CN106084283B - Production of PVC recycling monomer processing unit and Production of PVC recycling monomer processing method - Google Patents

Production of PVC recycling monomer processing unit and Production of PVC recycling monomer processing method Download PDF

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Publication number
CN106084283B
CN106084283B CN201610495582.4A CN201610495582A CN106084283B CN 106084283 B CN106084283 B CN 106084283B CN 201610495582 A CN201610495582 A CN 201610495582A CN 106084283 B CN106084283 B CN 106084283B
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monomer
recycling
tower
rectifying
recycling monomer
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CN106084283A (en
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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

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  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Polymerisation Methods In General (AREA)
  • Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)

Abstract

It is that a kind of Production of PVC recycling monomer processing unit and Production of PVC recycle monomer processing method the present invention relates to Production of PVC recycling monomer technical field.Including caustic wash tower, recycling first-stage condenser, recycling secondary condenser, liquid seal trough, recycling monomer rectifying tower, recycling monomer delivery pump and polymerization inhibitor storage tank；It is fixedly installed with gas phase recycling monomer general pipeline in the tower body lower part of caustic wash tower, lye is fixedly installed with into tower tube line on the tower body top of caustic wash tower, is fixedly installed with lye in the tower bottom of caustic wash tower and goes out tower tube line.The present invention can effectively effectively remove high-boiling components impurity and remaining auxiliary agent in recycling monomer, to improve recycling monomer mass, so that recycling monomer mass is stable, initiator amount keeps balance, resin whiteness effectively improves, while solving the problems, such as subsequent technique pipeline, equipment autohemagglutination, the saving and product quality for realizing production auxiliary agent raw material are promoted.

Description

Production of PVC recycling monomer processing unit and Production of PVC are single with recycling Body processing method
Technical field
The present invention relates to Production of PVC recycling monomer technical fields, are a kind of Production of PVC recycling monomers Processing unit and Production of PVC recycling monomer processing method.
Background technique
Domestic PVC industry dog-eat-dog at present is promoted by technological transformation and optimization and is produced to adapt to market environment Quality, packaging process units stable operation are significant to production cost is reduced.The quality of recycling monomer is to influence PVC product In quality whiteness index, process unit line equipment occur initiator amount in autohemagglutination and polymerization production process it is big it is crucial because Element, and monomer mass is recycled can effectively control residual initiator, initiator free radical, high-boiling components and other residuals therein Auxiliary agent content is emphasis influence factor.PVC industry in China does not always carry out the above influence factor of recycling monomer special for many years Fixed processing, resin whiteness norm controlling aspect, which remains in, produces the recycling monomer decrement jump after polymerization to upstream vinyl chloride Process increases in polymerization production process in the dosage of heat stabilizer, and then to recovery process assembling device pipeline and equipment autohemagglutination It is controlled by polymerization inhibitor dosage in annual periodic inspection or increase pipeline system.Promotion can also be realized on these method surfaces PVC product whiteness index reduces the purpose that system autohemagglutination influences, but PVC resulting from production auxiliary agent cost increases, in PVC PVC manufacturing enterprise is still annoying in the problems such as quality decline.
Summary of the invention
It is single with recycling that the present invention provides a kind of Production of PVC recycling monomer processing units and Production of PVC Body processing method, overcomes the defects of the prior art, and can effectively solve China's PVC industry always not to recycling monomer The influence factors such as residual initiator, initiator free radical, high-boiling components and other residual auxiliary agent contents carry out the problem of particular procedure.
Technical solution of the present invention first is that being realized by following measures: a kind of Production of PVC recycles monomer Processing unit, including caustic wash tower, recycling first-stage condenser, recycling secondary condenser, liquid seal trough, recycling monomer rectifying tower, recycling Monomer delivery pump and polymerization inhibitor storage tank；It is fixedly installed with gas phase recycling monomer general pipeline in the tower body lower part of caustic wash tower, in caustic wash tower Tower body top be fixedly installed with lye into tower tube line, be fixedly installed with lye in the tower bottom of caustic wash tower and go out tower tube line, in alkali cleaning It is fixedly installed with recycling monomer between the tower top of tower and the thermal medium feed inlet for recycling first-stage condenser and goes out tower tube line, recycles level-one It is fixedly installed with condenser connecting pipeline between the gas outlet of condenser overhead and the thermal medium feed inlet for recycling secondary condenser, Exhaust line, the thermal medium discharging of recycling first-stage condenser bottom are fixedly installed on gas outlet at the top of recycling secondary condenser It is fixedly installed with lower liquid pipe respectively between the feed inlet of the thermal medium discharge port and liquid seal trough of mouth and recycling secondary condenser bottom Line, fluid-tight trench bottom are fixedly installed with condensed water delivery pipe, the charging of the feed opening and recycling monomer rectifying tower of liquid seal trough lower part It is fixedly installed with rectifying column feed line between mouthful, recycling monomer delivery pump is fixedly installed on rectifying column feed line, is returned The tower top for receiving monomer rectifying tower is fixedly installed with rectifying gas phase discharge pipe, recycles and is fixedly mounted on the discharge port of monomer rectifying tower There is recycling monomer finished product feed-stock pipeline, recycles and be fixedly installed with reboiler discharge line on the reboiler of monomer rectifying tower, inhibit It is fixedly installed with polymerization inhibitor charge pipe between agent storage tank and the rectifying column feed line of close recycling monomer rectifying tower, polymerization inhibitor adds Polymerization inhibitor charge pump is fixedly installed in expects pipe.
Here is further optimization or/and improvement of one of the above technical solutions of the invention:
Above-mentioned Production of PVC recycling monomer processing unit further includes Alkali liquid compounding tank and caustic wash tower circulating pump；Lye Discharge end into the other end and Alkali liquid compounding tank of tower tube line is fixedly installed togather, in lye into being fixedly installed on tower tube line Caustic wash tower circulating pump, lye between caustic wash tower circulating pump and caustic wash tower into being fixedly installed with alkaline stream meter on tower tube line respectively With flux of alkaline liquor regulating valve, the lye between Alkali liquid compounding tank and caustic wash tower circulating pump goes out the another of tower tube line into tower tube line and lye One end is fixedly installed togather；The upper end of Alkali liquid compounding tank is fixedly installed with Alkali liquid compounding tank exhaust line.
The above-mentioned lye after alkaline stream meter and flux of alkaline liquor regulating valve is pre- into lye is fixedly installed on tower tube line Hot device, lye are fixedly installed togather into tower tube line and the cold medium inlet and outlet of lye preheater；Or/and Alkali liquid compounding tank row Internally piloted valve is fixedly installed on gas pipeline；Or/and the other end of Alkali liquid compounding tank exhaust line is located at lye security personnel and accepts cylinder It is interior.
Above-mentioned Production of PVC recycling monomer processing unit further includes recycling monomer finished product condenser, recycling monomer time Flow tank and recycling monomer finished product delivery pump, the other end of rectifying gas phase discharge pipe and the thermal medium of recycling monomer finished product condenser Feed end is fixedly installed togather, and recycles and is fixedly installed with condenser exhaust gas pipeline on monomer finished product condenser, recycling monomer at It is fixedly installed with overhead condenser blanking pipeline between the thermal medium discharge end and recycling monomers flow back tank of product condenser, recycling is single Return tank discharging pipeline is fixedly installed between body return tank and recycling monomer finished product feed-stock pipeline, on return tank discharging pipeline It is fixedly installed with recycling monomer finished product delivery pump, polymerization inhibitor charge pipe and rectifying gas phase discharge pipe after polymerization inhibitor charge pump It is fixedly installed with rectifying tower top polymerization inhibitor charge pipe and the cold blanking polymerization inhibitor of finished product respectively between overhead condenser blanking pipeline Charge pipe, it is fixed respectively on recycling the recycling monomer finished product feed-stock pipeline between monomer rectifying tower and return tank discharging pipeline to pacify Equipped with return flow control valve and return flow meter, in the polymerization inhibitor charge pipe close to recycling monomer rectifying tower, rectifying tower top resistance It is fixedly installed with control valve respectively on poly- agent charge pipe and the cold blanking polymerization inhibitor charge pipe of finished product.
It is above-mentioned that recycling monomer rectifying feed is fixedly installed on recycling the rectifying column feed line after monomer delivery pump Slot is fixedly installed with recycling list recycling monomer rectifying feeder channel and recycling on the rectifying column feed line between monomer rectifying tower Body rectifying column feed pump；Or/and the other end of condensed water delivery pipe is fixedly installed with condensate water collecting tank, condensate water collecting tank Tank base be fixedly installed with condensation water drainage pipeline, automatic valve is installed on condensation water drainage pipeline, condensed water receive Liquidometer is fixedly installed on collection tank；Or/and recycling monomer finished product feed-stock pipeline the other end be fixedly installed with recycling monomer at Product slot.
