CN1279064C - Method for stopping or controlling reaction of olefinic polyumerization - Google Patents
Method for stopping or controlling reaction of olefinic polyumerization Download PDFInfo
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- CN1279064C CN1279064C CN 200310117342 CN200310117342A CN1279064C CN 1279064 C CN1279064 C CN 1279064C CN 200310117342 CN200310117342 CN 200310117342 CN 200310117342 A CN200310117342 A CN 200310117342A CN 1279064 C CN1279064 C CN 1279064C
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- 238000000034 method Methods 0.000 title claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 title abstract description 19
- 239000000203 mixture Substances 0.000 claims abstract description 67
- OLBVUFHMDRJKTK-UHFFFAOYSA-N [N].[O] Chemical compound [N].[O] OLBVUFHMDRJKTK-UHFFFAOYSA-N 0.000 claims abstract description 64
- 150000001336 alkenes Chemical class 0.000 claims abstract description 40
- 238000006116 polymerization reaction Methods 0.000 claims abstract description 38
- 238000007334 copolymerization reaction Methods 0.000 claims abstract description 37
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000001301 oxygen Substances 0.000 claims abstract description 35
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 35
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000003054 catalyst Substances 0.000 claims abstract description 8
- 238000000926 separation method Methods 0.000 claims abstract description 6
- 229910001873 dinitrogen Inorganic materials 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 41
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 12
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 12
- 239000010953 base metal Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 6
- 230000007704 transition Effects 0.000 claims description 6
- 239000011954 Ziegler–Natta catalyst Substances 0.000 claims description 4
- 231100000572 poisoning Toxicity 0.000 claims description 3
- 230000000607 poisoning effect Effects 0.000 claims description 3
- 238000012685 gas phase polymerization Methods 0.000 claims 2
- 238000012725 vapour phase polymerization Methods 0.000 claims 2
- 238000004519 manufacturing process Methods 0.000 abstract description 12
- 230000008901 benefit Effects 0.000 abstract description 2
- 239000000178 monomer Substances 0.000 abstract 1
- 229910000831 Steel Inorganic materials 0.000 description 23
- 239000010959 steel Substances 0.000 description 23
- 239000011541 reaction mixture Substances 0.000 description 10
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 239000012071 phase Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 7
- 229920001155 polypropylene Polymers 0.000 description 6
- 230000008859 change Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 229920000098 polyolefin Polymers 0.000 description 5
- 229920013730 reactive polymer Polymers 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 3
- 239000004743 Polypropylene Substances 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 239000012467 final product Substances 0.000 description 3
- 239000008246 gaseous mixture Substances 0.000 description 3
- -1 polypropylene Polymers 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 description 2
- 229920000089 Cyclic olefin copolymer Polymers 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229920001577 copolymer Polymers 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000006772 olefination reaction Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 229920005606 polypropylene copolymer Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
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- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The present invention provides a method for stopping or controlling reaction of olefin polymerization reaction. When oxygen is used as polymerization retarder to stop polymerization reaction, air from an air separation device is mixed with pure nitrogen gas, and an oxygen-nitrogen mixture can be obtained; the oxygen-nitrogen mixture is pressurized by a compressor to be compressed into a pressure vessel; the oxygen-nitrogen mixture pressurized by the compressor is compressed into the pressure vessel to make catalyst poisoned, and accordingly, olefin polymerization reaction is stopped. The present invention also provides a method for controlling olefin polymerization reaction. In the same way, the oxygen-nitrogen mixture obtained by the method of the present invention is added in an olefin copolymerization reactor in order to control the copolymerization speed of olefin and the content of each monomer in copolymerization products. The method of the present invention can make polymerization reaction in the reactor rapidly stopped in emergency; the production rate can be accurately and conveniently controlled, cost is saved, the stable production and the operation safety factor of devices are also improved, and great benefits are brought.
Description
Technical field:
The present invention relates to a kind of method of ending or controlling olefinic polyreaction, relate in particular to and use oxygen to end or control the method for olefinic polyreaction as stopper.
