WO2002088103A1 - Procede de fabrication d'oxyde de propylene - Google Patents
Procede de fabrication d'oxyde de propylene Download PDFInfo
- Publication number
- WO2002088103A1 WO2002088103A1 PCT/JP2002/003848 JP0203848W WO02088103A1 WO 2002088103 A1 WO2002088103 A1 WO 2002088103A1 JP 0203848 W JP0203848 W JP 0203848W WO 02088103 A1 WO02088103 A1 WO 02088103A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- propylene
- propylene oxide
- reaction
- present
- cumene
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/02—Synthesis of the oxirane ring
- C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
- C07D301/19—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with organic hydroperoxides
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/02—Synthesis of the oxirane ring
- C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
- C07D301/14—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with organic peracids, or salts, anhydrides or esters thereof
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/32—Separation; Purification
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D303/00—Compounds containing three-membered rings having one oxygen atom as the only ring hetero atom
- C07D303/02—Compounds containing oxirane rings
- C07D303/04—Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the present invention relates to a method for producing propylene oxide. More specifically, the present invention relates to a method for producing propylene oxide, which can convert propylene to propylene oxide using cumene hydroperoxide as an oxygen carrier and can be carried out at a high yield. It is. Art
- the process of oxidizing propylene by using hydroxybenzene of ethylbenzene as an oxygen carrier to obtain propylene oxide and styrene is known as the Halcon method.
- cumyl alcohol is generated simultaneously with propylene oxide, and cumyl alcohol is dehydrated to ⁇ -methylstyrene or hydrogenated to cumene and then oxidized. By doing so, it can be returned to cumene hydroperoxide and used repeatedly.
- the problem to be solved by the present invention is to use propylene oxide as a carrier for oxygen using cumene hydroboxide.
- the present invention is directed to providing a method for producing propylene oxide which can be carried out at a high yield, and which is extremely advantageous especially from the viewpoint of industrial implementation. Obtaining propylene oxide by reacting propylene with cumene hydroperoxide in the presence; and
- a method for producing propylene oxide comprising a step of subjecting the reaction mixture obtained in the reaction step to distillation and recovering unreacted propylene from the top of the distillation column, wherein the temperature at the bottom of the distillation column is 20%.
- the present invention relates to a method for producing propylene oxide at 0 ° C or lower.
- FIG. 1 is a schematic flow chart of the manufacturing method according to the present invention.
- FIG. 2 is a schematic flow chart of the manufacturing method according to the present invention.
- Fresh cumene hydroperoxide solution is fed through line 1 and propylene is fed into the reaction process through line 2.
- reaction solution flowing out of the reaction step is supplied to the recovery step through line 3
- propylene is recycled to the reaction step through line 5 by distillation
- propylene consumed in the reaction step is supplied through line 6.
- the reaction solution containing propylene oxide from which propylene has been recovered in the recovery step is sent to the next step via line 4.
- the reaction step in the present invention refers to a step of producing propylene oxide by reacting propylene with a peroxide at a cumenehydride port in the presence of a catalyst.
- propylene oxide is obtained by performing an epoxidation reaction between propylene and cumene hydride peroxide obtained by autoxidation of cumene with an oxygen-containing gas such as air or oxygen-enriched air in the presence of a catalyst.
- a catalyst comprising a titanium-containing silicon oxide.
- These catalysts are preferably so-called titanium-silica catalysts containing titanium chemically bonded to silicon oxide.
- a titanium compound supported on a silica carrier, a compound compounded with a silicon oxide by a coprecipitation method or a sol-gel method, or a zeolite compound containing titanium can be used.
- cumene hydroperoxide used as a starting material in the reaction step may be a dilute or concentrated purified product or a non-purified product.
- the reaction step in the present invention can be carried out in a liquid phase using a solvent.
- the solvent is liquid at the temperature and pressure at the time of the reaction and is substantially inert to the reactants and products.
- the solvent may consist of the substances present in the cumenehydride peroxide solution used.