Technical solution of the present invention second is that being realized by following measures: it is a kind of to be used using above-mentioned Production of PVC The Production of PVC recycling monomer processing method that monomer processing unit carries out is recycled, is carried out in the steps below: the first step, gas Mutually recycling monomer recycles monomer general pipeline by gas phase and enters caustic wash tower lower part, gas phase recycling monomer in caustic wash tower from bottom to top Flowing send the lye that concentration is 15% to 20% to the top into caustic wash tower into tower tube line by lye, lye exists at the same time It is flowed from above to below in caustic wash tower and gas phase recycling monomer is inversely contacted and washed with gas phase recycling monomer, wherein gas phase recycling is single It is 700m3/h to 15000m3/h, each layer in caustic wash tower that the pressure of body into caustic wash tower, which is controlled in 0.15Mpa to 0.25Mpa, flow, The temperature of tower tray is 40 DEG C to 50 DEG C, and the pressure difference of alkali cleaning column overhead and tower bottom is less than 0.01Mpa；Second step is washed by caustic wash tower After washing gas phase recycling monomer by recycling monomer go out tower tube line sequentially enter recycling first-stage condenser and recycling secondary condenser into Row cooling liquid, wherein the temperature for the liquid phase recycling monomer that control is come out by recycling first-stage condenser and recycling secondary condenser It is 15 DEG C to 25 DEG C；Third step, liquid phase recycle monomer and enter the single intracorporal water of removal recycling in liquid seal trough through lower liquid pipe line, In, the water content of liquid phase recycling monomer of liquid seal trough is controlled out less than 0.04%；4th step, by liquid phase recycling monomer by rectifying column Feed line and recycling monomer delivery pump be delivered to recycling monomer rectifying tower in carry out rectification process, by polymerization inhibitor charge pipe to Into polymerization inhibitor is added in the liquid phase recycling monomer of recycling monomer rectifying tower, by recycling monomer rectifying tower treated gas phase by Rectifying gas phase discharge pipe discharge, by recycling monomer rectifying tower treated recycling monomer by recycling monomer finished product feed-stock pipeline Discharge, wherein the flow that control enters the liquid phase recycling monomer of recycling monomer rectifying tower is 10m3/h to 35m3/h, control recycling The pressure of monomer rectifying column overhead is 0.25Mpa to 0.30Mpa, temperature is 21 DEG C to 23 DEG C, again by recycling monomer rectifying tower The pressure of boiling device control recycling monomer rectifying tower tower bottom is 0.30Mpa to 0.35Mpa, temperature is 30 DEG C to 40 DEG C, recycling monomer The discharge amount of rectifying column high-boiling components is 5kg/h to 35kg/h, and the additional amount of polymerization inhibitor is that liquid phase per ton recycles monomer addition 3g extremely 6g polymerization inhibitor.
Technical solution of the present invention third is that being realized by following measures: it is a kind of to be used using above-mentioned Production of PVC The Production of PVC recycling monomer processing method that monomer processing unit carries out is recycled, carry out in the steps below: the first step is beaten Internally piloted valve is opened, 15% to 20% lye is prepared in Alkali liquid compounding tank；Second step, gas phase recycle monomer and recycle list by gas phase Body general pipeline enters caustic wash tower lower part, and gas phase recycling monomer flows from bottom to top in caustic wash tower, at the same time, will be matched by lye The prepared lye of tank processed send the top into caustic wash tower into tower tube line by lye, lye flowed from above to below in caustic wash tower with Gas phase recycling monomer inversely contacts and washs gas phase recycling monomer, and the lye of washed gas phase recycling monomer goes out tower tube by lye Line goes out the discharge of tower tube line by lye, and is delivered to caustic wash tower top by caustic wash tower circulating pump and is recycled, wherein gas phase is returned It is 700m3/h to 15000m3/h that the pressure control of monomer into caustic wash tower, which is received, in 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 difference of alkali cleaning column overhead and tower bottom is less than 0.01Mpa, by alkaline stream meter and The circular flow that flux of alkaline liquor regulating valve controls lye is 40m3/h to 50m3/h；Third step, the gas after caustic wash tower washs Phase recycling monomer goes out tower tube line by recycling monomer and sequentially enters recycling first-stage condenser and recycling secondary condenser progress coolant liquid Change, wherein control by recycling first-stage condenser and recycling secondary condenser come out liquid phase recycling monomer temperature be 15 DEG C extremely 25℃；4th step, liquid phase recycle monomer and enter the single intracorporal water of removal recycling in liquid seal trough through lower liquid pipe line, wherein control out The water content of the liquid phase recycling monomer of liquid seal trough is less than 0.04%；5th step, by liquid phase recycling monomer by rectifying column feed line It is delivered in recycling monomer rectifying tower with recycling monomer delivery pump and carries out rectification process, recycled by polymerization inhibitor charge pipe to entrance Polymerization inhibitor is added in the liquid phase recycling monomer of monomer rectifying tower, by recycling monomer rectifying tower treated gas phase by rectifying gas phase Discharge pipe discharge, by recycling monomer rectifying tower treated recycling monomer by recycling monomer finished product feed-stock pipeline be discharged, In, the flow that control enters the liquid phase recycling monomer of recycling monomer rectifying tower is 10m3/h to 35m3/h, control recycling monomer essence The pressure for evaporating column overhead is 0.25Mpa to 0.30Mpa, temperature is 21 DEG C to 23 DEG C, recycles the discharge of monomer rectifying tower high-boiling components Amount is 5kg/h to 35kg/h, and the pressure by recycling monomer rectifying tower reboiler control recycling monomer rectifying tower tower bottom is 0.30Mpa to 0.35Mpa, temperature are 30 DEG C to 40 DEG C, and the additional amount of polymerization inhibitor is that liquid phase per ton recycles monomer addition 3g to 6g Polymerization inhibitor.
Technical solution of the present invention fourth is that being realized by following measures: it is a kind of to be used using above-mentioned Production of PVC The Production of PVC recycling monomer processing method that monomer processing unit carries out is recycled, is carried out in the steps below: the first step, gas Mutually recycling monomer recycles monomer general pipeline by gas phase and enters caustic wash tower lower part, gas phase recycling monomer in caustic wash tower from bottom to top Flowing, at the same time, send lye to the top into caustic wash tower into tower tube line by lye, lye flows from top to bottom in caustic wash tower Dynamic that gas phase recycling monomer is inversely contacted and washed with gas phase recycling monomer, the lye of washed gas phase recycling monomer goes out by lye Tower tube line goes out the discharge of tower tube line by lye, and is delivered to caustic wash tower top by caustic wash tower circulating pump and is recycled, wherein gas It is 700m3/h to 15000m3/h, alkali cleaning that mutually the pressure of recycling monomer into caustic wash tower, which is controlled in 0.15Mpa to 0.25Mpa, flow, The temperature of each layer tower tray is 40 DEG C to 50 DEG C in tower, and the pressure difference of alkali cleaning column overhead and tower bottom is less than 0.01Mpa；Second step passes through Gas phase recycling monomer after caustic wash tower washing goes out tower tube line by recycling monomer and sequentially enters recycling first-stage condenser and recycling second level Condenser carries out cooling liquid, wherein control is recycled single by the liquid phase that recycling first-stage condenser and recycling secondary condenser come out The temperature of body is 15 DEG C to 25 DEG C；Third step, liquid phase recycle monomer and enter in liquid seal trough in removal recycling monomer through lower liquid pipe line Water, wherein control out liquid seal trough liquid phase recycling monomer water content less than 0.04%；Liquid phase is recycled monomer by the 4th step It is delivered in recycling monomer rectifying tower by rectifying column feed line and recycling monomer delivery pump and carries out rectification process, pass through polymerization inhibitor Charge pipe, rectifying tower top polymerization inhibitor charge pipe and the cold blanking polymerization inhibitor charge pipe of finished product are respectively to rectifying column feed line, rectifying Polymerization inhibitor is added in gas phase discharge pipe and overhead condenser blanking pipeline, by recycling monomer rectifying tower treated gas phase by Rectifying gas phase discharge pipe drains into remaining recycling monomer in recycling monomer finished product condenser condensation gas phase, by recycling monomer at Treated that gas is discharged by condenser exhaust gas pipeline for product condenser, the recycling condensed out by recycling monomer finished product condenser Monomer is delivered to recycling monomers flow back tank by overhead condenser blanking pipeline, then through return tank discharging pipeline and recycling monomer finished product The recycling monomer a part recycled in monomers flow back tank is back to recycling monomer rectifying tower, a part and passed through and recycled by delivery pump Treated that recycling monomer is discharged by recycling monomer finished product feed-stock pipeline together for monomer rectifying tower, wherein it is single that control enters recycling The flow of the liquid phase recycling monomer of body rectifying column is 10m3/h to 35m3/h, and the pressure of control recycling monomer rectifying column overhead is 0.25Mpa to 0.30Mpa, temperature are 21 DEG C to 23 DEG C, pass through recycling monomer rectifying tower reboiler control recycling monomer rectifying tower The pressure of tower bottom is 0.30Mpa to 0.35Mpa, temperature is 30 DEG C to 40 DEG C, the discharge amount of recycling monomer rectifying tower high-boiling components is 5kg/h to 35kg/h, the additional amount of polymerization inhibitor is that liquid phase per ton recycles monomer addition 3g to 6g polymerization inhibitor everywhere, is back to recycling The flow of the recycling monomer of monomer rectifying tower is 20m3/h to 25m3/h, recycles the inlet water temperature control of monomer finished product condenser At 15 DEG C to 30 DEG C, the flow for the gas being discharged by condenser exhaust gas pipeline is 1m3/h to 2m3/h, recycles monomer in gas system Content be 10% to 35%.
