CN213506693U - Preparation system of vinyl chloride polymer - Google Patents
Preparation system of vinyl chloride polymer Download PDFInfo
- Publication number
- CN213506693U CN213506693U CN201921530825.9U CN201921530825U CN213506693U CN 213506693 U CN213506693 U CN 213506693U CN 201921530825 U CN201921530825 U CN 201921530825U CN 213506693 U CN213506693 U CN 213506693U
- Authority
- CN
- China
- Prior art keywords
- reactor
- vinyl chloride
- separation tank
- chloroethylene
- micro
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 title claims abstract description 162
- 229920000642 polymer Polymers 0.000 title claims description 16
- 238000002360 preparation method Methods 0.000 title abstract description 12
- 238000000926 separation method Methods 0.000 claims abstract description 84
- 238000003860 storage Methods 0.000 claims abstract description 51
- 229920000915 polyvinyl chloride Polymers 0.000 claims abstract description 37
- 239000007788 liquid Substances 0.000 claims abstract description 25
- 238000006116 polymerization reaction Methods 0.000 claims abstract description 25
- 239000003999 initiator Substances 0.000 claims abstract description 21
- 230000006835 compression Effects 0.000 claims abstract description 16
- 238000007906 compression Methods 0.000 claims abstract description 16
- 239000012071 phase Substances 0.000 claims abstract description 13
- 239000007791 liquid phase Substances 0.000 claims abstract description 11
- 239000000463 material Substances 0.000 claims description 68
- 238000006243 chemical reaction Methods 0.000 claims description 35
- 239000004800 polyvinyl chloride Substances 0.000 claims description 35
- 238000004519 manufacturing process Methods 0.000 claims description 5
- ZACVGCNKGYYQHA-UHFFFAOYSA-N 2-ethylhexoxycarbonyloxy 2-ethylhexyl carbonate Chemical compound CCCCC(CC)COC(=O)OOC(=O)OCC(CC)CCCC ZACVGCNKGYYQHA-UHFFFAOYSA-N 0.000 claims description 2
- NMOALOSNPWTWRH-UHFFFAOYSA-N tert-butyl 7,7-dimethyloctaneperoxoate Chemical compound CC(C)(C)CCCCCC(=O)OOC(C)(C)C NMOALOSNPWTWRH-UHFFFAOYSA-N 0.000 claims description 2
- 239000000839 emulsion Substances 0.000 abstract description 16
- 238000002156 mixing Methods 0.000 abstract description 9
- 230000005501 phase interface Effects 0.000 abstract description 3
- 238000005728 strengthening Methods 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 2
- 239000002994 raw material Substances 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 14
- 238000000034 method Methods 0.000 description 11
- 239000011347 resin Substances 0.000 description 9
- 229920005989 resin Polymers 0.000 description 9
- 239000002245 particle Substances 0.000 description 6
- 239000000654 additive Substances 0.000 description 5
- 230000000996 additive effect Effects 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 239000000178 monomer Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 239000011259 mixed solution Substances 0.000 description 3
- 230000000379 polymerizing effect Effects 0.000 description 3
- 238000000576 coating method Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 239000006260 foam Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 238000012662 bulk polymerization Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000007720 emulsion polymerization reaction Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 238000005187 foaming Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 239000010985 leather Substances 0.000 description 1
- 239000002649 leather substitute Substances 0.000 description 1
- 239000012046 mixed solvent Substances 0.000 description 1
- 238000003541 multi-stage reaction Methods 0.000 description 1
- 239000002101 nanobubble Substances 0.000 description 1
- 239000002105 nanoparticle Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 239000007779 soft material Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
Images
Landscapes
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The utility model relates to a preparation system of chloroethylene polymer, include: chloroethylene storage tank, pre-reactor, micro-interface generator, first separation tank, second separation tank, post-reactor, third separation tank, centrifugal machine, compression pump and heat exchanger. The utility model discloses a broken chloroethylene makes it form micron order bubble of micron yardstick, each micron order bubble all can form the gas-liquid emulsion with the initiator intensive mixing of liquid phase, through with the gaseous-liquid double-phase intensive mixing, can guarantee that chloroethylene in the system can fully contact with initiator, has improved the polymerization efficiency of system; meanwhile, the micron-sized bubbles are mixed with the initiator to form a gas-liquid emulsion, and the raw materials are fully mixed, so that the phase interface area of gas phase and liquid phase is increased, the thickness of a liquid film is reduced, the mass transfer resistance is reduced, and the effect of strengthening mass transfer within a lower preset operating condition range is achieved.
Description
Technical Field
The utility model relates to a polymer preparation technical field especially relates to a preparation system of chloroethylene polymer.
