CN1410456A - Cyclic recovery method of propylene in production of polypropylene - Google Patents
Cyclic recovery method of propylene in production of polypropylene Download PDFInfo
- Publication number
- CN1410456A CN1410456A CN 01136035 CN01136035A CN1410456A CN 1410456 A CN1410456 A CN 1410456A CN 01136035 CN01136035 CN 01136035 CN 01136035 A CN01136035 A CN 01136035A CN 1410456 A CN1410456 A CN 1410456A
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- Prior art keywords
- propylene
- polypropylene
- circulation
- washing tower
- reactor
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- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 142
- 239000004743 Polypropylene Substances 0.000 title claims abstract description 44
- 229920001155 polypropylene Polymers 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 39
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims description 136
- -1 polypropylene Polymers 0.000 title claims description 42
- 238000011084 recovery Methods 0.000 title claims description 17
- 238000004519 manufacturing process Methods 0.000 title abstract description 10
- 125000004122 cyclic group Chemical group 0.000 title description 2
- 238000005406 washing Methods 0.000 claims abstract description 49
- 239000000463 material Substances 0.000 claims abstract description 22
- 238000006116 polymerization reaction Methods 0.000 claims abstract description 15
- 239000000843 powder Substances 0.000 claims abstract description 10
- 230000004087 circulation Effects 0.000 claims description 38
- 238000005360 mashing Methods 0.000 claims description 21
- 239000000178 monomer Substances 0.000 claims description 15
- 238000007906 compression Methods 0.000 claims description 11
- 230000006835 compression Effects 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 9
- 238000010992 reflux Methods 0.000 claims description 8
- 239000002994 raw material Substances 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 230000008569 process Effects 0.000 abstract description 12
- 230000008901 benefit Effects 0.000 abstract description 2
- 238000005516 engineering process Methods 0.000 description 14
- 238000007872 degassing Methods 0.000 description 8
- 238000007599 discharging Methods 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 4
- 230000006872 improvement Effects 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- 241000282326 Felis catus Species 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000003963 antioxidant agent Substances 0.000 description 1
- 230000003078 antioxidant effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 125000004980 cyclopropylene group Chemical group 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 210000003205 muscle Anatomy 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
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- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
A process for cyclically recovering propene in the production of polypropene features that a circulating tube reactor is so reformed that the washed material containing polypropene powder collected at the bottom of a washing tower is cooled and then pumped directly to the polymerization step for polymerization so as to decrease the propene quantity in the circulating process. Its advantages are less consumption of propene and energy and low cost.
Description
Technical field
The present invention relates to the polypropylene production technology, say further, relate in the annular-pipe reactor buck polymerization polypropylene production technology, a kind of method that the relevant polymkeric substance degassing, propylene circulation are reclaimed.
Background technology
The polypropylene plant of using annular-pipe reactor bulk technique technology mainly comprises Preparation of Catalyst, polyreaction, the polymkeric substance degassing and propylene circulation recovery, decatize and technique units such as drying, extruding and granulation.In the technique unit that the polymkeric substance degassing and propylene circulation are reclaimed, comprise equipment such as flash tank, high pressure propylene washing tower, bag filter, low pressure propylene washing tower, circulation propylene compressor.A large amount of polypropylene of discharging from polymerization workshop section and propylene liquid monomer enter flash tank makes the propylene flash of steam, and at this with polypropylene and propylene steam monomer separation.Isolated polypropylene enters bag filter and carries out gas solid separation again from flash tank, solid phase flows into downstream decatize drying treatment, isolated propylene steam is sent into the washing of high pressure propylene washing tower through the washing of low pressure propylene washing tower, circulation propylene compressor compression back in the lump with the isolated propylene steam of flash tank, again after condensation, a part refluxes, a part is pumped into polymerization workshop section through the propylene feed jar by propylene feed and carries out polymerization, thereby the circulation that realizes the propylene monomer in the polypropylene production technique is reclaimed.Among this, for preventing high pressure propylene washing tower bottom solid accumulation, existing processes is after bottoms material (propylene that contains the polypropylene powder that washes on a small quantity) is vaporized through a little flash lines, be returned to bag filter continuously and carry out gas solid separation again, isolated propylene gas carries out circulation cleaning through low pressure propylene washing tower, high pressure propylene washing tower again.The circulation of this propylene monomer between high pressure scrubber, bag filter, low pressure propylene washing tower and circulation propylene compressor makes that the treatment capacity of equipment is big, and facility investment and energy consumption are big.