Technical solution of the present invention fifth is that being realized by following measures: it is a kind of to be used using above-mentioned Production of PVC The Production of PVC recycling monomer processing method that monomer processing unit carries out is recycled, carry out in the steps below: the first step is beaten Internally piloted valve is opened, 15% to 20% lye is prepared in Alkali liquid compounding tank；Second step, gas phase recycle monomer and recycle list by gas phase Body general pipeline enters caustic wash tower lower part, and gas phase recycling monomer flows from bottom to top in caustic wash tower, at the same time, will be matched by lye The prepared lye of tank processed send the top into caustic wash tower into tower tube line by lye, lye flowed from above to below in caustic wash tower with Gas phase recycling monomer inversely contacts and washs gas phase recycling monomer, and the lye of washed gas phase recycling monomer goes out tower tube by lye Line goes out the discharge of tower tube line by lye, and is delivered to caustic wash tower top by caustic wash tower circulating pump and is recycled, wherein gas phase is returned It is 700m3/h to 15000m3/h that the pressure control of monomer into caustic wash tower, which is received, in 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 difference of alkali cleaning column overhead and tower bottom is less than 0.01Mpa, by alkaline stream meter and The circular flow that flux of alkaline liquor regulating valve controls lye is 40m3/h to 50m3/h；Third step, the gas after caustic wash tower washs Phase recycling monomer goes out tower tube line by recycling monomer and sequentially enters recycling first-stage condenser and recycling secondary condenser progress coolant liquid Change, wherein control by recycling first-stage condenser and recycling secondary condenser come out liquid phase recycling monomer temperature be 15 DEG C extremely 25℃；4th step, liquid phase recycle monomer and enter the single intracorporal water of removal recycling in liquid seal trough through lower liquid pipe line, wherein control out The water content of the liquid phase recycling monomer of liquid seal trough is less than 0.04%；5th step, by liquid phase recycling monomer by rectifying column feed line It is delivered in recycling monomer rectifying tower with recycling monomer delivery pump and carries out rectification process, pass through polymerization inhibitor charge pipe, rectifying tower top Polymerization inhibitor charge pipe and the cold blanking polymerization inhibitor charge pipe of finished product are respectively to rectifying column feed line, rectifying gas phase discharge pipe and tower Polymerization inhibitor is added in the condenser blanking pipeline of top, by recycling monomer rectifying tower treated gas phase by rectifying gas phase discharge pipe Recycling monomer remaining in recycling monomer finished product condenser condensation gas phase is drained into, treated by recycling monomer finished product condenser Gas is discharged by condenser exhaust gas pipeline, and the recycling monomer condensed out by recycling monomer finished product condenser is by overhead condenser Blanking pipeline is delivered to recycling monomers flow back tank, then will recycle monomer through return tank discharging pipeline and recycling monomer finished product delivery pump Recycling monomer a part in return tank is back to recycling monomer rectifying tower, a part and after recycling monomer rectifying tower processing Recycling monomer together by recycling monomer finished product feed-stock pipeline be discharged, wherein control enter recycling monomer rectifying tower liquid phase return Receive monomer flow be 10m3/h to 35m3/h, control recycling monomer rectifying column overhead pressure be 0.25Mpa to 0.30Mpa, Temperature is 21 DEG C to 23 DEG C, and the pressure by recycling monomer rectifying tower reboiler control recycling monomer rectifying tower tower bottom is 0.30Mpa to 0.35Mpa, temperature are 30 DEG C to 40 DEG C, the discharge amount of recycling monomer rectifying tower high-boiling components is 5kg/h to 35kg/ H, the additional amount of polymerization inhibitor is that liquid phase per ton recycles monomer addition 3g to 6g polymerization inhibitor everywhere, is back to recycling monomer rectifying tower The flow for recycling monomer is 20m3/h to 25m3/h, and the inlet water temperature of recycling monomer finished product condenser is controlled at 15 DEG C to 30 DEG C, the flow for the gas being discharged by condenser exhaust gas pipeline is 1m3/h to 2m3/h, the content of recycling monomer is 10% in gas To 35%.
The present invention can effectively effectively remove high-boiling components impurity and remaining auxiliary agent in recycling monomer, so that it is single to improve recycling Weight, so that recycling monomer mass is stable, initiator amount keeps balance, and resin whiteness effectively improves, solving Determined subsequent technique pipeline, equipment autohemagglutination problem while, realize production auxiliary agent raw material saving and product quality promoted.
Detailed description of the invention
Fig. 1 is the process pipelines flow diagram 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 caustic wash tower inlet and outlet recycle acetaldehyde curve in monomer in the present invention.
Fig. 5 is that caustic wash tower inlet and outlet recycle carbon dioxide content curve in monomer in the present invention.
Coding in attached drawing is respectively as follows: 1 and recycles monomer general pipeline for caustic wash tower, 2 for gas phase, and 3 go out tower tube line for lye, and 4 are First-stage condenser is recycled, 5 go out tower tube line for recycling monomer, and 6 be recycling secondary condenser, and 7 be condenser connecting pipeline, and 8 be row Gas pipeline, 9 be liquid seal trough, and 10 be lower liquid pipe line, and 11 be condensed water delivery pipe, and 12 be recycling monomer rectifying tower, and 13 be rectifying column Feed line, 14 be recycling monomer delivery pump, and 15 be rectifying gas phase discharge pipe, and 16 be to recycle monomer finished product feed-stock pipeline, 17 For reboiler discharge line, 18 be polymerization inhibitor storage tank, and 19 be polymerization inhibitor charge pipe, and 20 be polymerization inhibitor charge pump, 21 for lye into Tower tube line, 22 be Alkali liquid compounding tank, and 23 be caustic wash tower circulating pump, and 24 be alkaline stream meter, and 25 be flux of alkaline liquor regulating valve, and 26 are Alkali liquid compounding tank exhaust line, 27 be lye preheater, and 28 be internally piloted valve, and 29 accept cylinder for lye security personnel, and 30 be recycling monomer Finished product condenser, 31 be condenser exhaust gas pipeline, and 32 is recycle monomers flow back tank, and 33 be overhead condenser blanking pipeline, and 34 are Return tank discharging pipeline, 35 be recycling monomer finished product delivery pump, and 36 be rectifying tower top polymerization inhibitor charge pipe, and 37 be the cold blanking of finished product Polymerization inhibitor charge pipe, 38 be return flow control valve, and 39 be return flow meter, and 40 be control valve, and 41 supply for recycling monomer rectifying Hopper, 42 be recycling monomer rectifying tower feed pump, and 43 be condensate water collecting tank, and 44 be condensation water drainage pipeline, and 45 be automatic valve Door, 46 be liquidometer, and 47 be recycling monomer pan tank.
Specific embodiment
The present invention is not limited by the following examples, can determine according to the technique and scheme of the present invention with actual conditions specific Embodiment.In the present invention, all percentage is mass percent, and lye is sodium hydrate aqueous solution.
In the present invention, for ease of description, the description of the relative positional relationship of each component is according to Figure of description 1 Butut mode be described, such as: the positional relationship of upper and lower, left and right is come according to the Butut direction of Figure of description Determining.
Below with reference to examples and drawings, the invention will be further described:
Embodiment 1, as shown in Fig. 1, Production of PVC recycling monomer processing unit include caustic wash tower 1, recycling First-stage condenser 4, recycling secondary condenser 6, liquid seal trough 9, recycling monomer rectifying tower 12, recycling monomer delivery pump 14 and polymerization inhibitor Storage tank 18；It is fixedly installed with gas phase recycling monomer general pipeline 2 in the tower body lower part of caustic wash tower 1, is fixed on the tower body top of caustic wash tower 1 Lye is installed into tower tube line 21, is fixedly installed with lye in the tower bottom of caustic wash tower 1 and goes out tower tube line 3, caustic wash tower 1 tower top with It is fixedly installed with recycling monomer between the thermal medium feed inlet of recycling first-stage condenser 4 and goes out tower tube line 5, recycles first-stage condenser 4 It is fixedly installed with condenser connecting pipeline 7 between the gas outlet at top and the thermal medium feed inlet for recycling secondary condenser 6, is recycled Exhaust line 8, the thermal medium discharging of recycling 4 bottom of first-stage condenser are fixedly installed on the gas outlet at 6 top of secondary condenser It is fixedly installed with lower liquid respectively between the feed inlet of the thermal medium discharge port and liquid seal trough 9 of mouth and recycling 6 bottom of secondary condenser Pipeline 10,9 bottom of liquid seal trough are fixedly installed with condensed water delivery pipe 11, the feed opening and recycling monomer rectifying of 9 lower part of liquid seal trough It is fixedly installed with rectifying column feed line 13 between the feed inlet of tower 12, recycling is fixedly installed on rectifying column feed line 13 The tower top of monomer delivery pump 14, recycling monomer rectifying tower 12 is fixedly installed with rectifying gas phase discharge pipe 15, recycles monomer rectifying It is fixedly installed with recycling monomer finished product feed-stock pipeline 16 on the discharge port of tower 12, recycles fixed on the reboiler of monomer rectifying tower 12 Reboiler discharge line 17 is installed, polymerization inhibitor storage tank 18 and close to recycling monomer rectifying tower 12 rectifying column feed line 13 it Between be fixedly installed with polymerization inhibitor charge pipe 19, polymerization inhibitor charge pump 20 is fixedly installed on polymerization inhibitor charge pipe 19.Lye is defeated It send to the top of caustic wash tower 1 and inversely contacts washing with the gas phase recycling monomer progress for entering 1 lower part of caustic wash tower, the gas phase after washing Recycling monomer goes out the discharge of tower tube line 5 by recycling monomer；By recycling first-stage condenser 4 and recycling 6 coolant liquid of secondary condenser Recycling vinyl chloride monomer after change is kept in by lower liquid pipe line 10 into liquid seal trough 9；Liquid phase recycling monomer in liquid seal trough 9 is by rectifying Recycling monomer delivery pump 14 on tower feed line 13 is delivered to recycling monomer rectifying tower 12 and carries out rectification process, recycling monomer essence It evaporates 12 bottom of tower and is connected with rectifying tower reboiler, be used to be tower bottom Unit heating, rectifying tower reboiler can be set to 2, just It is spare often to operate to 1 operation 1；It recycles the gas phase after washing at the top of monomer rectifying tower 12 and passes through rectifying gas phase discharge pipe 15 Discharge, the recycling monomer after recycling 12 rectification process of monomer rectifying tower send out conduct by recycling monomer finished product feed-stock pipeline 16 Polymeric kettle raw materials for production are spare, are embodied as subsequent PVC polymerization and provide raw material；Pressure can be installed in the entrance of caustic wash tower 1 Power teletransmission monitoring, polymerization are returned gaseous monomer and are directly entered at caustic wash tower 1 with the high pressure conditions of 0.2MPa to 0.3MPa Reason.Gas phase recycling monomer is sent into caustic wash tower, is first removed with certain density liquid alkaline remaining in polyvinyl chloride recycling monomer Acidic initiator and living radical recycle recycling first-stage condenser 4 and recycling secondary condenser 6 to carry out recycling monomer gas phase Liquefaction, after be sent to recycling monomer rectifying tower 12 in carry out rectification process, initiator aid is residual in the recycling monomer handled It stays and a variety of high-boiling components contents is greatly lowered, to improve recycling monomer mass, improve recycling monomer purity to reach to clean Purpose, for improve Corvic whiteness index provide safeguard.
