EP2013194A2 - Procédé de production d'oxyde d'éthylène dans un réacteur à microcanaux - Google Patents

Procédé de production d'oxyde d'éthylène dans un réacteur à microcanaux

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Publication number
EP2013194A2
EP2013194A2 EP07727831A EP07727831A EP2013194A2 EP 2013194 A2 EP2013194 A2 EP 2013194A2 EP 07727831 A EP07727831 A EP 07727831A EP 07727831 A EP07727831 A EP 07727831A EP 2013194 A2 EP2013194 A2 EP 2013194A2
Authority
EP
European Patent Office
Prior art keywords
microchannel reactor
reactor
ethylene oxide
microchannel
ethylene
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP07727831A
Other languages
German (de)
English (en)
Inventor
Torsten Mäurer
Markus Gitter
Frank Rosowski
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
BASF SE
Original Assignee
BASF SE
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Priority to EP07727831A priority Critical patent/EP2013194A2/fr
Publication of EP2013194A2 publication Critical patent/EP2013194A2/fr
Withdrawn legal-status Critical Current

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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
    • C07D301/04—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen
    • C07D301/08—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen in the gaseous phase
    • C07D301/10—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with air or molecular oxygen in the gaseous phase with catalysts containing silver or gold
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00781—Aspects relating to microreactors