Background
Polyvinyl chloride (PVC) paste resin belongs to a product branch of PVC resin, and the particle size range of the PVC paste resin is generally 0.1-2.0 μm (the particle size distribution of the general suspension method resin is generally 20-200 μm). The PVC paste resin is named after the high-dispersity powder is used for paste processing, and is mainly applied to the field of soft materials of PVC resin due to excellent paste forming performance and good dispersity. The PVC paste resin can also be applied to processing technologies such as coating, dipping, spraying, foaming and the like, and is widely applied to the fields of various materials and products such as artificial leather, decorative materials, floor leather, wall paper, industrial conveying belts, sports grounds, coatings, adhesives, toys, medical disposable gloves, daily decorative materials, electrical instruments, electrical tools and the like. At present, the industrial production methods of polyvinyl chloride paste resin mainly include emulsion polymerization, mixed microsuspension, microsuspension polymerization and the like. The bulk polymerization method mainly comprises a prepolymerization kettle and a post-polymerization kettle. The polymerization is carried out in two stages. The monomer and the initiator are prepolymerized for 1 hour in a prepolymerization reactor to generate seed particles, the conversion rate reaches 8-10%, and then the seed particles flow into a second-stage polymerization reactor, and the monomer with the same amount as the prepolymer is added for continuous polymerization. When the conversion rate reaches 85-90%, discharging residual monomers, and crushing and sieving to obtain the finished product. The particle size and the particle shape of the resin are controlled by the stirring speed, and the reaction heat is brought out by monomer reflux condensation. The method has simple production process, good product quality and lower production cost. However, after the initiator is used in the system, vinyl chloride is mixed with the liquid-phase solvent, and the quality of the prepared polyvinyl chloride is degraded in the case of non-uniform mixing, thereby reducing the preparation efficiency of the process.
Disclosure of Invention
Therefore, the utility model provides a preparation system of chloroethylene polymer for overcome the problem that the preparation efficiency that chloroethylene and initiating agent mix the inhomogeneous preparation that leads to among the prior art is low.
In order to solve the above problems, the present invention provides a vinyl chloride polymer production system, comprising:
a vinyl chloride storage tank for storing vinyl chloride;
the pre-reactor is connected with the vinyl chloride storage tank and is used for carrying out prepolymerization reaction on vinyl chloride;
the micro-interface generator is respectively arranged at the bottom ends in the pre-reactor and the post-reactor and is respectively connected with the chloroethylene storage tank, the pressure energy of gas and/or the kinetic energy of liquid are converted into bubble surface energy and are transferred to chloroethylene, and the chloroethylene is crushed to form micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm so as to improve the phase boundary mass transfer area, reduce the thickness of a liquid film and reduce the mass transfer resistance;
the first separation tank is connected with the pre-reactor and is used for separating the mixed materials output by the pre-reactor;
the second separation tank is connected with the first separation tank and is used for carrying out secondary separation on the lower-layer material output by the first separation tank;
the post reactor is respectively connected with the chloroethylene storage tank and the second separation tank and is used for carrying out post polymerization reaction on the chloroethylene;
the third separation tank is connected with the post reactor and is used for separating materials output by the post reactor;
the centrifugal machine is respectively connected with the separation tanks and is used for separating the materials output by the separation tanks;
the compression pump is respectively connected with the pre-reactor, the post-reactor, the first separation tank and the second separation tank and is used for conveying vinyl chloride output by each reactor and each separation tank;
and the heat exchanger is arranged at the outlet of the compression pump and used for exchanging heat of the chloroethylene output by the compression pump.
Further, the micro-interface generator comprises a first micro-interface generator and a second micro-interface generator, wherein:
the first micro-interface generator is arranged at the bottom end in the pre-reactor and used for crushing chloroethylene into micron-sized bubbles;
the second micro-interface generator is arranged at the bottom end in the rear reactor and is used for crushing the chloroethylene into micron-sized bubbles.
Furthermore, a discharge port of the chloroethylene storage tank is provided with a shunt pipeline, and the micro-interface generator is respectively connected with the tail ends of the branches.
Further, the side wall of the pre-reactor is provided with a feeding pipeline for conveying the liquid-phase initiator.
Further, the initiator is one or more of di (2-ethylhexyl) peroxydicarbonate (EHP), cumyl peroxyneodecanoate (CNP) and tert-butyl peroxyneodecanoate (BNP).