Embodiment 2, as the optimization of above-described embodiment, as shown in Fig. 1, Production of PVC recycling monomer processing Device further includes Alkali liquid compounding tank 22 and caustic wash tower circulating pump 23；The other end and Alkali liquid compounding tank 22 of the lye into tower tube line 21 Discharge end is fixedly installed togather, in lye into being fixedly installed with caustic wash tower circulating pump 23, caustic wash tower circulating pump on tower tube line 21 Lye between 23 and caustic wash tower 1 into being fixedly installed with alkaline stream meter 24 and flux of alkaline liquor regulating valve on tower tube line 21 respectively 25, the other end that the lye between Alkali liquid compounding tank 22 and caustic wash tower circulating pump 23 goes out tower tube line 3 into tower tube line 21 and lye is solid Dingan County is fitted together；The upper end of Alkali liquid compounding tank 22 is fixedly installed with Alkali liquid compounding tank exhaust line 26.Lye in caustic wash tower 1 Lye circulation is carried out by caustic wash tower circulating pump 23；Alkali liquid compounding tank 22 is provided with fixed preparation method and concentration；Alkali liquid compounding Alkali liquid compounding tank exhaust line 26 is opened in the process, and Alkali liquid compounding operating process and caustic wash tower 1 completely cut off completely, in atmospheric conditions Complete formulation operations；Alkaline stream meter 24 and flux of alkaline liquor regulating valve 25 can be according to the flows into gas phase in caustic wash tower 1 to alkali Flow quantity carries out size control.
Embodiment 3, as the optimization of embodiment 2, as shown in Fig. 1, in alkaline stream meter 24 and flux of alkaline liquor regulating valve Lye after 25 is into being fixedly installed with lye preheater 27 on tower tube line 21, and lye is into tower tube line 21 and lye preheater 27 Cold medium inlet and outlet are fixedly installed togather；Or/and internally piloted valve 28 is fixedly installed on Alkali liquid compounding tank exhaust line 26；Or/ It is located at lye security personnel with, the other end of Alkali liquid compounding tank exhaust line 26 to accept in cylinder 29.Lye preheater 27 can be to circulation alkali Liquid carries out cooling and warming temperature.
Embodiment 4, as the optimization of above-described embodiment, as shown in Fig. 1, Production of PVC recycling monomer processing Device further includes recycling monomer finished product condenser 30, recycling monomers flow back tank 32 and recycling monomer finished product delivery pump 35, rectifying gas The other end of phase discharge pipe 15 and the thermal medium feed end of recycling monomer finished product condenser 30 are fixedly installed togather, and recycling is single It is fixedly installed with condenser exhaust gas pipeline 31 on body finished product condenser 30, recycles the thermal medium discharge end of monomer finished product condenser 30 Overhead condenser blanking pipeline 33 is fixedly installed between recycling monomers flow back tank 32, recycling monomers flow back tank 32 and recycling are single It is fixedly installed with return tank discharging pipeline 34 between body finished product feed-stock pipeline 16, is fixedly installed on return tank discharging pipeline 34 Recycle monomer finished product delivery pump 35, polymerization inhibitor charge pipe 19 and rectifying gas phase discharge pipe 15 after polymerization inhibitor charge pump 20 and Rectifying tower top polymerization inhibitor charge pipe 36 and the cold blanking polymerization inhibitor of finished product are fixedly installed between overhead condenser blanking pipeline 33 respectively Agent charge pipe 37, on recycling the recycling monomer finished product feed-stock pipeline 16 between monomer rectifying tower 12 and return tank discharging pipeline 34 It is fixedly installed with return flow control valve 38 and return flow meter 39 respectively, adds in the polymerization inhibitor close to recycling monomer rectifying tower 12 It is fixedly installed with control valve respectively on expects pipe 19, rectifying tower top polymerization inhibitor charge pipe 36 and the cold blanking polymerization inhibitor charge pipe 37 of finished product 40.Recycle monomer rectifying tower 12 at the top of wash after gas phase by rectifying gas phase discharge pipe 15 be discharged, send to recycle monomer at Product condenser 30 carries out cooling liquefaction, and recycling monomer finished product condenser 30 can be set 2, spare for 1 operation 1；Liquid Recycling monomer after change is delivered to recycling monomers flow back tank 32, recycling by lower pipelines overhead condenser blanking pipeline 33 by self weight 32 lower part of monomers flow back tank is connected to recycling monomer finished product delivery pump 35 by return tank discharging pipeline 34, and recycling monomer finished product is defeated Send pump 35 that monomer a part in recycling monomers flow back tank 32 is delivered to recycling monomer rectifying tower 12, another part is as polymeric kettle Raw materials for production are spare, are embodied as subsequent PVC polymerization and provide raw material；Return flow control valve 38 and return flow meter 39 can be certainly The control of control section is back to the amount of monomer of recycling monomer rectifying tower 12.
Embodiment 5, as the optimization of above-described embodiment, as shown in Fig. 1, the rectifying after recycling monomer delivery pump 14 Recycling monomer rectifying feeder channel 41 is fixedly installed on tower feed line 13, in recycling monomer rectifying feeder channel 41 and recycling monomer Recycling monomer rectifying tower feed pump 42 is fixedly installed on rectifying column feed line between rectifying column 12；Or/and condensed water is defeated The other end of pipe 11 is sent to be fixedly installed with condensate water collecting tank 43, the tank base of condensate water collecting tank 43 is fixedly installed with condensation Water drain line 44 is equipped with automatic valve 45 on condensation water drainage pipeline 44, is fixedly installed on condensate water collecting tank 43 Liquidometer 46；Or/and the other end of recycling monomer finished product feed-stock pipeline 16 is fixedly installed with recycling monomer pan tank 47.Condensation Automatic valve 45 is installed on water drain line 44, automatic control drain operation can be carried out according to the liquid level of condensed water.
Embodiment 6, the polyvinyl chloride carried out using Production of PVC described in embodiment 1 with recycling monomer processing unit Production is carried out in the steps below with recycling monomer processing method: the first step, and gas phase recycles monomer and recycles monomer general pipeline 2 by gas phase Enter 1 lower part of caustic wash tower, gas phase recycling monomer flows from bottom to top in caustic wash tower 1, at the same time, by concentration be 15% to 20% lye send the top into caustic wash tower 1 into tower tube line 21 by lye, and lye flows from above to below in caustic wash tower 1 and gas Mutually recycling monomer inversely contacts and washs gas phase recycling monomer, wherein the pressure control that gas phase recycles monomer into caustic wash tower 1 exists 0.15Mpa to 0.25Mpa, flow are 700m3/h to 15000m3/h, and the temperature of each layer tower tray is 40 DEG C to 50 in caustic wash tower 1 DEG C, the pressure difference of 1 tower top of caustic wash tower and tower bottom is less than 0.01Mpa；Second step, the gas phase after the washing of caustic wash tower 1 recycle monomer Tower tube line 5 is gone out by recycling monomer and sequentially enters recycling first-stage condenser 4 and the recycling progress cooling liquid of secondary condenser 6, wherein The temperature for the liquid phase recycling monomer that control is come out by recycling first-stage condenser 4 and recycling secondary condenser 6 is 15 DEG C to 25 DEG C；The Three steps, liquid phase recycle monomer and enter the single intracorporal water of removal recycling in liquid seal trough 9 through lower liquid pipe line 10, wherein control out fluid-tight The water content of the liquid phase recycling monomer of slot 9 is less than 0.04%；4th step, by liquid phase recycling monomer by 13 He of rectifying column feed line Recycling monomer delivery pump 14 is delivered in recycling monomer rectifying tower 12 and carries out rectification process, by polymerization inhibitor charge pipe 19 to entrance Polymerization inhibitor is added in the liquid phase recycling monomer of recycling monomer rectifying tower 12, by recycling monomer rectifying tower 12 treated gas phase by Rectifying gas phase discharge pipe 15 be discharged, by recycling monomer rectifying tower 12 treated recycling monomer by recycling monomer finished product feeding Pipeline 16 is discharged, wherein and the flow that control enters the liquid phase recycling monomer of recycling monomer rectifying tower 12 is 10m3/h to 35m3/h, The pressure of control recycling 12 tower top of monomer rectifying tower is 0.25Mpa to 0.30Mpa, temperature is 21 DEG C to 23 DEG C, single by recycling 12 reboiler of body rectifying column control recycling 12 tower bottom of monomer rectifying tower pressure be 0.30Mpa to 0.35Mpa, temperature be 30 DEG C extremely 40 DEG C, to recycle the discharge amount of 12 high-boiling components of monomer rectifying tower be 5kg/h to 35kg/h, the additional amount of polymerization inhibitor is liquid phase per ton time It receives monomer and 3g is added to 6g polymerization inhibitor.