Background technology:
As everyone knows, one or more alkene can carry out polyreaction and obtain olefin homo or multipolymer in the presence of catalyzer, as wanting polymeric olefin gas mixture and catalyzer to send in the Gas-phase reactor by containing, can make the polymerization in Gas-phase reactor of one or more alkene obtain olefin homo or multipolymer, unreacted gaseous mixture leaves behind the reactor to be compressed by the circulation gas pipeline and is recycled in the reactor, in working cycle, gaseous mixture is generally used heat exchanger cooling, so that remove the heat that produces in the polyreaction.In olefinic polymerization, general use can be created in the high activated catalyst of number of polymers, the step that just can avoid removing residual catalyst with such high activated catalyst from polymkeric substance in the short period of time.
Can the productive rate of manufacture of polyolefins device be generally higher, and olefinic polyreaction is more violent, needs stopped reaction immediately in case emergency situation takes place, otherwise can cause alkene implode, caking, therefore, end agent and in time add the key issue that just becomes production.At present, the oxygen-nitrogen mixture body that the manufacture of polyolefins device generally adopts steel cylinder gas to provide and contains low concentration oxygen is ended olefinic polyreaction, and there are the following problems for it:
When 1) in case of emergency needing, need a large amount of oxygen of adding, nitrogen mixed air to come stopped reaction with oxygen termination polyreaction.And provide when ending the gas stopped reaction with steel cylinder oxygen, need a plurality of steel cylinders that the termination gas of capacity just can be provided, this just needs to change steel cylinder, and the replacing steel cylinder needs operator to go to the production scene to change and needs the regular hour, if can not in time change steel cylinder, just timely stopped reaction can make alkene implode, caking like this, needs the cleaning of stopping.
During the oxygen stopped reaction that 2) provides with the steel cylinder form, steel cylinder generally is connected with reactor with pipeline by magnetic valve.When stand-by state, steel cylinder generally is in closing condition.When emergency situation took place, operator need go to the scene to open steel cylinder, and this also needs the time; The adding that can influence oxygen because of the fault and the leakage of reducing valve, magnetic valve so all can cause alkene implode, caking in addition.
In addition, when producing olefin copolymer, need each monomeric content in controlled polymerization speed and the final copolymer, for this reason, need to feed a certain amount of termination gas continuously and suppress activity of such catalysts, as when vapor phase process is produced the impact polypropylene multipolymer, two placed in-line reactors of general employing, in first reactor, add mixed gas and the catalyzer that contains propylene, make propylene polymerization obtain propylene homopolymerization reactive polymer, the propylene homopolymerization reactive polymer that will contain catalyzer is again sent into second reactor, feeds ethene and propylene and contain oxygen to end the content of gas with ethene in controlled polymerization speed of response and the final product in second reactor.At present, the oxygen nitrogen that the manufacture of polyolefins device generally adopts steel cylinder gas to provide and contains low concentration oxygen mixes the reaction of termination gas control alpha-olefinic copolymerization, there are the following problems for it: when producing impact copolymer of propylene, end gas and add the olefin-copolymerization reactor continuously, adding fashionable by steel cylinder with oxygen-nitrogen mixture do termination gas, average per 500 tons of products will consume 12 bottles of gases, this changes steel cylinder between just needing at regular intervals, when steel cylinder pressure descends the switching steel cylinder, can cause the quality product fluctuation in the short period of time because of the fluctuation of oxygen flow, influence quality; And when failing in time to switch steel cylinder, also can influence the quality of product because of a variety of causes.
Summary of the invention:
The object of the present invention is to provide a kind of method of ending olefinic polyreaction.
Another object of the present invention is to provide a kind of method of controlling olefinic polyreaction.
