WO2015141388A1 - オレフィン重合体の製造方法 - Google Patents
オレフィン重合体の製造方法 Download PDFInfo
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- WO2015141388A1 WO2015141388A1 PCT/JP2015/054809 JP2015054809W WO2015141388A1 WO 2015141388 A1 WO2015141388 A1 WO 2015141388A1 JP 2015054809 W JP2015054809 W JP 2015054809W WO 2015141388 A1 WO2015141388 A1 WO 2015141388A1
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- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
- C08F110/04—Monomers containing three or four carbon atoms
- C08F110/08—Butenes
- C08F110/10—Isobutene
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- C—CHEMISTRY; METALLURGY
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- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
- C08F10/04—Monomers containing three or four carbon atoms
- C08F10/08—Butenes
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
- C08F2/01—Processes of polymerisation characterised by special features of the polymerisation apparatus used
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- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
- C08F2/38—Polymerisation using regulators, e.g. chain terminating agents, e.g. telomerisation
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- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F4/00—Polymerisation catalysts
- C08F4/02—Carriers therefor
- C08F4/022—Magnesium halide as support anhydrous or hydrated or complexed by means of a Lewis base for Ziegler-type catalysts
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F4/00—Polymerisation catalysts
- C08F4/06—Metallic compounds other than hydrides and other than metallo-organic compounds; Boron halide or aluminium halide complexes with organic compounds containing oxygen
- C08F4/12—Metallic compounds other than hydrides and other than metallo-organic compounds; Boron halide or aluminium halide complexes with organic compounds containing oxygen of boron, aluminium, gallium, indium, thallium or rare earths
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F4/00—Polymerisation catalysts
- C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
- C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
- C08F4/52—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides selected from boron, aluminium, gallium, indium, thallium or rare earths
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- C—CHEMISTRY; METALLURGY
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- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
- C08F2500/03—Narrow molecular weight distribution, i.e. Mw/Mn < 3
Definitions
- the present invention relates to a method for producing an olefin polymer.
- Patent Document 1 describes a method for producing an isobutylene polymer, characterized in that the raw material liquid supplied to the reactor is cooled in advance by exchanging heat with the discharged reaction liquid. Yes.
- the present invention provides a method for producing an olefin polymer, which can efficiently recover the cooling energy required for the polymerization reaction and obtain an olefin compound having a good property having a narrow molecular weight distribution. With the goal.
- One aspect of the present invention relates to a method for producing an olefin polymer, wherein an olefin compound is obtained by polymerizing an olefin compound at a temperature of 0 ° C. or lower in the presence of a Lewis acid catalyst.
- the production method includes a supply step of supplying a raw material liquid containing the olefin compound into a reactor equipped with a cooling means, and a reaction liquid containing the olefin polymer by polymerizing the olefin compound in the reactor.
- a deactivation step of deactivating the Lewis acid catalyst by adding a deactivator to the reaction solution taken out from the reactor, and a means for cold recovery of the reaction solution after the deactivation step And a cold energy recovery step of recovering cold energy from the reaction solution.
- the amount of the Lewis acid catalyst may be 0.5 ⁇ 10 ⁇ 3 to 1.0 ⁇ 10 ⁇ 1 mol% based on the total amount of the olefin compound.
- the Lewis acid catalyst may be an aluminum compound represented by the following formula (1) or (2).
- R represents an alkyl group having 1 to 8 carbon atoms
- X represents a halogen atom
- m represents 1 or 2
- n represents an integer of 1 to 5.
- the amount of the Lewis acid catalyst may be 0.5 ⁇ 10 ⁇ 3 to 0.3 ⁇ 10 ⁇ 2 mol% with respect to the total amount of the olefin compound.
- the raw material liquid supplied to the reactor may be cooled in advance with the cold heat collected by the cold heat collecting means.
- the olefin compound may contain isobutene.
- the deactivator may contain water or an alcohol compound.
- an olefin polymer production method capable of efficiently recovering the cooling energy required for the polymerization reaction and obtaining an olefin compound having a good property having a narrow molecular weight distribution. can do.
