CN207685181U - The paradigmatic system of impact polypropylene - Google Patents
The paradigmatic system of impact polypropylene Download PDFInfo
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- CN207685181U CN207685181U CN201721493319.8U CN201721493319U CN207685181U CN 207685181 U CN207685181 U CN 207685181U CN 201721493319 U CN201721493319 U CN 201721493319U CN 207685181 U CN207685181 U CN 207685181U
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- -1 polypropylene Polymers 0.000 title claims abstract description 101
- 239000004743 Polypropylene Substances 0.000 title claims abstract description 98
- 229920001155 polypropylene Polymers 0.000 title claims abstract description 98
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 433
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 431
- 239000007791 liquid phase Substances 0.000 claims abstract description 147
- 238000006116 polymerization reaction Methods 0.000 claims abstract description 85
- 239000007788 liquid Substances 0.000 claims abstract description 80
- 238000012685 gas phase polymerization Methods 0.000 claims abstract description 69
- 239000002002 slurry Substances 0.000 claims abstract description 60
- 238000007334 copolymerization reaction Methods 0.000 claims abstract description 59
- 230000006835 compression Effects 0.000 claims abstract description 24
- 238000007906 compression Methods 0.000 claims abstract description 24
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000005977 Ethylene Substances 0.000 claims abstract description 17
- 229920001730 Moisture cure polyurethane Polymers 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 141
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 83
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 83
- 239000004571 lime Substances 0.000 claims description 83
- 239000012071 phase Substances 0.000 claims description 63
- 239000001257 hydrogen Substances 0.000 claims description 41
- 229910052739 hydrogen Inorganic materials 0.000 claims description 41
- 239000003054 catalyst Substances 0.000 claims description 35
- 238000006243 chemical reaction Methods 0.000 claims description 34
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 33
- 239000000463 material Substances 0.000 claims description 28
- 150000001336 alkenes Chemical class 0.000 claims description 23
- 238000000926 separation method Methods 0.000 claims description 20
- 238000001816 cooling Methods 0.000 claims description 16
- 239000007787 solid Substances 0.000 claims description 16
- 238000004064 recycling Methods 0.000 claims description 15
- 239000012190 activator Substances 0.000 claims description 10
- 238000004581 coalescence Methods 0.000 claims description 9
- 230000001351 cycling effect Effects 0.000 claims description 9
- 230000008859 change Effects 0.000 claims description 5
- 238000005265 energy consumption Methods 0.000 abstract description 19
- 239000002685 polymerization catalyst Substances 0.000 abstract description 11
- 239000000047 product Substances 0.000 description 57
- 238000000034 method Methods 0.000 description 44
- 230000008569 process Effects 0.000 description 27
- 238000012662 bulk polymerization Methods 0.000 description 25
- 238000011084 recovery Methods 0.000 description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 19
- 238000005406 washing Methods 0.000 description 18
- 239000000843 powder Substances 0.000 description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- 239000002994 raw material Substances 0.000 description 14
- 238000009834 vaporization Methods 0.000 description 13
- 230000008016 vaporization Effects 0.000 description 13
- 238000004519 manufacturing process Methods 0.000 description 12
- 238000006356 dehydrogenation reaction Methods 0.000 description 11
- 238000007872 degassing Methods 0.000 description 10
- 150000002431 hydrogen Chemical class 0.000 description 9
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 8
- 230000008901 benefit Effects 0.000 description 8
- 229920001971 elastomer Polymers 0.000 description 8
- 239000000806 elastomer Substances 0.000 description 8
- SJJCABYOVIHNPZ-UHFFFAOYSA-N cyclohexyl-dimethoxy-methylsilane Chemical compound CO[Si](C)(OC)C1CCCCC1 SJJCABYOVIHNPZ-UHFFFAOYSA-N 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 229920000642 polymer Polymers 0.000 description 7
- 238000003756 stirring Methods 0.000 description 7
- VOITXYVAKOUIBA-UHFFFAOYSA-N triethylaluminium Chemical compound CC[Al](CC)CC VOITXYVAKOUIBA-UHFFFAOYSA-N 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 5
- 238000006073 displacement reaction Methods 0.000 description 5
- 238000001035 drying Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 238000012805 post-processing Methods 0.000 description 4
- 239000001294 propane Substances 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 238000010574 gas phase reaction Methods 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
- 230000008018 melting Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000000178 monomer Substances 0.000 description 3
- 229920005629 polypropylene homopolymer Polymers 0.000 description 3
- 230000035939 shock Effects 0.000 description 3
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 2
- 125000005234 alkyl aluminium group Chemical group 0.000 description 2
- 239000002216 antistatic agent Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 229920001577 copolymer Polymers 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 230000002779 inactivation Effects 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 229920000058 polyacrylate Polymers 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 238000002207 thermal evaporation Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- OQOGEOLRYAOSKO-UHFFFAOYSA-N 1,1-dichloro-1-nitroethane Chemical compound CC(Cl)(Cl)[N+]([O-])=O OQOGEOLRYAOSKO-UHFFFAOYSA-N 0.000 description 1
- 206010024769 Local reaction Diseases 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 125000003342 alkenyl group Chemical group 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- 238000012661 block copolymerization Methods 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 125000000113 cyclohexyl group Chemical group [H]C1([H])C([H])([H])C([H])([H])C([H])(*)C([H])([H])C1([H])[H] 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- YQGOWXYZDLJBFL-UHFFFAOYSA-N dimethoxysilane Chemical compound CO[SiH2]OC YQGOWXYZDLJBFL-UHFFFAOYSA-N 0.000 description 1
- 239000004815 dispersion polymer Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 229920001038 ethylene copolymer Polymers 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000003306 harvesting Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 238000009439 industrial construction Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 230000000116 mitigating effect Effects 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000036314 physical performance Effects 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
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- 238000000746 purification Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Abstract
The utility model is related to impact polypropylene fields, disclose the paradigmatic system of impact polypropylene, including：Prepolymerization unit (A), liquid phase polymerization unit (B), gas-phase polymerization unit (C) and the copolymerization units (D) being sequentially connected to；Prepolymerization unit (A) includes the propylene surge tank being sequentially connected to, propylene compression pump and prepolymerization kettle (201), by the first propylene from propylene surge tank, through propylene compression pump boil down to liquid propylene, polymerization catalyst is carried again without condensing unit and is all passed through prepolymerization kettle (201) and carries out Propylene Pre-polymerization, is obtained containing propylene pre-polymer raw slurry；Raw slurry is carried out liquid phase polymerization, gas-phase polymerization successively and is copolymerized with ethylene, the second propylene by liquid phase polymerization unit (B), gas-phase polymerization unit (C) and copolymerization units (D), obtains impact polypropylene.The system reduces impact polypropylene energy consumption of unit product and propylene loss.
Description
Technical field
The utility model is related to impact polypropylenes to industrialize field, and in particular, to one kind is resisted with three-stage technique
Rush polyacrylic paradigmatic system.
Background technology
Polypropylene is using propylene as polymer made of monomer polymerization, is a very important kind in general-purpose plastics,
Its with abundant raw material, it is cheap, be easily worked the characteristics such as molding, nontoxic, can also pass through the measures such as copolymerization, blending, enhancing
It is modified, it is to be only second to the second largest plastics of polyethylene in vistanex to have very wide application field.But
Polyacrylic shock resistance is not so good, needs to improve to improve shock resistance.
Producing polyacrylic technology both at home and abroad at present mainly has：Liquid phase noumenal method, gas phase substance law and liquid-phase bulk
The polymerization being in series with gas phase ontology.According to the difference of reactor types, and endless tube method (Spheripol), gas can be divided into
Phase fluidized bed process (Unipol), vertical stirred tank method (Novolen, Hypol), horizontal agitated vessel method (Inoes, JPP) and difference
The combined method of reaction kettle.
In polypropylene production process, propylene monomer is polymerizeing under the action of major catalyst, activator, electron donor
Polymerisation is carried out in reactor obtains polypropylene slurry or solid material.The polypropylene of generation is using flash liberation, catalyst
Inactivation, the displacement of dry and nitrogen, obtain polypropylene powder product.In the propylene gas that reactor discharging is carried secretly in the process, pass through
Reaction system recycling is returned to after low pressure washing, gas compression, the separation of light gas, to reduce disappearing for raw material propylene and hydrogen
Consumption.
Current domestic and international polymarization method for prodcing polyacrylates, each own different advantage and disadvantage：
Batch process bulk technique：By the propylene polymerization process of domestic independent development, advantage have flow it is short, investment
Low, quick, disadvantage is that process energy consumption is high, the degree of automation is low, unstable product quality, monomer consumption are big.
