inversely contacts washing with the gas phase recovery monomer entering caustic wash tower 1 bottom, the gas phase after washing Recovery monomer goes out tower tube line 5 by recovery monomer and discharges；Through reclaiming first-stage condenser 4 and reclaiming secondary condenser 6 coolant Recovery Vinyl Chloride Monomer after change is entered liquid seal trough 9 by lower liquid pipeline 10 and keeps in；Liquid phase in liquid seal trough 9 reclaims monomer by rectification Recovery monomer delivery pump 14 on tower feed line 13 is delivered to reclaim monomer rectifying tower 12 and carries out rectification process, reclaims monomer essence Evaporating to connect bottom tower 12 and have rectifying column reboiler, be used for as Unit heating at the bottom of tower, rectifying column reboiler could be arranged to 2, just Often operate to 1 operation 1 standby；Reclaim the gas phase after the washing of monomer rectifying tower 12 top by rectification gas phase discharge pipe 15 Discharging, the recovery monomer after reclaiming monomer rectifying tower 12 rectification process is sent conduct by reclaiming monomer finished product feed-stock pipeline 16 Polymeric kettle raw materials for production are standby, it is achieved provide raw material for follow-up PVC polymerization；Pressure can be installed by import department at caustic wash tower 1 Power teletransmission is monitored, and polymerization is returned gaseous monomer and is directly entered at caustic wash tower 1 with the high pressure conditions of 0.2MPa to 0.3MPa Reason.Gas phase is reclaimed monomer and sends in caustic wash tower, first remove polrvinyl chloride with certain density liquid caustic soda and reclaim residual in monomer Acidic initiator and living radical, recycling reclaims first-stage condenser 4 and recovery secondary condenser 6 carries out reclaiming monomer gas phase Liquefaction, after be sent to reclaim in monomer rectifying tower 12 and carry out rectification process, in the recovery monomer processed, initiator auxiliary agent is residual Stay and multiple high-boiling components content is greatly lowered, thus improve recovery monomer mass, to arrive remove impurity raising recovery monomer purity Purpose, for improve Corvic whiteness index provide safeguard.
Embodiment 2, as the optimization of above-described embodiment, as shown in Figure 1, this Production of PVC processes with reclaiming monomer Device also includes Alkali liquid compounding tank 22 and caustic wash tower circulating pump 23；Alkali liquor enters the other end and the Alkali liquid compounding tank 22 of tower tube line 21 Discharge end is fixedly installed togather, and enters to be installed with caustic wash tower circulating pump 23 on tower tube line 21 at alkali liquor, caustic wash tower circulating pump Alkali liquor between 23 and caustic wash tower 1 enters to be installed with respectively on tower tube line 21 alkaline stream gauge 24 and alkaline stream adjustable valve 25, it is solid with the other end that alkali liquor goes out tower tube line 3 that the alkali liquor between Alkali liquid compounding tank 22 and caustic wash tower circulating pump 23 enters tower tube line 21 Dingan County is fitted together；The upper end of Alkali liquid compounding tank 22 is installed with Alkali liquid compounding tank exhaust line 26.Alkali liquor in caustic wash tower 1 Alkali liquor circulation is carried out by caustic wash tower circulating pump 23；Alkali liquid compounding tank 22 is provided with fixing compound method and concentration；Alkali liquid compounding During Alkali liquid compounding tank exhaust line 26 open, Alkali liquid compounding operating process completely cuts off completely with caustic wash tower 1, in atmospheric conditions Complete formulation operations；Alkaline stream gauge 24 and alkaline stream adjustable valve 25 can be according to the flow of gas phase in entrance caustic wash tower 1 to alkali Flow quantity carries out size control.
Embodiment 3, as the optimization of embodiment 2, as shown in Figure 1, at alkaline stream gauge 24 and alkaline stream adjustable valve Alkali liquor after 25 enters to be installed with alkali liquor preheater 27 on tower tube line 21, and alkali liquor enters tower tube line 21 and alkali liquor preheater 27 Cold medium is imported and exported and is fixedly installed togather；Or/and, Alkali liquid compounding tank exhaust line 26 is installed with internally piloted valve 28；Or/ With, the other end of Alkali liquid compounding tank exhaust line 26 is positioned at alkali liquor security personnel and accepts cylinder 29.Alkali liquor preheater 27 can be to circulation alkali Liquid carries out lowering the temperature and warming temperature.
Embodiment 4, as the optimization of above-described embodiment, as shown in Figure 1, this Production of PVC processes with reclaiming monomer Device also includes reclaiming monomer finished product condenser 30, reclaiming monomers flow back tank 32 and reclaim monomer finished product delivery pump 35, rectification gas The other end of phase discharge pipe 15 and the thermal medium feed end reclaiming monomer finished product condenser 30 are fixedly installed togather, and reclaim single It is installed with condenser exhaust gas pipeline 31 on body finished product condenser 30, reclaims the thermal medium discharge end of monomer finished product condenser 30 And reclaim and between monomers flow back tank 32, be installed with overhead condenser blanking pipeline 33, reclaim monomers flow back tank 32 and reclaim list It is installed with return tank discharging pipeline 34 between body finished product feed-stock pipeline 16, return tank discharging pipeline 34 is installed with Reclaim monomer finished product delivery pump 35, polymerization inhibitor charge pipe after polymerization inhibitor charge pump 20 19 and rectification gas phase discharge pipe 15 and Rectifying tower top polymerization inhibitor charge pipe 36 and finished product cold blanking inhibition it is installed with respectively between overhead condenser blanking pipeline 33 Agent charge pipe 37, on the recovery monomer finished product feed-stock pipeline 16 reclaimed between monomer rectifying tower 12 and return tank discharging pipeline 34 It is installed with return flow control valve 38 and return flow meter 39 respectively, is adding near the polymerization inhibitor reclaiming monomer rectifying tower 12 Control valve it is installed with respectively on material pipe 19, rectifying tower top polymerization inhibitor charge pipe 36 and finished product cold blanking polymerization inhibitor charge pipe 37 40.Reclaim the gas phase after the washing of monomer rectifying tower 12 top to be discharged by rectification gas phase discharge pipe 15, deliver to reclaim monomer and become Product condenser 30 carries out cooling liquefaction, reclaims monomer finished product condenser 30 and can be provided with 2, is that 1 operation 1 is standby；Liquid Recovery monomer after change is delivered to reclaim monomers flow back tank 32 by lower pipelines overhead condenser blanking pipeline 33 by deadweight, reclaims Monomers flow back tank 32 bottom is connected to reclaim monomer finished product delivery pump 35 by return tank discharging pipeline 34, reclaims monomer finished product defeated Sending pump 35 to be delivered to a monomer part in recovery monomers flow back tank 32 reclaim monomer rectifying tower 12, another part is as polymeric kettle Raw materials for production are standby, it is achieved provide raw material for follow-up PVC polymerization；Return flow control valve 38 and return flow meter 39 can be certainly Control regulation controls the amount of monomer being back to reclaim monomer rectifying tower 12.
