WO2014112768A1 - 폴리부텐의 제조 방법 - Google Patents
폴리부텐의 제조 방법 Download PDFInfo
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- WO2014112768A1 WO2014112768A1 PCT/KR2014/000391 KR2014000391W WO2014112768A1 WO 2014112768 A1 WO2014112768 A1 WO 2014112768A1 KR 2014000391 W KR2014000391 W KR 2014000391W WO 2014112768 A1 WO2014112768 A1 WO 2014112768A1
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- WO
- WIPO (PCT)
- Prior art keywords
- polybutene
- butene
- raw material
- isobutene
- fractional distillation
- Prior art date
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Classifications
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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
- 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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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/13—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation with simultaneous isomerisation
-
- 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
- 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
- C08F10/10—Isobutene
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/32—Selective hydrogenation of the diolefin or acetylene compounds
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/12—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
- C10G69/126—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step polymerisation, e.g. oligomerisation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/02—Stabilising gasoline by removing gases by fractioning
Definitions
- the present invention relates to a process for producing polybutene, and more particularly, to a process for economically producing high quality polybutene with low fluorine content and high vinylidene content with high catalyst mileage.
- Polybutene is a polymerized olefin component having 4 carbon atoms (C4) derived from hydrocarbon decomposition process using a Friedel-Craft type catalyst.
- the number average molecular weight (Mn) is about 300 to 5000. to be.
- the isobutene is mainly used in the production of methyl t-butylether (MTBE) or polybutene, which is used as an octane number enhancer, and isobutene has the highest reactivity of isobutene among the olefin components. Consists mainly of isobutene units.
- polybutene was mainly used as an adhesive, an adhesive or an insulating oil, a low reactivity product was preferred, and such a low reactivity polybutene is called a conventional polybutene (Conventional PIB).
- a polar group is introduced into polybutene and used as an anti-scuff agent, a viscosity index improver, or the like of an engine oil, or mixed with a fuel of an internal combustion engine such as an automobile and used as a cleaning agent.
- the highly reactive polybutene is referred to as High Reactive Polyisobutylene (HRPIB).
- PIBSA polyisobutenyl succinic anhydride
- HRPIB reactive polybutene
- the double bond is located inside the polybutene, and the number of alkyl groups substituted in the double bond is large, and in the case of general polybutene (Conventional PIB) having low reactivity due to steric hindrance, chlorine gas is used to form polybutene. After the chlorination reaction, it is reacted with maleic anhydride to prepare PIBSA.
- a method of controlling the polymerization conditions of the polybutene so that a double bond is positioned at the terminal of the polybutene is used.
- the double bond located at the terminal of the polybutene is called vinylidene
- the compound having a vinylidene content of 70% or more is called high reactive polybutene
- the compound having a vinylidene content of about 40 to 70% is referred to as an intermediate reactive polybutene ( MVPIB, Mid Vinylidene Polyisobutylene)
- a compound having a vinylidene content of 3 to 40% is called general polybutene.
- boron trifluoride (BF 3 ) is generally used as a catalyst, and alcohols, ether compounds and the like are generally used as a promoter.
- AlCl 3 the aluminum trichloride
- the product quality, product productivity per unit catalyst, and product productivity per unit raw material decrease due to normal butenes contained in the raw material, and the higher the isobutene content in the raw material, the higher the product quality and product productivity per unit catalyst. In addition, product productivity per unit raw material is improved.
- 5,674,955 discloses pretreatment of raw materials containing at least 5% by weight of 1-butene to reduce the content of 1-butene by at least 20% by weight than the initial content, and polybutene using a halogenated catalyst.
- a method for producing polybutene having a high vinylidene content and a low halogen content is disclosed.
- isomerized 2-butene still lowers catalyst activity and catalyst mileage.