Embodiment 7, the polyvinyl chloride carried out using Production of PVC described in embodiment 3 with recycling monomer processing unit Production is carried out in the steps below with recycling monomer processing method: the first step is opened internally piloted valve 28, is prepared in Alkali liquid compounding tank 29 15% to 20% lye；Second step, gas phase recycle monomer and enter 1 lower part of caustic wash tower, gas by gas phase recycling monomer general pipeline 2 Mutually recycling monomer flows from bottom to top in caustic wash tower 1, at the same time, will match 29 lye made by lye by Alkali liquid compounding tank The top into caustic wash tower 1 is sent into tower tube line 21, lye flows from above to below in caustic wash tower 1 inversely to be connect with gas phase recycling monomer Gas phase recycling monomer is touched and washs, the lye of washed gas phase recycling monomer goes out tower tube line 3 by lye and goes out tower tube line 3 by lye Discharge, and 1 top of caustic wash tower is delivered to by caustic wash tower circulating pump 23 and is recycled, wherein gas phase recycles monomer into alkali cleaning The pressure control of tower 1 is 700m3/h to 15000m3/h in 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 difference of 1 tower top of caustic wash tower and tower bottom is less than 0.01Mpa, passes through alkaline stream meter 24 and alkaline stream The circular flow that adjustable valve 25 controls lye is 40m3/h to 50m3/h；Third step, the gas phase after the washing of caustic wash tower 1 are returned Receipts monomer goes out tower tube line 5 by recycling monomer and sequentially enters recycling first-stage condenser 4 and the recycling progress coolant liquid of secondary condenser 6 Change, wherein the temperature for the liquid phase recycling monomer that control is come out by recycling first-stage condenser 4 and recycling secondary condenser 6 is 15 DEG C To 25 DEG C；4th step, liquid phase recycle monomer and enter the single intracorporal water of removal recycling in liquid seal trough 9 through lower liquid pipe line 10, wherein control The water content of liquid phase recycling monomer of liquid seal trough 9 is produced less than 0.04%；Liquid phase recycling monomer is fed by the 5th step by rectifying column Pipeline 13 and recycling monomer delivery pump 14, which are delivered in recycling monomer rectifying tower 12, carries out rectification process, passes through polymerization inhibitor charge pipe 19 are added polymerization inhibitor into the liquid phase recycling monomer for entering recycling monomer rectifying tower 12, after recycling monomer rectifying tower 12 is handled Gas phase be discharged by rectifying gas phase discharge pipe 15, by recycling monomer rectifying tower 12 treated recycling monomer by recycling monomer Finished product feed-stock pipeline 16 is discharged, wherein the flow that control enters the liquid phase recycling monomer of recycling monomer rectifying tower 12 is 10m3/h To 35m3/h, the pressure of control recycling 12 tower top of monomer rectifying tower is 0.25Mpa to 0.30Mpa, temperature is 21 DEG C to 23 DEG C, times The discharge amount for receiving 12 high-boiling components of monomer rectifying tower is 5kg/h to 35kg/h, is controlled back by recycling 12 reboiler of monomer rectifying tower The pressure for receiving 12 tower bottom of monomer rectifying tower is 0.30Mpa to 0.35Mpa, temperature is 30 DEG C to 40 DEG C, and the additional amount of polymerization inhibitor is 3g is added to 6g polymerization inhibitor in liquid phase recycling monomer per ton.
Embodiment 8, the polyvinyl chloride carried out using Production of PVC as described in example 4 with recycling monomer processing unit Production is carried out in the steps below with recycling monomer processing method: the first step, and gas phase recycles monomer and recycles monomer general pipeline 2 by gas phase Enter 1 lower part of caustic wash tower, gas phase recycling monomer flows from bottom to top in caustic wash tower 1, at the same time, by lye by lye into Tower tube line 21 send the top into caustic wash tower 1, and lye flows from above to below in caustic wash tower 1 inversely to be contacted with gas phase recycling monomer And gas phase recycling monomer is washed, the lye of washed gas phase recycling monomer goes out tower tube line 3 by lye and goes out 3 row of tower tube line by lye Out, it and is delivered to 1 top of caustic wash tower by caustic wash tower circulating pump 23 to be recycled, wherein gas phase recycles monomer into caustic wash tower 1 Pressure control in 0.15Mpa to 0.25Mpa, flow be 700m3/h to 15000m3/h, the temperature of each layer tower tray in caustic wash tower 1 It is 40 DEG C to 50 DEG C, the pressure difference of 1 tower top of caustic wash tower and tower bottom is less than 0.01Mpa；Second step, the gas after the washing of caustic wash tower 1 Mutually recycling monomer by recycling monomer go out tower tube line 5 sequentially enter recycling first-stage condenser 4 and recycling secondary condenser 6 cooled down Liquefaction, wherein the temperature for the liquid phase recycling monomer that control is come out by recycling first-stage condenser 4 and recycling secondary condenser 6 is 15 DEG C to 25 DEG C；Third step, liquid phase recycle monomer and enter the single intracorporal water of removal recycling in liquid seal trough 9 through lower liquid pipe line 10, wherein The water content of liquid phase recycling monomer of liquid seal trough 9 is controlled out less than 0.04%；4th step is supplied liquid phase recycling monomer by rectifying column Expects pipe line 13 and recycling monomer delivery pump 14, which are delivered in recycling monomer rectifying tower 12, carries out rectification process, is fed by polymerization inhibitor Pipe 19, rectifying tower top polymerization inhibitor charge pipe 36 and the cold blanking polymerization inhibitor charge pipe 37 of finished product respectively to rectifying column feed line 13, Polymerization inhibitor is added in rectifying gas phase discharge pipe 15 and overhead condenser blanking pipeline 33, is handled by recycling monomer rectifying tower 12 Gas phase afterwards drains into recycling monomer finished product condenser 30 by rectifying gas phase discharge pipe 15 and condenses recycling monomer remaining in gas phase, It is discharged by recycling monomer finished product condenser 30 treated gas by condenser exhaust gas pipeline 21, it is cold by recycling monomer finished product The recycling monomer that condenser 30 condenses out is delivered to recycling monomers flow back tank 32 by overhead condenser blanking pipeline 33, then through flowing back The recycling monomer a part recycled in monomers flow back tank 32 is back to by tank discharging pipeline 34 and recycling monomer finished product delivery pump 35 Recycle monomer rectifying tower 12, a part and by recycling monomer rectifying tower 12 treated recycling monomer together by recycling monomer at Product feed-stock pipeline 16 be discharged, wherein control enter recycling monomer rectifying tower 12 liquid phase recycling monomer flow be 10m3/h extremely 35m3/h, the pressure of control recycling 12 tower top of monomer rectifying tower is 0.25Mpa to 0.30Mpa, temperature is 21 DEG C to 23 DEG C, is passed through The pressure for recycling 12 reboiler of monomer rectifying tower control recycling 12 tower bottom of monomer rectifying tower is 0.30Mpa to 0.35Mpa, temperature is 30 DEG C to 40 DEG C, recycle 12 high-boiling components of monomer rectifying tower discharge amount be 5kg/h to 35kg/h, everywhere the additional amount of polymerization inhibitor be 3g is added to 6g polymerization inhibitor in liquid phase recycling monomer per ton, and the flow for being back to the recycling monomer of recycling monomer rectifying tower 12 is The inlet water temperature of 20m3/h to 25m3/h, recycling monomer finished product condenser 30 are controlled at 15 DEG C to 30 DEG C, are arranged by condenser The flow for the gas that gas pipeline 31 is discharged is 1m3/h to 2m3/h, the content of recycling monomer is 10% to 35% in gas.