Definitions

  • the present invention relates to an improved process for the production of ethylene oxide (EO) in a microchannel reactor, wherein an ethylene-containing material stream and an oxygen or oxygen source-containing material stream fed to the microchannel reactor and in the catalyst-containing microchannel reactor, the reaction takes place to ethylene oxide.
  • EO ethylene oxide
  • ethylene oxide from ethylene is assigned in principle to the reaction class of the epoxidations, which is to be understood as a subclass of the oxidations. Furthermore, a distinction between these terms is not made, which is to be understood by the term oxidation of ethylene, the epoxidation of ethylene.
  • US 2006/0036106 describes the preparation of ethylene oxide by reaction in a microchannel reactor. In general, this procedure may be advantageous, e.g. an improved heat dissipation and an intensified contact of the educt molecules (ethylene and oxygen source) possible.
  • a process for the production of ethylene oxide has been found in a microchannel reactor, wherein an ethylene-containing stream and an oxygen or oxygen source-containing material stream fed to the microchannel reactor and in the catalyst-containing microchannel reactor, the reaction takes place to ethylene oxide, which characterized characterized is that continuously fed to the microchannel reactor alkyl halides in a total concentration of 0.3 to 50 volume ppm, based on the total volume flow of all introduced into the reactor streams.
  • a process for the production of ethylene oxide has been found in a microchannel reactor, wherein an ethylene-containing stream and an oxygen or oxygen source-containing material stream fed to the microchannel reactor and in the catalyst-containing microchannel reactor, the reaction is carried out to ethylene oxide, which is characterized in that nitrogen-containing compounds in a total concentration of 0.3 to 50 ppm by volume, based on the total volume flow of all material streams introduced into the reactor, are continuously fed to the microchannel reactor.
  • the total volume flow to which the concentrations of alkyl halides or nitrogen-containing compounds according to the invention refer here is to be understood as meaning the total volume flow of all material streams introduced into the reactor, in particular O 2, ethylene and optionally contained inert gas components, for example N 2, methane, and If necessary, further existing impurities such as CO2, CO, Ar and H 2 O.
  • the proportion of CO2 possibly present in the total flow of material supplied to the microchannel reactor is suitably kept low. It has been found that a CO 2 concentration of less than 2% by volume, in particular less than 1% by volume, in the microchannel reactor is particularly advantageous for the effectiveness of the inventive production process of ethylene oxide by oxidation of ethylene.
  • both alkyl halides and nitrogen-containing compounds can be fed, the total concentration of these two additional added streams is 0.6-100 ppm by volume, based on the total volume flow of all introduced into the reactor streams, the proportion of alkyl halides prefers about between see 0.1 and 1, more preferably between 0.3 and 1 based on the two supplied streams is.
  • the targeted, continuous addition of alkyl halides and / or nitrogen-containing compounds in the concentration range according to the invention substantially improves the selectivity of the catalyst.
  • the feed of alkyl halides and / or nitrogen-containing compounds according to the invention reduces the formation of CO.sub.2 by total oxidation of ethylene. This advantageously achieves an increase in selectivity of 0.1-10% compared to a process for the oxidation of ethylene to ethylene oxide in the microchannel reactor without the introduction of alkyl halides and / or nitrogen-containing compounds.
  • the activity of the catalyst can be influenced or adjusted by the feed, since it can lead to the formation of a catalyst phase favorable for the oxidation of ethylene.
  • EP 266015 page 11, Table 2 it is disclosed to feed 0.3 to 20 ppm by volume of an alkyl halide as a reaction moderator.
  • Examples which are mentioned in EP 266015, page 11, line 3 1, 2-dichloroethane, vinyl chloride or chlorinated polyphenyl compounds.
  • the concentration range according to the invention proves to be particularly advantageous in the production process for ethylene oxide in a microchannel reactor.
  • concentration of alkyl halide and / or nitrogen-containing compound depends on the specific conditions.
  • the material stream to be supplied according to the invention to alkyl halides or nitrogen-containing compounds depends on the temperature, composition of the feed gas, type of catalysts used and the molecular structure of the alkyl halide or the nitrogen-containing compound.
  • microchannel reactors are suitable for carrying out the process according to the invention.
  • Tube (bundle) or fluidized bed reactors offer microchannel reactors inherent safety, i.e., due to the very small dimensions of the reaction channels (dimension in at least one spatial direction ⁇ 3mm, preferably 1mm). a spread of flames or explosions is not possible (falling below the minimum quench diameter).
  • a reactor design for maximum explosion pressures is eliminated.
  • microchannel reactors allow for more precise temperature control such that e.g. suppresses the formation of hot spots and a driving style with an optimally selected axial temperature profile can be made possible. The passage of the reactor is effectively prevented.
  • Microchannel reactors or microreactors are generally understood to mean reactors whose characteristic dimensions of the reaction channels, i. the dimensions in at least one spatial direction, e.g. Height or width or diameter, in the range of a few microns to a few millimeters, preferably ⁇ 3 mm.