- U.S. Patent No. 6,207,115 discloses the selective hydrogenation of diolefins (Ex. Butadiene) using an Olefin Conversion Unit (OCU), at the same time isomerizing 1-butene to 2-butene, followed by polybutene polymerization. And to produce propylene by Metathesis of 2-butene and ethylene.
- this method also has the disadvantage of low catalyst mileage, since polybutene is produced in the presence of large amounts of 2-butene.
- the C4 fraction produced during catalytic cracking of heavy oil and the C4 residue produced during pyrolysis of naphtha include 20 to 50 wt% of 1-butene or 2-butene component, and the C4 olefin
- the polybutene is manufactured using the components as it is, there is a disadvantage in that the halogen content in the product is high and the vinylidene content is low.
- a large amount of normal butene components such as 1-butene present in the C4 olefin component (raw material) lowers the catalytic activity, lowers the quality of the polybutene, or lowers the product productivity per unit raw material.
- the method of preparing (isolating) isobutene from a C4 mixture includes t-butyl alcohol (t-Butyl Alcohol: TBA) Dehydration method, Methyl t-Butyl Ether (MTBE) cracking method for adding methanol to isobutene using an acid catalyst and then cracking again to obtain isobutene, iso Butane dehydrogenation (Dehydrogenation) method and the like, all of the above methods are expensive to manufacture (separation) of isobutene, there is a disadvantage that the price of polybutene increases.
- TBA t-Butyl Alcohol
- MTBE Methyl t-Butyl Ether
- An object of the present invention is to provide a method for producing polybutene which can economically produce high-quality and high-reactivity polybutene having a low halogen content such as fluorine and high terminal vinylidene content with high catalyst mileage.
- Another object of the present invention is to provide a method for producing polybutene having excellent productivity per unit raw material or per unit catalyst.
- the present invention in the petroleum refining process for cracking crude oil or C4 hydrocarbon components generated in the naphtha cracking plant, selectively hydrogenated the diolefin, and at the same time isomerized 1-butene to 2-butene Then, separating the isobutene raw material through fractional distillation; And it provides a method for producing polybutene comprising the step of polymerizing the isobutene raw material obtained by the fractional distillation.
- a C4 hydrocarbon raw material generated from a petroleum refining process or naphtha cracking plant (NCC) which decomposes crude oil is used as it is, or 1-butene in this raw material is simply isomerized to 2-butene.
- NCC naphtha cracking plant
- diolefin for example, butadiene
- NCC naphtha cracking center
- the most reactive diolefin component that is, 1,3-butadiene
- the isomerization reaction of 1-butene to 2-butene is hydrogen isomerization converting 1-butene and 1-butene already present in the C4 hydrocarbon component into 2-butene generated by the conversion of the diolefin. (hydroisomerisation) reaction.
- the hydrogenation reaction of the diolefin and the isomerization reaction of 1-butene to 2-butene may be performed by supplying hydrogen gas to the C4 hydrocarbon component in the presence of a metal catalyst.
- a periodic table group 10 metal such as Ni, Pd, or Pt may be used, and the metal catalyst may be supported on a carrier.
- the amount of hydrogen used depends on the diolefin content in the C4 hydrocarbon component, preferably above the theoretical stoichiometry necessary for converting the diolefin to normal butene, preferably slightly above the theoretical amount. It can be used in an amount of, for example, 1 to 1.2 equivalents, preferably 1 to 1.1 equivalents, based on the diolefin. If the amount of hydrogen used is too high, the diolefin is converted to normal butane, which is not preferable.
- the temperature of the hydrogenation reaction and the hydroisomerization reaction is usually 20 to 200 °C, preferably 50 to 150 °C, more preferably 60 to 150 °C, the reaction pressure is 0.1 to 5 MPa, preferably 0.5 to 4 MPa More preferably 0.5 to 3 MPa.
- Conditions for the hydrogenation reaction and hydroisomerization reaction are disclosed in detail in US Pat. No. 6,207,115, the disclosure of which is incorporated herein by reference.