In order to achieve the above object, the invention provides a kind of method of ending olefinic polyreaction, and comprise and obtain oxygen-nitrogen mixture mixing with pure nitrogen gas from air separation facility from the air of air separation facility, after the compressed machine pressurization oxygen-nitrogen mixture is compressed in the pressurized vessel, oxygen-nitrogen mixture with q.s joins in the olefin polymerization reactor rapidly again, so that poisoning of catalyst, thereby end olefinic polyreaction.
The key of termination olefinic polyreaction of the present invention is rapidly a large amount of termination gas to be sent into each position of reactor, so that oxygen-nitrogen mixture whole catalyzer rapid and in the reactor contact, whole catalyzer is poisoned rapidly, thereby end polyreaction.For this reason, at least 2 oxygen-nitrogen mixtures preferably are set on olefin polymerization reactor add inlet, oxygen-nitrogen mixture is added simultaneously at the different positions of reactor, thereby whole catalyzer rapid and in the reactor contact, and reach the purpose of quick termination olefinic polyreaction.Oxygen-nitrogen mixture adds the many more oxygen-nitrogen mixture whole catalyzer rapid and in the reactor that help more of inlet and contacts, but can increase the difficulty that reactor is made, and takes all factors into consideration, and preferably is arranged to 2-10 oxygen-nitrogen mixture and adds inlet on olefin polymerization reactor.
The concentration of oxygen is 2-7% (molar percentage), is preferably 4-5% (molar percentage) in the oxygen-nitrogen mixture of the present invention.If oxygen concentration is too low in the oxygen-nitrogen mixture, just can not end olefinic polyreaction rapidly; If oxygen concentration is too high in the oxygen-nitrogen mixture, can set off an explosion.Therefore, the concentration of oxygen generally is controlled to be 2-7% (molar percentage) in the oxygen-nitrogen mixture.The pressure of the oxygen-nitrogen mixture in the described pressurized vessel should be higher than the pressure of reactor so that oxygen-nitrogen mixture adds rapidly in the reactor, generally is higher than reactor pressure 0.8～1.5Mpa and gets final product.
Catalyzer of the present invention is for being fit to olefinic polymerization and oxygen is ended responsive catalyzer, is preferably transition Base Metal catalyzer, Ziegler-natta catalyst more preferably.
Termination method of the present invention is suitable for ending alkene homopolymerization and/or olefin-copolymerization reaction, particularly equal polymerization of propylene or copolymerization.Be more suitable for being particularly suitable for terminating in equal polymerization of the gas-phase olefin that carries out in the horizontal reactor or copolymerization in ending equal polymerization of gas-phase olefin or copolymerization.
The present invention also provides a kind of method of controlling olefinic polyreaction, comprise to mix with pure nitrogen gas from the air of air separation facility and obtain oxygen-nitrogen mixture, after the pressurization of compressed machine oxygen-nitrogen mixture is compressed in the pressurized vessel and stores, continuously oxygen-nitrogen mixture is joined again in the alpha-olefinic copolymerization reactor, with each monomeric content in control speed of olefin-copolymerization and the copolymerization product.
The key of control olefinic polyreaction of the present invention is an amount of termination gas is sent in the alpha-olefinic copolymerization reactor continuously, so that oxygen-nitrogen mixture contacts with catalyzer in the reactor, make the part poisoning of catalyst, thereby the reaction of control alpha-olefinic copolymerization, and final control obtains each monomeric content in the multipolymer.For this reason, when enforcement is of the present invention, should control the add-on of oxygen-nitrogen mixture as required.The add-on of oxygen is according to the required productive rate of two reactors productive rate of first reactor when, calculates the productive rate of second reactor, thereby determines to add the amount of oxygen again according to speed of reaction.
