WO2004018089A1 - Vorrichtung zur herstellung von propylen aus methanol - Google Patents
Vorrichtung zur herstellung von propylen aus methanol Download PDFInfo
- Publication number
- WO2004018089A1 WO2004018089A1 PCT/EP2003/004290 EP0304290W WO2004018089A1 WO 2004018089 A1 WO2004018089 A1 WO 2004018089A1 EP 0304290 W EP0304290 W EP 0304290W WO 2004018089 A1 WO2004018089 A1 WO 2004018089A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- reaction
- methanol
- separating
- reaction mixture
- stages
- Prior art date
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0496—Heating or cooling the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
- B01J8/0085—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction promoting uninterrupted fluid flow, e.g. by filtering out particles in front of the catalyst layer
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
- B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
-
- 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 invention relates to a device for the production of propylene from methanol, consisting of a Nor reaction stage equipped with a highly active and highly selective ⁇ -aluminum oxide catalyst for forming a Nor, reaction mixture containing methanol, DfmethyleÜ ⁇ er (DME) and water vapor from methanol at operating temperatures of 250 to 460 ° C, several, preferably two or three successively arranged reaction stages each equipped with a shape-selective zeolite catalyst of the pentasil type for the reaction of the Nor reaction mixture at inlet temperatures of 400 to 460 ° C and pressures of 0.5 to 3.0 bar (abs), heat exchangers between the reaction stages for cooling the emerging reaction mixture to a temperature of 400 to ⁇ 460 ° C, several heat exchangers installed after the last reaction stage for cooling the emerging reaction mixture to a temperature of 100 to 200 ° C, a subsequent separation process device for separating the reaction mixture into a gas and a predominantly water-containing liquid phase, a compressor for compressing the gas phase
- the synthesis gas obtained from natural gas is used for the production of hydrogen, for example for use in refineries and fuel cells, for the production of Fischer-Tropsch products such as pure fuels, lubricants, waxes and ⁇ -olefins, for the production of DME, for example for use in gas turbines and fuel cells and especially for the production of methanol as a starting material for the extraction of formaldehyde, solvents, methyl tertiary butyl ether, pure fuels, acetic acid, olefins, etc.
- reaction product and the remaining portion of the methanol / water / DME stream are fed to a second and third reaction stage in order to produce further propylene
- Three reaction conditions prevailing ner process conditions are selected so that a max imal conversion of methanol to propylene.
- the product mixture is then cooled and the gas, organic liquid and water phases separated.
- the gas phase is then compressed, the traces of water, CO and DME are removed from it and propylene with a purity of at least 97% is obtained.
- the resulting olefin streams, which are free of propylene, are returned to the process circuit and serve as an additional source for the production of propylene.
- reaction stages each consist of a horizontal container with axially attached inlet and outlet connections, in the middle of which the horizontal catalyst bed made of pentasil type zeolite catalyst flows from top to bottom.
- the pressure losses per reaction stage given by the catalyst bed and the pressure losses at the inlet and outlet of the container, are in the range from 250 to 480 mbar.
- each reaction stage is given thermal insulation.
- the object of the present invention is to simplify the process of the device for producing propylene from methanol described at the outset, to keep the pressure loss over the catalyst bed as low as possible and to largely avoid sealing problems and heat losses to the outside.
- reaction stages equipped with the zeolite catalyst are accommodated vertically one above the other in a standing reactor vessel and the heat exchanger with the inlet opening, the cross-section of which corresponds to the cross-section of the catalyst bed, is directly attached between the reaction stages connects the underside of the reaction stage or is arranged at a short distance therefrom.
- the arrangement of the reaction stages and heat exchangers according to the invention in a vertical reactor vessel considerably reduces the pressure loss and considerably reduces the technical outlay by eliminating numerous pipes and fittings.
- a portion of the methanol / water / DME stream is fed between the reaction stages, mixed with the reaction product of the previous implementation stage and then fed to the corresponding heat exchangers.
- the height of the catalyst bed is 500 to 1000 mm in order to minimize the pressure loss here too, and thus to avoid channel formation and edge movement.
- the volume between two reaction stages is designed so that the pressure loss between the heat exchanger and the subsequent catalyst bed decreases significantly and the conversion of kinetic energy into pressure energy takes place without interference.
- Fig. 1 shows a longitudinal section through a reactor vessel with three reaction stages.