  • microchannel reactors are in principle suitable for reactions with fast kinetics (removal of diffusion limitations), strong heat of reaction (better temperature control) and explosive substances (blown through reactions or explosions not possible). Possibly.
  • microchannel reactors By using microchannel reactors a process intensification (higher space-time yields, product yields, selectivities) is possible. As a result both investment costs (smaller, more compact devices) and variable costs (raw material costs) can be reduced.
  • the inventive design of the production process of ethylene oxide using microchannel reactors advantageously a process intensification can be achieved. This leads u.a. to an increased productivity of the catalyst, i. In the microchannel reactor, an increased space-time yield is achieved compared to conventional tubular reactors at a defined temperature with the same catalyst.
  • the alkyl halides used in the microchannel reactor are preferably vinyl chloride, ethyl chloride, ethylene dichloride or mixtures thereof as reaction moderators. Particularly preferred is ethyl chloride.
  • an increase in the alkyl halide concentration during operation for performance optimization makes sense.
  • nitrogen-containing compounds are NH3, NO, NO2, N2O, N2O3, N2O3, organic nitro compounds such as e.g. Nitromethane, nitroethane, 1- or 2-nitropropane. Particularly preferred is the use of NO.
  • the feeding of nitrogen-containing compounds takes place in particular in combination with a nitrate or nitrite promotion, e.g. Alkali metal nitrate promotion, preferably KNO3, the catalytically active material.
  • a nitrogen-containing compound in a total concentration of 0.3 to 50 ppm by volume, based on the total volume of all introduced into the reactor reactants in particular O2, ethylene and optionally inert gas, such as N2, methane, and if necessary further (in cycle gas) contaminants such as CO2, CO, Ar and H2O.
  • ethylene and optionally inert gas such as N2, methane
  • further (in cycle gas) contaminants such as CO2, CO, Ar and H2O.
  • an increase in the selectivity of 0.1-5% is advantageously achieved in comparison with a process for the oxidation of ethylene to ethylene oxide in the microchannel reactor without feeding nitrogen-containing compound.
  • higher alkanes in the feed such as ethane, propane, butanes and even higher alkanes suppress the positive effect of the alkyl halides fed in.
  • the concentration of the sum of higher alkanes in the feed is therefore preferably less than 5% by volume, more preferably less than 1% by volume. Particularly preferred is a concentration of the sum of higher alkanes in the feed less than 500 ppm by volume.
  • the performance enhancement of the EO catalysts according to the invention by feeding in alkyl halides and / or nitrogen compounds requires precise, continuous metering.
  • the metering is usually carried out by feeding the alkyl halides and / or the nitrogen compounds through the inlet gas at the reactor inlet.
  • decomposition or oxidation of the alkyl halides and / or the nitrogen compounds can occur, so that the effective concentration of the metered alkyl halides and / or the nitrogen compounds can vary over the reactor length.
  • accumulation of the alkyl halides and / or the nitrogen compounds on the catalyst by e.g. Overdose due to excessive input concentration, come, which can lead to a reduced catalyst performance.
  • the optimum concentration of the fed alkyl halides and / or nitrogen compounds over the entire reactor length is then possibly no longer guaranteed.
  • the alkyl halides or the alkyl halides and / or the nitrogen compounds are passed in a stepped manner over the reactor length in the reaction space.
  • a very accurate, partial metering of the alkyl halides and / or the nitrogen compounds is possible.
  • a favorable for the / the catalyst (s) and / or operating point (e) concentration profile over the reactor length (concentration falling, constant or increasing) set and a further improved performance of the EO catalysts can be achieved.
  • the gradual addition can be ensured, for example, by dividing the total amount of alkyl halides and / or nitrogen compounds to be metered into equal or different partial streams, wherein a partial stream is metered into the reactor inlet via the input gas and at least one further partial stream is metered at a metering point or is metered in more than two streams several dosing points after the reactor inlet into the reactor.
  • the arrangement of the metering points for the partial streams after the reactor inlet is advantageously carried out along the reactor length so that optimum catalyst performance, ie in particular maximum selectivity, is achieved over the entire catalyst mass.
  • the total flow can be divided into four partial flows, the reactor length LR being divided into four sections, for example the length LR / 4.
  • the first partial stream is metered into the first reactor section via the reactor inlet.
  • the further three partial streams are then metered into the three reactor sections following the first reactor section after a reactor length of L R / 4 or 2 * L R / 4 or 3 * L R / 4.
  • the exothermic oxidation of ethylene to ethylene oxide according to the invention in the microchannel reactor is coupled with an endothermic reaction in order to be able to use or remove the heat released in the EO synthesis.
  • Coupling in this context means a thermal coupling.
  • both the exothermic reaction for producing the ethylene oxide and the thermally coupled endothermic reaction in the microchannel reactor preferably take place in adjacent reaction channels. The fact that these two reactions take place within the microchannel reactor in possibly adjacent reaction channels, a good heat exchange over the walls of the reaction channels is ensured, whereby the effectiveness of the overall process is further improved.