China has nearly 100 covers of polypropylene plant at present, and the device of scale more than 10 tons be 10 covers altogether, 4 cover scales are wherein arranged more than 200,000 tons, and all the other unit scales are mostly at 70,000 tons/year.Also have several covers to utilize crude propylene to go into operation before and after 2002 for the polyacrylic device of raw material production.Its production technique is in the majority with annular-pipe reactor bulk technique technology.Along with expanding economy, scale is faced with capacity expansion revamping less than 100,000 tons polypropylene plant.Expand can in often also because in the degassing of existing polymkeric substance and propylene circulation and recovery process process, increase from high pressure scrubber, bag filter to the propylene tolerance of the propylene compressor that circulates, and cause capacity of equipment deficiencies such as compression, washing, corresponding transformation will increase a bulk of investment, and the prolongation construction period, so that influence economic benefit.
Summary of the invention
Technology of the present invention provides the circulation recovery method of propylene in a kind of polypropylene production.This method has reduced the treatment capacity of propylene monomer in the propylene monomer circulation and recovery process unit, thereby has solved the problem that facility investment is big in the existing technology, energy consumption is high.
The present invention transforms the polypropylene plant of annular-pipe reactor bulk technique technology and puts forward in the experience of polypropylene technology field accumulation for many years according to the contriver.The present invention mainly is in the annular-pipe reactor buck polymerization polypropylene production technique, the polymkeric substance degassing and propylene circulation, the improvement of reclaiming technique unit.This technique unit comprises equipment such as flash tank, high pressure propylene washing tower, bag filter, low pressure propylene washing tower, circulation propylene compressor.A large amount of polypropylene of discharging from polymerization workshop section and propylene liquid monomer enter flash tank makes the propylene flash of steam, and at this with polypropylene and propylene steam monomer separation.Isolated polypropylene enters bag filter and carries out gas solid separation again from flash tank, isolated propylene steam is sent into the washing of high pressure propylene washing tower through the washing of low pressure propylene washing tower, circulation propylene compressor compression back in the lump with the isolated propylene steam of flash tank, again after condensation, a part refluxes, a part is pumped into polymerization workshop section through the propylene feed jar by propylene feed and carries out polymerization, thereby the circulation that realizes the propylene monomer in the polypropylene production technique is reclaimed.The invention is characterized in and in the propylene circulation and recovery process, adopt high pressure propylene washing tower bottoms material, the propylene that the propylene that promptly contains the polypropylene powder that washes the on a small quantity raw material propylene before advancing reactor and circulation after boosting are reclaimed directly is sent to reactor as the polyreaction charging, carries out polyreaction.Rather than with flash of steam, separation, loop compression, the washing again of bottoms material.Therefore reduce the propylene treatment capacity in working cyclees such as the degassing of this workshop section, washing, compression and flash distillation, reduced the operating load of a series of equipment in the propylene circulation removal process and the energy consumption that phase transformation brings thereof.
In the above-described propylene circulation recovery method of the present invention, with high pressure propylene washing tower bottoms material, by the mashing pump supercharging, raw material propylene before advancing reactor and circulation are reclaimed the propylene obtain and are delivered to reactor, make propylene that the propylene that contains a small amount of polypropylene powder of discharging at the bottom of the high pressure propylene washing tower tower and raw material propylene and circulation recovery obtain jointly as the polyreaction charging.In order to make the reactor feed amount stable, can in this process, carry out corresponding flow control.
Being provided with between above mashing pump entrance end of setting up and the exit end refluxes regulates, stable to guarantee discharging.Mashing pump can be set to two, an operation, and one is standby.Between two mashing pumps the interlocking self-starting is set, realizing two automatic switchovers between mashing pump, and participates in the interlocking that stops in emergency of reactor.If mashing pump is out of service, the automatic closing volume variable valve of interlocking system meeting is scurried into reactor to prevent material from reflux pipeline.
Propylene in the high pressure propylene washing tower bottoms material is a state of saturation, and gas-liquid phase transition takes place when it enters mashing pump easily, can bring infringement to mashing pump.For fear of this problem, need be with high pressure propylene washing tower frame height, or to entering the bottoms material cooling before the mashing pump.Generally select bottoms material refrigerative method, the type of cooling can adopt method commonly used in the chemical field, as jacket pipe, interchanger etc.
In addition, the original little flash lines that is connected with high pressure scrubber still can keep as standby.
The positively effect of this technology is: generally on the low side for present China polypropylene plant ability, demand capacity expansion revamping urgently, adopt above-mentioned improvement flow process, the major equipment of the propylene degassing, washing, compression section remains unchanged in the time of can making the polypropylene plant enlarging, save investment, cut down the consumption of energy, shorten construction period, and keep good quality of product.Also can adopt above-mentioned flow process for new device, can not establish little flash lines, and can strengthen at the bottom of the high pressure scrubber tower logistics capacity to reactor, to reduce the load of tower bottom reboiler and overhead condenser, reduce the phase variable of circulation propylene tolerance and propylene, the major equipment treatment capacity of washing, compression process is reduced, thereby reduce investment and energy consumption.