The Spheripol techniques of Lyondell Basell：Ring canal reaction kettle, using axial-flow pump forced circulation, liquid-phase bulk
Polymerization, the chuck outside endless tube remove heat.Its advantage is that reaction condition is relatively easy to control, reactor heat transfer coefficient is big, unit volume production
Rate is high, properties of product are stablized, and the covering of trade mark range is wide, and band gas-phase reactor can produce high-impact copolymerized product.
The Unipol techniques of Grace：Gas-phase fluidized-bed reactor, heat of polymerization are taken away by the sensible heat of gas, gas circulation amount
Greatly, need powerful booster fan that could realize, it is less uniform for mixed type, product quality entirely in reaction kettle.Its advantage has suitable
It closes ethylene and propylene is copolymerized, flow is simple, the covering of product good physical performance, the trade mark is wide, the second gas-phase reactor of band can produce height
Crushing-resistant copolymerization product.
The Innovene techniques of INEOS companies：Using Horizontal stirring reactor and high performance INcat CDi catalyst,
The reactor removes heat close to plug flow reactor, using liquid propylene vaporization.Its advantage has reactor to remove, and the thermal efficiency is high, produces
Smooth operation, residence time of material section is uniform in the reaction phase, and the product melting means range of production is wide, energy consumption is relatively low.
The Hypol techniques of Mitsui：Liquid-phase bulk and gas phase ontology group technology produce polypropylene, the first two reaction kettle
For vertical stirred tank, latter two is vertical gas fluidised bed polymerisation kettle；Its advantage can produce random copolymerization and block copolymerization product；
Its disadvantage long flow path, device efficiency are low, gas phase reaction is complete mixed type, product quality is uneven, catalyst adaptability is poor, device
Small scale；The Hypol process units without on newly domestic in recent years.
SPG techniques：Liquid-phase bulk and gas phase ontology group technology, gas phase kettle be Horizontal band stirred tank, advantage be flow it is short,
It invests that low, low energy consumption, but high-impact copolymerized product can not be produced.
But during above-mentioned polytechnic industrializing implementation, in the presence of producing, polyacrylic specific energy consumption is high to be lacked
Fall into, also so that influence subsequently may extend other reaction, influence polymeric articles quality and stability and device operation
Safety, increase the industrialized investment of project, influence the economic benefit of project.
Utility model content
Purpose of the utility model is to solve how improving polypropylene to obtain erosion-resisting characteristics, and reduce polypropylene production
The specific energy consumption of process improves the quality and stability of product and the safety of device operation, reduces asking for the loss of propylene
Topic, proposes the paradigmatic system of impact polypropylene.The system is taken including Propylene Pre-polymerization, liquid phase bulk propylene polymerization, propylene gas
Four sections of continuous polymerization devices of phase bulk polymerization and polypropylene and the copolymerization of ethylene, propylene, the mitigation that propylene may be implemented are pre-
Polymerization reduces catalyst amount, meets the requirement of acrylic polymers product, reduces the unit energy during entire process industryization is implemented
Consumption and propylene loss, improve the economy of propylene industrialized production.And polypropylene and ethylene are copolymerized, are copolymerized
Object can have compared to the better shock resistance of polypropylene.
To achieve the goals above, the utility model provides a kind of paradigmatic system of impact polypropylene, which includes：
Prepolymerization unit A, liquid phase polymerization unit B, gas-phase polymerization unit C and the copolymerization units D being sequentially connected to；
Prepolymerization unit A includes the propylene surge tank, propylene compression pump and prepolymerization kettle 201 being sequentially connected to, and will come from propylene
First propylene of surge tank through propylene compression pump boil down to liquid propylene, then carries major catalyst, activator and electron donor,
It is passed through prepolymerization kettle 201 without condensing unit and carries out Propylene Pre-polymerization, obtains the raw slurry containing propylene pre-polymer；
Liquid phase polymerization unit B carries out liquid propylene homopolymerization for the raw slurry, obtains liquid phase polymerization product；
Gas-phase polymerization unit C carries out gas-phase polymerization for the liquid phase polymerization product, obtains containing polyacrylic product；
Copolymerization units D is used to the polypropylene isolated containing polyacrylic product and ethylene, the second propylene being total to
Poly- reaction, obtains impact polypropylene.
Preferably, propylene surge tank is arranged the propylene that one is connected to propylene compression pump 2 and exports, and first in propylene surge tank
Propylene is passed through prepolymerization kettle 201 merely through propylene compression pump.
Preferably, the propylene compression pump in prepolymerization unit A and it is not provided with propylene condensing unit between prepolymerization kettle 201.
Preferably, propylene compression pump is directly connected to prepolymerization kettle 201 by pipeline 100, and main reminder is respectively set on pipeline 100
The addition mouth of agent, activator and electron donor.
Preferably, liquid phase polymerization unit B includes slurry line 101, liquid phase polymerizer 202 and propylene vaporization-reuse unit；
Slurry line 101 is connected to prepolymerization kettle 201 and liquid phase polymerizer 202, and reclaim liquid phase propylene entrance is provided in slurry line 101
With recycling circulating hydrogen entrance；Propylene vaporization-reuse unit is connected to liquid phase polymerizer 202, and being used for will be in liquid phase polymerizer 202
The propylene gas that liquid propylene vaporization changes into is condensed and is recycled back to liquid phase polymerizer 202.
Preferably, the propylene vaporization-reuse unit include the first propylene condenser 211, the first lime set knockout drum 212,
First circulation wind turbine 213, and it is connected to the pipeloop 102 of the first lime set knockout drum 212 and first circulation wind turbine 213；First
Propylene condenser 211 is connected to liquid phase polymerizer 202 and the first lime set knockout drum 212, for release liquid phase polymerizer 202
Part propylene air cooling coalescence is sent into the first lime set knockout drum 212 and carries out gas-liquid separation, and the liquid propylene rework solution isolated is met
Close kettle 202；First circulation wind turbine 213 is connected to the first lime set knockout drum 212 and liquid phase polymerizer 202, is used for lime set knockout drum
212 propylene gas isolated return to liquid phase polymerizer 202.
Preferably, gas-phase polymerization unit C includes polypropylene slurry line 103, gas-phase polymerization reactor 203 and propylene cycle
Unit；
Polypropylene slurry line 103 is connected to liquid phase polymerizer 202 and gas-phase polymerization reactor 203, in polypropylene slurry pipe
Control valve is set on line 103；
Propylene cycling element is connected to gas-phase polymerization reactor 203, and third for releasing gas-phase polymerization reactor 203
Alkene returns to propylene gas-phase polymerization.
Preferably, the propylene cycling element includes gas phase kettle propylene condenser 214,215 and of gas phase kettle propylene cooler
First propylene lime set pump 216；Concatenated gas phase kettle propylene condenser 214 is connected to gas-phase polymerization with gas phase kettle propylene cooler 215
Reactor 203 and the first propylene lime set pump 216, the part propylene air cooling coalescence for releasing gas-phase polymerization reactor 203
It sends gas-phase polymerization reactor 203 back to and carries out propylene gas-phase polymerization.
Preferably, copolymerization units D includes copolymerization kettle 204, the second propylene condenser 219, the second lime set knockout drum 220, the
Two propylene lime sets pump 221 and second circulation wind turbine 222；Second propylene condenser 219 connection copolymerization kettle 204 and the separation of the second lime set
Tank 220 is sent into the second lime set knockout drum 220 progress gas-liquid point for that will be copolymerized the part propylene air cooling coalescence that kettle 204 releases
From；Second propylene lime set pump, 221 connection copolymerization kettle 204 and the second lime set knockout drum 220, are used for the second lime set knockout drum 220
The propylene condensate liquid isolated returns to the top of copolymerization kettle 204；The connection of second circulation wind turbine 222 copolymerization kettle 204 and the second lime set
Knockout drum 220, the cycle propylene gas for isolating the second lime set knockout drum 220 return to the bottom of copolymerization kettle 204；Wherein,
Ethylene feed and the second propylene feed mouth are set on the second lime set knockout drum 220；It is connected to the second lime set knockout drum 220 and second
Hydrogen inlet is set on the pipeline of circulating fan 222.
Preferably, which further includes being connected to the gas-solid separator 217 and gas lock of gas-phase polymerization unit C and copolymerization units D
218, gas lock 218 is used to prevent the material of copolymerization units D from influencing polymerized unit C.
Through the above technical solutions, the utility model provides a kind of system for impact polypropylene industrialized production.