- FIG. 2 shows an enlarged detail (X) from FIG. 1
- Fig. 3 is a schematic process representation for the implementation of the pre-reaction mixture consisting of methanol / DME and water using the reactor vessel with three reaction stages
- FIGS. 1 and 2 In a standing reactor vessel (1) with inlet (2) and outlet opening (3) for the gas flow, three reaction stages (4, 5, 6) are arranged according to FIGS. 1 and 2, each of which consists of a support (7 ), an overlying support grid (8) with a mesh size of 1/4 "and a 300 m thick layer (9) arranged above it made of ceramic balls made of SiO and Al O 3.
- the balls of the first 100 mm of this layer have a Diameter of 1/2 ", the balls of the second 100 mm of this layer have a diameter of 1/4" and the balls of the third 100 mm of this layer have a diameter of 1/8 ".
- a 750 mm thick catalyst bed (10) from extra data of 1/16 "diameter and 1/8" length is supported, which is covered with a 200 mm thick layer (11) of ceramic spheres with a diameter of 1 / 2 "and one Wire mesh (12) is covered.
- a heat exchanger (13, 14) is suspended in the cross section of the container (1).
- the cross section of the inlet opening of the heat exchangers (13, 14) corresponds to the cross section of the underside of the respective catalyst bed.
- vaporous methanol is passed via line (15) into the pre-reactor (16).
- the majority of the methanol (80%) is converted to DME and water in an exothermic adiabatic reaction on a ⁇ -aluminum oxide fixed bed catalyst.
- the methanol / DME / water mixture is divided into three partial streams, of which the first partial stream via line (17) of the first reaction stage (4), the second partial stream via line (18) the heat exchanger arranged after the first reaction stage (4) ( 13) and the third partial stream via line (19) is fed to the heat exchanger (14) attached after the second reaction stage (5), the main reaction of DME and remaining methanol adiabatic to a hydrocarbon-containing product mixture and further water at temperatures of 480.degree he follows.
- Hot steam is added to the methanol / DME / water mixture flowing via line (17) via line (20), so that the mixture is preheated to 440 ° C. Since the reaction taking place in the three reaction stages (4,5,6) is exothermic, the gas stream emerging from the first and second reaction stages (4,5) is cooled to a temperature of 450 ° C. and that from the. third reaction stage (6) via line (21) emerging gas stream to a temperature of 110 ° C each by means of a heat exchanger (13,14,22).
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2003227673A AU2003227673A1 (en) | 2002-07-25 | 2003-04-25 | Device for producing propylene from methanol |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10233975.9 | 2002-07-25 | ||
DE10233975A DE10233975A1 (de) | 2002-07-25 | 2002-07-25 | Vorrichtung zur Herstellung von Propylen aus Methanol |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2004018089A1 true WO2004018089A1 (de) | 2004-03-04 |
Family
ID=30128410
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2003/004290 WO2004018089A1 (de) | 2002-07-25 | 2003-04-25 | Vorrichtung zur herstellung von propylen aus methanol |
Country Status (3)
Country | Link |
---|---|
AU (1) | AU2003227673A1 (de) |
DE (1) | DE10233975A1 (de) |
WO (1) | WO2004018089A1 (de) |