Furthermore, a return pipe is arranged at the top of the first separation tank and used for returning the separated upper layer chloroethylene to the chloroethylene storage tank,
furthermore, a shunt tube is arranged at the bottom of the first separation tank, and two ends of the shunt tube are respectively connected with the second separation tank and the centrifugal machine and used for conveying the lower-layer material output by the first separation tank.
Furthermore, return pipes are respectively arranged at the tops of the pre-reactor and the post-reactor and used for returning the reacted chloroethylene to a chloroethylene storage tank respectively.
Furthermore, a discharge pipe is arranged at the bottom of the second separation tank and used for conveying the separated bottom polyvinyl chloride finished product to the centrifugal machine, and a conveying pipe is arranged at the bottom of the side wall of the second separation tank and used for conveying the separated mixed material to the post reactor.
Furthermore, a return pipe is arranged at the top of the third separation tank and used for returning the reacted vinyl chloride to a vinyl chloride storage tank, and a discharge pipe is arranged at the bottom of the third separation tank and used for conveying the separated finished polyvinyl chloride product to the centrifugal machine.
Compared with the prior art, the utility model has the advantages that the utility model discloses a broken chloroethylene makes it form micron order bubble of micron scale, each micron order bubble all can form the gas-liquid emulsion with the initiator intensive mixing of liquid phase, through the intensive mixing of gas-liquid double-phase, can guarantee that chloroethylene in the system can fully contact with initiator, has improved the polymerization efficiency of system; meanwhile, the micron-sized bubbles are mixed with the initiator to form a gas-liquid emulsion, and the raw materials are fully mixed, so that the phase interface area of gas phase and liquid phase is increased, the thickness of a liquid film is reduced, the mass transfer resistance is reduced, and the effect of strengthening mass transfer within a lower preset operating condition range is achieved.
In addition, the range of the preset operation condition can be flexibly adjusted according to different product requirements or different catalysts, so that the full and effective reaction is further ensured, the reaction rate is further ensured, and the purpose of strengthening the reaction is achieved.
Further, the utility model discloses a multistage reaction, through using pre-reactor and after-reactor, the vinyl chloride system conversion rate in can effective control system makes the reaction heat fall into several stages and emits to effectively reduced the load of system, improved the operating efficiency of system.
Further, the utility model discloses a plurality of knockout drums, through using the knockout drum to the multistage separation of reaction back material, can effectively separate the chloroethylene that nonpolymerization and polymerization were accomplished in the mixed material, improved the utilization ratio of chloroethylene and the output of polyvinyl chloride in the system.
Further, still be equipped with centrifuge in the system, when system output polyvinyl chloride, centrifuge can carry out centrifugal treatment to polyvinyl chloride in order to get rid of the moisture in the polyvinyl chloride, has improved the purity of system output polyvinyl chloride, thereby has further improved the operating efficiency of system.
Further, still be equipped with the heat exchanger in the system, carry out the heat transfer to the chloroethylene of backward flow through using the heat exchanger, can effectively reduce system's heat load, and improve the operating efficiency of system.
Further, in the system prereactor, after reactor, first knockout drum and third knockout drum top all are equipped with the back flow, can carry out the recovery of maximum to the chloroethylene of system operation in-process not complete polymerization through using respectively the back flow on a plurality of equipment, thereby further improved the chloroethylene utilization ratio of system.
Drawings
FIG. 1 is a schematic view of a system for preparing vinyl chloride polymer according to the present invention.
Detailed Description
Preferred embodiments of the present invention will be described below with reference to the accompanying drawings. It should be understood by those skilled in the art that these embodiments are only for explaining the technical principle of the present invention, and do not limit the scope of the present invention.
It should be noted that in the description of the present invention, the terms of direction or positional relationship indicated by the terms "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, which are only for convenience of description, and do not indicate or imply that the device or element must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention.
Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Please refer to fig. 1, which is a schematic structural diagram of a vinyl chloride polymer preparation system according to the present invention, including a vinyl chloride storage tank 1, a pre-reactor 21, a post-reactor 22, a first micro-interface generator 31, a second micro-interface generator 32, a first separation tank 41, a second separation tank 42, a third separation tank 43, a centrifuge 5, a compression pump 6, and a heat exchanger 7. The first micro-interface generator 31 is arranged at the bottom side in the pre-reactor 21, the second micro-interface generator 32 is arranged at the bottom side in the post-preheater 22, and the first micro-interface generator 31 and the second micro-interface generator 32 are respectively connected with the vinyl chloride storage tank 1 to crush the conveyed vinyl chloride gas, so that the vinyl chloride gas forms micron-scale micro-bubbles and the micron-scale micro-bubbles are respectively output to the corresponding reactors. The pre-reactor 21 is connected with the vinyl chloride storage tank 1 for performing a prepolymerization reaction on vinyl chloride, and the post-reactor 22 is respectively connected with the vinyl chloride storage tank 1 and the second separation tank 42 for receiving the material output by the second separation tank 42 and vinyl chloride gas output by the vinyl chloride storage tank 1 and performing a post-polymerization reaction on vinyl chloride. The first separating tank 41 is connected with the pre-reactor 21 and used for separating mixed materials output by the pre-reactor 21, the second separating tank 42 is connected with the first separating tank 41 and used for further separating the materials separated by the first separating tank 41, and the third separating tank 43 is connected with the rear reactor 22 and used for separating the mixed materials output by the rear reactor 22. The centrifuger 5 is connected to the first separation tank 41, the second separation tank 42, and the third separation tank 43, respectively, to centrifuge the polyvinyl chloride prepared by the system to remove moisture. The compression pump 6 is connected to the pre-reactor 21, the post-reactor 22, the first separation tank 41 and the third separation tank 43, respectively, to transfer vinyl chloride, which is not polymerized during the operation of the above apparatus, to the vinyl chloride storage tank. The heat exchanger 7 is arranged at the discharge port of the compression pump 6 and used for exchanging heat for chloroethylene output by the compression pump 6.
Before the system is operated, vinyl chloride is firstly introduced into the vinyl chloride storage tank 1, and the initiator and the additive in liquid phase are conveyed to the pre-reactor 21. When the system is in operation, the chloroethylene gas is conveyed to the first micro-interface generator 31 and the second micro-interface generator 32 by the chloroethylene storage tank 1, each micro-interface generator can break the chloroethylene gas into micron-sized bubbles, and the micron-sized bubbles are output to the inside of the pre-reactor 21 by the first micro-interface generator 31; the micron-sized bubbles are mixed with an initiator and an additive in the pre-reactor 21 to form a gas-liquid emulsion and enable vinyl chloride to generate a polymerization reaction; after the reaction is finished, the pre-reactor 21 reflows the chloroethylene gas to the chloroethylene storage tank 1 and conveys the mixed material to the first separation tank 41; the first separation tank 41 separates the mixed materials, the chloroethylene gas is refluxed to the chloroethylene storage tank 1, and the mixed materials are respectively conveyed to the second separation tank 42 and the centrifuge 5; the second separation tank 42 performs secondary separation on the mixed materials conveyed by the first separation tank 41, and conveys the separated materials to the post-reactor 32 and the centrifuge 5 respectively; after the post-reactor 32 receives the mixed material, the mixed material is mixed with the micron-sized bubbles output by the second micro-interface generator to form a gas-liquid emulsion and perform a post-polymerization reaction, and after the reaction, the post-reactor 22 returns vinyl chloride to the vinyl chloride storage tank 1 and conveys the reacted mixed material to the third separation tank 43; the third separation tank 43 separates the materials, reflows the vinyl chloride to the vinyl chloride storage tank 1 and conveys the polyvinyl chloride to the centrifuge 5; the centrifugal machine 5 can carry out centrifugal dehydration on the polyvinyl chloride and output the polyvinyl chloride to the system after the dehydration; the compression pump 6 will transfer the vinyl chloride in the return pipe to the confluence storage tank 1; the heat exchanger 7 exchanges heat with the vinyl chloride output by the compression pump 6 to reduce the heat load of the system. It will be understood by those skilled in the art that the first micro-interface generator 31 and the second micro-interface generator 32 of the present invention can also be used in other multi-phase reactions, such as micro-interface, micro-nano interface, ultra-micro interface, micro-bubble biochemical reactor or micro-bubble bioreactor, using micro-mixing, micro-fluidization, ultra-micro fluidization, micro-bubble fermentation, micro-bubble bubbling, micro-bubble mass transfer, micro-bubble reaction, micro-bubble absorption, micro-bubble oxygenation, micro-bubble contact, etc. to form the material into multi-phase micro-mixed flow, multi-phase micro-nano flow, multi-phase emulsified flow, multi-phase micro-structured flow, gas-liquid-solid micro-mixed flow, gas-liquid-solid micro-nano flow, gas-liquid-solid emulsified flow, gas-liquid-solid micro-structured flow, micro-bubbles, micro-foams, micro-foam flow, micro-gas flow, gas-liquid micro-nano emulsified flow, Micro-turbulence, micro-bubble flow, micro-bubble flow, micro-nano-bubble flow and the like, or multi-phase fluid (micro-interface fluid for short) formed by micro-nano-scale particles, thereby effectively increasing the phase interface mass transfer area between the gas phase and/or liquid phase and the liquid phase and/or solid phase in the reaction process. Of course, the system can be used not only for the polymerization of vinyl chloride, but also for the polymerization of polyvinyl chloride, propylene or other kinds of organic matter, provided that the system is able to reach its specified operating state.