Liquid phase prepolymerization is taken to close when polymerizeing homopolypropylene in the system, three sections that liquid-phase bulk polymerization and gas phase bulk polymerization are combined
Paradigmatic system.It is combined by three stage polymerization so that this system can integrally improve Propylene Pre-polymerization, specifically, be not required in system
Want condensing propylene to the condensing unit of sub-zero temperature, Propylene Pre-polymerization can be carried out at 40~45 DEG C, 3.2~3.9MPaG, phase
It is more milder than 5~10 DEG C of the condition in the prior art.Polymerization catalyst can be taken primary all from prepolymerization addition, nothing
It needs the prior art to fill catalyst in batches, the addition mouth of setting polymerization catalyst is reduced in system.
Further more, system provided by the utility model, carry out propylene homo the first propylene can with boil down to liquid propylene into
The primary charging of row, all participates in Propylene Pre-polymerization, obtains the raw slurry with the propylene pre-polymer more preferably disperseed.In system only
There is pipeline 100 to be connected to propylene compression pump and prepolymerization kettle 201, liquid phase, the gas of subsequent coupling can also be conducive to by simplifying system setting
The homogeneous reaction of phase-polymerization improves the quality of polymeric articles.
Entire technical process no longer needs to setting fresh propylene also by unreacted propylene gas recycling in technical process
Supplement entrance.
Whole system provided by the utility model can reduce the energy consumption and propylene damage of unit impact polypropylene product
Consumption.After measured, using system provided by the utility model, unit of the product energy consumption can be less than 62kg and mark oil/ton impact polypropylene,
Minimum reachable 57kg marks oil/ton impact polypropylene, and unit product processing cost is about the same as scale same type imported technology product
1/2。
In addition the system is avoided that in force the case where hot spot and implode occurs in reaction part, is reduced product and is moulded
Change the probability of block, product particle is non-breakable.Polymerisation removes heat, propylene circulation and stress amount by the way of liquid propylene vaporization
Small, system is not necessarily to large-scale recycle unit, can effectively reduce system investments, the construction period is short, and economy is more preferable.
The system of the utility model can be used for obtaining impact polypropylene, and containing elastomer components, content reaches as high as 46
Weight % can improve polyacrylic toughness, not easily broken under low temperature (- 23 DEG C), and the Notched Charpy impact intensity of measurement is high.
And general homopolypropylene does not contain elastomer components, rigidity is strong, and brittleness is big, poor toughness.
Description of the drawings
Fig. 1 is the process flow diagram of the production impact polypropylene of the utility model.
Reference sign
201- prepolymerization kettle 202- liquid phase polymerizer 203- gas-phase polymerization reactors
204- is copolymerized kettle 211- the first propylene condenser 212- the first lime set knockout drums
213- first circulation wind turbine 214- gas phase kettle propylene condenser 215- gas phase kettle propylene coolers
216- the first propylene lime sets pump 217- gas-solid separator 218- gas locks
219- the second propylene condenser 220- the second lime set knockout drum 221- the second propylene lime sets pump
222- second circulation wind turbine 100- pipeline 101- stock lines
102- pipeloop 103- polypropylene slurry lines
Specific implementation mode
The endpoint of disclosed range and any value are not limited to the accurate range or value herein, these ranges or
Value should be understood as comprising the value close to these ranges or value.For numberical range, between the endpoint value of each range, respectively
It can be combined with each other between the endpoint value of a range and individual point value, and individually between point value and obtain one or more
New numberical range, these numberical ranges should be considered as specific open herein.
The utility model provides a kind of paradigmatic system of impact polypropylene, as shown in Figure 1, the system includes：
Prepolymerization unit A, liquid phase polymerization unit B, gas-phase polymerization unit C and the copolymerization units D being sequentially connected to；
Prepolymerization unit A includes the propylene surge tank, propylene compression pump and prepolymerization kettle 201 being sequentially connected to, and will come from propylene
First propylene of surge tank through propylene compression pump boil down to liquid propylene, then carries major catalyst, activator and electron donor,
It is passed through prepolymerization kettle 201 without condensing unit and carries out Propylene Pre-polymerization, obtains the raw slurry containing propylene pre-polymer；
Liquid phase polymerization unit B carries out liquid propylene homopolymerization for the raw slurry, obtains liquid phase polymerization product；
Gas-phase polymerization unit C carries out gas-phase polymerization for the liquid phase polymerization product, obtains containing polyacrylic product；
Copolymerization units D is used to the polypropylene isolated containing polyacrylic product and ethylene, the second propylene being total to
Poly- reaction, obtains impact polypropylene.
In the utility model, the prepolymerization unit A, liquid phase polymerization unit B and the gas-phase polymerization unit C that are sequentially connected to are used for third
Polyamino alkenyl.Liquid phase prepolymerization, liquid-phase bulk polymerization and the combined three stage polymerization system of gas phase bulk polymerization are taken, can be allowed pre-
Propylene feed in polymerized unit A before prepolymerization reactor 3 is improved.Preferably, a connection propylene is arranged in propylene surge tank
The propylene of compression pump exports, and the first propylene in propylene surge tank is passed through prepolymerization kettle 201 merely through propylene compression pump.I.e. with it is existing
Technology only part propylene raw material carries out prepolymerization, and another part is fed directly to the liquid phase or gas-phase polymerization in downstream without prepolymerization
Difference, system provided by the utility model may be implemented propylene feedstocks all by prepolymerization, reduce control operation, and make alkene
Polymerization catalyst system preferably disperses in propylene feedstocks.
In the utility model, further, take three stage polymerization system that can reduce the requirement of prepolymerization condition.It is preferred that
Ground is not provided with propylene condensing unit between the propylene compression pump and prepolymerization kettle 201 in prepolymerization unit A.Preferably, liquid propylene
Pressure is 4~4.5MPaG, and liquid propylene temperature is 40~45 DEG C.System provided by the utility model can allow propylene liquid phase
Prepolymerization carries out at 40~45 DEG C, the low temperature prepolymerization generally carried out at 5~10 DEG C or so higher than the prior art.It can reduce
Condensing steps simultaneously reduce corresponding energy consumption and operation needs.
It in the utility model, can simply be connected between propylene compression pump and prepolymerization kettle 201, reduce industrial construction expense.
Preferably, propylene compression pump is directly connected to prepolymerization kettle 201 by pipeline 100, and olefinic polymerization catalysis is respectively set on pipeline 100
The addition mouth of agent, activator and electron donor.
In the utility model, it can be gone successively to through the raw slurry containing propylene pre-polymer that prepolymerization unit A is obtained
Further polymerization reaches the industrial polymeric articles needed to improve for liquid phase polymerization and the concatenated polymerization process of gas-phase polymerization.It is preferred that
Ground, liquid phase polymerization unit B include slurry line 101, liquid phase polymerizer 202 and propylene vaporization-reuse unit；Slurry line 101
It is connected to prepolymerization kettle 201 and liquid phase polymerizer 202, reclaim liquid phase propylene entrance is provided in slurry line 101 and recycling recycles
Hydrogen inlet；Propylene vaporization-reuse unit is connected to liquid phase polymerizer 202, is used for liquid propylene vapour in liquid phase polymerizer 202
Change the propylene gas changed into be condensed and be recycled back to liquid phase polymerizer 202.
In the utility model, liquid phase polymerizer 202 can select vertical stirred autoclave, with cycle water leg.Paddle
The stirring of leaf makes reaction evenly, while the heat transfer between strength imparting material, prevents local reaction from overheating and luming.It is in polymeric kettle
Gas-liquid two-phase coexists, and is not necessarily to powerful hybrid control device, and equipment production intensity is big, and reaction operating mode is easy to control.According to life
It produces product or scale is different, polymeric kettle can also be arranged more parallel connections, system production capacity can be adjusted flexibly, also can be according to owner
It is required that the polypropylene product of production multimodal.
In the utility model, liquid phase polymerization unit B, which can be taken, utilizes the liquid propylene vaporization in liquid phase polymerizer 202
Mode helps to remove the heat that propylene polymerization releases, while the propylene vaporized can pass through the propylene vaporization-reuse
Unit recycles, and yield can be reduced compared with prior art, to reduce the industrialization investment of recycle unit.Preferably, institute
It states propylene vaporization-reuse unit and includes the first propylene condenser 211, the first lime set knockout drum 212, first circulation wind turbine 213, with
And the pipeloop 102 of connection the first lime set knockout drum 212 and first circulation wind turbine 213；First propylene condenser 211 is connected to liquid
Phase-polymerization kettle 202 and the first lime set knockout drum 212, the part propylene air cooling coalescence for releasing liquid phase polymerizer 202 are sent
Enter the first lime set knockout drum 212 and carry out gas-liquid separation, the liquid propylene isolated returns to liquid phase polymerizer 202；First circulation wind
Machine 213 is connected to the first lime set knockout drum 212 and liquid phase polymerizer 202, the propylene gas for isolating lime set knockout drum 212 return
Return liquid phase polymerizer 202.In the propylene vaporization-reuse unit, it can will be directly condensed out with the first propylene condenser 211
Liquid propylene returns to liquid phase polymerizer 202.The part propylene gas that liquid phase polymerizer 202 releases can be sent directly into the first lime set
Knockout drum 212 participates in gas-liquid separation.