The present invention preferably is provided with at least one oxygen-nitrogen mixture and adds inlet on the alpha-olefinic copolymerization reactor, more preferably at least 2 oxygen-nitrogen mixtures add inlet, oxygen-nitrogen mixture is added simultaneously at the different positions of reactor, thereby termination gas is contacted with the catalyzer of reactor different positions, reach the purpose of effective control alpha-olefinic copolymerization reaction.Oxygen-nitrogen mixture adds the many more oxygen-nitrogen mixtures that help more of inlet and contacts with the catalyzer of different positions in the reactor, but can increase the difficulty that reactor is made, and takes all factors into consideration, and preferably is arranged to 2～10 oxygen-nitrogen mixtures and adds inlet on olefin polymerization reactor
Oxygen-nitrogen mixture of the present invention preferably mixes the back and adds in the reactor with the circulation gas of copolymerization polymerization reactor.
In the oxygen-nitrogen mixture of the present invention the concentration of oxygen be 2～7% (being to ignite low line concentration in the oxygen reactor) (molar percentages), be preferably 4-5% (molar percentage).If oxygen concentration is too low in the oxygen-nitrogen mixture, just can not end olefinic polyreaction rapidly; If oxygen concentration is too high in the oxygen-nitrogen mixture, can set off an explosion.Therefore, the concentration of oxygen generally is controlled to be 2-7% (molar percentage) in the oxygen-nitrogen mixture.The pressure of the oxygen nitrogen mixing tank in the described pressurized vessel should be higher than the pressure of reactor so that oxygen-nitrogen mixture adds rapidly in the reactor, generally is higher than reactor pressure 0.5～1.5Mpa and gets final product.
Catalyzer of the present invention is for being fit to olefinic polymerization and oxygen is ended responsive catalyzer, is preferably transition Base Metal catalyzer, Ziegler-natta catalyst more preferably.
Method of the present invention is suitable for controlling the reaction of alkene gas phase copolymerization, preferred copolymerization of propylene reaction, is particularly suitable for being controlled at the gas-phase olefin copolymerization that carries out in the horizontal reactor.
Adopt the method for termination olefinic polyreaction of the present invention, when emergency situation takes place, the polyreaction in the reactor is ended rapidly, can not cause alkene implode, caking, can clear up reactor like this and directly resume production.
Adopting the method for termination of the present invention or control olefinic polyreaction mainly to change former useful steel cylinder, oxygen-nitrogen mixture is provided is the nitrogen oxygen atmosphere that disposes voluntarily, because the gas mixture of preparation is stored in the pressurized vessel, and the volumetrical volume is far longer than the volume of steel cylinder, guaranteed the normal use of device, when especially emergency situation taking place, the polyreaction in the reactor is ended rapidly; More accurate and convenient when the control productive rate, not only saved cost but also improved the steady production of device and the safety coefficient of operation, brought very high benefit, and can will end gas continuously reposefully and join in the alpha-olefinic copolymerization reactor, effectively control alpha-olefinic copolymerization reaction, the quality of assurance the finished product.
Description of drawings:
Fig. 1 controls the schematic flow sheet of specific embodiments of the method for olefinic polyreaction
Fig. 2 is the schematic flow sheet of specific embodiments of ending the method for olefinic polyreaction
Embodiment:
The present invention is further described below in conjunction with drawings and Examples, but the present invention is not limited to this.
As shown in Figure 1, air is mixed by under meter 1, valve 2 and with sending in the mixing tank 5 after nitrogen by under meter 3, valve 4 mixes, mixing tank 5 is provided with tensimeter 6 and blow-off valve 7.Mixing tank 5 air with obtain oxygen-nitrogen mixture after nitrogen mixes, send in the pressurized vessel 9 after compressed again machine 8 pressurizations of oxygen-nitrogen mixture and store, pressurized vessel is provided with tensimeter.Oxygen-nitrogen mixture in the pressurized vessel is passed through valve 10 and pipeline 11a, 11b, 11c, 11d and be arranged on source line 12a on the reactor R1,12b, 12c, 12d, 12e, 12f, 12g, 12h sends into to be needed to pass through valve 13 and pipeline 14a among the olefin polymerization reactor of the stopped reaction R1 and/or with the oxygen-nitrogen mixture in the pressurized vessel, 14b, 14c, 14d and be arranged on source line 15a on the reactor R2,15b, 15c, 15d, 15e, 15f, 15g, 15h sends into to be needed among the olefin polymerization reactor of the stopped reaction R2; Perhaps the oxygen-nitrogen mixture in the pressurized vessel is sent among the reactor R2 of needs control alpha-olefinic copolymerization by under meter 16a, 16b, valve 17, pipeline 18 and with compressed again machine 19, pipeline 20a, 20b, 20c, 20d after the circulation gas that comes autoreactor mixes and source line 15a, the 15b, 15c, 15d, 15e, 15f, 15g, the 15h that are arranged on the reactor.