As shown in fig. 1, the chloroethylene storage tank 1 of the present invention is a storage tank for storing chloroethylene gas, and when the system is in operation, the chloroethylene storage tank 1 outputs the chloroethylene gas to each of the micro-interface generators respectively, and receives the chloroethylene output by the compression pump 6 to reuse the chloroethylene. It is understood that the size and material of the vinyl chloride storage tank 1 are not particularly limited in this embodiment, as long as the vinyl chloride storage tank 1 can store and transport a specified amount of vinyl chloride gas.
Please continue to refer to fig. 1, the pre-reactor 21 of the present invention is a reaction tank, a feeding pipeline is disposed on a side wall of the pre-reactor 21 for conveying the liquid phase initiator and the additive, a return pipe is disposed on a top of the pre-reactor 21 for returning the unpolymerized vinyl chloride to the vinyl chloride storage tank 1, a discharge port is disposed at a bottom of the pre-reactor 21 for outputting the polymerized mixture to the next equipment, and a first micro-interface generator 31 is further disposed at a bottom of the pre-reactor 21 for outputting the micro-bubbles to an inside of the pre-reactor 21. When the system operates, the mixed solvent of the initiator and the additive is firstly introduced into the pre-reactor 21, at this time, the first micro-interface generator 31 outputs micron-sized bubbles into the pre-reactor 21, the micron-sized bubbles are mixed with the materials in the pre-reactor 21 to form a gas-liquid emulsion, after the mixing is completed, vinyl chloride in the gas-liquid emulsion is subjected to a polymerization reaction to generate polyvinyl chloride, and after the reaction is completed, the pre-reactor 21 reflows unpolymerized vinyl chloride to the vinyl chloride storage tank 1 and outputs the reacted mixed material containing the polyvinyl chloride to the first separation tank 41. It is understood that the pre-reactor 21 may be a stirred tank, a suspended bed, a fluidized bed or other type of reactor, as long as the pre-reactor 21 can achieve its specified operating conditions.
Referring to fig. 1, the first micro-interface generator 31 of the present invention is disposed at the bottom of the pre-reactor 31 for outputting micron-sized bubbles to the pre-reactor 21. When the system is in operation, the first micro-interface generator 31 receives the vinyl chloride conveyed by the vinyl chloride storage tank 1, crushes the vinyl chloride to form micron-sized bubbles, and outputs the micron-sized bubbles to the inside of the pre-reactor 21 so that the micron-sized bubbles are mixed with the materials in the pre-reactor 21 to form a gas-liquid emulsion.
Please continue to refer to fig. 1, the top of the first separation tank 41 is provided with a return pipe for returning vinyl chloride in the mixture to the vinyl chloride storage tank 1, the bottom of the first separation tank 41 is provided with a discharge port, the discharge port is provided with a shunt pipeline, each branch of the shunt pipeline is respectively connected with the second separation tank 42 and the centrifuge 5, and the separated mixture is output to the designated equipment. When the system is in operation, the first separation tank 41 receives the mixed material output by the pre-reactor, separates the mixed material, returns the separated vinyl chloride to the vinyl chloride storage tank through the return pipe, conveys the separated mixed material to the second separation tank 42, and conveys the polyvinyl chloride in the mixed material to the centrifuge 5.
Referring to fig. 1, the second separation tank 42 of the present invention has a discharge pipe at the bottom for conveying the separated pvc to the centrifuge 5, and the side wall of the second separation tank 42 is provided with a conveying pipe connected to the post reactor 22 for conveying the separated mixture to the post reactor 22. When the first separation tank 41 delivers the mixed material to the second reaction tank 42, the second reaction tank 42 separates the material, delivers the polyvinyl chloride at the bottom layer to the centrifuge 5 for centrifugal dehydration, and delivers the mixed material at the middle layer to the post-reactor 22 for post-polymerization.