  • reaction channels for the coupling of exothermic and endothermic reaction in a microchannel reactor is known in the art. Information on this can be found, for example, in US 2006/0036106 A1, page 16, paragraph 143. Therein it is disclosed that for the heat removal of the exothermic ethylene epoxidation to ethylene oxide can either use a suitable and well-known heat transfer medium or thermally coupled the reaction with endothermic reactions. As examples, steam reforming reactions and dehydrogenation reaction are generally mentioned.
  • the thermal coupling is achieved by a reforming reaction of an alcohol, since this reaction proceeds in the same temperature range as the production of ethylene oxide.
  • the product of the reforming reaction comprises H2 and CO, but these substances can not be used in the process for producing ethylene oxide.
  • US 2006/0036106 A1 page 4, paragraph 68, proposes to precede the ethylene oxide production in the microchannel reactor by an oxidative dehydrogenation of ethane ("upstream"), the ethylene thus formed together with an oxygen source via the EO catalyst
  • this above-mentioned reaction proves to be disadvantageous in the course of its use with the production of ethylene oxide according to the invention
  • the ethylene obtained in the oxidative dehydrogenation of ethane can be used as starting material for the production of ethylene oxide
  • the exothermic production of ethylene oxide is thermally coupled with the endothermic reaction of the dehydration of ethanol in the manner described above.
  • This proves to be particularly advantageous because it can be obtained as a product ethylene with very high yields.
  • the ethylene formed can be fed to the ethylene oxide synthesis.
  • the formed ethylene is separated after separation by e.g. Condensation of the water formed in the dehydration and / or other resulting products fed to the ethylene oxide synthesis.
  • ethylene can be made by steam cracking of oil or naphtha or by steam cracking of ethane.
  • Ethylene can also be prepared by catalytic, oxidative or autothermal dehydrogenation of ethane.
  • Other methods of making ethylene are the oxidative coupling of methane or metathesis reactions, higher olefins such as e.g. Propene.
  • the major disadvantage of all these methods is the dependence on fossil resources such as e.g. Oil and natural gas.
  • ethylene can also be prepared by catalytic dehydration of ethanol in addition to the methods mentioned.
  • the catalytic dehydration of ethanol is an endothermic reaction.
  • oxidic catalysts eg Al 2 O 3 , ZrO 2 (BuII.Soc.Chem.Jpn. 1975, 48, 3377
  • salts sulfates (J.Cal. 1971, 22, 23)
  • phosphates Kinet 1964, 5, 347
  • hetero polyphosphoric acids
  • ion exchange resins or supported mineral acids in the temperature range up to 400 ° C are used.
  • Particularly preferred catalysts for the dehydration of ethanol are zeolites which can be used in the temperature range from 200 to 300 ° C. (eg ZSM-5 (J. Catal. 1978, 53, 40), selectivity: 98%, conversion: 100% ).
  • the synthesis of EO on silver catalysts usually takes place in the temperature range of 200-300 ° C. It is therefore a particularly advantageous embodiment of the inventive method to couple the exothermic synthesis of ethylene oxide from ethylene in the microchannel reactor with an endothermic, catalytic dehydration of ethanol to ethylene.
  • coupling is again to be understood as meaning the above-described thermal coupling in preferably adjacent microchannels.
  • silver-containing catalysts As catalysts in microchannel reactors all for the production of ethylene oxide from ethylene and oxygen generally suitable silver-containing catalysts, optionally with a suitable support material can be used.
  • a suitable support material As examples of common and promoter-doped silver catalysts suitable for our process, e.g. the silver catalysts of DE-A 23 00 512, DE-A 25 21 906, EP-A 14 457, DE-A 24 54 972, EP-A 172 565, EP-A 357 293, EP-A 1 1 356, EP A 85 237, DE-A 25 60 684, DE-A 27 53 359 and EP 266015 may be mentioned.
  • Particularly suitable promoters for EO catalysts are the elements nitrogen, sulfur, phosphorus, boron, fluorine, Group IA metals, Group IIA metals, rhenium, molybdenum, tungsten, chromium, nickel, copper, platinum, palladium, titanium, hafnium , Zirconium, vanadium, thallium, thorium, tantalum, niobium, gallium, indium, tin and germanium and mixtures thereof.
  • examples are silver catalysts having a silver content of 5 to 50 wt .-%, in particular from 6 to 30 wt.%, Based on the total catalyst composition, a content of the light alkali metals lithium and / or sodium from 1 to 5000 ppm by weight, the content of the heavy alkali metals rubidium and / or cesium from 1 to 5000 ppm by weight, a content of tungsten from 1 to 5000 ppm by weight, a content of molybdenum from 1 to 3000 ppm by weight and / or a content of rhenium of 1 to 10,000 ppm by weight and a content of sulfur and / or phosphorus and / or boron of 1 to 3000 ppm by weight, based on the total catalyst mass called.
  • any porous material which is stable under the conditions of the ethylene oxide synthesis for example activated carbon, aluminum oxides, titanium, zirconium or silicon dioxides or other ceramic compositions or corresponding mixtures, can be used as the carrier material.
  • activated carbon aluminum oxides, titanium, zirconium or silicon dioxides or other ceramic compositions or corresponding mixtures
  • silver in the form of, for example, a film or a mesh or felt can be used as a catalyst in the microchannel reactor.
  • the inventive method provides an effective and procedurally simple way of producing ethylene oxide in a microchannel reactor.
  • the targeted, continuous addition of alkyl halides and / or nitrogen-containing compounds in the claimed range a particularly high increase in the effectiveness is achieved. These advantages are further increased in the case of a gradual addition.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Epoxy Compounds (AREA)