Description of drawings
Accompanying drawing 1 is the polypropylene degassing and propylene circulation and recovery process schematic flow sheet.The present technique invention mainly is that details are as follows in its technical process to the improvement that polymkeric substance outgases and propylene circulates, reclaims technique unit:
Discharge a large amount of polypropylene and liquid monomer from polymerization workshop section annular-pipe reactor, through the sudden strain of a muscle with steam jacket Steam pipeline 1 heating and make the propylene liguid vaporization, enter in the flash tank 2, make the further flash distillation of propylene in this step-down Vaporization, and make polypropylene and propylene steam monomer separation, under material level control, solid is discharged from pot bottom, Enter bag hose 4. Gas is discharged from flash tank 2 tops, is installed in the dynamic separator 3 on flash tank 2 tops, Can prevent from carrying secretly in the exit flow a large amount of solids. Exhaust Gas enters high pressure propylene washing tower 10, in this tower The small polypropylene powder of carrying secretly in the gas phase is isolated in washing. Tower bottom reboiler 11 is used for keeping the operation in the tower Temperature. Two strands of tower overhead gas flow points, one enters blowback gas tank 8, is used for back-blowing bag filter 4; Another stock-traders' know-how is followed After 9 condensations of cyclopropylene cooler, by propylene circulating pump 14 a condensate liquid part is returned tower as phegma In, another part is delivered in the propylene feed tank 13. Propylene in the propylene feed tank 13 passes through propylene feed again Pump 12 is sent into polymerization workshop section.
The polypropylene powder of discharging from flash tank 2 bottoms enters the bag filter 4, makes polypropylene powder at this The propylene of carrying secretly in the material under low pressure further separates. The bottom polypropylene powder is arranged under material level control continuously Go out, and the antioxidant that adds is delivered in the decatize tank of next workshop section.
The propylene steam of discharging from bag hose 4 tops enters the low pressure propylene after propylene protection filter 5 filters In the scrubbing tower 6, with the entrained little power of oil wash gas. Top gas is laggard through cat head cooler 7 The propylene compressor 17 that enters to circulate is discharged propylene gas with flash tank 2 after compression and is sent into the cycle of higher pressure propylene Scrubbing tower 10 circulations are reclaimed. Materials at bottom of tower in the low pressure propylene washing tower 6 is by in reflux pump 19 backflows and the tower Material constantly mixes. The part waste oil of discharging at the bottom of low pressure propylene washing tower 6 towers is by scavenge oil pump 18 fed downstream workers The waste oil disposal tank of section.
In the circulation of the degassed and propylene of above-mentioned polymer, reclaim in the technique unit, for preventing the high pressure propylene washing tower Bottom polypropylene material deposition, former technology be with materials at bottom of tower after little flash lines 15 vaporizations, return continuously Deliver in bag filter 3 feeding lines, shown in the circuit that is represented by dotted lines in the accompanying drawing. This technology pair Above-mentioned polymer is degassed and propylene circulates, being improved to of technology of recovery has high pressure propylene washing tower 10 tower tail bands The propylene of the polypropylene powder that washes is after cooling, by mashing pump 16 superchargings, with the raw material that advances before the reactor Propylene and circulation are reclaimed the propylene obtain and are delivered to together reactor, make this propylene material and raw material propylene and follow Loopback is received propylene jointly as the polymerisation charging. In order to make the reactor feed amount stable, can be in this process Carry out corresponding flow-control. The propylene mashing pump 16 band interlocking self-startings of setting up. Can arrange simultaneously one standby Use mashing pump. Mashing pump 16 can be set to two, one open one standby. Interlocking is set from opening between two mashing pumps Moving, realizing two automatic switchovers between mashing pump, and participate in the interlocking that stops in emergency of reactor. If slurry Pump is out of service, between interlock system meeting autoshutdown mashing pump 16 entrance points and the port of export on the reflux line Return valve. Scurry into reactor to prevent material from backflow official line.
In addition, original little flash lines still can keep as for subsequent use.
In the propylene circulation recovery method of the present invention, saved with high pressure propylene washing tower materials at bottom of tower again Flash of steam has reduced by bag hose 4 tops to low pressure propylene washing tower 6, enters the circulation propylene from cat head again Compressor 17 is delivered to high pressure propylene washing tower 10 and then a series of to low pressure propylene washing tower 6 etc. after the compression Propylene treating capacity in the cyclic process all can descend the machine utilization of said process. The equipment that it is related Have: high pressure propylene washing tower 10 (comprising tower bottom reboiler 11, overhead condenser 9), Propylene feed pump 12, Bag hose 4, low pressure propylene washing tower 6 (comprising overhead condenser 7, reflux pump 19), the compression of circulation propylene Machine 17 etc.