As shown in fig. 1, the side wall of the post-reactor 22 of the present invention is provided with a feeding pipe for receiving the mixed material output from the second separation tank 42, the top of the post-reactor 22 is provided with a return pipe for returning unpolymerized vinyl chloride to the vinyl chloride storage tank, the bottom of the post-reactor 22 is provided with a discharge port for outputting the mixed material after polymerization, and the bottom of the post-reactor 22 is further provided with a first micro-interface generator 31 for outputting micron-sized bubbles to the inside of the post-reactor 22. When the system is in operation, the post-reactor 22 receives the mixed material output by the second separation tank 42, at this time, the second micro-interface generator 32 outputs micron-sized bubbles to the inside of the post-reactor 22, the micron-sized bubbles and the material in the post-reactor 22 are mixed to form a gas-liquid emulsion, after the mixing is completed, vinyl chloride in the gas-liquid emulsion is subjected to a polymerization reaction to generate polyvinyl chloride, and after the reaction is completed, the post-reactor 22 returns unpolymerized vinyl chloride to the vinyl chloride storage tank 1 and outputs the reacted mixed material containing the polyvinyl chloride to the third separation tank 43. It will be appreciated that the post-reactor 22 may be a stirred tank, a suspended bed, a fluidized bed or other type of reactor, provided that the post-reactor 22 is capable of achieving its specified operating conditions.
Referring to fig. 1, the second micro-interface generator 32 of the present invention is disposed at the bottom end of the rear reactor 32 for outputting micron-sized bubbles to the rear reactor 22. When the system is in operation, the second micro-interface generator 32 receives the vinyl chloride conveyed by the vinyl chloride storage tank 1, crushes the vinyl chloride to form micron-sized bubbles, and outputs the micron-sized bubbles to the inside of the post-reactor 22 so that the micron-sized bubbles and the materials in the post-reactor 22 are mixed to form a gas-liquid emulsion.
Referring to fig. 1, the third separation tank 43 of the present invention has a return pipe at the top for returning unpolymerized vinyl chloride to the vinyl chloride storage tank 1, and a discharge pipe at the bottom of the third separation tank 43 for delivering the vinyl chloride to the centrifuge 5. When the system is in operation, the third separation tank 43 receives and separates the mixed material output from the post-reactor 22, and after separation, the unpolymerized vinyl chloride in the upper layer is refluxed to the vinyl chloride storage tank 1 and the polyvinyl chloride in the lower layer is conveyed to the centrifuge 5.
In order to make the objects and advantages of the present invention more apparent, the present invention will be further described with reference to the following embodiments; it should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Preparation system of vinyl chloride polymer
Step 1: respectively introducing chloroethylene and hydrogen into a chloroethylene storage tank, conveying an initiator to a pre-reactor, and starting to operate the system after the conveying is finished;
step 2: after the system operates, the chloroethylene is respectively conveyed to each micro-interface generator by the chloroethylene storage tank, each micro-interface generator can respectively crush the chloroethylene to form micron-sized bubbles, and the micron-sized bubbles are respectively output to the pre-reactor and the post-reactor after being crushed;
and step 3: mixing the micron-sized bubbles with an initiator and an additive in a pre-reactor to form a gas-liquid emulsion, heating the pre-reactor to perform prepolymerization reaction on vinyl chloride in the gas-liquid emulsion to generate a mixed material containing polyvinyl chloride, and after the reaction is finished, conveying unpolymerized vinyl chloride back to a vinyl chloride storage tank by a compression pump through a return pipe at the top of the pre-reactor for reuse;
and 4, step 4: after the prepolymerization reaction is finished, the pre-reactor outputs the mixed material to a first separation tank, the first separation tank separates the material, vinyl chloride in the material is pumped out and conveyed back to a vinyl chloride storage tank through a return pipe for reuse, and the mixed material is output after separation;
and 5: the mixed materials pass through a flow dividing pipe in the conveying process, the flow dividing pipe separates the materials, polyvinyl chloride is conveyed to a centrifugal machine, and the mixed materials are conveyed to a second separation tank;
step 6: the second separation tank separates the mixed materials, the polyvinyl chloride on the bottom layer is conveyed to a centrifugal machine, and the mixed materials on the upper layer are conveyed to a post reactor;
and 7: the post reactor receives the micron-sized bubbles and the mixed material respectively, the micron-sized bubbles and the mixed material are fully mixed to form gas-liquid emulsion, the post reactor is heated,
and 8: enabling chloroethylene in the gas-liquid emulsion to undergo a prepolymerization reaction to generate a mixed material containing polyvinyl chloride, outputting the mixed material to a third separation tank through a discharge pipe at the bottom of a rear reactor after the reaction is finished, and conveying unpolymerized chloroethylene to a chloroethylene storage tank through a return pipe at the top of the rear reactor by a compression pump for reuse;
and step 9: the third separation tank separates the mixed material output by the post reactor, the chloroethylene on the upper layer flows back to a chloroethylene storage tank, and the polyvinyl chloride on the lower layer is conveyed to a centrifugal machine;
step 10: the centrifugal machine is used for centrifugally dewatering the polyvinyl chloride, and the dewatered dry polyvinyl chloride is conveyed to the system.