The reaction mixture that contains alkene adds among the reactor R1 by pipeline 22, catalyzer adds among the reactor R1 by pipeline 23, alkene polymerization under the effect of catalyzer obtains olefin polymer, polymkeric substance is discharged from pipeline 24, unreacted reaction mixture gas is circulated among the reactor R1 by pipeline 28a, 28b, 28c, 28d and source line 12a, 12b, 12c, 12d, 12e, 12f, 12g, 12h after valve 25, circulation line 26 and compressor 27 pressurizations, and blow-off valve 29 also is set on the reactor R1.When polyreaction is normally carried out, add valve 10 and the blow-off valve 29 of ending gas and close; Be in an emergency when need ending polyreaction, can feeding and end open blow-off valve 29 in the gases opening valve 10, the valve 25 of the recycle system can end cut out in the gas feeding, also shut-off valve 25 not.
The reaction mixture that can contain two kinds of alkene adds among the reactor R2 by pipeline 30, the material that contains catalyzer adds among the reactor R2 by pipeline 31, alkene polymerization under the effect of catalyzer obtains olefin polymer, polymkeric substance is discharged from pipeline 32, unreacted reaction mixture gas is circulated among the reactor R2 by pipeline 20a, 20b, 20c, 20d and source line 15a, 15b, 15c, 15d, 15e, 15f, 15g, 15h after valve 33, circulation line 34 and compressor 19 pressurizations, and blow-off valve 35 also is set on the reactor R2.When copolymerization normally carries out, adding valve 13 and the blow-off valve 35 of ending gas closes, valve 17 is opened, can join among the reactor R2 by valve 17, pipeline 18, compressor 19, pipeline 20a, 20b, 20c, 20d and source line 15a, 15b, 15c, 15d, 15e, 15f, 15g, 15h ending gas in right amount, like this each monomeric content in the speed of may command copolymerization and the polymkeric substance.Be in an emergency when need ending polyreaction, can feeding rapidly and end open blow-off valve 35 in the gases opening valve 13; The valve 25 of the recycle system can cut out when feed ending gas, also shut-off valve 25 not; Valve 18 cuts out simultaneously.
Production with impact polypropylene is example explanation the present invention below, but does not limit to its scope.
