WO2016028123A1 - 폴리부텐의 제조방법 - Google Patents
폴리부텐의 제조방법 Download PDFInfo
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- WO2016028123A1 WO2016028123A1 PCT/KR2015/008776 KR2015008776W WO2016028123A1 WO 2016028123 A1 WO2016028123 A1 WO 2016028123A1 KR 2015008776 W KR2015008776 W KR 2015008776W WO 2016028123 A1 WO2016028123 A1 WO 2016028123A1
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- C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
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- C08F236/04—Copolymers of compounds having one or more unsaturated aliphatic radicals, at least one having two or more carbon-to-carbon double bonds the radical having only two carbon-to-carbon double bonds conjugated
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Definitions
- the present invention relates to a method for producing polybutene, and more particularly, to a method for producing polybutene which has improved productivity compared to producing polybutene with conventional C4 mixture by maximizing utilization of isobutene in C4 mixture. It is about.
- Polybutenes are generally prepared by the use of Friedel-Craft type catalysts to polymerize olefin components having 4 carbon atoms (C4) derived from hydrocarbon cracking, with a number average molecular weight (Mn) of about 300. To 5,000.
- C4 carbon atoms
- Mn number average molecular weight
- Isobutene is mainly used for the preparation of methyl-t-butylether (MTBE) or polybutene, which is an octane number enhancer, and the polybutene produced is mainly isobutane because it has the highest reactivity among the olefin components having 4 carbon atoms. It consists of ten units.
- isobutene is also a raw material of ETB (Ethylene Glycol mono-t-butyl Ether), DETB (Diethylene Glycol mono-t-butyl Ether), which is a raw material for electronic cleaners, and DIB (Diisobutene) and IIR (Isobutylene Isoprene). It is also used as a raw material such as rubber), and is usefully used in fields such as petrochemical and fine chemistry.
- polyisobutenyl succinic anhydride prepared by reacting polybutene and maleic anhydride is well known, and most lubricant additives and fuel cleaners are prepared using PIBSA as an intermediate.
- the highly reactive polybutene in which the double bond of polybutene is located at the terminal of polybutene, reacts directly with maleic anhydride to obtain PIBSA in high yield.
- the chlorination reaction is performed using chlorine gas. After that, it is reacted with maleic anhydride to prepare PIBSA.
- a double bond may be placed at the molecular end to form vinylidene.
- Polybutenes having a vinylidene content of more than 70 mol% i.e., 70% vinylidene relative to the total number of double bonds
- highly reactive polybutenes i.e., 70% vinylidene relative to the total number of double bonds
- Polybutene is referred to as Mid-Reactive Polybutene (MVPB)
- MVPB Mid-Reactive Polybutene
- low-reactivity polybutene Low-reactivity polybutene
- boron trifluoride BF3
- alcohols, ethers, etc. are used as a catalyst.
- AlCl 3 aluminum trichloride
- US Patent 5,674,955 uses a raw material containing at least 5% of 1-butene, and a halogen compound It is disclosed that the production of polybutene containing high vinylidene content and low halogen can be made by reducing the 1-butene content of the initial raw material to 20% or less through the pretreatment of the raw material under the condition of using the catalyst. .
- 6,207,115 discloses the use of an olefin conversion unit (OCU, Olefin Conversion Unit) to selectively hydrogenate diolefins (butadiene, etc.) and to isomerize 1-butene to 2-butene at the same time.
- OCU Olefin Conversion Unit
- 1-butene and isobutene are difficult to separate because their boiling points are similar, but raw materials that have undergone isomerization can be easily separated into isobutene and 2-butene using the difference in boiling points.
- 2-butene having a relatively high boiling point separated to the bottom of the distillation column is used for propylene production by reacting with ethylene, and isobutene having a lower boiling point separated to the top of the distillation column is used for producing polybutene.
- isobutene in order to produce high purity isobutene, it is also possible to separate isobutene from the C4 mixture.
- methanol is added to isobutene using a t-butyl alcohol (TBA) dehydration method combining an hydration reaction and a dehydration reaction, an acid catalyst, and then cracked again to crack isobutane.
- TSA t-butyl alcohol
- MTBE Methyl t-Butyl Ether
- An object of the present invention is to provide a method for producing polybutene which can reduce production costs and increase the amount of polybutene produced by efficiently utilizing or increasing isobutene used as a raw material of polybutene.
- the C4 mixture is fed to the isomerization reactor, 1-butene isomerized to 2-butene by hydrogen isomerization reaction using an isomerization catalyst in the isomerization zone of the isomerization reactor, fractional distillation zone Isobutene and 2-butene are separated by fractional distillation;
- the C4 mixture containing 2-butene separated in the isomerization reactor is fed to the skeletal isomerization reactor, and a portion of the normal butene is skeletal isomerized to isobutene by skeletal isomerization using a skeletal isomerization catalyst, and the skeleton isomerization obtained therefrom.
- the mixture is fed to the isomerization reactor and recycled; And a reaction raw material containing a high concentration of isobutene separated from the isomerization reactor and a polymerization catalyst are supplied to the polybutene polymerization reactor, thereby producing polybutene by a polymerization reaction.
- the method for producing polybutene according to the present invention can increase the production of polybutene, and can increase the product (polybutene) production by 20% or more as compared to simply using a conventional mixed C4 hydrocarbon mixture. .
- a C4 hydrocarbon mixture containing relatively high purity isobutene high reactivity polybutene having a high vinylidene content and a low halogen content, as well as a general polybutene having a low halogen content can be prepared. have.
- a high quality product having excellent productivity per unit raw material and productivity per unit catalyst can be produced.
- the catalyst mileage is also improved by more than two times, thereby lowering the manufacturing cost of the product.
- FIG. 1 is a process chart for explaining a polybutene manufacturing method according to an embodiment of the present invention.
- FIG. 1 is a process chart for explaining a polybutene manufacturing method according to an embodiment of the present invention.
- a C4 mixture hydrocarbons containing 4 carbon atoms
- the isomerization zone 12 uses an isomerization catalyst.
- 1-butene isomerized to 2-butene by the hydroisomerization reaction, and at the same time, isobutene and 2-butene have boiling points in the fractionated distillation region 14.
- the hydroisomerization and fractional distillation processes are carried out by fractional distillation and separation by difference.
- the C4 mixture is a C4 residue obtained during the naphtha pyrolysis process or a C4 fraction produced during the catalytic cracking of heavy oil in the petroleum refining process, and is preferably at least 5% by weight of normal butenes, preferably at least 10% by weight of normal butenes, more preferably. 20 to 45% by weight, even more preferably 25 to 40% by weight of normal butenes and 10 to 60% by weight, preferably 20 to 55% by weight, more preferably 30 to 50% by weight of isobutene It may include.
- a C4 residue such as the composition of Table 1 or a C4 fraction such as the composition of Table 2 may be used.
- the isobutene recycling efficiency is less than about 1/8 of the composition raw materials of the following Tables 1 and 2 (more than 5% by weight of normal butenes) used in the present invention. do. This is a result of the isobutene recycling efficiency is very low, substantially isobutene content obtainable through the recycling process is very small, it is difficult to recycle the process to maximize the utilization of isobutene through the present invention.
- a C4 mixture (high concentration isobutene raw material) containing a high concentration of isobutene is ejected from the isomerization reactor (column) 10 (preferably, as shown in FIG. 1). , Blowing to the top of the isomerization reactor 10).
- the high concentration isobutene raw material obtained in the isomerization reactor 10 is 70% by weight or more, preferably 80 to 98% by weight, more preferably 85 to 95% by weight of isobutene and 3% by weight or less, preferably 2% by weight. Up to%, more preferably from 0.1 to 1.5% by weight of normal butene.
- the composition shown in Table 3 may be exemplified.
- a C4 mixture comprising a high concentration of 2-butene is ejected from the isomerization reactor (column 10) (preferably, as shown in FIG. 1, the isomerization reactor 10 Eruption to the bottom of)).
- the high concentration 2-butene raw material obtained in the isomerization reactor 10 is at least 55% by weight, preferably 60 to 90% by weight, more preferably 65 to 80% by weight of 2-butene and 5% by weight or less, preferably 3 wt% or less, more preferably 0.5 to 2 wt% of isobutene may be included.
- a composition as shown in Table 4 may be exemplified.
- the hydroisomerization reaction is to change the hydrogen position, that is, the position of the double bond in the molecule, and isomerize to 2-butene without changing the molecular formula of 1-butene, and is 30 to 100 ° C., preferably 40 to 80 ° C. More preferably at a temperature of from 50 to 70 ° C.
- a conventional acid catalyst or a base catalyst may be used, and metals such as platinum (Pt), palladium (Pd) and nickel (Ni) may also be used. Can be.
- a C4 mixture containing a large amount of high concentration of 2-butene separated in the isomerization reactor 10 (some 1-butenes which may not be isomerized in the isomerization reactor 10 may be included) is a skeleton isomerization reactor (or, To the skeletal isomerization column 20 (preferably, as shown in FIG. 1, to the top of the skeletal isomerization reactor 20), and through the skeletal isomerization reaction using a skeletal isomerization catalyst, the normal butene (n ⁇ ) butene) is skeletal isomerized with isobutene, and the skeletal isomerization mixture (C4 mixture) obtained therefrom is ejected from the skeletal isomerization reactor 20 (preferably as shown in FIG. 1). Likewise, the lower part of the skeleton isomerization reactor 20 is ejected, and the skeleton isomerization process, which is supplied to the isomerization reactor 10 and recycled, is performed.
- the isobutene raw material obtained in the skeletal isomerization reactor 20 is 10 to 60% by weight, preferably 20 to 50% by weight, more preferably 25 to 40% by weight of isobutene and 20 to 53% by weight, preferably 30 to 50% by weight, more preferably 35 to 45% by weight of normal butene.
- a composition as shown in Table 5 may be illustrated.
- the skeletal isomerization reaction generally means a conversion between a normal form and an iso form, preferably a conversion from a normal form to an iso form, which also has a molecular formula, but has a structure of a carbon skeleton. It is to change itself.
- the normal butenes which are isomerized with isobutene are about 30 to 50%, preferably 35 to 45%, and the remaining normal butenes are present as 1-butene and 2-butene.
- the skeletal isomerization reaction should be carried out under high temperature conditions of 250 to 350 ° C, preferably 280 to 320 ° C, more preferably 290 to 310 ° C. When the reaction is carried out at less than 250 °C, the reaction conversion rate is low, or there is a fear that the amount of isobutene produced by the skeleton isomerization is small, and if it exceeds 350 °C, the production rate of by-products is faster, the yield of isobutene Low or deactivation may occur suddenly.
- the skeletal isomerization catalyst used in the skeletal isomerization reaction a conventional acid catalyst may be used, and zeolite, aluminum phosphate, tungsten oxide, or the like is preferably used. Most preferably, FER (ferrierite) type zeolite is used. Meanwhile, while the skeletal isomerization process is performed, a simple isomerization reaction may proceed to an equilibrium level to cause side reactions that partially generate 1-butene.
- polybutenes is difficult to prepare polybutenes containing high amounts of vinylidene and halogen components with 1-butene and other butenes (such as normal butene) contained in large amounts in the C4 mixture.
- 1-butene and other butenes such as normal butene contained in large amounts in the C4 mixture.
- 1-butene and other butenes included in the C4 mixture are reduced or eliminated, so that a high content of vinylidene and halogen
- reaction raw material for example, C4 mixture as shown in the composition of Table 3
- diluted C4 mixture for example, C4 mixture as shown in Table 7 below
- a polybutene manufacturing process is performed, in which polybutene is produced.
- a general polybutene having a content of vinylidene having a double bond at the terminal of less than 70 mol% may be polymerized using an aluminum trichloride catalyst, and the content of vinylidene exceeds 70 mol%.
- the reactive polybutene can be polymerized using a main catalyst such as boron trifluoride and a cocatalyst of alcohol or ether.
- a complex form consisting of a main catalyst and a cocatalyst, or a main catalyst and a cocatalyst are added directly to the polybutene polymerization reactor 30, respectively, or as a main catalyst and a cocatalyst.
- the complex form, or the main catalyst and the cocatalyst, which are formed alone, may be prepared and introduced into separate injection tanks, respectively, and then supplied to the polybutene polymerization reactor 30.
- the reaction heat is sufficiently removed to maintain the stability of the catalyst. It is preferably to be carried out at a low temperature of 10 °C or less, preferably 0 °C or less, more preferably -40 to -10 °C.
- the alcohol in the cocatalyst may be a primary, secondary or tertiary alcohol having 1 to 4 carbon atoms, and specific examples thereof include methanol, ethanol, isopropanol, normal propanol, isobutanol, tertiary butanol, and the like.
- a primary, secondary or tertiary ether having 2 to 8 carbon atoms may be used. Examples thereof include dimethyl ether, diethyl ether, diisopropyl ether, methyl propyl ether, and methyl isopropyl ether.
- methyl ethyl ether methyl butyl ether, methyl tertiary butyl ether, ethyl propyl ether, ethyl isopropyl ether, ethyl butyl ether, ethyl isobutyl ether and ethyl tertiary butyl ether.
- the above-listed ones may be used without limitation.
- the amount of catalyst used for the said polymerization reaction it is preferable to use main catalysts, such as boron trifluoride, at 0.02-1.0 weight part with respect to 100 weight part of reaction raw materials.
- main catalysts such as boron trifluoride
- the productivity per catalyst may be lowered and the economic efficiency may be low.
- the yield of the polybutene to be produced is lowered, which may also lower the economic efficiency.
- the polymerization reaction for preparing the polybutene may be performed by a conventional method, and the reaction temperature is maintained at -30 to 40 ° C, preferably -30 to 20 ° C, and the reaction The pressure is preferably maintained at 3 kg / cm 2 or more so that the reaction raw material can be maintained in the liquid state under the reaction temperature.
- the conversion rate of isobutene is 70% or more, preferably 80 to 90%, and it is advantageous economically to set the residence time required for obtaining the conversion rate to 5 to 100 minutes.
- the polybutene prepared according to the present invention has a number average molecular weight (Mn) of 300 to 5,000, the vinylidene content is 80 mol% or more (ie, 80% or more relative to the total number of double bonds).
- the polybutene may be polymerized with a catalyst mileage of 300 to 1200 g-polymer / g-catalyst.
- the method for producing polybutene according to the present invention in order to improve the use efficiency of isobutene raw material (recycling), as well as to dilute isobutene, as shown in Figure 1, polybutene polymerization reactor 30 ),
- the unreacted C4 recovered from the C4 distillation column 40 can be returned to two methods (A path and B path in FIG. 1) for recycling.
- Unreacted C4 recovered from the C4 distillation column 40 is 2 to 20% by weight, preferably 5 to 15% by weight, more preferably 8 to 12% by weight of isobutene and 3 to 20% by weight, preferably 5 to 15 weight percent, more preferably 8 to 12 weight percent of normal butene.
- the composition shown in Table 6 can be exemplified.
- the recycling method of unreacted C4 along the A route is described.
- the C4 mixture (reaction raw material) containing a high concentration of isobutene supplied to the polymerization reactor 30 can be diluted to facilitate polybutene polymerization (to a concentration suitable for polybutene polymerization).
- the recycling method of the unreacted C4 according to the B route is for improving the use efficiency of isobutene raw material (recycling), and in this case, all or part of the unreacted C4 is used in the isomerization reactor 10 or the isomerization reactor. It is returned to be mixed with the C4 mixture supplied to (10) and recycled. Meanwhile, the unreacted C4 may be simultaneously returned to the isomerization reactor 10 and the polybutene polymerization reactor 30 through the two paths.
- the high concentration of isobutene separated in the isomerization reactor is preferably diluted to an isobutene concentration of 25 to 65% by weight, preferably 25 to 60% by weight.
- it may have a composition similar to the following Table 7.
- the reason for diluting isobutene to lower the content (concentration) of isobutene in the C4 mixture is that if the content of isobutene is too high, the heat of reaction generated during polymerization in the polybutene polymerization reactor 30 is exchanged. This is because it is difficult to control.
- the content of isobutene in the C4 mixture is excessively low, making it difficult to prepare a high molecular weight polybutene, and the production yield is also too low, thereby lowering economic efficiency.
- the unreacted C4 may include organic substances such as alcohols or ethers containing oxygen (O) atoms, halogen acids, and the like, so that the adsorption tower 42 filled with an adsorbent is removed to remove them. It is desirable to install.
- organic substances such as alcohols or ethers containing oxygen (O) atoms, halogen acids, and the like, so that the adsorption tower 42 filled with an adsorbent is removed to remove them. It is desirable to install.
- Examples of the adsorbent packed in the adsorption tower 42 include calcium hydroxide (Ca (OH) 2), calcium oxide (CaO), calcium carbonate (CaCO 3), calcium chloride (CaCl 2), potassium hydroxide (KOH), potassium carbonate (K 2 CO 3) Potassium hydrogen carbonate (KHCO3), potassium chloride (KCl), sodium hydroxide (NaOH), sodium carbonate (Na2CO3), sodium bicarbonate (NaHCO3), solid silica, solid alumina, resin amine Anion exchange resins with groups and cation exchange resins with sulfone groups in resins, among which calcium hydroxide, which is insoluble in water after adsorbing halogen ions (X-), for example, fluorine ions (F-), , Calcium oxide, calcium carbonate, calcium chloride, solid silicas, solid aluminas and resins are preferred.
- Ca (OH) 2 calcium oxide
- CaCO 3 calcium chloride
- KOH potassium carbonate
- the adsorption tower 42 is provided with an adsorption tower for removing organic substances (oxygen organic substances) such as alcohols or ethers containing oxygen (O) atoms, and an adsorption tower for removing halogen acids, respectively. It is possible to improve the removal effect and process operation efficiency.
- organic substances oxygen organic substances
- O oxygen
- the adsorbent particles should be packed to an appropriate size to facilitate application to a tubular fixed bed reactor in the form of immobilizing the catalyst and flowing the reactant material, the size (diameter) of which is from 0.1 to 100 mm, preferably from 0.5 to 100 mm, more preferably 1 to 100 mm. In the case of fine powder particles smaller than 0.1 mm in diameter, it may be difficult to apply to the tubular fixed bed reactor, and in the case of particles larger than 100 mm in diameter, the adsorption efficiency may be drastically reduced.
- the particles of the adsorbent need to be processed (molded) in a certain form, for example, they can be processed into a spherical form, a cylinder form, a tablet form, and the like, of which a spherical form is most preferred.
- a spherical form is most preferred.
- CSTR Continuous Flow Stirred-Tank Reactor
- MFR mixed flow reactor
- a polybutene polymerization reactor 30, which is mixed with reaction C4, to which a diluted C4 mixture (reaction raw material) and a polymerization catalyst are fed and polymerized to produce a reactant.
- the production apparatus of the present invention the unreacted C4 distilled from the reactant and the remaining organic compounds, the unreacted C4 distillation column 40 and the unreacted C4 distillation column 40 unreacted and discharged and recovered from Adsorption tower (42) for removing organic substances and halogen acid included in the unreacted C4 before the C4 is sent back to the isomerization reactor 10 and / or polybutene polymerization reactor 30 for recycling
- the light polymer (LP) may further include a light polymer (LP) distillation column which is discharged and recovered to obtain the remaining polybutene.
- the effect of increasing the isobutene content in the C4 mixture (reaction raw material) is not limited to the production of polybutene.
- Ibutyl Isobutylene Isoprene Rubber
- ETB Ethylene Glycol mono-t-butyl Ether
- DETB Diethylene Glycol mono-t-butyl ether
- DIB Diisobutene
- the C4 mixture is fed to the isomerization reactor, in which the 1-butene isomerized to 2-butene by hydrogen isomerization reaction using an isomerization catalyst in the isomerization zone, and isobutene and 2 in the fractionation distillation zone.
- the butenes are fractionally distilled to separate;
- the C4 mixture containing 2-butene separated in the isomerization reactor is fed to the skeletal isomerization reactor, and a portion of the normal butene is skeletal isomerized to isobutene by skeletal isomerization using a skeletal isomerization catalyst, and the skeleton isomerization obtained therefrom.
- the mixture is fed to the isomerization reactor and recycled; And obtaining an isobutene raw material having an increased isobutene content from the fractional distillation zone.
- the C4 residue oil raw material (composition shown in Table 1) in which the butadiene was removed from the C4 mixture was injected into an isomerization reactor (column) filled with 200 g of a catalyst impregnated with platinum (0.5%) on an alumina support, and then 1 h ⁇ WHSV (weight hour space velocity) of 1, to conduct the isomerization and fractionation in the temperature, pressure of 8 bar for 60 °C, the reactor top to was ejected a C4 mixture of the composition shown in Table 3, the bottom of the reactor are provided in Table A C4 mixture of the same composition was ejected.
- the C4 mixture of the composition of Table 4 ejected to the bottom of the isomerization reactor was injected into the top of the skeletal isomerization reactor filled with 200 g of zeolite catalyst, having a WHSV of 5 h ⁇ 1 , a temperature of 300 ° C., and a pressure of 2 bar. Skeletal isomerization was performed by. After the completion of the skeletal isomerization reaction, the continuous process was carried out by injecting some of the unreacted C4 discharged and recovered from the C4 distillation column into the isomerization reactor together with the C4 mixture having the composition shown in Table 5 ejected to the bottom of the skeletal isomerization reactor. Was carried out.
- an isopropyl alcohol / boron trifluoride complex catalyst having 0.19 parts by weight based on 100 parts by weight of the reaction raw material (C4 mixture) having the composition as shown in Table 7 below. (1.5 mol) was injected continuously.
- the reaction temperature was -18 °C
- the reaction pressure was maintained at 3 kg / cm 2 or more to maintain the liquid phase, the average residence time was to be 30 minutes.
- the reaction was passed through a water bath using a neutralization tank treated with a 5% by weight caustic soda solution and a liquid bath, followed by washing with C4 at a temperature of 160 ° C and atmospheric pressure.
- the content and absolute amount of isobutene per unit raw material can be increased.
- the amount of polybutene polymerized is also greatly increased.
- the amount of catalyst used in the production of the product (polybutene) is also reduced by more than two times, which leads to an excellent reduction in the manufacturing cost, thereby increasing the amount of polybutene that can be produced in a single plant.
- the vinylidene content which is an important physical property of the highly reactive polybutene, is also excellent.
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Abstract
Description
이소부텐 | n-부탄 | 1-부텐 | C-2-부텐 | T-2-부텐 | i-부탄 | |
함량(중량%) | 46.5 | 9.9 | 26.2 | 4.5 | 9.4 | 3.5 |
이소부텐 | n-부탄 | 1-부텐 | C-2-부텐 | T-2-부텐 | i-부탄 | |
함량(중량%) | 35.4 | 16.1 | 35.0 | 2.3 | 7.5 | 3.7 |
이소부텐 | n-부탄 | 1-부텐 | C-2-부텐 | T-2-부텐 | i-부탄 | |
함량(중량%) | 92.9 | 0.9 | 0.6 | 0.2 | 0.3 | 5.1 |
이소부텐 | n-부탄 | 1-부텐 | C-2-부텐 | T-2-부텐 | i-부탄 | |
함량(중량%) | 1.6 | 27.6 | 0.5 | 23.3 | 46.3 | 0.7 |
이소부텐 | n-부탄 | 1-부텐 | C-2-부텐 | T-2-부텐 | i-부탄 | |
함량(중량%) | 29.5 | 29.1 | 10.5 | 10.5 | 19.7 | 0.7 |
이소부텐 | n-부탄 | 1-부텐 | C-2-부텐 | T-2-부텐 | i-부탄 | |
함량(중량%) | 10.0 | 39.3 | 7.2 | 0.9 | 1.6 | 41.0 |
이소부텐 | n-부탄 | 1-부텐 | C-2-부텐 | T-2-부텐 | i-부탄 | |
함량(중량%) | 53.0 | 17.2 | 4.4 | 4.0 | 3.3 | 18.1 |
촉매 마일리지 | 비닐리덴 함량(몰%) | 제품 수율 (폴리부텐/원료, %) | 폴리부텐 생성량(g) | |
실시예 3 | 608 | 90 | 56.8 | 568 |
실시예 4 | 683 | 90 | 56.5 | 565 |
실시예 5 | 832 | 89 | 55.3 | 553 |
비교예 1 | 276 | 85 | 38.1 | 381 |
비교예 2 | 173 | 83 | 21.0 | 210 |
Claims (17)
- C4 혼합물이 이성화 반응기에 공급되어, 상기 이성화 반응기의 이성화 영역에서는 이성화 촉매를 이용한 수소이성화 반응에 의해 1-부텐이 2-부텐으로 이성화되고, 분별 증류 영역에서는 이소부텐 및 2-부텐이 분별 증류되어 분리되는 단계;상기 이성화 반응기에서 분리된 2-부텐이 포함된 C4 혼합물이 골격 이성화 반응기로 공급되어, 골격 이성화 촉매를 이용한 골격 이성화 반응에 의해, 노르말부텐 중 일부가 이소부텐으로 골격 이성화되고, 이로부터 얻어진 골격 이성화 혼합물은, 상기 이성화 반응기로 공급되어 재순환되는 단계; 및상기 이성화 반응기에서 분리된 고농도의 이소부텐이 포함된 반응 원료 및 중합 촉매가 폴리부텐 중합 반응기에 공급되어, 중합 반응에 의해 폴리부텐이 생성되는 단계를 포함하는, 폴리부텐의 제조방법.
- 청구항 1에 있어서, 상기 중합 반응 후, 미반응 C4의 전체 또는 일부를, 상기 이성화 반응기 및/또는 폴리부텐 중합 반응기로 되돌려 보내 재순환시키는 단계를 더욱 포함하는, 폴리부텐의 제조방법.
- 청구항 2에 있어서, 상기 미반응 C4 전체 또는 일부가 상기 폴리부텐 중합 반응기로 재순환되어, 상기 이성화 반응기에서 분리된 고농도 이소부텐 원료의 이소부텐 함량이 25 내지 65 중량%의 농도로 희석되는 것인, 폴리부텐의 제조방법.
- 청구항 1에 있어서, 상기 미반응 C4의 이소부텐을 재활용 하기 위하여, 상기 미반응 C4를 상기 이성화 반응기로 재순환시키는 것인, 폴리부텐의 제조방법.
- 청구항 1에 있어서, 상기 중합 촉매는 주촉매, 조촉매 및 보조 조촉매를 포함하고, 상기 주촉매는 삼불화붕소, 삼염화붕소, 삼염화알루미늄 및 염화아연으로 이루어진 군으로부터 선택되는 루이스산이며, 상기 조촉매는 물 및 알코올 화합물로 이루어진 군으로부터 선택되며, 상기 보조 조촉매는 알킬에테르 화합물인 것인, 폴리부텐의 제조방법.
- 청구항 1에 있어서, 상기 폴리부텐 중합 반응 후 미반응 C4 중 이소부텐 함량이 2 내지 20 중량%인 것인, 폴리부텐의 제조방법.
- 청구항 1에 있어서, 상기 폴리부텐은 300 ~ 1200 g-polymer/ g-catalyst의 촉매 마일리지로 중합되는 것인, 폴리부텐의 제조방법.
- 청구항 1에 있어서, 상기 폴리부텐은, 이중결합이 말단에 위치한 비닐리덴의 함량이 70 몰% 이하인 일반 폴리부텐인 것인, 폴리부텐의 제조방법.
- 청구항 1에 있어서, 상기 폴리부텐은, 이중결합이 말단에 위치한 비닐리덴의 함량이 70 몰%를 초과하는 고반응성 폴리부텐이며, 분자량은 300 내지 5,000인 것인, 폴리부텐의 제조방법.
- 청구항 1에 있어서, 상기 중합 반응은 -30 내지 40 ℃의 온도 및 3 kg/cm2이상의 압력에서 5 내지 100 분의 체류 시간 동안 수행되는 것인, 폴리부텐의 제조방법.
- 청구항 1에 있어서, 상기 폴리부텐의 제조방법은, 흡착제가 구비된 불순물 흡착탑을 통하여, 상기 미반응 C4에 포함된 함산소 유기물질 및 할로겐 산을 제거하는 단계를 더욱 포함하는 것인, 폴리부텐의 제조방법.
- 청구항 11에 있어서, 상기 흡착제가, 수산화칼슘(Ca(OH)2),산화칼슘(CaO), 탄산칼슘(CaCO3),염화칼슘(CaCl2),수산화칼륨(KOH), 탄산칼륨(K2CO3),탄산수소칼륨(KHCO3),염화칼륨(KCl), 수산화나트륨(NaOH), 탄산나트륨(Na2CO3),탄산수소나트륨(NaHCO3),고체 실리카류(solid silica), 고체 알루미나류(solid alumina), 제올라이트류(Zeolite), 레진에 아민기가 붙어 있는 음이온 교환 수지 및 레진에 술폰기가 붙어 있는 양이온 교환 수지로 이루어진 군으로부터 선택된 화합물인 것인, 폴리부텐의 제조방법.
- 청구항 11에 있어서, 상기 흡착탑은, 상기 미반응 C4에 포함된 함산소 유기물질을 제거하는 흡착탑 및 할로겐 산(halogen acid)을 제거하는 흡착탑을 각각 구비하는 것인, 폴리부텐의 제조방법.
- C4 혼합물이 이성화 반응기에 공급되어, 상기 이성화 반응기의 이성화 영역에서는 이성화 촉매를 이용한 수소이성화 반응에 의해 1-부텐이 2-부텐으로 이성화되고, 분별 증류 영역에서는 이소부텐 및 2-부텐이 분별 증류되어 분리되는 단계;상기 이성화 반응기에서 분리된 2-부텐이 포함된 C4 혼합물이 골격 이성화 반응기로 공급되어, 골격 이성화 촉매를 이용한 골격 이성화 반응에 의해, 노르말부텐 중 일부가 이소부텐으로 골격 이성화되고, 이로부터 얻어진 골격 이성화 혼합물은, 상기 이성화 반응기로 공급되어 재순환되는 단계; 및상기 분별 증류 영역으로부터 증가된 이소부텐 함량의 이소부텐 원료를 얻는 단계를 포함하는 이소부텐의 증량방법.
- 청구항 14에 있어서, 상기 증가된 이소부텐 함량의 이소부텐 원료는, 이소부틸렌 이소프렌 러버(IIR), 에틸렌 글리콜 모노-터셔리-부틸 에테르(ETB), 디에틸렌 글리콜 모노-터셔리-부틸 에테르(DETB) 및 디이소부텐(DIB)으로 이루어진 군으로부터 선택되는 화합물의 제조 원료로 사용되는 것인, 이소부텐의 증량방법.
- 공급되는 C4 혼합물의 1-부텐이 이성화 반응에 의해 2-부텐으로 이성화되고, C4 혼합물의 이소부텐 및 2-부텐은 분별 증류되어 분리되는 이성화 반응기;상기 이성화 반응기에서 분리된 2-부텐이 포함된 C4 혼합물이 공급되어, 노르말부텐 중 일부가 이소부텐으로 골격 이성화되며, 이로부터 얻어진 골격 이성화 혼합물을 상기 이성화 반응기로 투입 및 재순환시키는 골격 이성화 반응기; 및상기 이성화 반응기에서 분리된 고농도의 이소부텐이 포함된 반응 원료 및 중합 촉매가 공급 및 중합되어 반응물을 생성하는 폴리부텐 중합 반응기를 포함하는, 폴리부텐 제조장치.
- 청구항 16에 있어서, 상기 반응물을 증류시킨 미반응 C4 및 잔여 유기화합물 중, 미반응 C4를 증류시켜 배출 및 회수하는 C4 증류탑;상기 C4 증류탑에서 배출된 미반응 C4를 상기 이성화 반응기 및/또는 폴리부텐 중합 반응기로 되돌려 보내 재순환시키기 전, 흡착제가 구비되어 상기 미반응 C4에 포함된 유기물질 및 할로겐 산을 제거하는 흡착탑; 및상기 C4 증류탑에서 공급되는 잔여 유기화합물 중, LP(light polymer)는 배출 및 회수하여, 나머지 폴리부텐을 얻을 수 있는 LP 증류탑을 더욱 포함하는, 폴리부텐 제조장치.
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SG11201701392VA SG11201701392VA (en) | 2014-08-22 | 2015-08-21 | Polybutene preparation method |
BR112017003296-1A BR112017003296B1 (pt) | 2014-08-22 | 2015-08-21 | Método de preparação de polibuteno |
JP2017510637A JP6673904B2 (ja) | 2014-08-22 | 2015-08-21 | ポリブテンの製造方法 |
MYPI2017700563A MY182242A (en) | 2014-08-22 | 2015-08-21 | Polybutene preparation method |
EP15833046.4A EP3184557B1 (en) | 2014-08-22 | 2015-08-21 | Polybutene preparation method |
CN201580045007.8A CN106604936A (zh) | 2014-08-22 | 2015-08-21 | 聚丁烯制备方法 |
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KR930006910B1 (ko) * | 1990-03-28 | 1993-07-24 | 재단법인 한국화학연구소 | 폴리부텐의 제조방법과 그 장치 |
JPH10231256A (ja) * | 1996-12-23 | 1998-09-02 | Inst Fr Petrole | 水素異性化反応蒸留および骨格異性化を組合せた高純度イソブテンの製造法 |
JP2002220411A (ja) * | 2001-01-29 | 2002-08-09 | Nippon Petrochem Co Ltd | ブテンポリマー処理における分解反応抑制方法 |
KR100851639B1 (ko) * | 2007-03-22 | 2008-08-13 | 대림산업 주식회사 | 고농도 이소부텐을 이용한 고반응성 폴리이소부텐의제조방법 |
KR20120096389A (ko) * | 2011-02-22 | 2012-08-30 | 대림산업 주식회사 | 글리콜 모노-터셔리-부틸에테르 화합물의 제조 방법 |
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GB9404368D0 (en) * | 1994-03-07 | 1994-04-20 | Bp Chem Int Ltd | Production of polyisobutenes |
US5981818A (en) * | 1995-03-21 | 1999-11-09 | Stone & Webster Engineering Corp. | Integrated cracking and olefins derivative process utilizing dilute olefins |
FR2733986B1 (fr) * | 1995-05-11 | 1997-06-13 | Inst Francais Du Petrole | Procede et installation pour la conversion de coupes c4 olefiniques en polyisobutenes et en propylene |
FR2757505B1 (fr) * | 1996-12-23 | 1999-02-19 | Inst Francais Du Petrole | Procede de production d'isobutene de haute purete combinant une distillation reactive d'hydroisomerisation, une distillation et une isomerisation squelettale |
GB9707075D0 (en) * | 1997-04-08 | 1997-05-28 | Bp Chem Int Ltd | Polymerisation process |
DE19952031A1 (de) * | 1999-10-28 | 2001-05-03 | Basf Ag | Verfahren zur Herstellung hochreaktiver Polyisobutene |
KR100486044B1 (ko) | 2000-11-13 | 2005-04-29 | 대림산업 주식회사 | 폴리부텐의 제조방법 |
KR20040014688A (ko) * | 2002-08-10 | 2004-02-18 | 주식회사 엑스텔테크놀러지 | 음성통신 단말기의 잡음제거장치 및 그 방법 |
DE10361633A1 (de) * | 2003-12-30 | 2005-07-28 | Basf Ag | Herstellung hochreaktiver Polyisobutene mit niedrigem Halogengehalt |
ATE444314T1 (de) * | 2005-07-12 | 2009-10-15 | Basf Se | Verfahren zur herstellung von polyisobuten hoher qualität |
US20100234542A1 (en) | 2006-06-06 | 2010-09-16 | Basf Se | Preparation of reactive, essentially halogen-free polyisobutenes from c4-hydrocarbon mixtures which are low in isobutene |
KR101458404B1 (ko) * | 2013-01-17 | 2014-11-05 | 대림산업 주식회사 | 폴리부텐의 제조 방법 |
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KR930006910B1 (ko) * | 1990-03-28 | 1993-07-24 | 재단법인 한국화학연구소 | 폴리부텐의 제조방법과 그 장치 |
JPH10231256A (ja) * | 1996-12-23 | 1998-09-02 | Inst Fr Petrole | 水素異性化反応蒸留および骨格異性化を組合せた高純度イソブテンの製造法 |
JP2002220411A (ja) * | 2001-01-29 | 2002-08-09 | Nippon Petrochem Co Ltd | ブテンポリマー処理における分解反応抑制方法 |
KR100851639B1 (ko) * | 2007-03-22 | 2008-08-13 | 대림산업 주식회사 | 고농도 이소부텐을 이용한 고반응성 폴리이소부텐의제조방법 |
KR20120096389A (ko) * | 2011-02-22 | 2012-08-30 | 대림산업 주식회사 | 글리콜 모노-터셔리-부틸에테르 화합물의 제조 방법 |
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BR112017003296A2 (pt) | 2017-11-28 |
US10202476B2 (en) | 2019-02-12 |
US20170267795A1 (en) | 2017-09-21 |
SG11201701392VA (en) | 2017-04-27 |
JP6673904B2 (ja) | 2020-03-25 |
CN106604936A (zh) | 2017-04-26 |
EP3184557A1 (en) | 2017-06-28 |
KR101658545B1 (ko) | 2016-09-21 |
MY182242A (en) | 2021-01-18 |
EP3184557A4 (en) | 2018-04-18 |
BR112017003296B1 (pt) | 2022-02-08 |
EP3184557C0 (en) | 2023-12-20 |
KR20160023321A (ko) | 2016-03-03 |
EP3184557B1 (en) | 2023-12-20 |
JP2017526779A (ja) | 2017-09-14 |
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