Cited By (31)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7205376B2 (en) | 2004-05-04 | 2007-04-17 | General Electric Company | Processes for the production of cumene, polyetherimides, and polycarbonates |
US7465845B2 (en) | 2004-12-22 | 2008-12-16 | Exxonmobil Chemical Patents Inc. | Increasing ethylene and/or propylene production in an oxygenate to olefins reaction systems |
US7678953B2 (en) | 2005-01-31 | 2010-03-16 | Exxonmobil Chemical Patents Inc. | Olefin oligomerization |
US7678954B2 (en) | 2005-01-31 | 2010-03-16 | Exxonmobil Chemical Patents, Inc. | Olefin oligomerization to produce hydrocarbon compositions useful as fuels |
US7741526B2 (en) | 2006-07-19 | 2010-06-22 | Exxonmobil Chemical Patents Inc. | Feedstock preparation of olefins for oligomerization to produce fuels |
CN101869819A (zh) * | 2010-06-18 | 2010-10-27 | 王伟跃 | 一种由含氧化合物制备丙烯的反应器 |
DE102010042216A1 (de) | 2010-10-08 | 2011-06-09 | Basf Se | Verfahren zur Hemmung der unerwünschten radikalischen Polymerisation von in einer flüssigen Phase P befindlicher Acrylsäure |
CN102190546A (zh) * | 2010-03-03 | 2011-09-21 | 中国石油化工股份有限公司 | 甲醇转化制丙烯和芳烃的方法 |
US8049054B2 (en) | 2006-05-19 | 2011-11-01 | Shell Oil Company | Process for the preparation of C5 and/or C6 olefin |
CN101239872B (zh) * | 2007-02-07 | 2011-11-30 | 中国石油化工股份有限公司 | 提高低碳烯烃选择性的方法 |
US8083815B2 (en) | 2008-12-22 | 2011-12-27 | Shell Oil Company | Process to prepare methanol and/or dimethylether |
CN102345848A (zh) * | 2011-06-30 | 2012-02-08 | 神华集团有限责任公司 | 适用于煤基甲醇制丙烯工艺的提高工艺蒸汽塔负荷的方法及系统 |
US8168842B2 (en) | 2006-05-19 | 2012-05-01 | Shell Oil Company | Process for the alkylation of a cycloalkene |
US8269056B2 (en) | 2007-11-19 | 2012-09-18 | Shell Oil Company | Process for the preparation of an olefinic product |
CN103028434A (zh) * | 2011-09-29 | 2013-04-10 | 中国石油化工股份有限公司 | 甲醇转化制丙烯的催化剂及其制备方法 |
CN103030504A (zh) * | 2011-09-29 | 2013-04-10 | 中国石油化工股份有限公司 | 丙烯的生产方法 |
CN103623859A (zh) * | 2013-12-06 | 2014-03-12 | 陕西煤化工技术工程中心有限公司 | 高空速下获得高丙乙比的甲醇制丙烯催化剂及其制备方法 |
CN104109072A (zh) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | 甲醇制烯烃的反应装置及其应用 |
US8884090B2 (en) | 2007-11-19 | 2014-11-11 | Shell Oil Company | Process for the preparation of an olefin |
CN106010626A (zh) * | 2016-07-08 | 2016-10-12 | 成都赛普瑞兴科技有限公司 | 一种等温法甲醇转化制稳定轻烃的工艺 |
WO2017202040A1 (zh) * | 2016-05-25 | 2017-11-30 | 上海交通大学 | 一种甲醇制丙烯的反应再生系统和方法 |
US9856183B2 (en) | 2013-01-31 | 2018-01-02 | Shanghai Bi Ke Clean Energy Technology Co., Ltd. | Catalyst with high C4 olefin selectivity for preparing olefin from methanol and preparation method thereof |
WO2018072141A1 (zh) | 2016-10-19 | 2018-04-26 | 中国科学院大连化学物理研究所 | 一种由含氧化合物制备丙烯、c4烃类的快速流化床反应器、装置及方法 |
WO2018072142A1 (zh) | 2016-10-19 | 2018-04-26 | 中国科学院大连化学物理研究所 | 一种制备丙烯、c4烃类的方法及其装置 |
WO2018072140A1 (zh) | 2016-10-19 | 2018-04-26 | 中国科学院大连化学物理研究所 | 一种制备丙烯和c4烃类的方法及其装置 |
WO2018072139A1 (zh) | 2016-10-19 | 2018-04-26 | 中国科学院大连化学物理研究所 | 一种由含氧化合物制备丙烯和c4烃类的湍动流化床反应器、装置及方法 |
WO2020020697A1 (de) | 2018-07-26 | 2020-01-30 | Basf Se | Verfahren zur hemmung der unerwünschten radikalischen polymerisation von in einer flüssigen phase p befindlicher acrylsäure |
WO2021191042A1 (de) | 2020-03-26 | 2021-09-30 | Basf Se | Verfahren zur hemmung der unerwünschten radikalischen polymerisation von in einer flüssigen phase p befindlicher acrylsäure |
WO2023196289A1 (en) | 2022-04-06 | 2023-10-12 | ExxonMobil Technology and Engineering Company | Isoparaffinic kerosene compositions |