Abstract

Procédé de production d'oxyde d'éthylène dans un réacteur à microcanaux, consistant à introduire dans le réacteur à microcanaux un courant de substances renfermant de l'éthylène et un courant de substances renfermant de l'oxygène ou une source d'oxygène, et à effectuer la transformation en oxyde d'éthylène dans le réacteur à microcanaux renfermant un catalyseur, procédé caractérisé en ce qu'on introduit en continu dans le réacteur à microcanaux, un halogénure d'alkyle à une concentration de 0,3 à 50 volumes ppm, par rapport au flux volumique total de tous les courants de substances introduits dans le réacteur.
EP07727831A 2006-04-21 2007-04-05 Procédé de production d'oxyde d'éthylène dans un réacteur à microcanaux Withdrawn EP2013194A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP07727831A EP2013194A2 (fr) 2006-04-21 2007-04-05 Procédé de production d'oxyde d'éthylène dans un réacteur à microcanaux

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP06112890 2006-04-21
EP07727831A EP2013194A2 (fr) 2006-04-21 2007-04-05 Procédé de production d'oxyde d'éthylène dans un réacteur à microcanaux
PCT/EP2007/053363 WO2007122090A2 (fr) 2006-04-21 2007-04-05 Procédé de production d'oxyde d'éthylène dans un réacteur à microcanaux

Publications (1)

Publication Number Publication Date
EP2013194A2 true EP2013194A2 (fr) 2009-01-14

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US (1) US20090270640A1 (fr)
EP (1) EP2013194A2 (fr)
CN (1) CN101448804A (fr)
WO (1) WO2007122090A2 (fr)

Families Citing this family (37)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2024351B1 (fr) * 2006-05-19 2011-03-09 Basf Se Production d'anhydride phtalique par oxydation en phase gazeuse d'o-xylol
WO2007135102A2 (fr) * 2006-05-19 2007-11-29 Basf Se Production d'anhydride phtalique par oxydation en phase gazeuse d'o-xylol dans un réacteur principal et un réacteur secondaire
EP2106290B1 (fr) 2006-12-21 2016-04-13 Basf Se Système catalytique et procédé d'oxydation en phase gazeuse en utilisant une pré-couche
CA2686825C (fr) * 2007-05-09 2016-09-13 Shell Internationale Research Maatschappij B.V. Catalyseur d'epoxydation, procede de preparation de ce catalyseur, et procede de production d'un oxyde d'olefine, d'un 1,2-diol, d'un ether de 1,2-diol, d'un 1,2-carbonate ou d'une alcanolamine
CA2685512C (fr) 2007-05-09 2016-12-06 Shell Internationale Research Maatschappij B.V. Catalyseur d'epoxydation, procede de preparation de ce catalyseur, et procede de production d'un oxyde d'olefine, d'un 1,2-diol, d'un ether de 1,2-diol, d'un 1,2-carbonate ou d'une alcanolamine
US20110028740A1 (en) * 2008-04-07 2011-02-03 Basf Se Method for starting a gas phase oxidation reactor that contains a catalytically active silver-vanadium oxide bronze
US8492566B2 (en) 2008-04-07 2013-07-23 Basf Se Method for starting a gas-phase oxidation reactor
WO2009137427A2 (fr) 2008-05-07 2009-11-12 Shell Oil Company Procédé pour le démarrage d'un procédé d'époxydation, procédé pour la fabrication d'oxyde d'éthylène, d'un 1,2-diol, d'un éther de 1,2-diol, d'un 1,2-carbonate ou d'une alcanolamine
KR101629038B1 (ko) 2008-05-07 2016-06-09 셀 인터나쵸나아레 레사아치 마아츠샤피 비이부이 산화올레핀, 1,2-디올, 1,2-디올 에테르, 1,2-카보네이트 또는 알칸올아민의 생산방법
EP2313385A2 (fr) * 2008-07-14 2011-04-27 Velocys Inc. Processus de fabrication d oxyde d éthylène au moyen de la technologie de processus en microcanal
BRPI0915854A2 (pt) 2008-07-14 2015-08-04 Basf Se Processo para preparar óxido de etileno
US8524927B2 (en) 2009-07-13 2013-09-03 Velocys, Inc. Process for making ethylene oxide using microchannel process technology
US9079154B2 (en) 2012-05-04 2015-07-14 Basf Se Catalyst for the epoxidation of alkenes
KR20150013704A (ko) 2012-05-04 2015-02-05 바스프 에스이 알켄의 에폭시화용 촉매
US9714227B2 (en) 2013-12-09 2017-07-25 Basf Se Catalyst for the epoxidation of alkenes
CN105330617B (zh) * 2014-07-18 2018-12-28 中国石油化工股份有限公司 一种生产环氧乙烷的方法
CN104292187B (zh) * 2014-10-10 2016-05-18 南京工业大学 一种制备高品质环氧大豆油的方法
CN106311228B (zh) * 2015-07-02 2019-06-28 中国石油化工股份有限公司 银催化剂、其制备方法及应用
CN108368080B (zh) * 2015-12-15 2022-04-15 国际壳牌研究有限公司 从环氧乙烷制造中的循环气体流去除乙烯基碘杂质的方法和系统
BR112018012058B1 (pt) 2015-12-15 2021-01-05 Shell Internationale Research Maatschappij B.V. processo para operar um sistema de leito de guarda
EP3390356B1 (fr) * 2015-12-15 2019-11-13 Shell International Research Maatschappij B.V. Procédés et systèmes permettant d'éliminer les impuretés d'iodure à partir d'un flux de gaz de recyclage dans la production d'oxyde d'éthylène
CN107216296B (zh) * 2016-03-22 2020-07-17 中国石油化工股份有限公司 在微通道反应器内制备环氧丙烷的方法
WO2018029189A1 (fr) 2016-08-08 2018-02-15 Basf Se Catalyseur pour l'oxydation de l'éthylène en oxyde d'éthylène
TWI772330B (zh) 2016-10-14 2022-08-01 荷蘭商蜆殼國際研究所 用於定量分析氣態製程流之方法及設備
JP6887284B2 (ja) * 2017-03-30 2021-06-16 日立Astemo株式会社 排ガス浄化システム
WO2019020793A1 (fr) 2017-07-28 2019-01-31 Basf Se Procédé de production d'un corps moulé de catalyseur comprenant de l'argent appliqué sur un support d'alumine
US12629664B2 (en) 2018-02-07 2026-05-19 Basf Se Method for preparing a silver impregnation solution
TWI808125B (zh) 2018-02-07 2023-07-11 德商巴斯夫歐洲公司 有效地將乙烯氧化轉化為環氧乙烷之催化劑
CN110201487B (zh) * 2019-06-24 2021-06-25 浙江天采云集科技股份有限公司 一种乙烯法制环氧乙烷中高纯度高收率甲烷致稳气净化与再利用方法
EP3858820A1 (fr) * 2020-01-29 2021-08-04 Clariant International Ltd Concept de réacteur et procédé de préparation d'oxyde d'éthylène à partir d'éthanol
US20240408585A1 (en) 2021-01-26 2024-12-12 Basf Se Epoxidation catalyst
EP4082996B1 (fr) * 2021-04-29 2023-10-11 TotalEnergies OneTech Couplage oxydatif non catalytique de méthane
CN120051334A (zh) 2022-10-12 2025-05-27 巴斯夫欧洲公司 环氧化催化剂
CN120129671A (zh) 2022-10-28 2025-06-10 巴斯夫欧洲公司 由可再生来源的乙醇制造异壬醇的方法
EP4638400A1 (fr) 2022-12-20 2025-10-29 Basf Se Fabrication d'un produit chimique d'intérêt dérivé de l'éthylène, en particulier de l'acide acrylique, en combinaison avec la génération de vapeur chauffée
WO2025078359A1 (fr) 2023-10-09 2025-04-17 Basf Se Fabrication de produits chimiques dérivés d'éthylène ayant une teneur en carbone d'origine biologique à partir de bio-naphta
CN121969593A (zh) 2023-10-09 2026-05-01 巴斯夫欧洲公司 由热解油制造具有生物基碳含量的乙烯衍生的化学品