- cumene can be used as a solvent instead of adding a solvent.
- Other useful solvents include aromatic monocyclic compounds (eg, benzene, toluene, cyclobenzene, orthodichlorobenzene) and alkanes (eg, octane, decane, dodecane).
- the reaction temperature in the reaction step in the present invention is generally 0 to 200 ° C, but is 25 to 200 ° C. A temperature of C is preferred.
- the pressure is usually from 100 to 2000 kPa, but a pressure of from 100 to 100 kPa is preferable in consideration of the reaction temperature and economy.
- the reaction step in the present invention can be advantageously carried out using a catalyst in the form of a slurry or a fixed bed. For large-scale industrial operations, it is preferred to use a fixed bed. It can be carried out by a batch method, a semi-continuous method, a continuous method, or the like. When the liquid containing the reactants is passed through the fixed bed, the liquid mixture leaving the reaction zone contains no or substantially no catalyst.
- the catalyst layer when used in the form of a fixed bed, the catalyst layer may be multi-staged, and fresh cumene hydroperoxide or propylene may be divided and fed to each catalyst layer.
- the effluent reactant from the outlet of each catalyst layer may be recycled and used at the inlet of the catalyst layer. This method is effective for preventing the runaway of the reaction due to the heat generated by the reaction and for performing the reaction stably at a high yield.
- the propylene used in the reaction step of the present invention is usually 1 to 20 times, preferably 5 to 5 times the molar amount of fresh cumene hydroperoxide used in the epoxidation reaction. ⁇ 20 times the molar amount. Using an excess of propylene with respect to fresh cumene hydrooxide is effective in maintaining a high yield of propylene oxide produced.
- Propylene to be subjected to the reaction step in the present invention is usually at a concentration of at least 70% by weight, preferably at least 80% by weight.
- Other impurities may include components that are substantially inert to the epoxidation reaction, such as propane, ethane, ethylene, methane, and propylene oxide.
- the reaction mixture obtained in the reaction step is subjected to distillation, and unreacted propylene is recovered from the top of the distillation column. It is necessary that the operating tower bottom temperature of the distillation tower is 200 ° C or less. When the temperature at the bottom reaches 200 ° C or higher, dimerization of unreacted propylene in the column generates hydrocarbons having 6 carbon atoms, not only loss of propylene but also propylene in the next step. In the oxide purification process, a large amount of energy is required for separation by distillation.
- Examples of a method of lowering the bottom temperature include a method of lowering the operating pressure and a method of collecting a part of propylene at the bottom to lower the bottom boiling point.
- a method of lowering the operating pressure In order to lower the bottom temperature by lowering the operating pressure, if the bottom temperature is to be lowered below 50 ° C, a high vacuum of 0.07 MPa or less will be required, and the condensation temperature of propylene recovered from the top Is less than 50 ° C below zero, it is difficult to implement industrially. Therefore, when the operating pressure is lowered to lower the tower bottom temperature, the range of the tower bottom temperature is usually 50 to 200 ° C, preferably 80 to 200 ° C, and more preferably 1 to 200 ° C. The temperature is from 00 to 200 ° C.
- the operating temperature is 2.0MPa or higher.
- Propylene recovered from the bottom can be easily recovered.
- propylene oxide-containing liquid containing propylene is subjected to recovery step 2 as a distillation column through line 7, and propylene obtained from the top is condensed and liquefied, and the pressure is increased by a pump.
- Propylene loss by reducing or increasing the pressure by a compressor to recover and recycle propylene through line 11 or directly through line 9 to the reaction process.
- recovering propylene in two or more distillation columns is effective for suppressing a decrease in propylene yield.
- the reaction solution obtained in the reaction step was placed in a 150 cc pressure vessel, and then propylene was injected thereinto to dissolve it, and 0.2% by weight of cumene hydroperoxide was added.