Embodiment 5, as the optimization of above-described embodiment, as shown in Figure 1, the rectification after recovery monomer delivery pump 14 It is installed with recovery monomer rectifying feeder channel 41 on tower feed line 13, is reclaiming monomer rectifying feeder channel 41 and reclaiming monomer Recovery monomer rectifying tower feed pump 42 it is installed with on rectifying column feed line between rectifying column 12；Or/and, condense water defeated The other end sending pipe 11 is installed with condensate water collecting tank 43, and the tank base of condensate water collecting tank 43 is installed with condensation Water drain line 44, condensation water drainage pipeline 44 is provided with automatic valve 45, is installed with on condensate water collecting tank 43 Liquidometer 46；Or/and, the other end reclaiming monomer finished product feed-stock pipeline 16 is installed with recovery monomer pan tank 47.Condense Automatic valve 45 is installed on water drain line 44, automatic control drain operation can be carried out according to the liquid level condensing water.
Embodiment 6, uses the Production of PVC described in embodiment 1 to reclaim the polrvinyl chloride that monomer processing means is carried out Production is reclaimed monomer processing method and is carried out in the steps below: the first step, and gas phase reclaims monomer and reclaims monomer house steward 2 by gas phase Entering into caustic wash tower 1 bottom, gas phase reclaims monomer and flows from bottom to top in caustic wash tower 1, meanwhile, by concentration be 15% to The alkali liquor of 20% is entered tower tube line 21 by alkali liquor and delivers to the top in caustic wash tower 1, and alkali liquor flows and gas in caustic wash tower 1 from top to bottom Reclaiming monomer mutually and inversely contact and wash gas phase recovery monomer, wherein, gas phase recovery monomer enters the Stress control of caustic wash tower 1 and exists 0.15Mpa to 0.25Mpa, flow are 700m3/h to 15000m3/h, in caustic wash tower 1 temperature of each layer tower tray be 40 DEG C to 50 DEG C, the pressure reduction at the bottom of caustic wash tower 1 tower top and tower is less than 0.01Mpa；Second step, the gas phase after caustic wash tower 1 washs reclaims monomer Gone out tower tube line 5 and sequentially enter recovery first-stage condenser 4 by reclaiming monomer and reclaim secondary condenser 6 and carry out cooling liquid, wherein, Controlling the temperature by the liquid phase recovery monomer reclaiming first-stage condenser 4 and reclaim secondary condenser 6 out is 15 DEG C to 25 DEG C；The Three steps, liquid phase reclaims monomer and removes the water reclaimed in monomer in lower liquid pipeline 10 enters liquid seal trough 9, wherein, controls fluid-tight The liquid phase of groove 9 reclaims the water content of monomer less than 0.04%；4th step, reclaims monomer by rectifying column feed line 13 He by liquid phase Reclaim in monomer delivery pump 14 is delivered to reclaim monomer rectifying tower 12 and carry out rectification process, by polymerization inhibitor charge pipe 19 to entrance Reclaim the liquid phase of monomer rectifying tower 12 to reclaim monomer adds polymerization inhibitor, the gas phase after reclaiming monomer rectifying tower 12 and processing by Rectification gas phase discharge pipe 15 is discharged, and the recovery monomer after reclaiming monomer rectifying tower 12 and processing is by reclaiming monomer finished product feeding Pipeline 16 is discharged, and wherein, the flow controlling to enter the liquid phase recovery monomer reclaiming monomer rectifying tower 12 is 10m3/h to 35m3/h, The pressure controlling to reclaim monomer rectifying tower 12 tower top is 0.25Mpa to 0.30Mpa, temperature is 21 DEG C to 23 DEG C, single by reclaiming Body rectifying column 12 reboiler control to reclaim pressure at the bottom of monomer rectifying tower 12 tower be 0.30Mpa to 0.35Mpa, temperature be 30 DEG C extremely 40 DEG C, reclaim monomer rectifying tower 12 high-boiling components discharge capacity be 5kg/h to 35kg/h, the addition of polymerization inhibitor is that liquid phase per ton is returned Receive monomer and add 3g to 6g polymerization inhibitor.
Embodiment 7, uses the Production of PVC described in embodiment 3 to reclaim the polrvinyl chloride that monomer processing means is carried out Production is reclaimed monomer processing method and is carried out in the steps below: the first step, opens internally piloted valve 28, prepares in Alkali liquid compounding tank 29 The alkali liquor of 15% to 20%；Second step, gas phase reclaims monomer and enters into caustic wash tower 1 bottom, gas by gas phase recovery monomer house steward 2 Reclaim monomer mutually to flow from bottom to top in caustic wash tower 1, meanwhile, 29 alkali liquor made will be joined by alkali liquor by Alkali liquid compounding tank Entering tower tube line 21 and deliver to the top in caustic wash tower 1, alkali liquor flowing from top to bottom and gas phase in caustic wash tower 1 reclaim monomer and inversely connect Touching and wash gas phase and reclaim monomer, the alkali liquor of washed gas phase recovery monomer goes out tower tube line 3 through alkali liquor and is gone out tower tube line 3 by alkali liquor Discharging, and be delivered to caustic wash tower 1 top by caustic wash tower circulating pump 23 and be circulated utilization, wherein, gas phase reclaims monomer and enters alkali cleaning The Stress control of tower 1 is 700m3/h to 15000m3/h at 0.15Mpa to 0.25Mpa, flow, each layer tower tray in caustic wash tower 1 Temperature is 40 DEG C to 50 DEG C, and the pressure reduction at the bottom of caustic wash tower 1 tower top and tower is less than 0.01Mpa, by alkaline stream gauge 24 and alkaline stream It is 40m3/h to 50m3/h that adjustable valve 25 controls the circular flow of alkali liquor；3rd step, the gas phase after caustic wash tower 1 washs is returned Receive monomer and go out tower tube line 5 and sequentially enter recovery first-stage condenser 4 and reclaim secondary condenser 6 and carry out coolant by reclaiming monomer Changing, wherein, the temperature controlling to be reclaimed monomer by recovery first-stage condenser 4 and recovery secondary condenser 6 liquid phase out is 15 DEG C To 25 DEG C；4th step, liquid phase reclaims monomer and removes the water reclaimed in monomer, wherein, control in lower liquid pipeline 10 enters liquid seal trough 9 The liquid phase making liquid seal trough 9 reclaims the water content of monomer less than 0.04%；5th step, reclaims monomer by rectifying column feed by liquid phase Pipeline 13 and recovery monomer delivery pump 14 carry out rectification process, by polymerization inhibitor charge pipe in being delivered to reclaim monomer rectifying tower 12 19 reclaim addition polymerization inhibitor in monomer to entering the liquid phase reclaiming monomer rectifying tower 12, after reclaiming monomer rectifying tower 12 and processing Gas phase discharged by rectification gas phase discharge pipe 15, through recovery monomer rectifying tower 12 process after recovery monomer by reclaiming monomer Finished product feed-stock pipeline 16 is discharged, and wherein, the flow controlling to enter the liquid phase recovery monomer reclaiming monomer rectifying tower 12 is 10m3/h To 35m3/h, the pressure controlling to reclaim monomer rectifying tower 12 tower top is 0.25Mpa to 0.30Mpa, temperature be 21 DEG C to 23 DEG C, times The discharge capacity receiving monomer rectifying tower 12 high-boiling components is 5kg/h to 35kg/h, controls back by reclaiming monomer rectifying tower 12 reboiler Receipts pressure at the bottom of monomer rectifying tower 12 tower is 0.30Mpa to 0.35Mpa, temperature is 30 DEG C to 40 DEG C, and the addition of polymerization inhibitor is Liquid phase per ton reclaims monomer and adds 3g to 6g polymerization inhibitor.