Embodiment 9, as shown in Fig. 1, using Production of PVC as described in example 4 with recycling monomer processing unit into Capable Production of PVC can also be carried out in the steps below with recycling monomer processing method: the first step opens internally piloted valve 28, 15% to 20% lye is prepared in Alkali liquid compounding tank 22；Second step, gas phase recycle monomer by gas phase recycling monomer general pipeline 2 into Enter to 1 lower part of caustic wash tower, gas phase recycling monomer flows from bottom to top in caustic wash tower 1, at the same time, will be by Alkali liquid compounding tank 22 Prepared lye send the top into caustic wash tower 1 into tower tube line 21 by lye, lye flowed from above to below in caustic wash tower 1 with Gas phase recycling monomer inversely contacts and washs gas phase recycling monomer, and the lye of washed gas phase recycling monomer goes out tower tube by lye Line 3 goes out tower tube line 3 by lye and is discharged, and is delivered to 1 top of caustic wash tower by caustic wash tower circulating pump 23 and is recycled, wherein It is 700m3/h to 15000m3/h, alkali that gas phase, which recycles the pressure control of monomer into caustic wash tower 1 in 0.15Mpa to 0.25Mpa, flow, The temperature for washing each layer tower tray in tower 1 is 40 DEG C to 50 DEG C, and the pressure difference of 1 tower top of caustic wash tower and tower bottom is less than 0.01Mpa, passes through lye The circular flow that flowmeter 24 and flux of alkaline liquor regulating valve 25 control lye is 40m3/h to 50m3/h；Third step, by alkali cleaning Tower 1 wash after gas phase recycling monomer by recycling monomer go out tower tube line 5 sequentially enter recycling first-stage condenser 4 and recycling second level it is cold Condenser 6 carries out cooling liquid, wherein control is recycled single by the liquid phase that recycling first-stage condenser 4 and recycling secondary condenser 6 come out The temperature of body is 15 DEG C to 25 DEG C；4th step, liquid phase recycle monomer and enter removal recycling monomer in liquid seal trough 9 through lower liquid pipe line 10 Interior water, wherein control out the water content of liquid phase recycling monomer of liquid seal trough 9 less than 0.04%；5th step recycles liquid phase single Body is delivered in recycling monomer rectifying tower 12 by rectifying column feed line 13 and recycling monomer delivery pump 14 and carries out rectification process, is led to Polymerization inhibitor charge pipe 29, rectifying tower top polymerization inhibitor charge pipe 36 and the cold blanking polymerization inhibitor charge pipe 37 of finished product are crossed respectively to rectifying column Polymerization inhibitor is added in feed line 13, rectifying gas phase discharge pipe 15 and overhead condenser blanking pipeline 33, by recycling monomer Treated the gas phase of rectifying column 12 by rectifying gas phase discharge pipe 15 drain into recycling monomer finished product condenser 30 condense it is residual in gas phase Remaining recycling monomer is discharged by condenser exhaust gas pipeline 31 by recycling monomer finished product condenser 30 treated gas, is passed through The recycling monomer that recycling monomer finished product condenser 30 condenses out is delivered to recycling monomer by overhead condenser blanking pipeline 33 and returns Tank 32 is flowed, then the recycling list in monomers flow back tank 32 will be recycled through return tank discharging pipeline 34 and recycling monomer finished product delivery pump 35 Body a part be back to recycling monomer rectifying tower 12, a part and by recycling monomer rectifying tower 12 treated recycling monomer one It rises and is discharged by recycling monomer finished product feed-stock pipeline 16, wherein control enters the liquid phase recycling monomer of recycling monomer rectifying tower 12 Flow is 10m3/h to 35m3/h, and the pressure of control recycling 12 tower top of monomer rectifying tower is 0.25Mpa to 0.30Mpa, temperature is 21 DEG C to 23 DEG C, the pressure by recycling 12 reboiler of monomer rectifying tower control recycling 12 tower bottom of monomer rectifying tower is 0.30Mpa To 0.35Mpa, temperature be 30 DEG C to 40 DEG C, to recycle the discharge amount of 12 high-boiling components of monomer rectifying tower be 5kg/h to 35kg/h, everywhere The additional amount of polymerization inhibitor is that liquid phase per ton recycles monomer addition 3g to 6g polymerization inhibitor, is back to the recycling of recycling monomer rectifying tower 12 The flow of monomer is 20m3/h to 25m3/h, and the inlet water temperature of recycling monomer finished product condenser 30 is controlled at 15 DEG C to 30 DEG C, the flow for the gas being discharged by condenser exhaust gas pipeline 31 is 1m3/h to 2m3/h, the content of recycling monomer is in gas 10% to 35%.
Polymerization inhibitor is mounted on rectifying column feed line, rectifying gas phase discharge pipe and overhead condenser blanking pipeline The pipeline and control valve of charging can arbitrarily select addition point to carry out adding for polymerization inhibitor.
Gas phase recycling monomer is sent into caustic wash tower by the present invention, and it is single first to remove polyvinyl chloride recycling with certain density liquid alkaline Remaining acidic initiator and living radical in body, such as acetaldehyde and carbon dioxide recycle recycling first-stage condenser 4 and return Receive secondary condenser 6 carry out recycling monomer gas phase liquefaction, after be sent to recycling monomer rectifying tower 12 in carry out rectification process into Chloroethanes, acetaldehyde, Trans-dichloroethylene, 1.1 dichloroethanes, cis- dichloroethylene, three chloroethenes in one step removal recycling monomer The high-boiling components impurity such as alkene, the recycling monomer initiator auxiliary agent residual handled and a variety of high-boiling components contents are greatly lowered, thus Recycling monomer mass is improved, subsequent handling process equipment, pipeline recycling monomer autohemagglutination odds are alleviated, due to polychlorostyrene The promotion of ethylene production material quality, effectively improves the whiteness quality index of polyvinyl chloride product, while reducing polymerization The usage amount of initiator raw material in production process, to reduce PVC production cost.
Polyvinyl-chloride use recycling monomer is carried out production it can be seen from Fig. 2 and Fig. 3 to feed intake, through to two production lines of A, B Initiator amount comparison after feeding intake, as shown in attached drawing 2 and attached drawing 3, for using unused polychlorostyrene second of the present invention before June 1 Alkene production recycling monomer processing unit and Production of PVC use the polyvinyl-chloride use of recycling monomer processing method to recycle monomer Initiator one-pot inventory when production Corvic is carried out, uses Production of PVC of the present invention after June 1 to use It is given birth to the polyvinyl-chloride use recycling monomer of recycling monomer processing unit and Production of PVC recycling monomer processing method Initiator one-pot inventory when producing Corvic uses it can be seen from the curve in attached drawing 2 and attached drawing 3 and uses this hair The polyvinyl-chloride use of bright Production of PVC recycling monomer processing unit and Production of PVC recycling monomer processing method Recycling monomer carries out production Corvic, and initiator one-pot inventory is decreased obviously, and initiator total amount one-pot feeds intake average Have dropped 1.5kg, and initiator feed intake it is relatively steady.
Caustic wash tower has preferable removal effect, domestic and international polychlorostyrene to carbon dioxide and acetaldehyde it can be seen from Fig. 4 and Fig. 5 Ethylene polymerization pertinent literature shows that carbon dioxide and acetaldehyde can hinder polymerization reaction and influence the whiteness of Corvic And therefore thermal stability using the technology of the present invention, can effectively remove the carbon dioxide and acetaldehyde recycled in monomer It removes, is provided safeguard for going on smoothly for polymerization reaction, and effectively improve 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 to recycling monomer rectifying tower inlet and outlet The recycling monomer mass data at place are analyzed, and detection data is as shown in table 1, and monomer is recycled it can be seen from data in table 1 Purity averagely increases 0.55%；The high-boiling components impurity component such as chloroethanes, acetaldehyde reduces by 10 times or more in recycling monomer, instead The high-boiling components impurity such as formula-dichloroethylene, 1.1 dichloroethanes, cis- dichloroethylene, trichloro ethylene are completely removed, and effect is bright It is aobvious.
By treated according to embodiments of the present invention, recycling monomer carries out production feeds intake, and produces to polymerization reaction poly- Vinyl chloride resin whiteness index is detected, as shown in table 2, at unused Production of PVC of the present invention recycling monomer Reason device and the polyvinyl-chloride use recycling monomer of Production of PVC recycling monomer processing method carry out production polyvinyl chloride tree The whiteness of rouge is 76% to 82%, and using using, Production of PVC of the present invention recycles monomer processing unit and polyvinyl chloride is raw Produce with recycling monomer processing method polyvinyl-chloride use recycling monomer carry out production Corvic whiteness for 84% to 87%, it can thus be seen that using Production of PVC of the present invention recycling monomer processing unit and Production of PVC is used The whiteness quality index for carrying out production Corvic with the polyvinyl-chloride use recycling monomer of recycling monomer processing method is average Rise 6 percentage points.
After the technology of the present invention, recycling monomer mass is stable, and initiator amount keeps balance, and resin whiteness obtains It effectively improves, illustrates effectively effectively remove high-boiling components impurity and remaining auxiliary agent in recycling monomer using the technology of the present invention, from And recycling monomer mass is improved, while solving the problems, such as subsequent technique pipeline, equipment autohemagglutination, it is former to realize production auxiliary agent The saving of material and product quality are promoted, and are calculated according to 800,000 tons of PVC are produced per year, can be saved 5,350,000 yuan of auxiliary agent cost every year, thus Greatly reduce production cost；In addition, the promotion of polyvinyl chloride resin whiteness index, is also the interior quality for promoting product, wins the market Occupation rate creates huge intangible benefit.
The above technical characteristic constitutes highly preferred embodiment of the present invention, with stronger adaptability and best implementation effect Fruit can increase and decrease non-essential technical characteristic, according to actual needs to meet the needs of different situations.