Example one
Polymerizing vinyl chloride using the above system and process, wherein:
the initiator is selected from mixed solution of EHP and CNP, the reaction temperature of the pre-reactor is 35 ℃, and the temperature of the post-reactor is 55 ℃. After the system operates, the materials are detected as follows: the polymerization conversion rate of the vinyl chloride is 23 percent, and the utilization rate of the vinyl chloride is 98.1 percent.
Example two
Polymerizing vinyl chloride using the above system and process, wherein:
the initiator is a mixed solution of EHP and BNP, the reaction temperature of the pre-reactor is 38 ℃, and the temperature of the post-reactor is 61 ℃. After the system operates, the materials are detected as follows: the polymerization conversion rate of the vinyl chloride is 26 percent, and the utilization rate of the vinyl chloride is 98.5 percent.
EXAMPLE III
Polymerizing vinyl chloride using the above system and process, wherein:
the initiator is a mixed solution of CNP and BNP, the reaction temperature of the pre-reactor is 40 ℃, and the temperature of the post-reactor is 70 ℃. After the system operates, the materials are detected as follows: the polymerization conversion rate of the chloroethylene is 30 percent, and the utilization rate of the chloroethylene is 99.3 percent.
Comparative example
Vinyl chloride was polymerized using the prior art, wherein the process parameters during the preparation were the same as in the third example. After the system operates, the materials are detected as follows: the polymerization conversion rate of vinyl chloride was 21%, and the utilization rate of vinyl chloride was 97.6%.
Therefore, use the utility model discloses behind system and the technology, can effectively improve the polymerization conversion rate of chloroethylene and the chloroethylene utilization ratio of system.
So far, the technical solution of the present invention has been described with reference to the preferred embodiments shown in the drawings, but it is easily understood by those skilled in the art that the scope of the present invention is obviously not limited to these specific embodiments. Without departing from the principle of the present invention, a person skilled in the art can make equivalent changes or substitutions to the related technical features, and the technical solutions after these changes or substitutions will fall within the protection scope of the present invention.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention; various modifications and changes may occur to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A vinyl chloride polymer production system, comprising:
a vinyl chloride storage tank for storing vinyl chloride;
the pre-reactor is connected with the vinyl chloride storage tank and is used for carrying out prepolymerization reaction on vinyl chloride;
the micro-interface generator is respectively arranged at the bottom ends in the pre-reactor and the post-reactor and is respectively connected with the chloroethylene storage tank, the pressure energy of gas and/or the kinetic energy of liquid are converted into bubble surface energy and are transferred to chloroethylene, and the chloroethylene is crushed to form micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm so as to improve the phase boundary mass transfer area, reduce the thickness of a liquid film and reduce the mass transfer resistance;
the first separation tank is connected with the pre-reactor and is used for separating the mixed materials output by the pre-reactor;
the second separation tank is connected with the first separation tank and is used for carrying out secondary separation on the lower-layer material output by the first separation tank;
the post reactor is respectively connected with the chloroethylene storage tank and the second separation tank and is used for carrying out post polymerization reaction on the chloroethylene;
the third separation tank is connected with the post reactor and is used for separating materials output by the post reactor;
the centrifugal machine is respectively connected with the separation tanks and is used for separating the materials output by the separation tanks;
the compression pump is respectively connected with the pre-reactor, the post-reactor, the first separation tank and the second separation tank and is used for conveying vinyl chloride output by each reactor and each separation tank;
and the heat exchanger is arranged at the outlet of the compression pump and used for exchanging heat of the chloroethylene output by the compression pump.
2. The vinyl chloride polymer production system of claim 1, wherein the micro-interface generator comprises a first micro-interface generator and a second micro-interface generator, wherein:
the first micro-interface generator is arranged at the bottom end in the pre-reactor and used for crushing chloroethylene into micron-sized bubbles;
the second micro-interface generator is arranged at the bottom end in the rear reactor and is used for crushing the chloroethylene into micron-sized bubbles.
3. The system for preparing vinyl chloride polymer according to claim 1, wherein a discharge port of the vinyl chloride storage tank is provided with a bypass pipe, and the micro-interface generator is connected to each branch end.
4. The system for preparing vinyl chloride polymer according to claim 1, wherein the pre-reactor sidewall is provided with a feeding pipe for feeding a liquid phase initiator.
5. The system for preparing vinyl chloride polymer according to claim 4, wherein the initiator is one or more of bis (2-ethylhexyl) peroxydicarbonate (EHP), cumyl peroxyneodecanoate (CNP), and tert-butyl peroxyneodecanoate (BNP).