Embodiment 8, uses the Production of PVC described in embodiment 4 to reclaim the polrvinyl chloride that monomer processing means is carried out Production is reclaimed monomer processing method and is carried out in the steps below: the first step, and gas phase reclaims monomer and reclaims monomer house steward 2 by gas phase Entering into caustic wash tower 1 bottom, gas phase reclaims monomer and flows from bottom to top in caustic wash tower 1, meanwhile, is entered by alkali liquor by alkali liquor The top in caustic wash tower 1 delivered to by tower tube line 21, and alkali liquor flowing from top to bottom in caustic wash tower 1 is reclaimed monomer with gas phase and inversely contacted And washing gas phase recovery monomer, the alkali liquor of washed gas phase recovery monomer goes out tower tube line 3 through alkali liquor and is gone out tower tube line 3 row by alkali liquor Going out, and be delivered to caustic wash tower 1 top by caustic wash tower circulating pump 23 and be circulated utilization, wherein, gas phase reclaims monomer and enters caustic wash tower 1 Stress control be 700m3/h to 15000m3/h at 0.15Mpa to 0.25Mpa, flow, the temperature of each layer tower tray in caustic wash tower 1 Being 40 DEG C to 50 DEG C, the pressure reduction at the bottom of caustic wash tower 1 tower top and tower is less than 0.01Mpa；Second step, the gas after caustic wash tower 1 washs Reclaim monomer mutually and go out tower tube line 5 and sequentially enter recovery first-stage condenser 4 and reclaim secondary condenser 6 and cool down by reclaiming monomer Liquefaction, wherein, the temperature controlling to be reclaimed monomer by recovery first-stage condenser 4 and recovery secondary condenser 6 liquid phase out is 15 DEG C to 25 DEG C；3rd step, liquid phase reclaim monomer remove through lower liquid pipeline 10 enters liquid seal trough 9 in recovery monomer in water, wherein, The liquid phase controlling liquid seal trough 9 reclaims the water content of monomer less than 0.04%；4th step, reclaims monomer by liquid phase and is supplied by rectifying column Material pipeline 13 and recovery monomer delivery pump 14 carry out rectification process in being delivered to reclaim monomer rectifying tower 12, are fed by polymerization inhibitor Pipe 19, rectifying tower top polymerization inhibitor charge pipe 36 and finished product cold blanking polymerization inhibitor charge pipe 37 respectively to rectifying column feed line 13, Rectification gas phase discharge pipe 15 and overhead condenser blanking pipeline 33 add polymerization inhibitor, processes through reclaiming monomer rectifying tower 12 After gas phase drained into by rectification gas phase discharge pipe 15 and reclaim monomer finished product condenser 30 and condense in gas phase remaining recovery monomer, Gas after reclaiming monomer finished product condenser 30 and processing is discharged by condenser exhaust gas pipeline 21, cold through reclaiming monomer finished product The recovery monomer that condenser 30 condenses out is delivered to reclaim monomers flow back tank 32 by overhead condenser blanking pipeline 33, then through backflow The recovery monomer part reclaimed in monomers flow back tank 32 is back to by tank discharging pipeline 34 and recovery monomer finished product delivery pump 35 Reclaim monomer rectifying tower 12, a part is become by recovery monomer together with the recovery monomer after reclaiming monomer rectifying tower 12 and processing Product feed-stock pipeline 16 is discharged, wherein, control enter reclaim monomer rectifying tower 12 liquid phase reclaim monomer flow be 10m3/h extremely 35m3/h, control reclaim monomer rectifying tower 12 tower top pressure be 0.25Mpa to 0.30Mpa, temperature be 21 DEG C to 23 DEG C, pass through Recovery monomer rectifying tower 12 reboiler control recovery pressure at the bottom of monomer rectifying tower 12 tower is 0.30Mpa to 0.35Mpa, temperature is 30 DEG C to 40 DEG C, reclaim monomer rectifying tower 12 high-boiling components discharge capacity be 5kg/h to 35kg/h, the addition of polymerization inhibitor is everywhere Liquid phase per ton reclaims monomer and adds 3g to 6g polymerization inhibitor, and the flow reclaiming monomer being back to reclaim monomer rectifying tower 12 is 20m3/h to 25m3/h, the inlet water temperature reclaiming monomer finished product condenser 30 controls at 15 DEG C to 30 DEG C, to arrange condenser The flow of gas pipeline 31 expellant gas is that to reclaim the content of monomer in 1m3/h to 2m3/h, gas be 10% to 35%.