The recycling monomer mass data of the recycling monomer rectifying tower import and export of table 1
The present invention of table 2 treated Corvic whiteness index that recycling monomer produced

Claims (5)

1. a kind of Production of PVC recycling monomer processing unit, it is characterised in that including caustic wash tower, recycling first-stage condenser, Recycle secondary condenser, liquid seal trough, recycling monomer rectifying tower, recycling monomer delivery pump and polymerization inhibitor storage tank；In the tower of caustic wash tower Body lower part is fixedly installed with gas phase recycling monomer general pipeline, is fixedly installed with lye into tower tube line on the tower body top of caustic wash tower, The tower bottom of caustic wash tower is fixedly installed with lye and goes out tower tube line, feeds in the tower top of caustic wash tower and the thermal medium of recycling first-stage condenser It is fixedly installed with recycling monomer between mouthful and goes out tower tube line, recycle the gas outlet at the top of first-stage condenser and recycles secondary condenser It is fixedly installed with condenser connecting pipeline between thermal medium feed inlet, recycles and is fixedly mounted on the gas outlet at the top of secondary condenser There is exhaust line, recycles the thermal medium discharge port of first-stage condenser bottom and the thermal medium discharge port of recycling secondary condenser bottom It is fixedly installed with lower liquid pipe line respectively between the feed inlet of liquid seal trough, fluid-tight trench bottom is fixedly installed with condensed water delivery pipe, It is fixedly installed with rectifying column feed line between the feed opening of liquid seal trough lower part and the feed inlet for recycling monomer rectifying tower, in rectifying Recycling monomer delivery pump is fixedly installed on tower feed line, the tower top of recycling monomer rectifying tower is fixedly installed with rectifying gas phase row Pipeline out recycles and is fixedly installed with recycling monomer finished product feed-stock pipeline on the discharge port of monomer rectifying tower, recycles monomer rectifying tower Reboiler on be fixedly installed with reboiler discharge line, polymerization inhibitor storage tank and the rectifying column close to recycling monomer rectifying tower are fed It is fixedly installed with polymerization inhibitor charge pipe between pipeline, polymerization inhibitor charge pump is fixedly installed on polymerization inhibitor charge pipe；Wherein:
Above-mentioned Production of PVC recycling monomer processing unit further includes Alkali liquid compounding tank and caustic wash tower circulating pump；Lye is into tower The other end of pipeline and the discharge end of Alkali liquid compounding tank are fixedly installed togather, in lye into being fixedly installed with alkali cleaning on tower tube line Tower circulating pump, lye between caustic wash tower circulating pump and caustic wash tower into being fixedly installed with alkaline stream meter and alkali on tower tube line respectively Liquid stream adjustable valve, the lye between Alkali liquid compounding tank and caustic wash tower circulating pump go out the other end of tower tube line into tower tube line and lye It is fixedly installed togather；The upper end of Alkali liquid compounding tank is fixedly installed with Alkali liquid compounding tank exhaust line；
In the lye after above-mentioned alkaline stream meter and flux of alkaline liquor regulating valve into being fixedly installed with lye preheater on tower tube line, Lye is fixedly installed togather into tower tube line and the cold medium inlet and outlet of lye preheater；It is fixed on Alkali liquid compounding tank exhaust line Internally piloted valve is installed；Or/and the other end of Alkali liquid compounding tank exhaust line is located at lye security personnel and accepts in cylinder；
Above-mentioned Production of PVC recycling monomer processing unit further includes recycling monomer finished product condenser, recycling monomers flow back tank With recycling monomer finished product delivery pump, the other end of rectifying gas phase discharge pipe and the thermal medium of recycling monomer finished product condenser are fed End is fixedly installed togather, and recycles and is fixedly installed with condenser exhaust gas pipeline on monomer finished product condenser, and recycling monomer finished product is cold It is fixedly installed with overhead condenser blanking pipeline between the thermal medium discharge end and recycling monomers flow back tank of condenser, recycling monomer returns Return tank discharging pipeline is fixedly installed between stream tank and recycling monomer finished product feed-stock pipeline, it is fixed on return tank discharging pipeline Recycling monomer finished product delivery pump, polymerization inhibitor charge pipe and rectifying gas phase discharge pipe and tower after polymerization inhibitor charge pump are installed Rectifying tower top polymerization inhibitor charge pipe and the cold blanking polymerization inhibitor charging of finished product are fixedly installed between the condenser blanking pipeline of top respectively Pipe is fixedly installed with respectively on recycling the recycling monomer finished product feed-stock pipeline between monomer rectifying tower and return tank discharging pipeline Return flow control valve and return flow meter, in polymerization inhibitor charge pipe, the rectifying tower top polymerization inhibitor close to recycling monomer rectifying tower It is fixedly installed with control valve respectively on charge pipe and the cold blanking polymerization inhibitor charge pipe of finished product；
Recycling monomer rectifying feeder channel is fixedly installed on the rectifying column feed line after above-mentioned recycling monomer delivery pump, Recycling monomer essence is fixedly installed on rectifying column feed line between recycling monomer rectifying feeder channel and recycling monomer rectifying tower Evaporate tower feed pump；Or/and the other end of condensed water delivery pipe is fixedly installed with condensate water collecting tank, the tank of condensate water collecting tank Body bottom is fixedly installed with condensation water drainage pipeline, is equipped with automatic valve on condensation water drainage pipeline, in condensate water collecting tank On be fixedly installed with liquidometer；Or/and the other end of recycling monomer finished product feed-stock pipeline is fixedly installed with recycling monomer finished product Slot.
2. a kind of carry out polyvinyl chloride life with recycling monomer processing unit using Production of PVC according to claim 1 Produce the method with recycling monomer processing, it is characterised in that carry out in the steps below: the first step, gas phase recycle monomer and are returned by gas phase It receives monomer general pipeline and enters caustic wash tower lower part, gas phase recycling monomer flows from bottom to top in caustic wash tower, at the same time, by concentration Send the top into caustic wash tower into tower tube line by lye for 15% to 20% lye, lye flowed from above to below in caustic wash tower with Gas phase recycling monomer inversely contacts and washs gas phase recycling monomer, wherein the pressure control that gas phase recycles monomer into caustic wash tower exists 0.15Mpa to 0.25Mpa, flow 700m3/ h to 15000m3/ h, the temperature of each layer tower tray is 40 DEG C to 50 DEG C in caustic wash tower, The pressure difference of alkali cleaning column overhead and tower bottom is less than 0.01Mpa；Second step, the gas phase recycling monomer after caustic wash tower washs is by recycling Monomer goes out tower tube line and sequentially enters recycling first-stage condenser and recycling secondary condenser progress cooling liquid, wherein control is by returning The temperature received first-stage condenser and recycle the liquid phase recycling monomer that secondary condenser comes out is 15 DEG C to 25 DEG C；Third step, liquid phase Recycling monomer enters the single intracorporal water of removal recycling in liquid seal trough through lower liquid pipe line, wherein controls out the liquid phase recycling of liquid seal trough The water content of monomer is less than 0.04%；It is defeated by rectifying column feed line and recycling monomer delivery pump to be recycled monomer by the 4th step for liquid phase Send to recycling monomer rectifying tower in carry out rectification process, by polymerization inhibitor charge pipe to enter recycling monomer rectifying tower liquid phase return It receives in monomer and polymerization inhibitor is added, be discharged, passed through by rectifying gas phase discharge pipe by recycling monomer rectifying tower treated gas phase Recycle monomer rectifying tower treated that recycling monomer is discharged by recycling monomer finished product feed-stock pipeline, wherein it is single that control enters recycling The flow of the liquid phase recycling monomer of body rectifying column is 10m3/ h to 35m3/ h, the pressure that monomer rectifying column overhead is recycled in control are 0.25Mpa to 0.30Mpa, temperature are 21 DEG C to 23 DEG C, pass through recycling monomer rectifying tower reboiler control recycling monomer rectifying tower The pressure of tower bottom is 0.30Mpa to 0.35Mpa, temperature is 30 DEG C to 40 DEG C, the discharge amount of recycling monomer rectifying tower high-boiling components is 5kg/h to 35kg/h, the additional amount of polymerization inhibitor are that liquid phase per ton recycles monomer addition 3g to 6g polymerization inhibitor.
It is recycled 3. Production of PVC according to claim 1 carries out Production of PVC with recycling monomer processing unit The method of monomer processing, it is characterised in that carry out in the steps below: the first step is opened internally piloted valve, is prepared in Alkali liquid compounding tank 15% to 20% lye；Second step, gas phase recycle monomer and enter caustic wash tower lower part by gas phase recycling monomer general pipeline, and gas phase is returned Monomer is received to flow from bottom to top in caustic wash tower, at the same time, will by the prepared lye of Alkali liquid compounding tank by lye into tower tube Line send the top into caustic wash tower, and lye flows from above to below in caustic wash tower inversely to be contacted with gas phase recycling monomer and wash gas Mutually recycling monomer, the lye of washed gas phase recycling monomer go out tower tube line by lye and go out the discharge of tower tube line by lye, and by alkali It washes tower circulating pump and is delivered to caustic wash tower top and recycled, wherein the pressure control that gas phase recycles monomer into caustic wash tower exists 0.15Mpa to 0.25Mpa, flow 700m3/ h to 15000m3/ h, the temperature of each layer tower tray is 40 DEG C to 50 DEG C in caustic wash tower, The pressure difference of alkali cleaning column overhead and tower bottom is less than 0.01Mpa, controls following for lye by alkaline stream meter and flux of alkaline liquor regulating valve Circulation is 40 m3/ h to 50m3/h；Third step, the gas phase recycling monomer after caustic wash tower washs go out tower tube by recycling monomer Line sequentially enters recycling first-stage condenser and recycling secondary condenser carries out cooling liquid, wherein control is condensed by recycling level-one The temperature for the liquid phase recycling monomer that device and recycling secondary condenser come out is 15 DEG C to 25 DEG C；4th step, liquid phase recycle monomer warp Lower liquid pipe line enters the single intracorporal water of removal recycling in liquid seal trough, wherein controls out the aqueous of the liquid phase recycling monomer of liquid seal trough Amount is less than 0.04%；Liquid phase is recycled monomer and is delivered to recycling list by rectifying column feed line and recycling monomer delivery pump by the 5th step Body rectifying column is interior to carry out rectification process, is recycled in monomer and is added to the liquid phase for entering recycling monomer rectifying tower by polymerization inhibitor charge pipe Enter polymerization inhibitor, be discharged by recycling monomer rectifying tower treated gas phase by rectifying gas phase discharge pipe, by recycling monomer essence Evaporate tower treated that recycling monomer is discharged by recycling monomer finished product feed-stock pipeline, wherein control enters recycling monomer rectifying tower The flow that liquid phase recycles monomer is 10m3/ h to 35m3/ h, control recycling monomer rectifying column overhead pressure be 0.25Mpa extremely 0.30Mpa, temperature are 21 DEG C to 23 DEG C, the discharge amount of recycling monomer rectifying tower high-boiling components is 5kg/h to 35kg/h, pass through recycling The pressure of monomer rectifying tower reboiler control recycling monomer rectifying tower tower bottom is 0.30Mpa to 0.35Mpa, temperature is 30 DEG C to 40 DEG C, the additional amount of polymerization inhibitor is that liquid phase per ton recycles monomer addition 3g to 6g polymerization inhibitor.