WO2023196305A1 (en) | 2022-04-06 | 2023-10-12 | ExxonMobil Technology and Engineering Company | Isoparaffinic and iso-olefinic distillate compositions |
WO2024027452A1 (zh) * | 2022-08-01 | 2024-02-08 | 润和催化剂股份有限公司 | 一种甲醇转化制丙烯的工艺方法和反应系统 |
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DE102005015923B4 (de) * | 2005-04-06 | 2014-12-04 | Air Liquide Global E&C Solutions Germany Gmbh | Verfahren zur Herstellung von C2- bis C4-Olefinen aus einem Oxygenate und Wasserdampf enthaltenden Einsatzstrom |
DE102005048931B8 (de) | 2005-10-13 | 2015-06-18 | Air Liquide Global E&C Solutions Germany Gmbh | Verfahren und Anlage zur Herstellung von C2-C4-Olefinen aus Methanol und/oder Dimethylether |
US7687671B2 (en) | 2005-12-05 | 2010-03-30 | Uop Llc | Integrated oxygenate conversion and product cracking |
DE102006026103B4 (de) | 2006-06-03 | 2010-05-06 | Lurgi Gmbh | Reaktor zur Herstellung von C2- bis C8- Olefinen aus einem Oxygenat, Wasserdampf und einen oder mehrere Kohlenwasserstoffe enthaltendem Stoffstrom |
DE102008061300A1 (de) | 2008-12-11 | 2010-07-08 | Lurgi Gmbh | Verfahren zum Herstellen eines C3H6 und C2H4 enthaltenden Produkts |
CN105949021B (zh) * | 2016-05-25 | 2019-01-18 | 上海交通大学 | 一种由甲醇催化脱水制备丙烯的系统和方法 |
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EP0088494A1 (de) * | 1982-02-05 | 1983-09-14 | Mobil Oil Corporation | Verfahren zur Umwandlung von Methanol in Olefine |
US4542252A (en) * | 1984-07-20 | 1985-09-17 | Mobil Oil Corporation | Multi-stage adiabatic process for methanol conversion to light olefins |
US4988431A (en) * | 1986-09-17 | 1991-01-29 | Linde Aktiengesellschaft | Process for performing catalytic reactions |
US6033633A (en) * | 1993-04-05 | 2000-03-07 | Catalytic Distillation Technologies | Boiling point reactor with heat removal |
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DE2221288C3 (de) * | 1972-04-29 | 1975-04-17 | Deggendorfer Werft Und Eisenbau Gmbh, 8360 Deggendorf | Reaktionsapparat zur Durchführung katalytischer Reaktionen in mehreren Stufen |
DE10027159A1 (de) * | 2000-05-31 | 2001-12-13 | Mg Technologies Ag | Verfahren zum Erzeugen von Propylen aus Methanol |
-
2002
- 2002-07-25 DE DE10233975A patent/DE10233975A1/de not_active Ceased
-
2003
- 2003-04-25 AU AU2003227673A patent/AU2003227673A1/en not_active Abandoned
- 2003-04-25 WO PCT/EP2003/004290 patent/WO2004018089A1/de not_active Application Discontinuation
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
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EP0088494A1 (de) * | 1982-02-05 | 1983-09-14 | Mobil Oil Corporation | Verfahren zur Umwandlung von Methanol in Olefine |
US4542252A (en) * | 1984-07-20 | 1985-09-17 | Mobil Oil Corporation | Multi-stage adiabatic process for methanol conversion to light olefins |
US4988431A (en) * | 1986-09-17 | 1991-01-29 | Linde Aktiengesellschaft | Process for performing catalytic reactions |
US6033633A (en) * | 1993-04-05 | 2000-03-07 | Catalytic Distillation Technologies | Boiling point reactor with heat removal |
Cited By (44)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7205376B2 (en) | 2004-05-04 | 2007-04-17 | General Electric Company | Processes for the production of cumene, polyetherimides, and polycarbonates |
US7465845B2 (en) | 2004-12-22 | 2008-12-16 | Exxonmobil Chemical Patents Inc. | Increasing ethylene and/or propylene production in an oxygenate to olefins reaction systems |