Embodiment 9, as shown in Figure 1, uses the Production of PVC described in embodiment 4 to reclaim monomer processing means and enters The Production of PVC of row reclaims monomer processing method and can also carry out in the steps below: the first step, opens internally piloted valve 28, Alkali liquid compounding tank 22 is prepared the alkali liquor of 15% to 20%；Second step, gas phase is reclaimed monomer and is entered by gas phase recovery monomer house steward 2 Entering to caustic wash tower 1 bottom, gas phase reclaims monomer and flows from bottom to top in caustic wash tower 1, meanwhile, and will be by Alkali liquid compounding tank 22 The alkali liquor prepared is entered tower tube line 21 by alkali liquor and delivers to the top in caustic wash tower 1, alkali liquor in caustic wash tower 1 from top to bottom flowing with Gas phase reclaims monomer and inversely contacts and wash gas phase recovery monomer, and washed gas phase reclaims the alkali liquor of monomer and goes out tower tube through alkali liquor Line 3 is gone out tower tube line 3 by alkali liquor and discharges, and is delivered to caustic wash tower 1 top by caustic wash tower circulating pump 23 and is circulated utilization, wherein, It is 700m3/h to 15000m3/h at 0.15Mpa to 0.25Mpa, flow that gas phase reclaim monomer to be entered the Stress control of caustic wash tower 1, alkali Washing the temperature of each layer tower tray in tower 1 is 40 DEG C to 50 DEG C, and the pressure reduction at the bottom of caustic wash tower 1 tower top and tower is less than 0.01Mpa, passes through alkali liquor It is 40m3/h to 50m3/h that effusion meter 24 and alkaline stream adjustable valve 25 control the circular flow of alkali liquor；3rd step, through alkali cleaning Gas phase after tower 1 washing reclaim monomer by reclaim monomer go out tower tube line 5 sequentially enter recovery first-stage condenser 4 and reclaim two grades cold Condenser 6 carries out cooling liquid, wherein, controls the liquid phase recovery by reclaiming first-stage condenser 4 with reclaim secondary condenser 6 out single The temperature of body is 15 DEG C to 25 DEG C；4th step, liquid phase reclaims monomer and removes recovery monomer in lower liquid pipeline 10 enters liquid seal trough 9 Interior water, wherein, the liquid phase controlling liquid seal trough 9 reclaims the water content of monomer less than 0.04%；5th step, reclaims single by liquid phase Body carries out rectification process in being delivered to reclaim monomer rectifying tower 12 by rectifying column feed line 13 and recovery monomer delivery pump 14, logical Cross polymerization inhibitor charge pipe 29, rectifying tower top polymerization inhibitor charge pipe 36 and finished product cold blanking polymerization inhibitor charge pipe 37 respectively to rectifying column Feed line 13, rectification gas phase discharge pipe 15 and overhead condenser blanking pipeline 33 add polymerization inhibitor, through reclaiming monomer Gas phase after rectifying column 12 process is drained into recovery monomer finished product condenser 30 by rectification gas phase discharge pipe 15 and condenses in gas phase residual Remaining recovery monomer, the gas after reclaiming monomer finished product condenser 30 and processing is discharged by condenser exhaust gas pipeline 31, passes through The recovery monomer that recovery monomer finished product condenser 30 condenses out is delivered to reclaim monomer by overhead condenser blanking pipeline 33 and returns Stream tank 32, then the recovery list in monomers flow back tank 32 will be reclaimed through return tank discharging pipeline 34 and recovery monomer finished product delivery pump 35 A body part is back to reclaim monomer rectifying tower 12, a part and the recovery monomer one after reclaiming monomer rectifying tower 12 and processing Rising and discharged by recovery monomer finished product feed-stock pipeline 16, wherein, the liquid phase controlling to enter recovery monomer rectifying tower 12 reclaims monomer Flow is 10m3/h to 35m3/h, and the pressure controlling to reclaim monomer rectifying tower 12 tower top is 0.25Mpa to 0.30Mpa, temperature is 21 DEG C to 23 DEG C, be 0.30Mpa by reclaim monomer rectifying tower 12 reboiler controlling to reclaim the pressure at the bottom of monomer rectifying tower 12 tower To 0.35Mpa, temperature be 30 DEG C to 40 DEG C, the discharge capacity that reclaims monomer rectifying tower 12 high-boiling components be 5kg/h to 35kg/h, everywhere The addition of polymerization inhibitor is that liquid phase per ton reclaims monomer addition 3g to 6g polymerization inhibitor, is back to reclaim the recovery of monomer rectifying tower 12 The flow of monomer is 20m3/h to 25m3/h, and the inlet water temperature reclaiming monomer finished product condenser 30 controls at 15 DEG C to 30 DEG C, the flow of condenser exhaust gas pipeline 31 expellant gas it is that the content reclaiming monomer in 1m3/h to 2m3/h, gas is 10% to 35%.
Rectifying column feed line, rectification gas phase discharge pipe and overhead condenser blanking pipeline are mounted on polymerization inhibitor The pipeline of charging and control valve, can arbitrarily select addition point to carry out adding of polymerization inhibitor.
Gas phase is reclaimed monomer and sends in caustic wash tower by the present invention, first removes polrvinyl chloride with certain density liquid caustic soda and reclaims single The acidic initiator remained in body and living radical, such as acetaldehyde and carbon dioxide, recycling reclaims first-stage condenser 4 and returns Receive secondary condenser 6 and carry out reclaiming the liquefaction of monomer gas phase, after be sent to reclaim in monomer rectifying tower 12 and carry out rectification process and enter One step removes the ethyl chloride in recovery monomer, acetaldehyde, Trans-dichloroethylene, 1.1 dichloroethanes, cis dichloroethylene, three chloroethenes The high-boiling components impurity such as alkene, the recovery monomer initiator auxiliary agent processed remains and multiple high-boiling components content is greatly lowered, thus Improve recovery monomer mass, alleviate subsequent handling process equipment, pipeline recovery monomer autohemagglutination odds, due to polychlorostyrene The lifting of ethylene production raw materials quality, is effectively improved the whiteness quality index of polyvinyl chloride product, reduces polymerization simultaneously The usage amount of initiator raw material in production process, thus reduce PVC production cost.
By Fig. 2 and Fig. 3 it can be seen that polyvinyl-chloride use is reclaimed monomer and carries out production and feed intake, through to two production lines of A, B Initiator amount contrast after feeding intake, as shown in accompanying drawing 2 and accompanying drawing 3, did not used polychlorostyrene second of the present invention for using before June 1 The polyvinyl-chloride use that alkene produces with reclaiming monomer processing means and Production of PVC recovery monomer processing method reclaims monomer Initiator one-pot inventory when carrying out producing Corvic, uses Production of PVC of the present invention for using after June 1 Reclaim monomer with the polyvinyl-chloride use reclaiming monomer processing means and Production of PVC recovery monomer processing method to give birth to Initiator one-pot inventory when producing Corvic, by the curve in accompanying drawing 2 and accompanying drawing 3 it can be seen that use and use this Bright Production of PVC reclaims monomer processing means and the polyvinyl-chloride use of Production of PVC recovery monomer processing method Reclaiming monomer to carry out producing Corvic, initiator one-pot inventory is decreased obviously, and initiator total amount one-pot feeds intake averagely Have dropped 1.5kg, and initiator feed intake more steady.