- the production method is a method for producing an olefin polymer by polymerizing an olefin compound at a temperature of 0 ° C. or lower in the presence of a Lewis acid catalyst, and includes (1) an olefin compound.
- the amount of the Lewis acid catalyst is 0.5 ⁇ 10 ⁇ 3 to 1.0 ⁇ 10 ⁇ 1 mol% with respect to the total amount of the olefin compound.
- the cold acid recovery step is performed after deactivating the Lewis acid catalyst in the reaction solution. According to such a production method, the cooling energy required for the polymerization reaction can be efficiently recovered, and an olefin compound having a good property having a narrow molecular weight distribution can be obtained.
- the Lewis acid catalyst when the Lewis acid catalyst is deactivated, the cold heat of the reaction solution is lost, and it is difficult to recover the cooling energy by heat exchange or the like. Further, when the cold recovery step is carried out without deactivating the Lewis acid catalyst, an unnecessary reaction may occur due to the temperature rise of the reaction solution, which may deteriorate the properties of the olefin polymer.
- the Lewis acid catalyst is suppressed to a predetermined amount, and the reaction solution that has undergone the deactivation process is subjected to the cold recovery process, so that the properties of the olefin polymer are not deteriorated. It is possible to sufficiently recover cold from the reaction solution.
- the Lewis acid catalyst is preferably an aluminum compound represented by the following formula (1) or (2).
- the amount of the Lewis acid catalyst is preferably 0.5 ⁇ 10 ⁇ 3 to 0.3 ⁇ 10 ⁇ 2 mol% with respect to the total amount of the olefin compound.
- R represents an alkyl group having 1 to 8 carbon atoms
- X represents a halogen atom
- m represents 1 or 2
- n represents an integer of 1 to 5.
- the polymerization reaction of the olefin compound can proceed efficiently with a small amount of catalyst. Further, by setting the amount of catalyst within the above-mentioned preferable range, the amount of the deactivator required for deactivation of the catalyst can be suppressed, and heat generation due to deactivation of the catalyst can be suppressed to a minimum. For this reason, the loss of the cooling energy in the deactivation process is sufficiently suppressed.
- an olefin compound having 3 to 10 carbon atoms for example, an olefin compound having 3 to 10 carbon atoms (more preferably 4 to 6 carbon atoms) can be suitably used.
- olefin compound examples include isobutylene, propylene, 1-butene, 2-butene, 2-methyl-1-butene, 2-methyl-2-butene, butadiene, pentene, 4-methyl-1-pentene, and isoprene.
- isobutylene, 1-butene, 2-butene, and isoprene can be preferably used, and isobutylene is particularly preferable.
- the raw material liquid may contain one or more olefin compounds.
- the raw material liquid may further contain a solvent.
- a solvent a known solvent used for the polymerization reaction of an olefin compound can be used without particular limitation.
- the raw material liquid does not necessarily need to contain a solvent.
- the solvent can be supplied to the reactor separately from the raw material liquid, and can also be supplied to the reactor together with the Lewis acid catalyst described later.
- solvent examples include propylene, butane, 1-butene, 2-butene, 2-methyl-1-butene, 2-methyl-2-butene, butadiene, pentene, 4-methyl-1-pentene, isoprene, cyclopentene, and cyclopentadiene.
- butane, 1-butene, 2-butene, 2-methyl-1-butene, 2-methyl-2-butene, hexane, and octane can be preferably used.
- the raw material liquid may be supplied to the reactor at room temperature, but it is preferable that the raw material liquid is supplied to the reactor after being cooled by the raw material liquid cooling means.
- the raw material liquid cooling means By cooling in advance with the raw material liquid cooling means and supplying it to the reactor, for example, even when the polymerization reaction is carried out continuously, the property degradation of the olefin polymer due to the temperature rise in the reactor is sufficiently suppressed can do.
- the raw material liquid can be cooled to 5 ° C. or lower and supplied to the reactor, for example. Further, the temperature of the raw material liquid supplied to the reactor does not need to be lower than the reaction temperature of the polymerization reaction, and may be, for example, 10 ° C. or less.
- reactors and cooling means used for the polymerization reaction of olefin compounds can be used.