In the utility model, can propylene homo further be continued by the gas-phase polymerization unit C of the system.It is preferred that
Ground, gas-phase polymerization unit C include polypropylene slurry line 103, gas-phase polymerization reactor 203 and propylene cycling element；Polypropylene
Slurry line 103 is connected to liquid phase polymerizer 202 and gas-phase polymerization reactor 203, is arranged in polypropylene slurry line 103 and adjusts
Valve；Propylene cycling element is connected to gas-phase polymerization reactor 203, the propylene for releasing gas-phase polymerization reactor 203
Return to propylene gas-phase polymerization.
In the utility model, gas-phase polymerization reactor 203 can be selected the horizontal reactor of belt stirrer, material in reactor
It is big, adaptable to the slightly tacky material such as high melting means and copolymer that residence time is uniformly, equipment produces intensity；Blender can be with
Using "ON" type structure, powder is made to be uniformly mixed.Gas-phase polymerization reactor 203 has chuck recirculated water to realize that reaction heat is removed.Gas
Radioactivity level-sensing device is also set up in phase polymerization reaction device 203 or by electric current come the material position of control material.Gas-phase polymerization reactor
203 can be arranged wise temperature automatic control system, can be divided into 6~8 temperature control areas according to reactor scale.Blender has simultaneously
The function of having stirring and powder product is pushed to move forward, specific paddle angle have according to reaction kettle scale and residence time
Institute is different.
In the utility model, the propylene cycling element can recycle the unreacted that gas-phase polymerization reactor 203 releases
Propylene, and partially recycled propylene can be returned with gas phase and be used to help stirring in gas-phase polymerization reactor 203.
Preferably, the propylene cycling element includes gas phase kettle propylene condenser 214, gas phase kettle propylene cooler 215 and the first propylene
Lime set pump 216；Concatenated gas phase kettle propylene condenser 214 is connected to gas-phase polymerization reactor 203 with gas phase kettle propylene cooler 215
With the first propylene lime set pump 216, the part propylene air cooling coalescence for releasing gas-phase polymerization reactor 203 is sent gas phase back to and is gathered
It closes reactor 203 and carries out propylene gas-phase polymerization.
In the utility model, copolymerization units D includes copolymerization kettle 204, the second propylene condenser 219, the second lime set knockout drum
220, the second propylene lime set pump 221 and second circulation wind turbine 222；Second propylene condenser 219 connection copolymerization kettle 204 and second is solidifying
Liquid knockout drum 220 is carried out for that will be copolymerized part propylene air cooling coalescence the second lime set knockout drum 220 of feeding that kettle 204 releases
Gas-liquid separation；Second propylene lime set pump, 221 connection copolymerization kettle 204 and the second lime set knockout drum 220, for detaching the second lime set
The propylene condensate liquid that tank 220 is isolated returns to the top of copolymerization kettle 204；The connection copolymerization kettle 204 and second of second circulation wind turbine 222
Lime set knockout drum 220, the cycle propylene gas for isolating the second lime set knockout drum 220 return to the bottom of copolymerization kettle 204；Its
In, ethylene feed and the second propylene feed mouth are set on the second lime set knockout drum 220；It is connected to 220 He of the second lime set knockout drum
Hydrogen inlet is set on the pipeline of second circulation wind turbine 222.
In the utility model, it is preferable that the system further includes being connected to the gas-solid point of gas-phase polymerization unit C and copolymerization units D
From device 217 and gas lock 218, gas lock 218 is used to prevent the material of copolymerization units D from influencing polymerized unit C.
In the utility model, it is preferable that the system further includes post-processing unit E, and post-processing unit E is connected to gas-phase polymerization list
First C, copolymerization units D and gas-solid separator 217 pass through returning in slurry line 101 again after the propylene gas purification for that will recycle
It receives liquid propylene entrance and is passed through liquid phase polymerizer 4, while recycling the upper fresh hydrogen of hydrogen mixing, by slurry line 101
Recycling circulating hydrogen entrance is passed through liquid phase polymerizer 202；And copolymerization units D is obtained into copolymerization product and carries out gas solid separation, it obtains
Impact polypropylene.
Specifically, post-processing unit E includes drying device and gas separating and reclaiming device.
The drying device includes：Inside carries the degassing cabin of cyclone separator and bag filter, is provided with deactivator
With the drier of filter, the displacement kettle that is connected with nitrogen heater and water sealed tank, with water scrubber condenser and washing pump
Water scrubber and propylene recovery compressor.
Wherein, degassing cabin will be from the copolyreaction product (containing propylene gas, hydrogen, impact polypropylene) for being copolymerized kettle 204
Gas solid separation is carried out, the propylene gas isolated is passed through the gas separating and reclaiming device, and the polymer powders isolated are passed through mistake
Device living；
Degassing is dried in deactivated polymer powder from deactivator by drier, and the gas of abjection is passed through through filter
Gas is passed through displacement kettle through water scrubber, dry polymer powders；
The polymer powders of the drying are subjected to the hot nitrogen that nitrogen heater provides by displacement kettle, deviate from trace amount gas
Final impact polypropylene is obtained afterwards；The propylene gas of abjection high altitude discharge after water sealed tank, spark arrester；
Gas is passed through propylene recovery compressor after the washing of the gas of water scrubber inherent filtration in future device, then can directly return
It receives propylene and is used for other processes.
The gas separating and reclaiming device includes：The oil scrubber that is pumped with oil scrubber condenser and oil wash carries reboiler
High pressure propylene washing tower, dehydrogenation tower and propylene condensate pipe.
Wherein, the propylene that oil scrubber will come from gas-phase polymerization reactor 203, copolymerization kettle 204 and degassing cabin 15 are isolated
The impurity such as the alkyl aluminum and oligomer of gas washing removing entrainment, may be used the white oil containing antistatic agent as cleaning solvent.
In the utility model, oil scrubber is connected to high pressure third by propylene gas surge tank, the propylene air compressor being sequentially communicated
Alkene scrubbing tower will be sent into high pressure propylene washing tower by the gas of white oil washing.Portion can also be added in high pressure propylene washing tower
The unreacted propylene gas for dividing gas-phase polymerization reactor 203 to be discharged.High pressure propylene washing tower bottom of tower can be used for it with discharge part
The Propylene recovery of his process.
In the utility model, dehydrogenation tower is connected to the tower top of high pressure propylene washing tower, and tower top fixed gas is isolated hydrogen rich gas
With propylene lime set.Dehydrogenation tower by the Propylene recovery condenser that is sequentially communicated, circulating hydrogen surge tank, circulating hydrogen compressor and
Hydrogen gas buffer is connected with the recycling circulating hydrogen entrance in slurry line 101, and the hydrogen rich gas is mixed upper fresh hydrogen
It is passed through liquid phase polymerizer 202 as circulating hydrogen.The setting connection of propylene lime set tank is below dehydrogenation tower, for containing described third
Alkene lime set.Propylene lime set tank pumps the recycling in connection slurry line 101 by Propylene recovery lime set and recycles propylene entrance, and being used for will
The propylene lime set returns to liquid phase polymerizer 202 as recycling cycle propylene.
Course of work combination Fig. 1 of the paradigmatic system of impact polypropylene provided by the utility model makees further specifically
It is bright.
(A) it stocks up
It is up to the first propylene that polymerization requires and enters propylene surge tank, then exported from unique propylene of propylene surge tank
Propylene is conveyed and is forced into 4~4.5MPaG into propylene compression pump and liquefies to obtain the liquid propylene that temperature is 40~45 DEG C.Liquid phase
Propylene is conveyed by pipeline 100 into prepolymerization kettle 201, meanwhile, major catalyst, activator and electron donor pass through on pipeline 100
Respective addition mouth is mixed into liquid propylene, and prepolymerization kettle 201 is entered under the carrying of liquid propylene.