By Fig. 4 and Fig. 5 it can be seen that caustic wash tower has preferable removal effect, domestic and international polychlorostyrene to carbon dioxide and acetaldehyde Ethylene polymerization pertinent literature shows, carbon dioxide and acetaldehyde can hinder polyreaction and affect the whiteness of Corvic And heat stability, therefore, use the technology of the present invention, it is possible to carbon dioxide and acetaldehyde to reclaiming in monomer effectively go Remove, for polyreaction be smoothed out provide safeguard, and be effectively improved the whiteness quality index of polyvinyl chloride product.
After apparatus of the present invention and method come into operation, through effect tracking verification 4 months, periodically import and export reclaiming monomer rectifying tower The recovery monomer mass data at place are analyzed, and detection data are as shown in table 1, by data in table 1 it can be seen that reclaim monomer Purity averagely increases 0.55%；Reclaim the high-boiling components impurity component such as ethyl chloride, acetaldehyde in monomer and all reduce by more than 10 times, instead The high-boiling components impurity such as formula-dichloroethylene, 1.1 dichloroethanes, cis dichloroethylene, trichloro ethylene are all completely removed, and effect is bright Aobvious.
Recovery monomer after processing according to embodiments of the present invention carries out production and feeds intake, and obtain polyreaction production is poly- Vinyl chloride resin whiteness index detects, and as shown in table 2, uses and does not uses Production of PVC of the present invention to reclaim at monomer Reason device and Production of PVC reclaim the polyvinyl-chloride use recovery monomer of monomer processing method and carry out producing polrvinyl chloride tree The whiteness of fat is 76% to 82%, uses and uses Production of PVC of the present invention to reclaim monomer processing means and polrvinyl chloride life Product reclaim monomer processing method polyvinyl-chloride use reclaim monomer carry out produce Corvic whiteness be 84% to 87%, use Production of PVC of the present invention to reclaim monomer processing means and Production of PVC it can thus be seen that use The whiteness quality index carrying out producing Corvic with the polyvinyl-chloride use recovery monomer reclaiming monomer processing method is average Rise 6 percentage points.
After using the technology of the present invention, reclaiming monomer mass stable, initiator amount keeps balance, and resin whiteness obtains It is effectively improved, illustrates to use the technology of the present invention can the most effectively remove high-boiling components impurity and the auxiliary agent of residual in recovery monomer, from And improve recovery monomer mass, while solving subsequent technique pipeline, equipment autohemagglutination problem, it is achieved that produce auxiliary agent former The saving of material and product quality promote, and calculate according to producing 800000 tons of PVC per year, can save auxiliary agent cost 5,350,000 yuan every year, thus Greatly reduce production cost；It addition, the lifting of polyvinyl chloride resin whiteness index, also it is the interior quality of improving product, wins the market Occupation rate creates huge intangible benefit.
Above technical characteristic constitutes highly preferred embodiment of the present invention, and it has stronger adaptability and most preferably implements effect Really, non-essential technical characteristic can be increased and decreased according to actual needs, meet the demand of different situations.
Table 1 reclaims the recovery monomer mass data of monomer rectifying tower import and export
The monomer that reclaims after table 2 present invention processes carries out producing the Corvic whiteness index obtained

Claims (10)

1. a Production of PVC is with reclaiming monomer processing means, it is characterised in that include caustic wash tower, reclaim first-stage condenser, Reclaim secondary condenser, liquid seal trough, recovery monomer rectifying tower, reclaim monomer delivery pump and polymerization inhibitor storage tank；Tower at caustic wash tower Body bottom is installed with gas phase and reclaims monomer house steward, is installed with alkali liquor on the tower body top of caustic wash tower and enters tower tube line, It is installed with alkali liquor at the bottom of the tower of caustic wash tower and goes out tower tube line, in tower top and the thermal medium charging reclaiming first-stage condenser of caustic wash tower It is installed with recovery monomer between Kou and goes out tower tube line, reclaim gas outlet and the recovery secondary condenser at first-stage condenser top It is installed with condenser between thermal medium charging aperture and connects pipeline, reclaim and fixedly mount on the gas outlet at secondary condenser top There is exhaust line, reclaim the thermal medium discharging opening bottom first-stage condenser and the thermal medium discharging opening reclaimed bottom secondary condenser And it is installed with lower liquid pipeline between the charging aperture of liquid seal trough respectively, bottom liquid seal trough, is installed with condensation water conveying pipe, It is installed with rectifying column feed line, in rectification between feed opening and the charging aperture reclaiming monomer rectifying tower of liquid seal trough bottom Being installed with recovery monomer delivery pump on tower feed line, the tower top reclaiming monomer rectifying tower is installed with rectification gas phase row Go out pipeline, reclaim and on the discharging opening of monomer rectifying tower, be installed with recovery monomer finished product feed-stock pipeline, reclaim monomer rectifying tower Reboiler on be installed with reboiler discharge line, polymerization inhibitor storage tank with near the rectifying column feed reclaiming monomer rectifying tower It is installed with polymerization inhibitor charge pipe between pipeline, polymerization inhibitor charge pipe is installed with polymerization inhibitor charge pump.
Production of PVC the most according to claim 1 reclaims monomer processing means, it is characterised in that polrvinyl chloride is raw Product reclaims monomer processing means and also includes Alkali liquid compounding tank and caustic wash tower circulating pump；Alkali liquor enters the other end and the alkali liquor of tower tube line The discharge end of preparing tank is fixedly installed togather, and enters to be installed with caustic wash tower circulating pump on tower tube line at alkali liquor, and caustic wash tower follows Alkali liquor between ring pump and caustic wash tower enters to be installed with respectively on tower tube line alkaline stream gauge and alkaline stream adjustable valve, alkali liquor Alkali liquor between preparing tank and caustic wash tower circulating pump enters the other end that tower tube line and alkali liquor goes out tower tube line and is fixedly installed togather；Alkali The upper end of liquid preparing tank is installed with Alkali liquid compounding tank exhaust line.
Production of PVC the most according to claim 2 reclaims monomer processing means, it is characterised in that at flux of alkaline liquor Alkali liquor after meter and alkaline stream adjustable valve enters to be installed with alkali liquor preheater on tower tube line, and alkali liquor enters tower tube line and alkali liquor The cold medium of preheater is imported and exported and is fixedly installed togather；Or/and, Alkali liquid compounding tank exhaust line is installed with automatic control Valve；Or/and, the other end of Alkali liquid compounding tank exhaust line is positioned at alkali liquor security personnel and accepts cylinder.