Embodiment 1
As shown in Figure 1, the reaction mixture that will contain propylene feeds among the horizontal type fixed bed reactor R1 by pipeline 22, the catalyzer that reaction is used adds among the reactor R1 by pipeline 23, alkene polymerization under the effect of catalyzer obtains the alkene reactive polymer, unreacted reaction mixture gas is through valve 25, circulation line 26 and compressor 27 pressurization backs are by pipeline 28a, 28b, 28c, 28d and source line 12a, 12b, 12c, 12d, 12e, 12f, 12g, 12h is circulated among the reactor R1, the service temperature of reactor R1 is 70 ℃, working pressure is 2.2Mpa, and reactive polymer and catalyzer are through pipeline 24, pipeline 31 enters reactor R2.Ethene and propylene are added among the reactor R2 by pipeline 30, the reaction mixture of alkene adds among the reactor R2 by pipeline 30, send into pressurized vessel 9 after simultaneously air institute nitrogen being made the compressed again machine compression of nitrogen mixed gas that oxygen level is 4.5% (molar percentage) by method shown in Figure 1, again the oxygen-nitrogen mixture in the pressurized vessel is passed through under meter 16a, 16b, valve 17, pipeline 18 and with compressed again machine 19 after the circulation gas that comes autoreactor mixes, pipeline 20a, 20b, 20c, 20d and be arranged on source line 21a on the reactor, 21b, 21c, 21d, 21e, 21f, 21g, 21h sends among the reactor R2 that needs the control alpha-olefinic copolymerization, adjusting nitrogen oxygen mixes, the add-on of gas, the amount that makes the polymkeric substance that reactor R2 discharges is needed size with the amount of reactor R1 discharge.The service temperature of reactor R2 is that 66 ℃, working pressure are 2.2Mpa, the further polymerization under the effect of catalyzer of alkene and reactive polymer obtains the anti-impact propene polymer, unreacted reaction mixture gas is circulated among the reactor R2 by pipeline 20a, 20b, 20c, 20d and source line 15a, 15b, 15c, 15d, 15e, 15f, 15g, 15h after valve 33, circulation line 35 and compressor 19 pressurizations, and for preventing the reaction mixture gas condensation, the full cycle pipeline adopts omnidistance companion's heat, and gained anti-impact propene polymer product is discharged from pipeline 32.
Comparative Examples 1
With oxygen level be the nitrogen mixed gas of 5% (molar percentage) by steel cylinder by under meter 16a, 16b, valve 17, pipeline 18 and with compressed again machine 19 after the circulation gas that comes autoreactor mixes, pipeline 20a, 20b, 20c, 20d and be arranged on source line 15a on the reactor, 15b, 15c, 15d, 15e, 15f, 15g, 15h sends into outside the reactor R2 that needs the control alpha-olefinic copolymerization, other operation and condition are with embodiment 1, reacting needs to change steel cylinder after 17 hours, can see that the performance index of changing steel cylinder front and back gained anti-impact propene polymer product fluctuate, and cause the quality instability.
Embodiment 2
When the production equipment of embodiment 1 is in an emergency, stop to send into the reaction mixture gas that contains propylene to reactor R1, and open valve 10, valve 13 feed reaction R1 and R2 (as shown in Figure 1) rapidly with a large amount of oxygen-nitrogen mixtures automatically, simultaneously automatic open valve 29 and valve 35; Selfclosing gate valve 18,25 and 33, polyreaction was ended in 1 minute among reactor R1 and the R2, implode, caking phenomenon did not occur.In this case, can be by restarting the entire reaction device, and needn't the emptying reaction bed, even must be from reactor the cleaning reaction gaseous mixture.
Comparative Examples 2
At the production equipment A Moke of embodiment 1 (AMOCO) gas phase polypropylene (when being in an emergency, in reactor R1, feed oxygen-nitrogen mixture rapidly by pipeline pipeline 11a, 11b, 11c, 11d independently with 4 steel cylinders in the past, in reactor R2, feed oxygen-nitrogen mixture rapidly by pipeline pipeline 14a, 14b, 14c, 14d independently with other 4 steel cylinders simultaneously, device repeatedly takes place because of adding oxygen untimely, polymerization is uncontrollable and cause the reactor caking phenomenon, annual about 3 times.Must stop behind the reactor caking, the cleaning reactor needs 3 day time at every turn approximately, has influenced carrying out smoothly of producing.
Claims (18)
1. method of ending olefinic polyreaction, comprise to mix with pure nitrogen gas from the airborne oxygen of air separation facility and obtain oxygen-nitrogen mixture, after the compressed machine pressurization oxygen-nitrogen mixture is compressed in the pressurized vessel, oxygen-nitrogen mixture with q.s joins in the olefin polymerization reactor rapidly again, so that poisoning of catalyst, thereby end olefinic polyreaction.
2. the method for termination olefinic polyreaction according to claim 1 is characterized in that being provided with at least 2 oxygen-nitrogen mixtures and adds inlet on olefin polymerization reactor, so that oxygen-nitrogen mixture whole catalyzer rapid and in the reactor contact.