Because Propylene Pre-polymerization of the present invention is mutually tied with liquid phase bulk propylene polymerization, the bulk polymerization of propylene gas phase during this
It closes, the prepolymerization condition used can make propylene feedstocks be not necessarily to frozen cooling, and can all feed pre- into propylene is crossed
The whole preparation process of polymerization, final impact polypropylene reduces energy consumption and propylene loss.
(B) paradigmatic system
(1) Propylene Pre-polymerization：In prepolymerization kettle 201, effect of the liquid propylene in major catalyst, activator and electron donor
Lower progress Propylene Pre-polymerization reaction.Prepolymerization kettle 201 carry blender, reaction temperature be 40~45 DEG C, reaction pressure be 3.2~
3.9MPaG, reaction time are about 4~5min, and propylene polymerization multiple is about 50~100 times.
Prepolymerization kettle is fed：Major catalyst (Ti catalyst) is about 0.02~0.05 weight %, the activator (three of liquid propylene
Aluminium ethide) be about 0.2~0.4 weight %, the electron donor (Cyclohexyl Methyl Dimethoxysilane) of liquid propylene it is about liquid phase
0.04~0.06 weight % of propylene.
(2) liquid phase propylene polymerization
Raw slurry containing propylene pre-polymer is obtained by prepolymerization kettle 201, reclaim liquid phase third is mixed into through slurry line 101
Alkene, hydrogen become liquid phase polymerization raw material, polyacrylic a concentration of 150~300g/L in liquid phase polymerization raw material；Reclaim liquid phase propylene
Addition be liquid propylene 25~30 weight %；Relative to the 1000kg polypropylene in liquid phase polymerization raw material, hydrogen adds
It is 0.04~0.3kg to enter amount.Liquid phase polymerizer 202 is the vertical reactor with stirring.
Liquid phase polymerization raw material enters liquid phase polymerizer 202 and carries out propylene liquid phase homopolymerization.Propylene liquid phase homopolymerization temperature be 65~
70 DEG C, propylene liquid phase homopolymerization pressure is 3~3.8MPaG, residence time about 40min.Liquid phase polymerization raw material in liquid phase polymerizer 202
Level control liquid phase polymerizer 202 45~57 volume %.The reaction heat of liquid phase homopolymerization can pass through the vapour of liquid propylene
Change and chuck recirculated water is taken away, wherein the part propylene gas after vaporization is after the cooling of the first propylene condenser 211, part is straight
It connects and returns to liquid phase polymerizer 202, enter the first lime set after partly being mixed with uncooled propylene gas (coming from liquid phase polymerizer 202)
Knockout drum 212, the propylene lime set through isolating return in liquid phase polymerizer 202；The gas phase isolated is passed through through pipeloop 102
It is communicated to first circulation wind turbine 213, returns and is bubbled in the liquid phase of liquid phase polymerizer 202, on the one hand can make gas and reaction liquid phase
It is uniformly mixed, so that gas is reduced the liquidus temperature among polymeric kettle, the pressure of liquid phase polymerizer 202 is also by outer circulation
The amount of cooling system controls；
(3) propylene gas-phase polymerization
The polypropylene slurries (containing propylene and polypropylene) being discharged from liquid phase polymerizer 202 are by pressure difference by carrying valve
Polypropylene slurry line 103 enter gas-phase polymerization reactor 203, wherein carrying unreacted propylene secretly and continuing polymerisation and be
Polypropylene；Gas-phase polymerization temperature is 70~85 DEG C, and reaction pressure is 2.6~2.8MPaG, and polypropylene slurries are in gas phase polymerization
Residence time in device 203 is about 45~60min, obtains containing polyacrylic product.
The material position of material can be controlled by radioactivity level-sensing device or electric current in gas-phase polymerization reactor 203, material position one
As control in 35~60 volume %.Gas-phase polymerization reactor 203 can be selected the horizontal reactor of belt stirrer, object in reactor
Expect that the residence time is uniform, equipment production intensity is big, adaptable to the slightly tacky material such as high melting means and copolymer；Agitating paddle can
To use "ON" type structure, powder is made to be uniformly mixed.Polymerization reaction heat in gas-phase polymerization reactor 203 can be swashed by propylene
The vaporization of cold liquid and chuck recirculated water are taken away；Unreacted propylene gas is heavy by the settling section on 203 top of gas-phase polymerization reactor
After dropping part powder, a part of gas is distributed by adjusting to Propylene Recovery System, and another part gas passes through gas phase kettle third
Alkene condenser 214 and gas phase kettle propylene cooler 215 are returned by the first propylene lime set pump 216 to gas phase polymerization after cooling down
Device 203 reabsorbs polymerisation thermal evaporation and withdraws reaction heat.Gas-phase polymerization reactor 203 may be used wise temperature and control automatically
System processed can be divided into 6~8 temperature control areas according to reactor scale.Blender has stirring and pushes powder product forward simultaneously
Mobile function, specific paddle angle are different according to reaction kettle scale and residence time.
(4) gas solid separation
From what gas-phase polymerization reactor 203 was discharged gas-solid separator 217, unreacted propylene are passed through containing polyacrylic product
Gas discharge is passed through Propylene Recovery System.The polypropylene material isolated also carries non-deactivated polymerization catalyst, enters gas together
Lock 218.Gas lock 218 is for preventing the material reflux in follow-up copolyreaction into the propylene homo process of front.Gas solid separation exists
Pressure is to be carried out under 2~3MPaG.
(5) impact polypropylene copolyreaction
By the polypropylene material from gas lock 218 be passed through copolymerization kettle 204 in ethylene, the second propylene, at 65~80 DEG C
Copolyreaction is carried out under the copolymerization pressure of copolymerization temperature and 2~2.4MPaG, the copolyreaction time is 30~60min.Copolyreaction
Polymerization reaction heat can be taken away by the vaporization and chuck recirculated water of propylene Quench liquid.A unreacted propylene gas part is divided
It send to Propylene Recovery System, another part gas enters the second lime set knockout drum after the cooling of the second propylene condenser 219
220, and the ethylene and the second propylene for participating in copolyreaction are mixed into the second lime set knockout drum 220, the addition of ethylene is liquid
8~15 weight % of phase propylene, the addition of the second propylene are 15~20 weight % of liquid propylene.Second lime set knockout drum
The 220 cycle propylene gas isolated, which can mix, takes fresh hydrogen, and the bottom of copolymerization kettle 204 is returned to through second circulation wind turbine 222
Copolymerization material is stirred in portion, help.It returns to gas-phase polymerization reactor 203, reabsorbs polymerisation thermal evaporation and withdraw reaction heat.The
The propylene condensate liquid that two lime set knockout drums 220 are isolated mixes and pumps 221 through the second propylene lime set with ethylene, propylene, from copolymerization kettle
204 top feed.
(C) post-processing of copolyreaction product
(first) gas solid separation：Copolyreaction product from copolymerization kettle 204 (is contained into propylene gas, hydrogen, anti-impact poly- third
Alkene) rely on pressure to enter degassing cabin through exporting powder control valve.
Setting cyclone separator and bag filter inside degassing cabin, to separate and recover the dust in propylene gas；Degassing
The polymer powders that storehouse separates, to deactivator, are passed through suitable steam to the product by gravity fall in deactivator
The catalyst of interior entrainment is inactivated, and the powder inactivated enters drier and degassing, further Propylene recovery is dried.
Drier is a horizontal indirectly heat blade stirring drier, and hollow hot axis and external jacket are passed through low pressure steaming
Gas is thermally dried wet mash by wall, while wet stock can also be moved to material outlet, drier operation by agitating shaft
Temperature is 100~105 DEG C, and pressure is micro-positive pressure.
(second) harvests polymeric articles：Powder after inactivation, drying falls on displacement kettle by gravity under drier, is replacing
The hot nitrogen provided with nitrogen heater in kettle is further backing out the denier propylene gas carried secretly in powder；The gas of exclusion passes through
High-altitude qualified discharge after water sealed tank, spark arrester；Powder after degassing is sent by nitrogen supply air system to follow-up workshop section, is obtained
Final impact polypropylene product.
(the third) Propylene Recovery System：Wet mash in drier is heated into the propylene gas released through the filter on drier
Enter water scrubber after filtering to wash.Water scrubber is used as washing medium using desalted water, and entrained catalyst decomposition is atomic in gas
Hydrogen chloride is measured, therefore the hydrochloric acid in appropriate alkaline liquor and in water is added in desalted water.Propylene gas after washing is through water scrubber cooler
It after cooling, then is recycled after the pressurization of propylene recovery compressor, can be used for sending outside.