- Fractional distillation is a method of separating various liquid mixtures by boiling point (boiling point) using a fractional distillation column.
- the isobutene raw material obtained by the fractional distillation (isolated) has isobutene as its main component and contains trace amounts of 1-butene and 2-butene, but most of the normal butene components (1-butene, etc.) are removed, Relatively high purity isobutene.
- the number of stages, the operating temperature, the operating pressure, and the like of the distillation tower can be enumerated.
- the number of stages of the distillation tower for obtaining an isobutene raw material suitable for the present invention is 20 to 150 stages, preferably 50 to 130 stages, more preferably 70 to 130 stages, and the tower stage is less than 20 stages. This lowers and the purity of isobutene (IB) may fall, and when it exceeds 150 steps, the apparatus cost more than necessary will arise.
- Said fractional distillation temperature is 0-100 degreeC, Preferably it is 10-80 degreeC, More preferably, it is 20-80 degreeC.
- the fractional distillation pressure is 0 to 30 atm, preferably 2 to 15 atm, more preferably 3 to 10 atm, even more preferably 5 to 10 atm. When the fractional distillation pressure is 0 atm, it means a vacuum.
- the composition of the C4 residue oil removed by selective hydrogenation of diolefin and acetylene is shown in Table 2 below.
- the C4 residue oil of the components shown in Table 2 below contains a large amount of normal butene components (such as 1-butene, C (cis) or T (trans) -2-butene), and therefore high reactivity of high vinylidene and low halogen content Polybutene production is difficult
- an isobutene raw material obtained through simple isomerization obtained by selectively hydrogenating diolefin and acetylene by using an olefin conversion unit (OCU, Olefin Conversion Unit) and isomerizing 1-butene to 2-butene.
- OCU Olefin Conversion Unit
- the composition of the isobutene raw material is shown in Table 3 below.
- the isobutene raw material manufactured (separated) as mentioned above is polymerized by a conventional method to produce polybutene.
- the method for producing polybutene from the isobutene raw material includes a method of preparing general polybutene using an aluminum trichloride (AlCl 3 ) catalyst, and a highly reactive polybutene using a boron trifluoride (BF 3 ) catalyst and a promoter. And methods for preparing the intermediate reactive polybutenes. Since a method for producing a general polybutene using an aluminum trichloride catalyst is well known, a brief description of a method for producing a highly reactive polybutene using a boron trifluoride (BF 3 ) catalyst is given here.
- a promoter (alcohol, ether, etc.) and boron trifluoride (BF 3 ) may be directly introduced into the reactor together or prepared in a complex form in a separate tank and introduced into the reactor.
- the alcohol compound used as the cocatalyst may be a primary, secondary or tertiary alcohol having 1 to 4 carbon atoms, for example, methanol, ethanol, isopropanol, normal propanol, isobutanol, tert-butanol, etc.
- ether compound used as the cocatalyst a primary, secondary or tertiary ether having 2 to 8 carbon atoms may be used.
- dimethyl ether, diethyl ether, diisopropyl ether, methyl Propyl ether, 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, ethyl tertiary butyl ether and the like can be used.
- the promoter may be used alone or in combination of two or more.
- the complex compound may be easily prepared by adding a promoter alone or in the form of a mixture into a tank, and then introducing boron trifluoride gas.
- the complex formation reaction of boron trifluoride and alcohol is an exothermic reaction, it is preferable to remove the heat of reaction in order to reduce the risk of decomposition and explosion of the catalyst.
- the complexing reaction is preferably performed at a low temperature of 10 ° C. or less, more preferably 0 ° C. or less, most preferably ⁇ 40 ° C. to ⁇ 10 ° C., so that the heat of reaction is sufficiently removed to maintain catalyst stability.
- the amount of the catalyst used is preferably used so that the amount of boron trifluoride in the catalyst component is 0.05 to 1.0 parts by weight based on 100 parts by weight of isobutene in the isobutene raw material.
- the use amount of the boron trifluoride exceeds 1.0 parts by weight, a product having a molecular weight that is too low is obtained, the productivity per catalyst is lowered and there is no economical efficiency. I can't.
- the polymerization (reaction) temperature of the highly reactive polybutene is generally -30 to 20 °C
- the polymerization (reaction) pressure is set to maintain the isobutene raw material in the liquid state at the reaction temperature, usually 3 kg / cm 2 or more to be.
- the conversion of isobutene is at least 70%, more preferably about 80-95%.
- the residence time required for obtaining the above conversion rate is generally 5 to 100 minutes, and outside the above range, it is economically undesirable.
- a high reactivity polybutene may be obtained by performing a subsequent process such as neutralization commonly performed in the art.
- the highly reactive polybutenes prepared according to the invention have a number average molecular weight (Mn) of 300 to 5000, a vinylidene content of at least 80% and a conversion of isobutene at least 85%.
- a highly reactive polybutene having a vinylidene content (a ratio of double bonds (vinylidene) located at the terminal of polybutene among the total double bonds present in polybutene) is 70% or more.
- MVPIB intermediate reactive polybutene
- conventional polybutene Conventional Polyisobutylene
- polybutene In the production of polybutene, in particular in the production of highly reactive polybutene having a vinylidene content of 80% or more and an isobutene conversion of 85% or more, a conventional boron trifluoride complex catalyst is used and conventionally high purity isobutane If the ten is separated and used, the raw material cost increases too much, and the product is not competitive. However, if polybutene is prepared using the isobutene raw material separated according to the present invention, high-quality polybutenes of low fluorine content and high vinylidene content, as well as general polybutene, can be economically produced with high catalyst mileage.
- the high reactivity polybutene of the high vinylidene content prepared according to the present invention not only increases the content of the active ingredient which plays a clean role in the production of lubricants, fuel cleaners, etc., but also has a low halogen content, and therefore, a detergent and a lubricant additive. There is an advantage that can prevent reactor corrosion that may occur during manufacture.
- Diolefin (butadiene) is selectively hydrogenated in a petroleum refining process or a naphtha cracking plant (NCC) raw material to decompose crude oil, and at the same time, 1-butene isomerized to 2-butene, and then fractional distillation.
- NCC naphtha cracking plant
- Butadiene was removed from the C4 hydrocarbon raw material generated in the naphtha cracking plant (NCC) to obtain C4 residue oil-1 (Raffinate-1) consisting of the components shown in Table 2, which was used as an isobutene raw material.
- C4 residue oil-1 Raffinate-1
- isobutene raw materials of the components shown in Table 2 were continuously injected, and the polymerization temperature (reaction temperature), catalyst (BF 3 ) and cocatalysts (methanol and ethanol) shown in Table 4 below And diisopropyl ether) to polymerize polybutene (Comparative Examples 1 and 2).
- diolefin butadiene
- 1-butene simply isomerized to 2-butene.
- the isobutene raw material which consists of a component shown to the obtained.
- isobutene raw materials of the components shown in Table 3 were continuously injected, and the polymerization temperature (reaction temperature), catalyst (BF 3 ) and cocatalysts (methanol and ethanol) shown in Table 4 below And diisopropyl ether) to polymerize polybutene (Comparative Examples 3 and 4).
- promoter / BF 3 represents the ratio of the mole number of promoter / mole of BF 3 .
- the polybutene prepared according to Examples 1 to 4 of the present invention has a vinylidene content of 88% or more (higher is better), an F content of 10 ppm or less (lower is better), high quality and high Meets reactive conditions.
- Comparative Examples 1 and 2 when C4 residue oil-1 is used as a raw material, although the raw material cost is low, the amount of catalyst and cocatalyst used is high, the yield of product is low, and the product cost is rather increased. There is a disadvantage in that the physical properties of the produced polybutene are lowered.
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Abstract
Description
성 분 | 이소부텐 | n-부탄 | 1-부텐 | C-2-부텐 | T-2-부텐 | i-부탄 |
함량(중량%) | 45.2 | 0.4 | 1.9 | 0.1 | 0.9 | 51.3 |
성 분 | 이소부텐 | n-부탄 | 1-부텐 | C-2-부텐 | T-2-부텐 | i-부탄 |
함량(중량%) | 49.5 | 10.9 | 24.8 | 4.2 | 9.3 | 2.9 |
성 분 | 이소부텐 | n-부탄 | 1-부텐 | C-2-부텐 | T-2-부텐 | i-부탄 |
함량(중량%) | 44.9 | 10.9 | 1.7 | 14.2 | 23.4 | 4.9 |
실시예1 | 실시예2 | 실시예3 | 실시예4 | 비교예1 | 비교예2 | 비교예3 | 비교예4 | |
메탄올 | 1.70 | 1.0 | 1.7 | |||||
에탄올 | 1.65 | 1.0 | 1.65 | 2.0 | 1.65 | |||
IPE | 0.6 | 0.55 | ||||||
조촉매/BF3 Mole Ratio | 1.7 | 1.65 | 1.60 | 1.55 | 1.65 | 2.0 | 1.7 | 1.65 |
반응 후 IB 함량(%) | 7.5 | 8.6 | 9.0 | 8.4 | 14.6 | 14.3 | 8.2 | 8.4 |
IB 전환율(%) | 93 | 92 | 91 | 92 | 83 | 83 | 92 | 92 |
반응온도(℃) | -25 | -25 | -18 | -18 | -25 | -25 | -25 | -25 |
촉매 마일리지 (PIB/BF3) | 634 | 610 | 603 | 642 | 412 | 162 | 240 | 266 |
Vinyldene(%) | 88.3 | 89.3 | 90.5 | 90.3 | 80.2 | 85.6 | 86.0 | 87.8 |
F(ppm) | 6 | 4 | 3 | 4 | 41 | 31 | 5 | 4 |
Mn(MWD) | 1830 (1.85) | 2350 (1.90) | 1060 (1.34) | 1370 (1.47) | 2250 (1.88) | 1270 (1.55) | 1980 (1.79) | 2410 (1.88) |
Claims (8)
- 원유를 분해하는 석유 정제 과정 혹은 납사분해설비에서 발생하는 C4 탄화수소 성분 중, 디올레핀을 선택적으로 수소 첨가 반응시키고, 동시에 1-부텐을 2-부텐으로 이성화한 후, 분별 증류를 통해 이소부텐 원료를 분리하는 단계; 및상기 분별 증류로 얻은 이소부텐 원료를 중합하는 단계를 포함하는 폴리부텐의 제조 방법.
- 청구항 1에 있어서, 상기 폴리부텐은 비닐리덴 함량이 70% 이상인 고반응성 폴리부텐, 비닐리덴 함량이 40 내지 70%인 중간 반응성 폴리부텐 및 비닐리덴 함량이 3 내지 40%인 일반 폴리부텐으로 이루어진 군으로부터 선택되는 것인, 폴리부텐의 제조방법.
- 청구항 2에 있어서, 상기 일반 폴리부텐은 삼염화알루미늄 촉매를 사용하여 제조되고, 상기 고반응성 폴리부텐 및 중간 반응성 폴리부텐은 삼불화붕소(BF3) 촉매 및 조촉매를 사용하여 제조되는 것인, 폴리부텐의 제조방법.
- 청구항 3에 있어서, 상기 조촉매는 탄소수 1 내지 4의 1차, 2차 또는 3차 알코올 또는 탄소수 2 내지 8의 1차, 2차 또는 3차 에테르인 것인, 폴리부텐의 제조방법.
- 청구항 1에 있어서, 상기 이소부텐 원료의 중합 온도는 -30 내지 20 ℃이고, 중합 압력은 3 kg/cm2 이상이며, 체류 시간은 5 내지 100분인 것인, 폴리부텐의 제조방법.
- 청구항 1에 있어서, 상기 디올레핀의 수소 첨가 반응 및 1-부텐의 이성화 반응은, 금속 촉매의 존재 하에서, 상기 C4 탄화수소 성분으로 수소 가스를 공급하여 수행되는 것인, 폴리부텐의 제조방법.
- 청구항 1에 있어서, 상기 분별 증류 단계는, 증류 타워 단수 20 내지 150단, 분별 증류 온도 20 내지 80 ℃, 및 분별 증류 압력 2 내지 10 기압으로 이소부텐 원료를 분리하는 것인 폴리부텐의 제조방법.
- 청구항 1 내지 청구항 7의 어느 한 항에 따른 제조방법으로 얻어지는 폴리부텐.
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CN201480005295.XA CN105073795A (zh) | 2013-01-17 | 2014-01-14 | 一种制备聚丁烯的方法 |
US14/801,357 US9683060B2 (en) | 2013-01-17 | 2015-07-16 | Method for preparing polybutene |
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KR101658545B1 (ko) * | 2014-08-22 | 2016-09-21 | 대림산업 주식회사 | 폴리부텐의 제조방법 |
US9617366B1 (en) | 2016-03-03 | 2017-04-11 | Tpc Group Llc | Low-fluoride, reactive polyisobutylene |
WO2017151341A1 (en) | 2016-03-03 | 2017-09-08 | Tpc Group Llc | Low-fluoride, reactive polyisobutylene |
US9617363B1 (en) | 2016-03-03 | 2017-04-11 | Tpc Group Llc | Low-fluoride, reactive polyisobutylene |
KR102589091B1 (ko) | 2017-07-27 | 2023-10-16 | 사빅 글로벌 테크놀러지스 비.브이. | 연료 첨가제의 제조 방법 |
WO2019180585A1 (en) | 2018-03-19 | 2019-09-26 | Sabic Global Technologies B.V. | Method of producing a fuel additive |
US11427518B2 (en) | 2018-03-19 | 2022-08-30 | Saudi Arabian Oil Company | Method of producing a fuel additive |
CN111989387B (zh) | 2018-04-19 | 2022-09-06 | 沙特基础工业全球技术有限公司 | 生产燃油添加剂的方法 |
EP3790944B1 (en) | 2018-05-07 | 2023-06-14 | SABIC Global Technologies B.V. | Method of producing a fuel additive |
EP3790854A1 (en) | 2018-05-07 | 2021-03-17 | SABIC Global Technologies B.V. | Method of producing a fuel additive |
CN112135809A (zh) | 2018-05-18 | 2020-12-25 | 沙特基础工业全球技术有限公司 | 利用水合单元生产燃料添加剂的方法 |
EP3853192B1 (en) | 2018-09-18 | 2024-03-13 | SABIC Global Technologies B.V. | Process for the production of fuel additives |
CN113056490B (zh) * | 2019-01-18 | 2023-07-28 | 株式会社Lg化学 | 聚丁烯的分离方法 |
US20230167208A1 (en) | 2021-11-30 | 2023-06-01 | Braskem S.A. | Heterogeneous catalyst for highly-reactive polyisobutylene |
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MY170215A (en) | 2019-07-09 |
SA515360793B1 (ar) | 2018-01-04 |
US9683060B2 (en) | 2017-06-20 |
EP2947102A1 (en) | 2015-11-25 |
EP2947102A4 (en) | 2016-08-17 |
EP2947102B1 (en) | 2018-03-21 |
KR20140092996A (ko) | 2014-07-25 |
BR112015017093B1 (pt) | 2021-01-19 |
SG11201505498YA (en) | 2015-09-29 |
CN105073795A (zh) | 2015-11-18 |
US20150322181A1 (en) | 2015-11-12 |
KR101458404B1 (ko) | 2014-11-05 |
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