3. the method for termination olefinic polyreaction according to claim 1 and 2 is characterized in that described olefinic polymerization is a vapour phase polymerization, and described reactor is a horizontal reactor, and described catalyzer is for being fit to alkene gas-phase polymerization and oxygen being ended responsive catalyzer.
4. the method for termination olefinic polyreaction according to claim 3, it is characterized in that described for catalyzer be transition Base Metal catalyzer.
5. the method for termination olefinic polyreaction according to claim 4 is characterized in that described transition Base Metal catalyzer is a Ziegler-natta catalyst.
6. the method for termination olefinic polyreaction according to claim 1 and 2, the concentration that it is characterized in that oxygen in the oxygen-nitrogen mixture is the 2-7 molar percentage.
7. the method for termination olefinic polyreaction according to claim 6, the concentration that it is characterized in that oxygen in the oxygen-nitrogen mixture is the 4-5 molar percentage.
8. the method for termination olefinic polyreaction according to claim 1 and 2 is characterized in that olefinic polymerization is equal polymerization of alkene or copolymerization.
9. the method for termination olefinic polyreaction according to claim 8 is characterized in that olefinic polymerization is equal polymerization of propylene or copolymerization.
10. method of controlling olefinic polyreaction, comprise to mix with pure nitrogen gas from the airborne oxygen of air separation facility and obtain oxygen-nitrogen mixture, after the compressed machine pressurization oxygen-nitrogen mixture is compressed in the pressurized vessel, again oxygen-nitrogen mixture is joined in the alpha-olefinic copolymerization reactor, with the content of each monomeric unit in control speed of olefin-copolymerization and the copolymerization product.
11. control alpha-olefinic copolymerization reaction method according to claim 10 is characterized in that being provided with at least one oxygen-nitrogen mixture and adds inlet on olefin polymerization reactor, so that oxygen-nitrogen mixture whole catalyzer rapid and in the reactor contact.
12. control alpha-olefinic copolymerization reaction method according to claim 11 is characterized in that being provided with at least two oxygen-nitrogen mixtures and adds inlet on olefin polymerization reactor, so that oxygen-nitrogen mixture whole catalyzer rapid and in the reactor contact.
13., it is characterized in that oxygen-nitrogen mixture adds in the reactor circulation gas mixing back of polymerization reactor together according to the method for claim 10 or 11 described control olefinic polyreactions.
14. method according to claim 10 or 11 described control olefinic polyreactions, it is characterized in that described olefin-copolymerization is combined into vapour phase polymerization, described reactor is a horizontal reactor, described olefin-copolymerization is combined into copolymerization of propylene, and described catalyzer is for being fit to alkene gas-phase polymerization and oxygen being controlled responsive catalyzer.
15. the method for control olefinic polyreaction according to claim 14, it is characterized in that described for catalyzer be transition Base Metal catalyzer.
16. the method for control olefinic polyreaction according to claim 15 is characterized in that described transition Base Metal catalyzer is a Ziegler-natta catalyst.
17. according to the method for claim 10 or 11 described control olefinic polyreactions, the concentration that it is characterized in that oxygen in the oxygen-nitrogen mixture is the 2-7 molar percentage.
18, the method for control olefinic polyreaction according to claim 17, the concentration that it is characterized in that oxygen in the oxygen-nitrogen mixture is the 4-5 molar percentage.
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| CN111924349A (en) * | 2020-07-07 | 2020-11-13 | 山西钢科碳材料有限公司 | Device for preventing acrylonitrile liquid from self-polymerization and control method |
| CN114073924A (en) * | 2020-08-20 | 2022-02-22 | 中国石油化工股份有限公司 | Polypropylene prepolymerization polymerization inhibition system and method and polypropylene production device |
| CN112762359A (en) * | 2021-01-05 | 2021-05-07 | 宁夏宝丰能源集团股份有限公司 | Device for inhibiting polymerization reaction and polymerization reaction complete equipment |
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