6. The system of claim 1, wherein a return pipe is provided at a top of the first separation tank to return the separated vinyl chloride of the upper layer to the vinyl chloride storage tank.
7. The system for preparing vinyl chloride polymer according to claim 6, wherein a bypass pipe is provided at the bottom of the first separation tank, and both ends of the bypass pipe are connected to the second separation tank and the centrifuge, respectively, for transferring the lower layer material outputted from the first separation tank.
8. The system for preparing vinyl chloride polymer according to claim 1, wherein the pre-reactor and the post-reactor are provided at the top thereof with return pipes, respectively, for returning the reacted vinyl chloride to the vinyl chloride storage tanks, respectively.
9. The system for preparing vinyl chloride polymer according to claim 1, wherein the second separation tank is provided at a bottom thereof with a discharge pipe for feeding the separated polyvinyl chloride product at a bottom layer to the centrifuge, and the second separation tank is provided at a bottom of a side wall thereof with a feeding pipe for feeding the separated mixed material to the post-reactor.
10. The system for preparing vinyl chloride polymer according to claim 1, wherein the third separation tank is provided at a top thereof with a return pipe for returning the reacted vinyl chloride to a vinyl chloride storage tank, and at a bottom thereof with a discharge pipe for feeding the separated vinyl chloride product to the centrifuge.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921530825.9U CN213506693U (en) | 2019-09-14 | 2019-09-14 | Preparation system of vinyl chloride polymer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921530825.9U CN213506693U (en) | 2019-09-14 | 2019-09-14 | Preparation system of vinyl chloride polymer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN213506693U true CN213506693U (en) | 2021-06-22 |
Family
ID=76378432
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921530825.9U Active CN213506693U (en) | 2019-09-14 | 2019-09-14 | Preparation system of vinyl chloride polymer |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN213506693U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112495320A (en) * | 2019-09-14 | 2021-03-16 | 南京延长反应技术研究院有限公司 | Preparation system and process of vinyl chloride polymer |
-
2019
- 2019-09-14 CN CN201921530825.9U patent/CN213506693U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112495320A (en) * | 2019-09-14 | 2021-03-16 | 南京延长反应技术研究院有限公司 | Preparation system and process of vinyl chloride polymer |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8217124B2 (en) | Ethylene polymerization in a high pressure reactor with improved initiator feeding | |
| CN101754987B (en) | System and process for production of polyethylene and polypropylene | |
| EP3186288B1 (en) | Process for separating components of a polymer-monomer mixture obtained by high-pressure polymerization of ethylenically unsaturated monomers | |
| CN101230114B (en) | Polymerization reactor and method for producing polypropylene by employing the same | |
| CN103254342B (en) | For the manufacture of the preparation method of the bimodal Linear low-density polyethylene composition of film | |
| CN213506693U (en) | Preparation system of vinyl chloride polymer | |
| CN108329433A (en) | A kind of middle anti-impact polystyrene resin production system | |
| CN104788593B (en) | A kind of method and device for producing low density polyethylene (LDPE) | |
| CN212119946U (en) | Reinforcing system for preparing polyethylene based on body method | |
| CN213506694U (en) | Intelligent strengthening system for preparing polyethylene based on ontology method | |
| CN112500512B (en) | Reinforcing system and process for preparing polyethylene based on bulk method | |
| CN107629210A (en) | A kind of preparation technology of polysiloxanes | |
| CN112495320A (en) | Preparation system and process of vinyl chloride polymer | |
| CN107312169A (en) | A kind of polyketone manufacturing technique method and its process unit | |
| CN112500508A (en) | Intelligent strengthening system and process for preparing polyethylene based on body method | |
| CN217989319U (en) | Multifunctional olefin polymerization device | |
| CN115197348B (en) | Ethylene polymer and high pressure radical polymerization process and apparatus for preparing ethylene polymer | |
| CN112495310A (en) | System and process for strengthening propylene polymerization | |
| CN212128041U (en) | Intelligent strengthening system for preparing polyethylene based on solution method | |
| CN112500509B (en) | System and process for strengthening ethylene polymerization | |
| CN104628904A (en) | Method for preparing olefin polymer by utilizing multiple temperature reaction areas | |
| CN211886852U (en) | Continuous production equipment for free radical polymerization | |
| CN112500506A (en) | Intelligent strengthening system and process for preparing polyethylene based on solution method | |
| CN207552224U (en) | A kind of production technology device of polyketone | |
| CN213506692U (en) | System for strengthening ethylene polymerization |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |