CN104356261B - A kind of ultra-high molecular weight polyethylene intermittent polyreaction successive flash vaporization balance method - Google Patents
A kind of ultra-high molecular weight polyethylene intermittent polyreaction successive flash vaporization balance method Download PDFInfo
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- CN104356261B CN104356261B CN201410678621.5A CN201410678621A CN104356261B CN 104356261 B CN104356261 B CN 104356261B CN 201410678621 A CN201410678621 A CN 201410678621A CN 104356261 B CN104356261 B CN 104356261B
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Abstract
The open a kind of ultra-high molecular weight polyethylene intermittent polyreaction successive flash vaporization balance method of the present invention, its feature is to use two polymeric kettles to set a timing difference parallel operation, during one polymeric kettle discharging, another polymeric kettle reacts, discharge unreacting ethylene by discharging flash distillation, hexane is reclaimed in condensation, compression supercharging gaseous ethylene is back in the polymeric kettle reacting, reuse unreacting ethylene.Present invention, avoiding and prior art has neither part nor lot in the low pressure ethylene of reaction be difficult to be back to polymeric kettle recycles, can only be to enter torch to burn, make ethene waste serious, and not environmentally, there is the unfavorable situations such as potential safety hazard；Ethylene raw is saved in the setting of the present invention, makes solvent hexane recycle simultaneously, simplifies technological process.
Description
Technical field
-the present invention proposes a kind of ultra-high molecular weight polyethylene intermittent polyreaction successive flash vaporization balance method, relates to the technical field of ultra-high molecular weight polyethylene device ethene batchwise polymerization.
Background technology
nullIn-existing ultra-high molecular weight polyethylene device，High-quality ultra-high molecular weight polyethylene product all uses batchwise polymerization mode to produce，I.e. first by solvent hexane、Master/co-catalyst disposably adds in polymeric kettle，Control temperature～80 DEG C，Control pressure～1.5MPa，And in 4～6 hours, be continuously added to ethene carry out polymerisation，After 4～6 hours, a discharging to flashed down in flash tank is " hexane+Ultra high molecular weight polyethylene particles " slurry，Flash distillation gas phase hexane and unreacting ethylene enter condenser condensation and collect hexane，And ethene is due to pressure low (typically at～0.1MPa) after flashed down，Unit interval inner volume amount is big，And batchwise polymerization is a kettle one kettle operation，Time cycle is long，The low pressure ethylene having neither part nor lot in reaction is caused to be difficult to be back to polymeric kettle recycles，Processing mode is to enter torch to burn；It is that ethene burns waste seriously that the method causes consequence, and not environmentally, there is potential safety hazard.
Content of the invention
In order to overcome prior art not enough, present invention aim at providing a kind of ultra-high molecular weight polyethylene intermittent polyreaction successive flash vaporization balance method.
The object of the present invention is achieved like this:
A kind of ultra-high molecular weight polyethylene intermittent polyreaction successive flash vaporization balance method, the steps include:
Step 1: after being stored in the master that configures in hermetically sealed can/co-catalyst metering through catalyst charge pump be pressurized to～1.5MPa enters 1A polymeric kettle, or 1B polymeric kettle；
Step 2: the refined hexane being stored in refined hexane storage tank is pressurized to 1.5MPa through hexane charge pump, sends into 1A polymeric kettle, or 1B polymeric kettle after cumulative measurement；
Step 3: the hexane in 1A polymeric kettle, or 1B polymeric kettle is heated to～80 DEG C；
Step 4: refine 20 DEG C, 1.5MPa hydrogen according to after gaseous ethylene inlet amount 3% metering with 20 DEG C, 1.5MPa ethene simultaneously enter 1A polymeric kettle, or 1B polymeric kettle；
Step 5: with～20 DEG C ,～1.5MPa gaseous ethylene be continuously added to, 1A polymeric kettle, or 1B polymeric kettle pressure rises to～1.5MPa, starts polymerization, gaseous ethylene and hydrogen terminate polymerisation after being passed through continuously 4～6 hours；
Step 6:1A polymeric kettle, or the reaction of 1B polymeric kettle carries out stopping charging after 4-6 hour, treat 1A polymeric kettle, or 1B polymeric kettle pressure is down to 0.5MPa, open 1A polymeric kettle, or discharge valve bottom 1B polymeric kettle, control discharge valve aperture makes " hexane+Ultra high molecular weight polyethylene particles " slurry rely on 1A polymeric kettle, or the pressure of 1B polymeric kettle itself is delivered in flash tank 2 be depressured flash distillation, the a small amount of ethene being dissolved in hexane separates in flash tank 2, " hexane+Ultra high molecular weight polyethylene particles " slurry is delivered to lower procedure process by slurry pump 3 by discharging bottom flash vaporization kettle 2；The ethylene gas flashing off and hexane gas are cached in surge tank 4, after condensing through first-stage condenser 5 and secondary condenser 6, liquid Recycling hexane is in hexane collecting tank 8, at 1A polymeric kettle, or carry out while 1B polymeric kettle feeding stage, it is delivered in 1A polymeric kettle, or 1B polymeric kettle recycle by hexane delivery pump 9；Ethylene gas enter compressor 7 be pressurized to～1.5MPa after be back to 1A polymeric kettle, or 1B polymeric kettle participates in polymerisation, reaches to reclaim 1A polymeric kettle, or 1B polymeric kettle；Participate in reacting ethylene and～80 DEG C of purposes that solvent hexane recycles.
Feature of the present invention
The present invention uses 1A polymeric kettle and two polymeric kettles of 1B polymeric kettle, sets a timing difference parallel operation, makes the reaction of another polymeric kettle during a polymeric kettle discharging carry out.
The invention have the advantages that: avoid and have neither part nor lot in the low pressure ethylene of reaction and be difficult to be back to polymeric kettle recycles, can only be to enter torch to burn, make ethene burn waste serious, and not environmentally, there is the unfavorable situations such as potential safety hazard；The present invention passes through 1A polymeric kettle and two the polymeric kettle time difference parallel operations of 1B polymeric kettle, reclaims polymeric kettle discharging phase and has neither part nor lot in the ethene of reaction, improve ethylene raw utilization rate, saves ethylene raw and put into；The a small amount of ethylene gas of dissolving and hexane gas that flash separation goes out no longer carry out any process, and return directly to reactor and recycle, it is to avoid the separation process of isolated and purified solvent hexane again, beneficially simplification of flowsheet.
Brief description
Fig. 1 is the process chart of the present invention
In figure: 1A-polymeric kettle, 1B-polymeric kettle, 2-flash tank, 3-slurry pump, 4-surge tank, 5-first-stage condenser, 6-secondary condenser, 7-compressor, 8-hexane collecting tank, 9-delivery pump.
Detailed description of the invention
Below in conjunction with the accompanying drawings technical scheme is described in any further:
A kind of ultra-high molecular weight polyethylene intermittent polyreaction successive flash vaporization balance method, the steps include:
Step 1: be pressurized to 1.5MPa through charge pump after being stored in the master/co-catalyst metering configuring in hermetically sealed can and enter 1A polymeric kettle；
Step 2: the refined hexane being stored in refined hexane storage tank is pressurized to 1.5MPa through hexane charge pump, sends into 1A polymeric kettle after cumulative measurement；
Step 3: the hexane in 1A polymeric kettle is heated to 80 DEG C；
Step 4: refine 20 DEG C, 1.5MPa hydrogen according to after gaseous ethylene inlet amount 3% metering with 20 DEG C, 1.5MPa ethene simultaneously enter 1A polymeric kettle；
Step 5: with 20 DEG C, 1.5MPa gaseous ethylene be continuously added to 1A polymeric kettle, pressure rises to 1.5MPa, start polymerization, gaseous ethylene and hydrogen be passed through continuously 4～6 hours after terminate polymerisation；
Step 6:1A polymeric kettle, reaction stops charging after carrying out 4-6 hour, treat that 1A polymeric kettle pressure is down to 0.5MPa, open 1A polymeric kettle, bottom discharge valve, control discharge valve aperture makes " hexane+ultra-high molecular weight polyethylene " slurry rely on 1A polymeric kettle, such operation is a polymeric kettle 1A discharging, control discharge valve aperture makes " hexane+ultra-high molecular weight polyethylene " slurry rely on polymeric kettle 1A, the pressure of itself is delivered in flash tank 2 be depressured flash distillation, the a small amount of ethene being dissolved in hexane separates in flash tank 2, " hexane+Ultra high molecular weight polyethylene particles " slurry is delivered to lower procedure process by slurry pump 3 by discharging bottom flash vaporization kettle 2；The ethylene gas flashing off and hexane gas are cached in surge tank 4, after condensing through first-stage condenser 5 and secondary condenser 6, (condenser is shell and tube condenser, or plate-type condenser, or finned cooler, cooling medium is cooling water, or chilled water, or refrigerated brine), liquid Recycling hexane is in hexane collecting tank 8, while 1A polymeric kettle feeding stage
It by discharging flash distillation, is cached in surge tank 4 ethylene gas and hexane gas and is delivered in 1B polymeric kettle recycle by delivery pump 9；Ethylene gas enters compressor 7 and is pressurized to 1.5MPa, is back to polymeric kettle 1A and participates in polymerisation.Treat that 1B polymeric kettle pressure is down to 0.5MPa, open 1B polymeric kettle discharge valve discharging, control discharge valve aperture makes " hexane+ultra-high molecular weight polyethylene " slurry rely on polymeric kettle 1B, the pressure of itself is delivered in flash tank 2 be depressured flash distillation, it is cached in surge tank 4 ethylene gas and hexane gas to be delivered in 1A polymeric kettle recycle by delivery pump 9. the purpose of aforesaid operations is to reclaim the ethene that polymeric kettle 1B has neither part nor lot in reaction, the hexane dissolving a small amount of ethene simultaneously making flash separation go out is not carrying out any process, and returns directly to reactor 1A.
It is delivered in 1B polymeric kettle recycle by delivery pump 9；Ethylene gas enters and is back to 1A polymeric kettle after compressor 7 is pressurized to 1.5MPa, or 1B polymeric kettle participates in polymerisation, reaches to reclaim 1A polymeric kettle, or 1B polymeric kettle；Participate in reacting ethylene and～80 DEG C of purposes that solvent hexane recycles.
Claims (1)
1. a ultra-high molecular weight polyethylene intermittent polyreaction successive flash vaporization balance method, use 1A polymeric kettle and two polymeric kettles of 1B polymeric kettle, set a timing difference parallel operation, make the reaction of another polymeric kettle during a polymeric kettle discharging carry out, the steps include:
Step 1: be pressurized to 1.5MPa through charge pump after being stored in the master/co-catalyst metering configuring in hermetically sealed can and enter 1A polymeric kettle, or 1B polymeric kettle；
Step 2: the refined hexane being stored in refined hexane storage tank is pressurized to 1.5MPa through hexane charge pump, sends into 1A polymeric kettle, or 1B polymeric kettle after cumulative measurement；
Step 3: the hexane in 1A polymeric kettle, or 1B polymeric kettle is heated to 80 DEG C；
Step 4: refine 20 DEG C, 1.5MPa hydrogen according to after gaseous ethylene inlet amount 3% metering with 20 DEG C, 1.5MPa ethene simultaneously enter 1A polymeric kettle, or 1B polymeric kettle；
Step 5: with 20 DEG C, 1.5MPa gaseous ethylene be continuously added to, 1A polymeric kettle, or 1B polymeric kettle pressure rises to 1.5MPa, starts polymerization, gaseous ethylene and hydrogen terminate polymerisation after being passed through continuously 4～6 hours；
Step 6:1A polymeric kettle, or the reaction of 1B polymeric kettle carries out stopping charging after 4-6 hour, treat 1A polymeric kettle, or 1B polymeric kettle pressure is down to 0.5MPa, open 1A polymeric kettle, or discharge valve bottom 1B polymeric kettle, control discharge valve aperture makes " hexane+ultra-high molecular weight polyethylene " slurry rely on 1A polymeric kettle, or the pressure of 1B polymeric kettle itself is delivered to step-down flash distillation in flash tank (2), the a small amount of ethene being dissolved in hexane separates in flash tank (2), " hexane+Ultra high molecular weight polyethylene particles " slurry is discharged by flash tank (2) bottom, slurry pump (3) is delivered to lower procedure process；The ethylene gas flashing off and hexane gas are cached in surge tank (4), after condensing through first-stage condenser (5) and secondary condenser (6), liquid Recycling hexane is in hexane collecting tank (8), at 1A polymeric kettle, or carry out while 1B polymeric kettle feeding stage, it is delivered in 1A polymeric kettle, or 1B polymeric kettle recycle by hexane delivery pump (9)；Ethylene gas enters and is back to 1A polymeric kettle after compressor (7) is pressurized to 1.5MPa, or 1B polymeric kettle participates in polymerisation, is recovered to 1A polymeric kettle, or 1B polymeric kettle；Participate in recycling of reacting ethylene and 80 DEG C of solvent hexanes.
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| CN111729616B (en) * | 2020-07-09 | 2022-09-23 | 唐山三友氯碱有限责任公司 | Automatic control method for feeding interval time in polyvinyl chloride resin production |
| CN114907505A (en) * | 2021-02-08 | 2022-08-16 | 中国科学院上海有机化学研究所 | Production process of ultrahigh molecular weight polyethylene |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6294494B1 (en) * | 1998-12-18 | 2001-09-25 | Phillips Petroleum Company | Olefin polymerization processes and products thereof |
| CN101113184A (en) * | 2007-09-03 | 2008-01-30 | 北京东方石油化工有限公司助剂二厂 | Method for producing polyvinyl resin with super-high molecular weight |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6294494B1 (en) * | 1998-12-18 | 2001-09-25 | Phillips Petroleum Company | Olefin polymerization processes and products thereof |
| CN101113184A (en) * | 2007-09-03 | 2008-01-30 | 北京东方石油化工有限公司助剂二厂 | Method for producing polyvinyl resin with super-high molecular weight |
Non-Patent Citations (1)
| Title |
|---|
| "先进控制在聚乙烯装置中的应用";申宇等;《石油化工自动化》;20020830(第4期);23-30 * |
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