It is recycled 4. Production of PVC according to claim 1 carries out Production of PVC with recycling monomer processing unit The method of monomer processing, it is characterised in that carry out in the steps below: the first step, it is total by gas phase recycling monomer that gas phase recycles monomer Pipe enters caustic wash tower lower part, and gas phase recycling monomer flows from bottom to top in caustic wash tower, at the same time, by lye by lye into Tower tube line send the top into caustic wash tower, and lye flows from above to below in caustic wash tower inversely to be contacted and wash with gas phase recycling monomer Scrubbing mutually recycles monomer, and the lye of washed gas phase recycling monomer goes out tower tube line by lye and goes out the discharge of tower tube line by lye, and It is delivered to caustic wash tower top by caustic wash tower circulating pump to be recycled, wherein gas phase recycles the pressure control of monomer into caustic wash tower System is in 0.15Mpa to 0.25Mpa, flow 700m3/ h to 15000m3/ h, the temperature of each layer tower tray is 40 DEG C to 50 in caustic wash tower DEG C, the pressure difference of alkali cleaning column overhead and tower bottom is less than 0.01Mpa；Second step, after caustic wash tower washs gas phase recycling monomer by Recycling monomer goes out tower tube line and sequentially enters recycling first-stage condenser and recycling secondary condenser progress cooling liquid, wherein control The temperature of the liquid phase recycling monomer come out by recycling first-stage condenser and recycling secondary condenser is 15 DEG C to 25 DEG C；Third step, Liquid phase recycles monomer and enters the single intracorporal water of removal recycling in liquid seal trough through lower liquid pipe line, wherein controls out the liquid phase of liquid seal trough The water content of monomer is recycled less than 0.04%；Liquid phase is recycled monomer by rectifying column feed line and recycling monomer conveying by the 4th step Pump be delivered to recycling monomer rectifying tower in carry out rectification process, by polymerization inhibitor charge pipe, rectifying tower top polymerization inhibitor charge pipe and The cold blanking polymerization inhibitor charge pipe of finished product is respectively to rectifying column feed line, rectifying gas phase discharge pipe and overhead condenser feeder pipe Polymerization inhibitor is added in line, by recycling monomer rectifying tower treated gas phase by rectifying gas phase discharge pipe drain into recycling monomer at Product condenser condenses remaining recycling monomer in gas phase, is arranged by recycling monomer finished product condenser treated gas by condenser Gas pipeline discharge is delivered to by recycling the recycling monomer that monomer finished product condenser condenses out by overhead condenser blanking pipeline Monomers flow back tank is recycled, then the recycling in monomers flow back tank will be recycled through return tank discharging pipeline and recycling monomer finished product delivery pump Monomer a part be back to recycling monomer rectifying tower, a part and by recycling monomer rectifying tower treated recycling monomer together By recycling monomer finished product feed-stock pipeline be discharged, wherein control enter recycling monomer rectifying tower liquid phase recycling monomer flow be 10m3/ h to 35m3/ h, the pressure of control recycling monomer rectifying column overhead is 0.25Mpa to 0.30Mpa, temperature is 21 DEG C to 23 DEG C, the pressure by recycling monomer rectifying tower reboiler control recycling monomer rectifying tower tower bottom is 0.30Mpa to 0.35Mpa, temperature Degree is 30 DEG C to 40 DEG C, the discharge amount of recycling monomer rectifying tower high-boiling components is 5kg/h to 35kg/h, everywhere the additional amount of polymerization inhibitor Monomer being recycled for liquid phase per ton, 3g being added to 6g polymerization inhibitor, the flow for being back to the recycling monomer of recycling monomer rectifying tower is 20m3/ h to 25m3The inlet water temperature of/h, recycling monomer finished product condenser are controlled at 15 DEG C to 30 DEG C, by condenser exhaust gas pipe The flow of the gas of line discharge is 1m3/ h to 2m3The content that monomer is recycled in/h, gas is 10% to 35%.
It is recycled 5. Production of PVC according to claim 1 carries out Production of PVC with recycling monomer processing unit The method of monomer processing, it is characterised in that carry out in the steps below: the first step is opened internally piloted valve, is prepared in Alkali liquid compounding tank 15% to 20% lye；Second step, gas phase recycle monomer and enter caustic wash tower lower part by gas phase recycling monomer general pipeline, and gas phase is returned Monomer is received to flow from bottom to top in caustic wash tower, at the same time, will by the prepared lye of Alkali liquid compounding tank by lye into tower tube Line send the top into caustic wash tower, and lye flows from above to below in caustic wash tower inversely to be contacted with gas phase recycling monomer and wash gas Mutually recycling monomer, the lye of washed gas phase recycling monomer go out tower tube line by lye and go out the discharge of tower tube line by lye, and by alkali It washes tower circulating pump and is delivered to caustic wash tower top and recycled, wherein the pressure control that gas phase recycles monomer into caustic wash tower exists 0.15Mpa to 0.25Mpa, flow 700m3/ h to 15000m3/ h, the temperature of each layer tower tray is 40 DEG C to 50 DEG C in caustic wash tower, The pressure difference of alkali cleaning column overhead and tower bottom is less than 0.01Mpa, controls following for lye by alkaline stream meter and flux of alkaline liquor regulating valve Circulation is 40 m3/ h to 50m3/h；Third step, the gas phase recycling monomer after caustic wash tower washs go out tower tube by recycling monomer Line sequentially enters recycling first-stage condenser and recycling secondary condenser carries out cooling liquid, wherein control is condensed by recycling level-one The temperature for the liquid phase recycling monomer that device and recycling secondary condenser come out is 15 DEG C to 25 DEG C；4th step, liquid phase recycle monomer warp Lower liquid pipe line enters the single intracorporal water of removal recycling in liquid seal trough, wherein controls out the aqueous of the liquid phase recycling monomer of liquid seal trough Amount is less than 0.04%；Liquid phase is recycled monomer and is delivered to recycling list by rectifying column feed line and recycling monomer delivery pump by the 5th step Rectification process is carried out in body rectifying column, is inhibited by polymerization inhibitor charge pipe, rectifying tower top polymerization inhibitor charge pipe and the cold blanking of finished product Polymerization inhibitor is added in agent charge pipe into rectifying column feed line, rectifying gas phase discharge pipe and overhead condenser blanking pipeline respectively Agent drains into recycling monomer finished product condenser condensation by rectifying gas phase discharge pipe by recycling monomer rectifying tower treated gas phase Remaining recycling monomer in gas phase is discharged by recycling monomer finished product condenser treated gas by condenser exhaust gas pipeline, Recycling monomer time is delivered to by overhead condenser blanking pipeline by recycling the recycling monomer that monomer finished product condenser condenses out Tank is flowed, then recycling monomer a part in monomers flow back tank will be recycled through return tank discharging pipeline and recycling monomer finished product delivery pump Be back to recycling monomer rectifying tower, a part and by recycling monomer rectifying tower treated recycling monomer together by recycling monomer Finished product feed-stock pipeline discharge, wherein the flow that control enters the liquid phase recycling monomer of recycling monomer rectifying tower is 10m3/ h is extremely 35m3/ h, the pressure of control recycling 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 recycling monomer rectifying tower tower bottom pressure be 0.30Mpa to 0.35Mpa, temperature be 30 DEG C extremely 40 DEG C, recycle monomer rectifying tower high-boiling components discharge amount be 5kg/h to 35kg/h, everywhere the additional amount of polymerization inhibitor be liquid phase per ton It recycles monomer and 3g is added to 6g polymerization inhibitor, the flow for being back to the recycling monomer of recycling monomer rectifying tower is 20m3/ h to 25m3/ h, The inlet water temperature for recycling monomer finished product condenser controls the gas at 15 DEG C to 30 DEG C, being discharged by condenser exhaust gas pipeline Flow is 1m3/ h to 2m3The content that monomer is recycled in/h, gas is 10% to 35%.
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
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

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
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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