- a stirred tank reactor can be used as the reactor.
- a tubular reactor, a stirring tank reactor, etc. can be used, for example.
- cooling means for example, a cooling jacket that covers the reactor and a cooler that supplies a refrigerant to the cooling jacket can be used.
- the cooling means may be a cooling means utilizing endothermic or the like due to evaporation of components existing as raw materials or solvents.
- the polymerization step is a step of obtaining a reaction liquid containing an olefin polymer by polymerizing an olefin compound in a reactor.
- the polymerization of the olefin compound can be carried out at a reaction temperature of 0 ° C. or lower in the presence of a Lewis acid catalyst.
- a Lewis acid catalyst include SnCl 4 , TiCl 4 , TiCl 3 , TiBr 4 , TiBr 3 , VCl 5 , FeCl 3 , ZrCl 3 , ZrCl 4 , ZnBr 2 , BF 3 , BCl 3 , Al (R) m ( And metal halides such as X) (3-m) and Al 2 (R) n (X) (6-n) , and organometallic halides.
- an aluminum compound represented by the following formula (1) or (2) is preferable.
- R represents an alkyl group having 1 to 8 carbon atoms
- X represents a halogen atom
- m represents 1 or 2
- n represents an integer of 1 to 5.
- the alkyl group represented by R may be linear or branched.
- the carbon number of the alkyl group is preferably 1 to 4, more preferably 1 or 2.
- Examples of the alkyl group represented by R include a methyl group, an ethyl group, a propyl group, and a butyl group, and among these, a methyl group and an ethyl group are preferable.
- halogen atom represented by X examples include a chlorine atom, a bromine atom and an iodine atom, and among these, a chlorine atom is preferable.
- the Lewis acid catalyst examples include CH 3 AlCl 2 , (CH 3 ) 2 AlCl, C 2 H 5 AlCl 2 , (C 2 H 5 ) 2 AlCl, (CH 3 ) 3 CAlCl 2 , [(CH 3 ) 3 C] 2 AlCl, (CH 3 ) 3 Al 2 Cl 3 , (C 2 H 5 ) 3 Al 2 Cl 3 and the like.
- C 2 H 5 AlCl 2 can be particularly preferably used from the viewpoint of excellent safety and the effects of the present invention more remarkably.
- the amount of the Lewis acid catalyst is 0.5 ⁇ 10 ⁇ 3 to 1.0 ⁇ 10 ⁇ 1 and preferably 0.5 ⁇ 10 ⁇ 3 to 1.0 ⁇ 10 ⁇ 2 with respect to the total amount of the olefin compound.
- the mol% is more preferably 0.5 ⁇ 10 ⁇ 3 to 0.7 ⁇ 10 ⁇ 2 mol%, and still more preferably 0.5 ⁇ 10 ⁇ 3 to 0.3 ⁇ 10 ⁇ 2 mol%. If the amount of the Lewis acid catalyst is less than 0.5 ⁇ 10 ⁇ 3 mol%, the polymerization reaction may not proceed sufficiently. On the other hand, when the amount of the Lewis acid catalyst exceeds 1.0 ⁇ 10 ⁇ 1 mol%, a large amount of deactivator is required, and the loss of cooling energy during deactivation tends to increase.
- the reaction temperature of the polymerization reaction can be appropriately selected according to the kind of the raw material olefin compound, the properties of the desired olefin polymer, and the like.
- the reaction temperature can be 10 ° C. or lower, and more preferably 0 ° C. or lower in order to obtain a polymer having a high degree of polymerization.
- the reaction pressure is not particularly limited, but can be, for example, 0.1 to 2.0 MPa, and preferably 0.2 to 1.0 MPa.
- a cocatalyst in the polymerization step, can be further used.
- the cocatalyst include water and alcohols.
- the amount of the cocatalyst can be, for example, 5 to 250 mol%, preferably 10 to 50 mol%, based on the total amount of the Lewis acid catalyst.
- the polymerization reaction of the olefin compound can be performed batchwise or continuously. From the viewpoint of production efficiency, the polymerization reaction is preferably carried out continuously.