- a mixed solution consisting of 0.2% by weight and 28.6% by weight of propylene was prepared and heated at a temperature shown in Table 1 for 0.5 hour in a closed system. After 0.5 hour, the amount of propylene dimer in the liquid produced was measured by gas chromatography. Table 1 shows the measurement results.
- propylene is converted to propylene oxide using cumene oxide peroxide as an oxygen carrier, and Propylene oxide, which has the excellent features of being able to carry out the process of obtaining propylene oxide from propylene with high yield, and of reducing the load on the purification process of propylene oxide as a product Can be provided.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Epoxy Compounds (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP02718608A EP1382601A4 (en) | 2001-04-27 | 2002-04-18 | PROCESS FOR PRODUCTION OF PROPYLENE OXIDE |
KR10-2003-7013962A KR20040030596A (ko) | 2001-04-27 | 2002-04-18 | 프로필렌 옥사이드의 제조방법 |
US10/475,998 US20040133018A1 (en) | 2001-04-27 | 2002-04-18 | Process for producing propylene oxide |
CA002445342A CA2445342A1 (en) | 2001-04-27 | 2002-04-18 | Process for producing propylene oxide |
BR0209197-6A BR0209197A (pt) | 2001-04-27 | 2002-04-18 | Processo para produção de óxido de propileno |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2001132004A JP2002322167A (ja) | 2001-04-27 | 2001-04-27 | プロピレンオキサイドの製造方法 |
JP2001-132004 | 2001-04-27 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2002088103A1 true WO2002088103A1 (fr) | 2002-11-07 |
Family
ID=18980090
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2002/003848 WO2002088103A1 (fr) | 2001-04-27 | 2002-04-18 | Procede de fabrication d'oxyde de propylene |
Country Status (9)
Country | Link |
---|---|
US (1) | US20040133018A1 (ja) |
EP (1) | EP1382601A4 (ja) |
JP (1) | JP2002322167A (ja) |
KR (1) | KR20040030596A (ja) |
CN (1) | CN1505616A (ja) |
BR (1) | BR0209197A (ja) |
CA (1) | CA2445342A1 (ja) |
TW (1) | TW528753B (ja) |
WO (1) | WO2002088103A1 (ja) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1484326A1 (en) * | 2002-02-15 | 2004-12-08 | Sumitomo Chemical Company, Limited | Method for recovering propylene oxide |
Families Citing this family (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2008266304A (ja) * | 2007-03-22 | 2008-11-06 | Sumitomo Chemical Co Ltd | プロピレンオキサイドの製造方法 |
CN105272941B (zh) * | 2014-07-24 | 2018-05-11 | 中国石油化工股份有限公司 | 环氧丙烷的生产方法 |
CN105330504B (zh) * | 2014-07-24 | 2017-10-27 | 中国石油化工股份有限公司 | 回收精制丙烯的装置 |
CN105294604B (zh) * | 2014-07-24 | 2017-12-15 | 中国石油化工股份有限公司 | 生产环氧丙烷的装置 |
TWI660942B (zh) | 2014-07-24 | 2019-06-01 | 大陸商中國石油化工科技開發有限公司 | Method and device for recovering refined propylene |
CN105272806B (zh) * | 2014-07-24 | 2017-07-14 | 中国石油化工股份有限公司 | 丙烯回收的方法 |
CN105294379B (zh) * | 2014-07-24 | 2017-10-27 | 中国石油化工股份有限公司 | 丙烯回收设备 |
CN105272939A (zh) * | 2014-07-24 | 2016-01-27 | 中国石油化工股份有限公司 | 环氧丙烷生产方法 |
CN105315238B (zh) * | 2014-07-24 | 2018-02-13 | 中国石油化工股份有限公司 | 环氧丙烷的生产设备 |
CN105272813A (zh) * | 2014-07-24 | 2016-01-27 | 中国石油化工股份有限公司 | 丙烯回收方法 |
CN105272808B (zh) * | 2014-07-24 | 2017-10-27 | 中国石油化工股份有限公司 | 丙烯回收的设备 |
CN105439792B (zh) * | 2014-07-24 | 2018-01-09 | 中国石油化工股份有限公司 | 回收精制丙烯的方法 |