Embodiment
To produce 70000 tons polypropylene plant per year is example; if this improvement technology of employing; that propylene recycle compressor load descends is about 40%, low pressure propylene washing tower, bag filter, propylene protection strainer gas phase load all descend about 40%; high pressure propylene washing tower load descends about 10%; propylene feed pump load descends about 5%; this workshop section is except that flash tank, and the miscellaneous equipment load also slightly descends.
Claims (4)
1. the circulation recovery method of propylene during a polypropylene is produced, comprise that a large amount of polypropylene that will discharge from polymerization workshop section and liquid monomer send into flash tank [2] and make the propylene flash of steam, and at this with polypropylene and propylene steam monomer separation, isolated polypropylene enters bag filter [4] and carries out gas solid separation again, isolated propylene steam is through low pressure propylene washing tower [6] washing, high pressure propylene washing tower [10] washing is sent in the lump with the isolated propylene steam of flash tank [2] in circulation propylene compressor [17] compression back, propylene monomer after the washing is sent into polymerization workshop section again and is carried out polymerization, realize the circulation recovery of propylene monomer, it is characterized in that high pressure propylene washing tower [10] bottoms material, promptly contain the propylene that washes polypropylene powder, the propylene that raw material propylene after boosting before advancing reactor and circulation are reclaimed is directly delivered to reactor as the polyreaction charging.
2. the circulation recovery method of propylene during a kind of polypropylene according to claim 1 is produced is delivered to reactor after it is characterized in that high pressure propylene washing tower [10] bottoms material boosted by mashing pump [16].
3. the circulation recovery method of propylene during a kind of polypropylene according to claim 2 is produced, it is characterized in that being provided with one at mashing pump [16] opens one and be equipped with two pumps, the interlocking self-starting is set between the two pumps, in order to realize that two mashing pumps automatically switch, and the interlocking that stops in emergency of participation reactor, if mashing pump is out of service, interlocking system can be closed the return valve on the reflux line between mashing pump [16] entrance end and the exit end automatically.
4. the circulation recovery method of propylene is characterized in that high pressure propylene washing tower [10] bottoms material in producing according to the described a kind of polypropylene of one of claim 1～3, delivers to reactor after cooling off earlier, boosting.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011360356A CN1137906C (en) | 2001-09-29 | 2001-09-29 | Cyclic recovery method of propylene in production of polypropylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011360356A CN1137906C (en) | 2001-09-29 | 2001-09-29 | Cyclic recovery method of propylene in production of polypropylene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1410456A true CN1410456A (en) | 2003-04-16 |
| CN1137906C CN1137906C (en) | 2004-02-11 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011360356A Expired - Fee Related CN1137906C (en) | 2001-09-29 | 2001-09-29 | Cyclic recovery method of propylene in production of polypropylene |
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| Country | Link |
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| CN (1) | CN1137906C (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102050900B (en) * | 2009-10-30 | 2012-11-21 | 中国石油化工股份有限公司 | Method for polymer degassing and propylene recycling in polymerization process of polypropylene liquid-phase loop reactor |
| CN101628845B (en) * | 2009-08-11 | 2013-02-13 | 北京帝力伟业科技开发有限公司 | Low pressure gas phase olefin recovery treatment method |
| CN112358560A (en) * | 2020-10-21 | 2021-02-12 | 中国石油化工股份有限公司 | System and method for producing odorless polypropylene granular product |
| WO2021253312A1 (en) * | 2020-06-17 | 2021-12-23 | 南京延长反应技术研究院有限公司 | Enhanced reaction system and method for preparing polypropylene by means of slurry process |
-
2001
- 2001-09-29 CN CNB011360356A patent/CN1137906C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101628845B (en) * | 2009-08-11 | 2013-02-13 | 北京帝力伟业科技开发有限公司 | Low pressure gas phase olefin recovery treatment method |
| CN102050900B (en) * | 2009-10-30 | 2012-11-21 | 中国石油化工股份有限公司 | Method for polymer degassing and propylene recycling in polymerization process of polypropylene liquid-phase loop reactor |
| WO2021253312A1 (en) * | 2020-06-17 | 2021-12-23 | 南京延长反应技术研究院有限公司 | Enhanced reaction system and method for preparing polypropylene by means of slurry process |
| CN112358560A (en) * | 2020-10-21 | 2021-02-12 | 中国石油化工股份有限公司 | System and method for producing odorless polypropylene granular product |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1137906C (en) | 2004-02-11 |
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