- a deactivation agent is added to the reaction liquid taken out from the reactor to deactivate the Lewis acid catalyst.
- the amount of the above-mentioned Lewis acid catalyst is small, the amount of the deactivator required at the time of deactivation and the amount of reaction heat generated at the time of deactivation can be sufficiently reduced. For this reason, in the manufacturing method which concerns on this embodiment, the loss of the cooling energy of the reaction liquid by the deactivation of a Lewis acid catalyst can fully be suppressed.
- the quenching agent may be any one that can deactivate the above-mentioned Lewis acid catalyst.
- the quencher for example, water, alcohol compounds, ethers, amines, acetonitrile, ammonia, mineral-based basic aqueous solutions, and the like can be used, and among these, water or alcohol compounds can be preferably used.
- the alcohol compound an alkyl alcohol having 1 to 5 carbon atoms can be suitably used, and an alcohol compound selected from methanol, ethanol, isopropyl alcohol, butanol and pentanol is preferable.
- the amount of the deactivator may be any as long as it can deactivate the above-mentioned Lewis acid catalyst.
- the amount of the deactivator can be, for example, 50 to 3000 mol% or 100 to 200 mol% with respect to the Lewis acid catalyst.
- the method for adding the deactivator is not particularly limited.
- the reaction solution is supplied to the second reactor, and the deactivator is added to the second reactor to which the reaction solution is supplied, whereby the Lewis acid is added.
- the catalyst can be deactivated.
- a deactivator inlet is provided in the middle of the transport line for transporting the reaction liquid from the reactor to the cold heat recovery means described later, and the deactivator is charged from the deactivator inlet to react the reaction liquid in the transport line. It is also possible to deactivate the Lewis acid catalyst by mixing it with a deactivator.
- the quenching agent may be dissolved or dispersed in a solvent and added to the reaction solution.
- Solvents for dissolving or dispersing the deactivator include, for example, propylene, butane, 1-butene, 2-butene, 2-methyl-1-butene, 2-methyl-2-butene, butadiene, pentene, 4-methyl- 1-pentene, isoprene, cyclopentene, cyclopentadiene, hexene, cyclohexene, cyclohexadiene, heptane, heptene, octane, octene, benzene, toluene, xylene, methyl chloride, dichloromethane, chloroform, carbon tetrachloride, ethyl chloride, dichloroethane, trichloroethane, Chlorobenzene, dichlorobenzene and the like can be used.
- the reaction liquid that has passed through the deactivation process is supplied to a cold energy recovery means to recover cold energy from the reaction liquid.
- a cold energy recovery means to recover cold energy from the reaction liquid.
- the cold energy recovery means is not particularly limited, and known cold energy recovery means can be adopted.
- the cold energy recovery means may include a heat exchanger.
- a heat exchanger well-known heat exchangers, such as a double tube type heat exchanger, a multi-tube type heat exchanger, a plate type heat exchanger, a counterflow type heat exchanger, can be used, for example.
- the cold energy recovered by the cold energy recovery means may be applied in any way, but is preferably applied in the manufacturing method according to the present embodiment.
- the cold heat collected by the cold heat collecting means can be used in order to pre-cool the raw material liquid supplied to the reactor with the cold heat collected by the cold heat collecting means.
- the cold energy recovered by the cold energy recovery means in order to cool the inside of the reactor together with the cooling means provided in the reactor, the cold energy recovered by the cold energy recovery means can be used.
- the cold heat recovery step may be a step of cooling the raw material liquid by performing heat exchange between the reaction liquid and the raw material liquid supplied to the reactor, for example, and the cold heat recovery means includes the reaction liquid and the raw material liquid. It may be a heat exchanger that performs heat exchange.
- the cold heat recovery step may be, for example, a step of cooling the refrigerant by exchanging heat between the reaction liquid and the refrigerant provided to the cooling means provided in the reactor.
- the cold heat recovery means May be a heat exchanger that performs heat exchange between the reaction liquid and the refrigerant.
- an olefin polymer can be obtained from a reaction solution that has undergone the cold recovery process by a known purification method. That is, the manufacturing method according to the present embodiment may include a step of obtaining an olefin polymer from the reaction liquid that has undergone the cold recovery step.