Production of PVC the most according to claim 1 reclaims monomer processing means, it is characterised in that polrvinyl chloride is raw Product reclaims monomer processing means and also includes reclaiming monomer finished product condenser, reclaiming monomers flow back tank and reclaim the conveying of monomer finished product Pump, the thermal medium feed end of the other end of rectification gas phase discharge pipe and recovery monomer finished product condenser is fixedly installed togather, Reclaim and on monomer finished product condenser, be installed with condenser exhaust gas pipeline, reclaim the thermal medium discharge end of monomer finished product condenser And reclaim and between monomers flow back tank, be installed with overhead condenser blanking pipeline, reclaim monomers flow back tank and reclaim monomer finished product It is installed with return tank discharging pipeline between feed-stock pipeline, return tank discharging pipeline is installed with recovery monomer finished product Delivery pump, the polymerization inhibitor charge pipe after polymerization inhibitor charge pump and rectification gas phase discharge pipe and overhead condenser blanking pipeline it Between be installed with rectifying tower top polymerization inhibitor charge pipe and finished product cold blanking polymerization inhibitor charge pipe respectively, reclaim monomer rectifying tower And it is installed with return flow control valve on the recovery monomer finished product feed-stock pipeline between return tank discharging pipeline respectively and returns Stream effusion meter, near reclaiming the polymerization inhibitor charge pipe of monomer rectifying tower, rectifying tower top polymerization inhibitor charge pipe and the cold blanking of finished product Control valve it is installed with respectively on polymerization inhibitor charge pipe.
5. according to the Production of PVC described in Claims 2 or 3 with reclaiming monomer processing means, it is characterised in that polrvinyl chloride Production is reclaimed monomer processing means and is also included reclaiming monomer finished product condenser, recovery monomers flow back tank and reclaim monomer finished product defeated Pump, the other end of rectification gas phase discharge pipe and the thermal medium feed end reclaiming monomer finished product condenser is sent to be fixedly mounted on one Rising, reclaim and be installed with condenser exhaust gas pipeline on monomer finished product condenser, the thermal medium reclaiming monomer finished product condenser goes out It is installed with overhead condenser blanking pipeline between material end and recovery monomers flow back tank, reclaims monomers flow back tank and reclaim monomer It is installed with return tank discharging pipeline between finished product feed-stock pipeline, return tank discharging pipeline is installed with recovery monomer Finished product delivery pump, the polymerization inhibitor charge pipe after polymerization inhibitor charge pump and rectification gas phase discharge pipe and overhead condenser tremie pipe It is installed with rectifying tower top polymerization inhibitor charge pipe and finished product cold blanking polymerization inhibitor charge pipe between line respectively, reclaims monomer essence Evaporate and be installed with return flow control valve respectively on the recovery monomer finished product feed-stock pipeline between tower and return tank discharging pipeline With return flow meter, near reclaim the polymerization inhibitor charge pipe of monomer rectifying tower, rectifying tower top polymerization inhibitor charge pipe and finished product cold Control valve it is installed with respectively on blanking polymerization inhibitor charge pipe.
6., according to the Production of PVC described in claim 1 or 2 or 3 or 4 or 5 with reclaiming monomer processing means, its feature exists Recovery monomer rectifying feeder channel it is installed with on the rectifying column feed line after reclaiming monomer delivery pump, single reclaiming It is installed with recovery monomer rectifying tower on rectifying column feed line between body rectification feeder channel and recovery monomer rectifying tower to enter Material pump；Or/and, the other end condensing water conveying pipe is installed with condensate water collecting tank, the tank base of condensate water collecting tank It is installed with condensation water drainage pipeline, condensation water drainage pipeline is provided with automatic valve, fixing on condensate water collecting tank Liquidometer is installed；Or/and, the other end reclaiming monomer finished product feed-stock pipeline is installed with recovery monomer pan tank.
7. one kind uses Production of PVC according to claim 1 recovery monomer processing means to carry out polrvinyl chloride life Producing with reclaiming the method that monomer processes, it is characterised in that carry out in the steps below: the first step, gas phase is reclaimed monomer and is returned by gas phase Receiving monomer house steward and enter into caustic wash tower bottom, gas phase reclaims monomer and flows from bottom to top in caustic wash tower, meanwhile, by concentration Be 15% to 20% alkali liquor entered, by alkali liquor, the top that tower tube line is delivered in caustic wash tower, alkali liquor in caustic wash tower from top to bottom flowing with Gas phase reclaims monomer and inversely contacts and wash gas phase recovery monomer, and wherein, gas phase recovery monomer enters the Stress control of caustic wash tower and exists 0.15Mpa to 0.25Mpa, flow are 700m3/ h to 15000m3/ h, in caustic wash tower, the temperature of each layer tower tray is 40 DEG C to 50 DEG C, Pressure reduction at the bottom of caustic wash tower tower top and tower is less than 0.01Mpa；Second step, the gas phase after caustic wash tower washs reclaims monomer by reclaiming Monomer goes out tower tube line and sequentially enters recovery first-stage condenser and reclaim secondary condenser and carry out cooling liquid, wherein, controls by returning The temperature receiving first-stage condenser and recovery secondary condenser liquid phase recovery monomer out is 15 DEG C to 25 DEG C；3rd step, liquid phase Reclaiming monomer and remove the water reclaimed in monomer in lower liquid pipeline enters liquid seal trough, wherein, the liquid phase controlling liquid seal trough reclaims The water content of monomer is less than 0.04%；4th step, reclaims monomer defeated by rectifying column feed line and recovery monomer delivery pump by liquid phase Carry out rectification process in delivering to reclaim monomer rectifying tower, returned to entering the liquid phase reclaiming monomer rectifying tower by polymerization inhibitor charge pipe Receiving and add polymerization inhibitor in monomer, the gas phase after reclaiming monomer rectifying tower and processing is discharged by rectification gas phase discharge pipe, passes through Reclaim the recovery monomer after monomer rectifying tower processes to be discharged by reclaiming monomer finished product feed-stock pipeline, wherein, control entrance and reclaim single It is 10m that the liquid phase of body rectifying column reclaims the flow of monomer3/ h to 35m3/ h, the pressure controlling to reclaim monomer rectifying column overhead is 0.25Mpa to 0.30Mpa, temperature are 21 DEG C to 23 DEG C, control to reclaim monomer rectifying tower by reclaiming monomer rectifying tower reboiler The discharge capacity that pressure at the bottom of tower is 0.30Mpa to 0.35Mpa, temperature is 30 DEG C to 40 DEG C, reclaim monomer rectifying tower high-boiling components is 5kg/h to 35kg/h, the addition of polymerization inhibitor is that liquid phase per ton reclaims monomer addition 3g to 6g polymerization inhibitor.