US7678953B2 (en) | 2005-01-31 | 2010-03-16 | Exxonmobil Chemical Patents Inc. | Olefin oligomerization |
US7678954B2 (en) | 2005-01-31 | 2010-03-16 | Exxonmobil Chemical Patents, Inc. | Olefin oligomerization to produce hydrocarbon compositions useful as fuels |
US8049054B2 (en) | 2006-05-19 | 2011-11-01 | Shell Oil Company | Process for the preparation of C5 and/or C6 olefin |
US8168842B2 (en) | 2006-05-19 | 2012-05-01 | Shell Oil Company | Process for the alkylation of a cycloalkene |
US7741526B2 (en) | 2006-07-19 | 2010-06-22 | Exxonmobil Chemical Patents Inc. | Feedstock preparation of olefins for oligomerization to produce fuels |
CN101239872B (zh) * | 2007-02-07 | 2011-11-30 | 中国石油化工股份有限公司 | 提高低碳烯烃选择性的方法 |
US8269056B2 (en) | 2007-11-19 | 2012-09-18 | Shell Oil Company | Process for the preparation of an olefinic product |
US8822749B2 (en) | 2007-11-19 | 2014-09-02 | Shell Oil Company | Process for the preparation of an olefinic product |
US8884090B2 (en) | 2007-11-19 | 2014-11-11 | Shell Oil Company | Process for the preparation of an olefin |
US8083815B2 (en) | 2008-12-22 | 2011-12-27 | Shell Oil Company | Process to prepare methanol and/or dimethylether |
CN102190546A (zh) * | 2010-03-03 | 2011-09-21 | 中国石油化工股份有限公司 | 甲醇转化制丙烯和芳烃的方法 |
CN101869819A (zh) * | 2010-06-18 | 2010-10-27 | 王伟跃 | 一种由含氧化合物制备丙烯的反应器 |
DE102010042216A1 (de) | 2010-10-08 | 2011-06-09 | Basf Se | Verfahren zur Hemmung der unerwünschten radikalischen Polymerisation von in einer flüssigen Phase P befindlicher Acrylsäure |
WO2012045738A1 (de) | 2010-10-08 | 2012-04-12 | Basf Se | Verfahren zur hemmung der unerwünschten radikalischen polymerisation von in einer flüssigen phase p befindlicher acrylsäure |
US9212122B2 (en) | 2010-10-08 | 2015-12-15 | Basf Se | Process for inhibiting unwanted free-radical polymerization of acrylic acid present in a liquid phase P |
CN102345848A (zh) * | 2011-06-30 | 2012-02-08 | 神华集团有限责任公司 | 适用于煤基甲醇制丙烯工艺的提高工艺蒸汽塔负荷的方法及系统 |
CN102345848B (zh) * | 2011-06-30 | 2014-01-29 | 神华集团有限责任公司 | 适用于煤基甲醇制丙烯工艺的提高工艺蒸汽塔负荷的方法及系统 |
CN103028434B (zh) * | 2011-09-29 | 2015-10-21 | 中国石油化工股份有限公司 | 甲醇转化制丙烯的催化剂及其制备方法 |
CN103030504A (zh) * | 2011-09-29 | 2013-04-10 | 中国石油化工股份有限公司 | 丙烯的生产方法 |
CN103028434A (zh) * | 2011-09-29 | 2013-04-10 | 中国石油化工股份有限公司 | 甲醇转化制丙烯的催化剂及其制备方法 |
US9856183B2 (en) | 2013-01-31 | 2018-01-02 | Shanghai Bi Ke Clean Energy Technology Co., Ltd. | Catalyst with high C4 olefin selectivity for preparing olefin from methanol and preparation method thereof |
CN104109072A (zh) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | 甲醇制烯烃的反应装置及其应用 |
CN104109072B (zh) * | 2013-04-16 | 2017-03-15 | 中国石油化工股份有限公司 | 甲醇制烯烃的反应装置及其应用 |
CN103623859A (zh) * | 2013-12-06 | 2014-03-12 | 陕西煤化工技术工程中心有限公司 | 高空速下获得高丙乙比的甲醇制丙烯催化剂及其制备方法 |
WO2017202040A1 (zh) * | 2016-05-25 | 2017-11-30 | 上海交通大学 | 一种甲醇制丙烯的反应再生系统和方法 |
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WO2021191042A1 (de) | 2020-03-26 | 2021-09-30 | Basf Se | Verfahren zur hemmung der unerwünschten radikalischen polymerisation von in einer flüssigen phase p befindlicher acrylsäure |
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WO2024030163A2 (en) | 2022-04-06 | 2024-02-08 | ExxonMobil Technology and Engineering Company | Isoparaffinic and iso-olefinic distillate compositions |
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