- the purification method is not particularly limited, and for example, an olefin polymer can be obtained by distilling the reaction solution to remove unreacted olefin compound and solvent.
- the olefin polymer obtained by the production method according to the present embodiment is sufficiently suppressed in property deterioration due to temperature rise at the time of cold recovery, and tends to have a narrow molecular weight distribution, for example.
- the molecular weight distribution (Mw / Mn, ratio of weight average molecular weight (Mw) to number average molecular weight (Mn)) of the olefin polymer is preferably 3.0 or less, more preferably 2.3 or less. Moreover, Mw / Mn may be 1.5 or more, and may be 1.8 or more.
- the weight average molecular weight and number average molecular weight of an olefin polymer show the value measured by gel permeation chromatography (GPC).
- Example device A cooling jacket was attached to a 500 ml autoclave, and the internal temperature was kept low by circulating brine through the cooling jacket.
- a countercurrent heat exchanger was connected to the outlet of the autoclave so that heat exchange between the raw material liquid introduced into the autoclave and the reaction liquid taken out from the autoclave was performed.
- a deactivator inlet was provided between the outlet of the autoclave and the countercurrent heat exchanger.
- Example 1 A mixed solution of isobutene and isobutane (isobutene content 50 mass%) is used as a raw material liquid, CH 3 CH 2 AlCl 2 (ethylaluminum dichloride) is used as a Lewis acid catalyst, and 0.5 mass of isopropyl alcohol is used as a deactivator. A% hexane solution was used.
- the temperature in the autoclave was set to ⁇ 15 ° C., the raw material liquid was continuously introduced at 600 g / h, and the Lewis acid catalyst was combined in the autoclave so as to have an amount of 2.4 ⁇ 10 ⁇ 3 mol% with respect to isobutene.
- the polymer was continuously introduced into the autoclave, and the polymerization was allowed to proceed continuously.
- the Lewis acid catalyst was dispersed in hexane and introduced into the autoclave.
- a deactivator was continuously introduced into the reaction solution taken out from the autoclave at a rate (0.6 ml / min) of isopropyl alcohol with respect to 1 mol of the Lewis acid catalyst from the deactivator introduction port. .
- the reaction liquid recovered through the heat exchanger was distilled to remove unreacted isobutene and isobutane, thereby obtaining an olefin polymer.
- the molecular weight distribution of the obtained olefin polymer was 2.2.
- the cold energy recovered by the heat exchanger was 16.9 kJ / h.
- the molecular weight distribution of the obtained olefin polymer was 2.2. Further, the cold energy recovered by the heat exchanger was 5.1 kJ / h.
- the molecular weight distribution of the obtained olefin polymer was 2.2. Moreover, the cold energy which could be collect
- Example 3 The reaction was performed in the same manner as in Example 1 except that the quencher was not introduced from the quencher inlet. A quenching agent was added to the reaction liquid recovered through the heat exchanger, and unreacted isobutene and isobutane were removed by distillation operation to obtain an olefin polymer.
- the molecular weight distribution of the obtained olefin polymer was 3.4.
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Abstract
Description
Al(R)m(X)(3-m) (1)
Al2(R)n(X)(6-n) (2)
[式中、Rは炭素数1~8のアルキル基を示し、Xはハロゲン原子を示し、mは1又は2を示し、nは1~5のいずれかの整数を示す。]
Al(R)m(X)(3-m) (1)
Al2(R)n(X)(6-n) (2)
供給工程では、オレフィン化合物を含む原料液を、冷却手段を備える反応器中に供給する。
重合工程は、反応器中でオレフィン化合物を重合させて、オレフィン重合体を含む反応液を得る工程である。
Al(R)m(X)(3-m) (1)
Al2(R)n(X)(6-n) (2)
失活工程では、反応器にから取り出された反応液に失活剤を加えて、ルイス酸触媒を失活させる。本実施形態における失活工程では、上述のルイス酸触媒の量が少ないため、失活時に要する失活剤の量及び失活時に生じる反応熱の量を十分に低減することができる。このため、本実施形態に係る製造方法では、ルイス酸触媒の失活による反応液の冷却エネルギーの損失を、十分に抑制することができる。
冷熱回収工程では、失活工程を経た反応液を冷熱回収手段に供して、反応液から冷熱を回収する。本実施形態では、失活工程でルイス酸触媒を失活させているため、冷熱回収によって反応液が昇温することによるオレフィン重合体の性状低下が十分に抑制される。また、失活工程で反応液の冷却エネルギーの損失が十分に抑えられているため、冷熱回収工程において、効率良く反応液から冷熱を回収することができる。
500mlのオートクレーブに冷却ジャケットを装着し、該冷却ジャケットへのブライン循環により、内部温度を低温に保てる構造とした。また、オートクレーブの出口に向流熱交換器を接続し、オートクレーブに導入される原料液とオートクレーブから取り出される反応液との熱交換を行うことができる構造とした。さらに、オートクレーブの出口から向流熱交換器までの間に失活剤導入口を設けた。
原料液として、イソブテン及びイソブタンの混合溶液(イソブテン含有量50質量%)を用い、ルイス酸触媒としてCH3CH2AlCl2(エチルアルミニウムジクロライド)を用い、失活剤としてイソプロピルアルコールの0.5質量%ヘキサン溶液を用いた。
ルイス酸触媒の量を、イソブテンに対して1.65×10-1mol%に変更し、失活剤の量を41ml/min(ルイス酸触媒1molに対してイソプロピルアルコールが15molとなる割合)に変更したこと以外は、実施例1と同様にして反応を行い、オレフィン重合体を得た。
ルイス酸触媒の量を、イソブテンに対して1.65×10-1mol%に変更し、失活剤としてイソプロピルアルコールの5.0質量%ヘキサン溶液を用い、失活剤の量を4.1ml/min(ルイス酸触媒1molに対してイソプロピルアルコールが15molとなる割合)に変更したこと以外は、実施例1と同様にして反応を行い、オレフィン重合体を得た。
失活剤導入口から失活剤を導入しなかったこと以外は、実施例1と同様にして反応を行った。熱交換器を経て回収された反応液に失活剤を添加し、蒸留操作によって未反応のイソブテン及びイソブタンを除去して、オレフィン重合体を得た。
Claims (6)
- ルイス酸触媒存在下、0℃以下の温度でオレフィン化合物を重合させてオレフィン重合体を得る、オレフィン重合体の製造方法であって、
前記オレフィン化合物を含む原料液を、冷却手段を備える反応器中に供給する供給工程と、
前記反応器中で、前記オレフィン化合物を重合させて、前記オレフィン重合体を含む反応液を得る重合工程と、
前記反応器から取り出された前記反応液に失活剤を加えて、前記ルイス酸触媒を失活させる失活工程と、
前記失活工程を経た前記反応液を冷熱回収手段に供して、前記反応液から冷熱を回収する冷熱回収工程と、
を含み、
前記ルイス酸触媒の量が、前記オレフィン化合物の総量に対して0.5×10-3~1.0×10-1mol%である、製造方法。 - 前記ルイス酸触媒が、下記式(1)又は(2)で表されるアルミニウム化合物である、請求項1に記載の製造方法。
Al(R)m(X)(3-m) (1)
Al2(R)n(X)(6-n) (2)
[式中、Rは炭素数1~8のアルキル基を示し、Xはハロゲン原子を示し、mは1又は2を示し、nは1~5のいずれかの整数を示す。] - 前記ルイス酸触媒の量が、前記オレフィン化合物の総量に対して0.5×10-3~0.3×10-2mol%である、請求項1又は2に記載の製造方法。
- 前記冷熱回収手段で回収された冷熱で、前記反応器に供給される原料液を予め冷却する、請求項1~3のいずれか一項に記載の製造方法。
- 前記オレフィン化合物が、イソブテンを含む、請求項1~4のいずれか一項に記載の製造方法。
- 前記失活剤が、水又はアルコール化合物を含む、請求項1~5のいずれか一項に記載の製造方法。
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CN201580012714.7A CN106068283B (zh) | 2014-03-19 | 2015-02-20 | 烯烃聚合物的制造方法 |
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