The propylene gas that degassing cabin is isolated and the propylene gas of gas-phase propene homopolymerization discharge, the propylene gas one of copolyreaction discharge
And it is buffered after enter oil scrubber washing, through propylene gas compressor compresses enter high pressure propylene washing tower separating heavy again；From
The propylene gas that high pressure propylene washing tower tower top is isolated enters back into dehydrogenation tower removing hydrogen rich gas, and it is recovered to isolate hydrogen rich gas from tower
The liquid propylene that propylene condenser condensation separation obtains returns to dehydrogenation tower, hydrogen rich gas and the fresh hydrogen after metering as phegma
After mixing, send to liquid phase polymerizer 202 and utilize after the pressurization of circulating hydrogen compressor；Dehydrogenation tower bottom of tower lime set is into propylene lime set tank
Then buffering is used Propylene recovery lime set pump pressurization rear portion to return to liquid phase polymerizer 202 and is utilized, a part is used as high pressure propylene
The overhead reflux liquid of scrubbing tower；Leave propylene (about 19 weight of propane content for containing a large amount of propane in high pressure propylene washing tower bottom of tower
Amount %) after filtering with propylene recovery compressor pressurization aqueous propylene mix after send out battery limit (BL) handle.
Wherein, oil scrubber is the plate column of a top tape washing oil tower condenser, inside it with containing the white of antistatic agent
Oil washs propylene gas, to deviate from the impurity such as the alkyl aluminum carried secretly in propylene gas and oligomer.High pressure propylene is washed
It is the sieve plate distillation column that a bottom carries reboiler to wash tower, phegma is done with the propylene lime set of propylene lime set tank, to detach
Propane in propylene, propane is accumulated in anti-locking system；Dehydrogenation tower is the concatenated sieve-plate tower after high pressure propylene washing tower, with recycling
The lime set body of propylene condenser contains to detach in propylene gas as the propylene in the phegma cooling dehydrogenation tower of dehydrogenation tower
Hydrogen rich gas, dehydrogenation tower bottom is direct-connected logical with propylene lime set tank, and propylene lime set tank is entered directly into after the liquid condensing that flows back.
The utility model will be described in detail by embodiment below.
Impact polypropylene measures Notched Charpy impact intensity by GB/T 1043.1-2008, is surveyed by heptane extraction process
Determine elastomer content.
Embodiment 1
According to flow shown in FIG. 1：
(1) prepolymerization
First propylene is pressurizeed and to obtain that pressure is about 4.2MPaG, temperature is 42 DEG C of liquid propylene；Using liquid propylene as load
Body is separately added into the triethyl aluminum that the content in liquid propylene is the Ti catalyst (CS-1) of 0.04 weight %, 0.3 weight %
With the Cyclohexyl Methyl Dimethoxysilane of 0.05 weight %；So all it is directly inputted in prepolymerization kettle and forms polymeric size, connects
It and carries out Propylene Pre-polymerization under the conditions of 42 DEG C, 3.2MPaG, residence time 4min, it is polyacrylic poly- in obtained raw slurry
It is 75 times to close multiple；
(2) liquid-phase bulk polymerization
Reclaim liquid phase propylene is added in the raw slurry that (1) obtains and hydrogen blendes together liquid phase polymerization raw material (wherein polypropylene
A concentration of 200g/L, reclaim liquid phase propylene addition is about 25 weight % of liquid propylene, added hydrogen 0.08kg/
1000kg polypropylene), propylene liquid phase homopolymerization is carried out at 68 DEG C, 3MPaG, material position is 45 volume % in reaction kettle, is stopped
40min；
In propylene liquid phase homopolymerization process, partially polymerized reaction heat is taken away in the vaporization of Partial Liquid Phase propylene.The propylene gas of vaporization passes through
Recycling returns to propylene liquid phase homopolymerization with gas phase or liquid phase.
(3) gas phase bulk polymerization
The polypropylene slurries that (2) are obtained are added in gas phase bulk polymerization device, and third is carried out at 90 DEG C, 2.6MPaG
Alkene gas-phase homopolymerization, residence time 45min, material position is 55 volume % in reactor.
In propylene gas phase homopolymerization process, the unreacted propylene gas in part of discharge is recovered, and third is returned with gas phase or liquid phase
Alkene gas-phase homopolymerization.
(4) gas solid separation is carried out containing polyacrylic product by what (3) obtained, obtained polypropylene is liquid propylene with dosage
The ethylene of 15 weight %, the second propylene that dosage is 18 weight % of liquid propylene in being copolymerized kettle, at 65 DEG C, 2.4MPaG into
Row copolyreaction, residence time 45min, obtains copolymerization product.
(5) copolymerization product is dried, obtains impact polypropylene.
Propylene recovery and hydrogen, which return, is used for liquid-phase bulk polymerization.
It calculates in above-mentioned entire technical process, the specific energy consumption for producing impact polypropylene is that 62kg marks oil/ton anti-impact poly- third
Alkene.1000kg impact polypropylenes are produced, propylene loss is 4kg.
Impact polypropylene carries out performance evaluating, and elastomer content is 46 weight % or more.The toughness of impact polypropylene is big, surveys
Determine Notched Charpy impact intensity not to be broken at 23 DEG C and -23 DEG C.
Embodiment 2
According to flow shown in FIG. 1：
(1) prepolymerization
First propylene is pressurizeed and to obtain that pressure is about 4MPaG, temperature is 45 DEG C of liquid propylene；Using liquid propylene as load
Body is separately added into the triethyl aluminum that the content in liquid propylene is the Ti catalyst (CS-1) of 0.06 weight %, 0.2 weight %
With the Cyclohexyl Methyl Dimethoxysilane of 0.06 weight %；Then all it is directly inputted in prepolymerization kettle and forms polymeric size,
Then Propylene Pre-polymerization is carried out under the conditions of 45 DEG C, 3.6MPaG, residence time 4min, it is polyacrylic in obtained raw slurry
It is 50 times to polymerize multiple；
(2) liquid-phase bulk polymerization
It is (wherein polyacrylic dense that raw slurry addition Propylene recovery and hydrogen that (1) obtains are blended together into liquid phase polymerization raw material
Degree is 150g/L, and Propylene recovery addition is about 27 weight % of liquid propylene, and added hydrogen is 0.12kg/1000kg poly- third
Alkene), propylene liquid phase homopolymerization is carried out at 70 DEG C, 3.5MPaG, material position is 60 volume % in reaction kettle, stops 35min；
In propylene liquid phase homopolymerization process, partially polymerized reaction heat is taken away in the vaporization of Partial Liquid Phase propylene.The propylene gas of vaporization passes through
Recycling returns to propylene liquid phase homopolymerization with gas phase or liquid phase.
(3) gas phase bulk polymerization
The polypropylene slurries that (2) are obtained are added in gas phase bulk polymerization device, and third is carried out at 65 DEG C, 2.7MPaG
Alkene gas-phase homopolymerization, residence time 60min, material position is 45 volume % in reactor.
In propylene gas phase homopolymerization process, the unreacted propylene gas in part of discharge is recovered, and third is returned with gas phase or liquid phase
Alkene gas-phase homopolymerization.
(4) gas solid separation is carried out containing polyacrylic product by what (3) obtained, obtained polypropylene is liquid propylene with dosage
The ethylene of 10 weight %, the second propylene that dosage is 20 weight % of liquid propylene in being copolymerized kettle, at 80 DEG C, 2.2MPaG into
Row copolyreaction, residence time 60min, obtains copolymerization product.
(5) copolymerization product is dried, obtains impact polypropylene.
Propylene recovery and hydrogen, continue on for liquid-phase bulk polymerization.
It calculates in above-mentioned entire technical process, the specific energy consumption for producing impact polypropylene is that 59kg marks oil/ton anti-impact poly- third
Alkene.1000kg impact polypropylenes are produced, propylene loss is 5kg.
Impact polypropylene carries out performance evaluating, and Notched Charpy impact intensity is 62 (kJ/m2, 23 DEG C), 6.4 (kJ/m2,-
23 DEG C), elastomer content is 21.6 weight %.
Embodiment 3
According to flow shown in FIG. 1：
(1) prepolymerization
First propylene is pressurizeed and to obtain that pressure is about 4.5MPaG, temperature is 40 DEG C of liquid propylene；Using liquid propylene as load
Body is separately added into the triethyl aluminum that the content in liquid propylene is the Ti catalyst (CS-1) of 0.05 weight %, 0.4 weight %
With the Cyclohexyl Methyl Dimethoxysilane of 0.04 weight %；Then all it is directly inputted in prepolymerization kettle and forms polymeric size,
Then Propylene Pre-polymerization is carried out under the conditions of 40 DEG C, 3.8MPaG, residence time 5min, it is polyacrylic in obtained raw slurry
It is 100 times to polymerize multiple；
(2) liquid-phase bulk polymerization
It is (wherein polyacrylic dense that raw slurry addition Propylene recovery and hydrogen that (1) obtains are blended together into liquid phase polymerization raw material
Degree is 300g/L, and Propylene recovery addition is about 30 weight % of liquid propylene, and added hydrogen is 0.2kg/1000kg poly- third
Alkene), propylene liquid phase homopolymerization is carried out at 69 DEG C, 3.7MPaG, material position is 40 volume % in reaction kettle, stops 45min；
In propylene liquid phase homopolymerization process, partially polymerized reaction heat is taken away in the vaporization of Partial Liquid Phase propylene.The propylene gas of vaporization passes through
Recycling returns to propylene liquid phase homopolymerization with gas phase or liquid phase.
(3) gas phase bulk polymerization
The polypropylene slurries that (2) are obtained are added in gas phase bulk polymerization device, and third is carried out at 70 DEG C, 2.8MPaG
Alkene gas-phase homopolymerization, residence time 48min, material position is 50 volume % in reactor.
In propylene gas phase homopolymerization process, the unreacted propylene gas in part of discharge is recovered, and third is returned with gas phase or liquid phase
Alkene gas-phase homopolymerization.
(4) gas solid separation is carried out containing polyacrylic product by what (3) obtained, obtained polypropylene is liquid propylene with dosage
The ethylene of 8 weight %, the second propylene that dosage is 15 weight % of liquid propylene carry out in being copolymerized kettle at 70 DEG C, 2.0MPaG
Copolyreaction, residence time 30min, obtains copolymerization product.
(5) copolymerization product is dried, obtains impact polypropylene.
Propylene recovery and hydrogen, continue on for liquid-phase bulk polymerization.
It calculates in above-mentioned entire technical process, the specific energy consumption for producing impact polypropylene is that 57kg marks oil/ton anti-impact poly- third
Alkene.1000kg impact polypropylenes are produced, propylene loss is 5kg.
Impact polypropylene carries out performance evaluating, and Notched Charpy impact intensity is 36 (kJ/m2, 23 DEG C), 4.4 (kJ/m2,-
23 DEG C), elastomer content is 15.8 weight %.
Comparative example 1
(1) prepolymerization
Take -5 DEG C, 50 weight % of the liquid propylene of 3.81MPaG mixed with polymerization catalyst, contain in polymerization catalyst
The Ti catalyst (CS-1) of the 0.08 weight % on the basis of whole liquid propylenes, the triethyl aluminum and 0.08 weight of 0.5 weight %
The Cyclohexyl Methyl Dimethoxysilane of % to be measured, is added in pre-polymerization endless tube and carries out low temperature prepolymerization, prepolymerization temperature is about 10 DEG C,
Pre-polymerization resultant pressure is about 3.8MPaG, residence time 12min, and polyacrylic polymerization multiple is about 60 in obtained raw slurry
Times；
(2) liquid-phase bulk polymerization
By raw material slurry and remaining 50 weight % liquid propylenes, (0.08kg/ is added in polyacrylic a concentration of 50 weight %
The polyacrylic hydrogen of 1000kg) it is mixed into liquid phase polymerization raw material, subsequently into the first annular-pipe reactor, in liquid phase polymerization raw material
A part of propylene polymerize, and remaining liquid makes the material in reactor be in paste-like as the diluent of polymer, passes through
Axial-flow pump beats cycle, keeps slurry flow at high speed in the reactor and is uniformly mixed；
The slurry in the first annular-pipe reactor is continuously sent into the second annular-pipe reactor by the industrial siding that discharges again and is continued
It carries out liquid phase polymerization and supplements fresh propylene (addition is 25 weight % of liquid propylene).First and second annular-pipe reactor reacts
Temperature is about 70~73 DEG C, and reaction pressure is about 3.8MPaG, residence time about 1h.
(3) and ethylene copolymer
The polymerisation slurry of second annular-pipe reactor discharge is subjected to gas solid separation, obtained polypropylene is liquid phase third with dosage
The ethylene of 8 weight % of alkene, the second propylene that dosage is 15 weight % of liquid propylene in being copolymerized kettle, at 70 DEG C, 2.0MPaG into
Row copolyreaction, residence time 30min, obtains copolymerization product.
Copolymerization product is dried, impact polypropylene is obtained.
Propylene recovery and hydrogen, continue on for liquid-phase bulk polymerization.
By calculating above-mentioned loop po lymerisation process, the specific energy consumption for producing impact polypropylene is about 70kg mark oil/ton anti-impacts
Polypropylene.1000kg impact polypropylenes are produced, propylene loss is 5kg.
Impact polypropylene carries out performance evaluating, and Notched Charpy impact intensity is 38 (kJ/m2, 23 DEG C), 4.4 (kJ/m2,-
23 DEG C), elastomer content is 14.8 weight %.
Above-mentioned annular-pipe reactor and technique be at present both at home and abroad use more propene polymerization reactor and technique, although
Impact polypropylene can be prepared, but heat is removed due to annular-pipe reactor and all realizes that slurry is in endless tube by chuck recirculated water
Flowing is realized by axial-flow pump promotion, and polypropylene slurry is liquid phase flash distillation discharging, must increase steam-heating system, further increase
The energy consumption of the technological reaction process is added.
Comparative example 2
Propylene pressurization is reached 3.5MPa and condensed to liquid phase after -5 DEG C and is entered in the poly- kettle of prepolymerization, with polymerization catalyst
(including Ti catalyst (CS-1), triethyl aluminum, Cyclohexyl Methyl Dimethoxysilane) is contacted at 0 DEG C, and catalyst components exist
Content in liquid propylene is the triethyl aluminum and 0.08 weight % of the Ti catalyst (CS-1) of 0.08 weight %, 0.5 weight %
Cyclohexyl Methyl Dimethoxysilane, be used in combination blender to pinch material mixing, herein generate catalyst activated centre, then open
The pre-polymerization of beginning propylene, prepolymerized residence time are 5min, and polyacrylic polymerization multiple is 75 times in obtained raw slurry.
What prepolymerization obtained enters containing active catalyst and propylene mixtures slurry in liquid phase polymerizer, 69 DEG C,
1~1.6h is stopped under 3.4MPa, and the reaction was continued.A concentration of 130g/L of polypropylene, propylene total amount are 10t/h in slurry, hydrogen is added
Amount is 150L/min.Material position is 45 volume % in liquid phase reactor kettle.
Polymerization catalyst is also added in liquid phase polymerization：Ti catalyst (CS-1) 0.4g/h, triethyl aluminum 3L/h, cyclohexyl first
Base dimethoxysilane 0.4L/h.
The slurry of liquid phase polymerizer discharge enters gas phase reaction kettle, and gas phase bulk polymerization is carried out at 90 DEG C, 2.8MPa, is stopped
Stay the time for 1.5h, material position is 40 volume % in gas phase reaction kettle.
After completing propylene gas-phase homopolymerization, the obtained product containing Noblen carries out gas solid separation, obtained polypropylene
With the ethylene that dosage is 8 weight % of liquid propylene, the second propylene that dosage is 15 weight % of liquid propylene in being copolymerized kettle, 70
DEG C, carry out copolyreaction under 2.0MPaG, residence time 30min obtains copolymerization product.
Copolymerization product is dried, impact polypropylene is obtained.
Propylene recovery and hydrogen, continue on for liquid-phase bulk polymerization.
It calculates in above-mentioned entire technical process, the specific energy consumption for producing impact polypropylene is that 65kg marks oil/ton anti-impact poly- third
Alkene.1000kg impact polypropylenes are produced, propylene loss is 6kg.
Impact polypropylene carries out performance evaluating, and Notched Charpy impact intensity is 36 (kJ/m2, 23 DEG C), 4.4 (kJ/m2,-
23 DEG C), elastomer content is 15.8 weight %.
Method provided by the invention is can be seen that by Propylene Pre-polymerization, third by the result of above-described embodiment and comparative example
Alkene liquid-phase bulk polymerization and propylene gas phase bulk polymerization are combined the polymerization for carrying out homopolypropylene, may not need propylene condensation letter
Change technological process.Liquid propylene all participates in prepolymerization, and reduces the addition of major catalyst, obtains propylene pre-polymer dispersion more
Good raw slurry is conducive to improve product quality.Propylene Pre-polymerization carries out under 40~45 DEG C of mild temperature, may finally
Reduce specific energy consumption and the propylene loss of entire production impact polypropylene.
Need propylene to condense to subzero in comparative example 1, and can only Partial Liquid Phase propylene carry out low temperature prepolymerization；Polymerization process
In need to add fresh propylene and polymerization catalyst, product needs flash distillation process, whole although impact polypropylene can also be prepared
Propylene polymerization energy consumption of unit product and the propylene loss of a technical process are high.
In comparative example 2, the prior art needs propylene to condense to subzero, and prepolymerization temperature is low, and catalyst charge is high,
Polymerization catalyst is also added, although impact polypropylene can also be prepared, completes the propylene polymerization list of entire technical process
Position product energy consumption and propylene loss are high.
Preferred embodiments of the present invention, still, the utility model and unlimited are described in detail above in association with attached drawing
In this.In the range of the technology design of the utility model, a variety of simple variants can be carried out to the technical solution of the utility model,
It is combined with any other suitable method including each technical characteristic, these simple variants and combination equally should be considered as this
Utility model disclosure of that, belongs to the scope of protection of the utility model.
Claims (10)
1. a kind of paradigmatic system of impact polypropylene, which is characterized in that the system includes：
Prepolymerization unit (A), liquid phase polymerization unit (B), gas-phase polymerization unit (C) and the copolymerization units (D) being sequentially connected to；
Prepolymerization unit (A) includes the propylene surge tank being sequentially connected to, propylene compression pump and prepolymerization kettle (201), will come from propylene
First propylene of surge tank through propylene compression pump boil down to liquid propylene, then carries major catalyst, activator and electron donor,
It is passed through prepolymerization kettle (201) without condensing unit and carries out Propylene Pre-polymerization, obtains the raw slurry containing propylene pre-polymer；
Liquid phase polymerization unit (B) carries out liquid propylene homopolymerization for the raw slurry, obtains liquid phase polymerization product；
Gas-phase polymerization unit (C) carries out gas-phase polymerization for the liquid phase polymerization product, obtains containing polyacrylic product；
Copolymerization units (D) are for the polypropylene isolated containing polyacrylic product and ethylene, the second propylene to be copolymerized
Reaction, obtains impact polypropylene.
2. system according to claim 1, which is characterized in that the third of a connection propylene compression pump is arranged in propylene surge tank
Alkene exports, and the first propylene in propylene surge tank is passed through prepolymerization kettle (201) merely through propylene compression pump.
3. system according to claim 1 or 2, which is characterized in that the propylene compression pump in prepolymerization unit (A) and pre-polymerization
Kettle is not provided with propylene condensing unit between (201).
4. system according to claim 3, which is characterized in that propylene compression pump and prepolymerization kettle (201) pass through pipeline (100)
It is directly connected to, the addition mouth of major catalyst, activator and electron donor is respectively set on pipeline (100).
5. system according to claim 1, which is characterized in that liquid phase polymerization unit (B) includes slurry line (101), liquid
Phase-polymerization kettle (202) and propylene vaporization-reuse unit；
Slurry line (101) is connected to prepolymerization kettle (201) and liquid phase polymerizer (202), and recycling is provided in slurry line (101)
Liquid propylene entrance and recycling circulating hydrogen entrance；
Propylene vaporization-reuse unit is connected to liquid phase polymerizer (202), is used for liquid propylene vapour in liquid phase polymerizer (202)
Change the propylene gas changed into be condensed and be recycled back to liquid phase polymerizer (202).
6. system according to claim 5, which is characterized in that the propylene vaporization-reuse unit includes that the first propylene is cold
Condenser (211), the first lime set knockout drum (212), first circulation wind turbine (213), and connection the first lime set knockout drum (212) and
The pipeloop (102) of first circulation wind turbine (213)；
First propylene condenser (211) is connected to liquid phase polymerizer (202) and the first lime set knockout drum (212), for gathering liquid phase
It closes the part propylene air cooling coalescence that kettle (202) releases and is sent into the progress gas-liquid separation of the first lime set knockout drum (212), isolate
Liquid propylene returns to liquid phase polymerizer (202)；
First circulation wind turbine (213) is connected to the first lime set knockout drum (212) and liquid phase polymerizer (202), is used for the first lime set
The propylene gas that knockout drum (212) is isolated returns to liquid phase polymerizer (202).
7. system according to claim 1, which is characterized in that gas-phase polymerization unit (C) includes polypropylene slurry line
(103), gas-phase polymerization reactor (203) and propylene cycling element；
Polypropylene slurry line (103) is connected to liquid phase polymerizer (202) and gas-phase polymerization reactor (203), in polypropylene slurries
Control valve is arranged on (103) in pipeline；
Propylene cycling element is connected to gas-phase polymerization reactor (203), and third for releasing gas-phase polymerization reactor (203)
Alkene returns to propylene gas-phase polymerization.
8. system according to claim 7, which is characterized in that the propylene cycling element includes gas phase kettle propylene condenser
(214), gas phase kettle propylene cooler (215) and the first propylene lime set pump (216)；
Concatenated gas phase kettle propylene condenser (214) is connected to gas-phase polymerization reactor (203) with gas phase kettle propylene cooler (215)
(216) are pumped with the first propylene lime set, for sending the part propylene air cooling coalescence that gas-phase polymerization reactor (203) releases back to gas
Phase polymerization reaction device (203) carries out propylene gas-phase polymerization.
9. system according to claim 1, which is characterized in that copolymerization units (D) include copolymerization kettle (204), the second propylene
Condenser (219), the second lime set knockout drum (220), the second propylene lime set pump (221) and second circulation wind turbine (222)；
Second propylene condenser (219) connection copolymerization kettle (204) and the second lime set knockout drum (220), for kettle (204) will to be copolymerized
The part propylene air cooling coalescence released is sent into the second lime set knockout drum (220) and carries out gas-liquid separation；
Second propylene lime set pumps (221) connection copolymerization kettle (204) and the second lime set knockout drum (220), for dividing the second lime set
From the top that the propylene condensate liquid that tank (220) is isolated returns to copolymerization kettle (204)；
Second circulation wind turbine (222) connection copolymerization kettle (204) and the second lime set knockout drum (220), for detaching the second lime set
The cycle propylene gas that tank (220) is isolated returns to the bottom of copolymerization kettle (204)；
Wherein, ethylene feed and the second propylene feed mouth are set on the second lime set knockout drum (220)；It is connected to the separation of the second lime set
Hydrogen inlet is set on the pipeline of tank (220) and second circulation wind turbine (222).
10. system according to claim 1, which is characterized in that the system further includes connection gas-phase polymerization unit (C) and is total to
The gas-solid separator (217) and gas lock (218) of poly- unit (D), gas lock (218) is for preventing the material of copolymerization units (D) from influencing
Polymerized unit (C).
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111100226A (en) * | 2018-10-25 | 2020-05-05 | 中国石油化工股份有限公司 | Production method capable of adjusting rigidity-toughness balance of impact-resistant polypropylene |
| EP4005669A1 (en) * | 2020-11-25 | 2022-06-01 | Borealis AG | Propylene polymerization plant revamping process |
| EP4006060A1 (en) * | 2020-11-25 | 2022-06-01 | Borealis AG | Propylene polymerization plant and propylene polymerization process |
| CN115558045A (en) * | 2022-09-06 | 2023-01-03 | 金澳科技（湖北）化工有限公司 | Method for preventing implosion in initial polymerization feeding stage |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111100226A (en) * | 2018-10-25 | 2020-05-05 | 中国石油化工股份有限公司 | Production method capable of adjusting rigidity-toughness balance of impact-resistant polypropylene |
| CN111100226B (en) * | 2018-10-25 | 2023-03-28 | 中国石油化工股份有限公司 | Production method capable of adjusting rigidity-toughness balance of impact-resistant polypropylene |
| EP4005669A1 (en) * | 2020-11-25 | 2022-06-01 | Borealis AG | Propylene polymerization plant revamping process |
| EP4006060A1 (en) * | 2020-11-25 | 2022-06-01 | Borealis AG | Propylene polymerization plant and propylene polymerization process |
| WO2022112159A1 (en) * | 2020-11-25 | 2022-06-02 | Borealis Ag | Propylene polymerization plant and propylene polymerization process |
| WO2022112349A1 (en) * | 2020-11-25 | 2022-06-02 | Borealis Ag | Propylene plant revamping process |
| CN115558045A (en) * | 2022-09-06 | 2023-01-03 | 金澳科技（湖北）化工有限公司 | Method for preventing implosion in initial polymerization feeding stage |
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