US11691955B2 (en) | 2021-08-30 | 2023-07-04 | Saudi Arabian Oil Company | Process for recovering propylene oxide and carbon dioxide in PPC polyol production |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4992566A (en) * | 1989-08-31 | 1991-02-12 | Texaco Chemical Company | Recovery of tertiary butyl hydroperoxide and tertiary butyl alcohol |
US5319114A (en) * | 1993-09-23 | 1994-06-07 | Arco Chemical Technology, L. P. | Olefin epoxidation using a carbon molecular sieve impregnated with a transition metal |
JPH09169751A (ja) * | 1995-12-20 | 1997-06-30 | Sumitomo Chem Co Ltd | プロピレンオキシドの回収方法 |
US5849938A (en) * | 1997-09-02 | 1998-12-15 | Arco Chemical Technology, L.P. | Separation of methanol and propylene oxide from a reaction mixture |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3350422A (en) * | 1966-02-01 | 1967-10-31 | Halcon International Inc | Catalytic epoxidation of an olefinically unsaturated compound using an organic hydroperoxide as an epoxidizing agent |
US3580819A (en) * | 1969-04-21 | 1971-05-25 | Shell Oil Co | Recovery of propylene and propylene oxide by selective separation with plural stage distillation,propylene oxide absorption and subsequent distillation |
US3947500A (en) * | 1969-11-07 | 1976-03-30 | Halcon International, Inc. | Process for treating reaction mixtures by chemical reduction |
-
2001
- 2001-04-27 JP JP2001132004A patent/JP2002322167A/ja not_active Withdrawn
-
2002
- 2002-04-18 KR KR10-2003-7013962A patent/KR20040030596A/ko not_active Application Discontinuation
- 2002-04-18 EP EP02718608A patent/EP1382601A4/en not_active Withdrawn
- 2002-04-18 WO PCT/JP2002/003848 patent/WO2002088103A1/ja not_active Application Discontinuation
- 2002-04-18 BR BR0209197-6A patent/BR0209197A/pt not_active Application Discontinuation
- 2002-04-18 CA CA002445342A patent/CA2445342A1/en not_active Abandoned
- 2002-04-18 US US10/475,998 patent/US20040133018A1/en not_active Abandoned
- 2002-04-18 CN CNA028089588A patent/CN1505616A/zh active Pending
- 2002-04-22 TW TW091108244A patent/TW528753B/zh not_active IP Right Cessation
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4992566A (en) * | 1989-08-31 | 1991-02-12 | Texaco Chemical Company | Recovery of tertiary butyl hydroperoxide and tertiary butyl alcohol |
US5319114A (en) * | 1993-09-23 | 1994-06-07 | Arco Chemical Technology, L. P. | Olefin epoxidation using a carbon molecular sieve impregnated with a transition metal |
JPH09169751A (ja) * | 1995-12-20 | 1997-06-30 | Sumitomo Chem Co Ltd | プロピレンオキシドの回収方法 |
US5849938A (en) * | 1997-09-02 | 1998-12-15 | Arco Chemical Technology, L.P. | Separation of methanol and propylene oxide from a reaction mixture |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1484326A1 (en) * | 2002-02-15 | 2004-12-08 | Sumitomo Chemical Company, Limited | Method for recovering propylene oxide |
Also Published As
Publication number | Publication date |
---|---|
EP1382601A4 (en) | 2005-09-14 |
JP2002322167A (ja) | 2002-11-08 |
CN1505616A (zh) | 2004-06-16 |
KR20040030596A (ko) | 2004-04-09 |
BR0209197A (pt) | 2004-06-08 |
CA2445342A1 (en) | 2002-11-07 |
US20040133018A1 (en) | 2004-07-08 |
EP1382601A1 (en) | 2004-01-21 |
TW528753B (en) | 2003-04-21 |
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