Production of PVC the most according to claim 3 reclaims monomer processing means and carries out Production of PVC recovery The method that monomer processes, it is characterised in that carry out in the steps below: the first step, open internally piloted valve, prepares in Alkali liquid compounding tank The alkali liquor of 15% to 20%；Second step, gas phase reclaims monomer and enters into caustic wash tower bottom by gas phase recovery monomer house steward, and gas phase is returned Receive monomer to flow from bottom to top in caustic wash tower, meanwhile, Alkali liquid compounding tank the alkali liquor prepared is entered tower tube by alkali liquor The top in caustic wash tower delivered to by line, and alkali liquor flowing from top to bottom in caustic wash tower is reclaimed monomer with gas phase and inversely contacted and wash gas Reclaiming monomer mutually, the alkali liquor of washed gas phase recovery monomer goes out tower tube line through alkali liquor and is gone out the discharge of tower tube line by alkali liquor, and by alkali Washing tower circulating pump to be delivered to caustic wash tower top and be circulated utilization, wherein, gas phase reclaims monomer and enters the Stress control of caustic wash tower and exist 0.15Mpa to 0.25Mpa, flow are 700m3/ h to 15000m3/ h, in caustic wash tower, the temperature of each layer tower tray is 40 DEG C to 50 DEG C, Pressure reduction at the bottom of caustic wash tower tower top and tower is less than 0.01Mpa, by following of alkaline stream gauge and flux of alkaline liquor governor valve control alkali liquor Circulation is 40 m3/ h to 50m3/h；3rd step, the gas phase after caustic wash tower washs reclaims monomer and is gone out tower tube by reclaiming monomer Line sequentially enters recovery first-stage condenser and recovery secondary condenser carries out cooling liquid, wherein, controls by reclaiming one-level condensation Device and the temperature reclaiming secondary condenser liquid phase recovery monomer out are 15 DEG C to 25 DEG C；4th step, liquid phase reclaims monomer warp The water reclaimed in monomer removed by lower liquid pipeline in entering liquid seal trough, wherein, the liquid phase controlling liquid seal trough reclaims the aqueous of monomer Amount is less than 0.04%；5th step, reclaims liquid phase monomer and is delivered to reclaim list by rectifying column feed line and recovery monomer delivery pump Carry out rectification process in body rectifying column, added in the liquid phase recovery monomer enter recovery monomer rectifying tower by polymerization inhibitor charge pipe Entering polymerization inhibitor, the gas phase after reclaiming monomer rectifying tower and processing is discharged by rectification gas phase discharge pipe, through reclaiming monomer essence Evaporate the recovery monomer after tower processes to be discharged by reclaiming monomer finished product feed-stock pipeline, wherein, control to enter and reclaim monomer rectifying tower It is 10m that liquid phase reclaims the flow of monomer3/ h to 35m3/ h, control reclaim monomer rectifying column overhead pressure be 0.25Mpa extremely The discharge capacity that 0.30Mpa, temperature be 21 DEG C to 23 DEG C, reclaims monomer rectifying tower high-boiling components is 5kg/h to 35kg/h, by reclaiming Monomer rectifying tower reboiler control to reclaim pressure at the bottom of monomer rectifying tower tower be 0.30Mpa to 0.35Mpa, temperature be 30 DEG C to 40 DEG C, the addition of polymerization inhibitor is that liquid phase per ton reclaims monomer addition 3g to 6g polymerization inhibitor.
Production of PVC the most according to claim 4 reclaims monomer processing means and carries out Production of PVC recovery The method that monomer processes, it is characterised in that carry out in the steps below: the first step, it is total by gas phase recovery monomer that gas phase reclaims monomer Pipe enters into caustic wash tower bottom, and gas phase reclaims monomer and flows from bottom to top in caustic wash tower, meanwhile, is entered by alkali liquor by alkali liquor The top in caustic wash tower delivered to by tower tube line, and alkali liquor flowing from top to bottom in caustic wash tower is reclaimed monomer with gas phase and inversely contacted and wash Scrubbing reclaims monomer mutually, and the alkali liquor of washed gas phase recovery monomer goes out tower tube line through alkali liquor and gone out the discharge of tower tube line by alkali liquor, and Being delivered to caustic wash tower top by caustic wash tower circulating pump and be circulated utilization, wherein, gas phase reclaims monomer and enters the pressure control of caustic wash tower System is 700m at 0.15Mpa to 0.25Mpa, flow3/ h to 15000m3/ h, in caustic wash tower the temperature of each layer tower tray be 40 DEG C to 50 DEG C, the pressure reduction at the bottom of caustic wash tower tower top and tower is less than 0.01Mpa；Second step, through caustic wash tower wash after gas phase reclaim monomer by Reclaim monomer to go out tower tube line and sequentially enter recovery first-stage condenser and reclaim secondary condenser and carry out cooling liquid, wherein, control It it is 15 DEG C to 25 DEG C by the temperature of the liquid phase recovery monomer reclaiming first-stage condenser and reclaim secondary condenser out；3rd step, Liquid phase reclaims monomer and removes the water reclaimed in monomer in lower liquid pipeline enters liquid seal trough, wherein, controls the liquid phase of liquid seal trough Reclaim the water content of monomer less than 0.04%；4th step, reclaims liquid phase monomer and by rectifying column feed line and reclaims monomer conveying Transport pump carries out rectification process to reclaiming in monomer rectifying tower, by polymerization inhibitor charge pipe, rectifying tower top polymerization inhibitor charge pipe and Finished product cold blanking polymerization inhibitor charge pipe is respectively to rectifying column feed line, rectification gas phase discharge pipe and overhead condenser tremie pipe Adding polymerization inhibitor in line, the gas phase after reclaiming monomer rectifying tower and processing is drained into recovery monomer by rectification gas phase discharge pipe and becomes Recovery monomer remaining in product condenser condensation gas phase, the gas after reclaiming monomer finished product condenser and processing is arranged by condenser Gas pipeline is discharged, and the recovery monomer condensed out through reclaiming monomer finished product condenser is delivered to by overhead condenser blanking pipeline Reclaim monomers flow back tank, then the recovery in monomers flow back tank will be reclaimed through return tank discharging pipeline and recovery monomer finished product delivery pump A monomer part is back to reclaim monomer rectifying tower, a part together with the recovery monomer after reclaiming monomer rectifying tower and processing Being discharged by reclaiming monomer finished product feed-stock pipeline, wherein, the liquid phase of control entrance recovery monomer rectifying tower reclaims the flow of monomer and is 10m3/ h to 35m3/ h, control reclaim monomer rectifying column overhead pressure be 0.25Mpa to 0.30Mpa, temperature be 21 DEG C to 23 DEG C, it is 0.30Mpa to 0.35Mpa, temperature by reclaim monomer rectifying tower reboiler controlling to reclaim the pressure at the bottom of monomer rectifying tower tower The discharge capacity that degree is 30 DEG C to 40 DEG C, reclaim monomer rectifying tower high-boiling components is 5kg/h to 35kg/h, the addition of polymerization inhibitor everywhere Reclaiming monomer for liquid phase per ton and add 3g to 6g polymerization inhibitor, the flow reclaiming monomer being back to reclaim monomer rectifying tower is 20m3/ h to 25m3/ h, the inlet water temperature reclaiming monomer finished product condenser controls at 15 DEG C to 30 DEG C, by condenser exhaust gas pipe The flow of line expellant gas is 1m3/ h to 2m3The content reclaiming monomer in/h, gas is 10% to 35%.
Production of PVC the most according to claim 5 recovery monomer processing means carries out Production of PVC and uses back Receive the method that monomer processes, it is characterised in that carry out in the steps below: the first step, open internally piloted valve, join in Alkali liquid compounding tank The alkali liquor of system 15% to 20%；Second step, gas phase reclaims monomer and enters into caustic wash tower bottom, gas phase by gas phase recovery monomer house steward Reclaim monomer to flow from bottom to top in caustic wash tower, meanwhile, Alkali liquid compounding tank the alkali liquor prepared is entered tower by alkali liquor The top in caustic wash tower delivered to by pipeline, and alkali liquor flowing from top to bottom in caustic wash tower is reclaimed monomer with gas phase and inversely contacted and wash Gas phase reclaim monomer, washed gas phase reclaim monomer alkali liquor through alkali liquor go out tower tube line by alkali liquor go out tower tube line discharge, and by Caustic wash tower circulating pump is delivered to caustic wash tower top and is circulated utilization, and wherein, gas phase reclaims monomer and enters the Stress control of caustic wash tower It is 700m at 0.15Mpa to 0.25Mpa, flow3/ h to 15000m3/ h, in caustic wash tower the temperature of each layer tower tray be 40 DEG C to 50 DEG C, the pressure reduction at the bottom of caustic wash tower tower top and tower is less than 0.01Mpa, by alkaline stream gauge and flux of alkaline liquor governor valve control alkali liquor Circular flow is 40 m3/ h to 50m3/h；3rd step, the gas phase after caustic wash tower washs reclaims monomer and is gone out tower by reclaiming monomer Pipeline sequentially enters recovery first-stage condenser and recovery secondary condenser carries out cooling liquid, wherein, controls by reclaiming one-level cold Condenser and the temperature reclaiming secondary condenser liquid phase recovery monomer out are 15 DEG C to 25 DEG C；4th step, liquid phase reclaims monomer Removing the water reclaimed in monomer in lower liquid pipeline enters liquid seal trough, wherein, the liquid phase controlling liquid seal trough reclaims containing of monomer The water yield is less than 0.04%；5th step, reclaims liquid phase monomer and is delivered to reclaim by rectifying column feed line and recovery monomer delivery pump Carry out rectification process in monomer rectifying tower, hindered by polymerization inhibitor charge pipe, rectifying tower top polymerization inhibitor charge pipe and the cold blanking of finished product Poly-agent charge pipe adds inhibition respectively in rectifying column feed line, rectification gas phase discharge pipe and overhead condenser blanking pipeline Agent, the gas phase after reclaiming monomer rectifying tower and processing is drained into recovery monomer finished product condenser condensation by rectification gas phase discharge pipe Recovery monomer remaining in gas phase, the gas after reclaiming monomer finished product condenser and processing discharged by condenser exhaust gas pipeline, The recovery monomer condensed out through reclaiming monomer finished product condenser is delivered to reclaim monomer by overhead condenser blanking pipeline and returns Stream tank, then the recovery monomer part in monomers flow back tank will be reclaimed through return tank discharging pipeline and recovery monomer finished product delivery pump It is back to reclaim monomer rectifying tower, a part together with the recovery monomer after reclaiming monomer rectifying tower and processing by reclaiming monomer Finished product feed-stock pipeline is discharged, and wherein, the flow controlling to enter the liquid phase recovery monomer reclaiming monomer rectifying tower is 10m3/ h is extremely 35m3/ h, the pressure controlling to reclaim monomer rectifying column overhead is 0.25Mpa to 0.30Mpa, temperature is 21 DEG C to 23 DEG C, by returning Receive monomer rectifying tower reboiler control to reclaim pressure at the bottom of monomer rectifying tower tower be 0.30Mpa to 0.35Mpa, temperature be 30 DEG C extremely 40 DEG C, reclaim monomer rectifying tower high-boiling components discharge capacity be 5kg/h to 35kg/h, the addition of polymerization inhibitor is liquid phase per ton everywhere Reclaiming monomer and add 3g to 6g polymerization inhibitor, the flow reclaiming monomer being back to reclaim monomer rectifying tower is 20m3/ h to 25m3/ h, The inlet water temperature reclaiming monomer finished product condenser controls at 15 DEG C to 30 DEG C, by condenser exhaust gas pipeline expellant gas Flow is 1m3/ h to 2m3The content reclaiming monomer in/h, gas is 10% to 35%.
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CN108948240A (en) * 2018-06-11 2018-12-07 新疆天业（集团）有限公司 A kind of PVC polymerization anti-polymerization method
CN112225943A (en) * 2020-09-21 2021-01-15 内蒙古中谷矿业有限责任公司 Monomer alkali washing refining device is retrieved in polymerization
CN112920453A (en) * 2021-02-24 2021-06-08 唐山三友氯碱有限责任公司 Special resin recovery monomer upgrading system for vinyl chloride and operation method thereof

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CN105214581A (en) * 2014-05-27 2016-01-06 新疆天业（集团）有限公司 The method of tail gas full-closed circulating recovery is polymerized in Production of PVC
CN105669360A (en) * 2015-12-30 2016-06-15 天津普莱化工技术有限公司 Vinyl chloride monomer recovery technology

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CN104072328A (en) * 2013-12-27 2014-10-01 江苏正丹化学工业股份有限公司 Rectification device and rectification method for producing vinyltoluene
CN105214581A (en) * 2014-05-27 2016-01-06 新疆天业（集团）有限公司 The method of tail gas full-closed circulating recovery is polymerized in Production of PVC
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Publication number Priority date Publication date Assignee Title
CN108948240A (en) * 2018-06-11 2018-12-07 新疆天业（集团）有限公司 A kind of PVC polymerization anti-polymerization method
CN112225943A (en) * 2020-09-21 2021-01-15 内蒙古中谷矿业有限责任公司 Monomer alkali washing refining device is retrieved in polymerization
CN112225943B (en) * 2020-09-21 2021-10-15 内蒙古中谷矿业有限责任公司 Monomer alkali washing refining device is retrieved in polymerization
CN112920453A (en) * 2021-02-24 2021-06-08 唐山三友氯碱有限责任公司 Special resin recovery monomer upgrading system for vinyl chloride and operation method thereof

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