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1491447A (en) * 1973-12-05 1977-11-09 Ici Ltd Alkylene oxide production and catalysts therefor
DE2904919A1 (de) * 1979-02-09 1980-08-21 Basf Ag Verfahren zur herstellung und regenerierung von traegerkatalysatoren sowie deren verwendung fuer die herstellung von aethylenoxid
DE3414717A1 (de) * 1984-04-18 1985-10-31 Linde Ag, 6200 Wiesbaden Verfahren und reaktor zur durchfuehrung exothermer katalytischer reaktionen
IL84232A (en) * 1986-10-31 1992-06-21 Shell Int Research Catalyst and process for the catalytic production of ethylene oxide
US6372925B1 (en) * 2000-06-09 2002-04-16 Shell Oil Company Process for operating the epoxidation of ethylene
DE60207299T2 (de) * 2001-11-20 2006-08-10 Shell Internationale Research Maatschappij B.V. Verfahren und systeme zur epoxidierung eines olefins
CN100376561C (zh) * 2002-06-28 2008-03-26 国际壳牌研究有限公司 环氧化方法的开车方法、烯烃环氧化的催化剂和方法
AU2003278999A1 (en) * 2002-09-30 2004-04-23 Shell Oil Company Calcium carbonate carrier for making silver based epoxidation catalysts
EP1786797B1 (fr) * 2004-08-12 2014-11-26 Velocys, Inc. Procédé de conversion de l' éthylène en oxyde d'éthylène en utilisant une technologie de procédé par microcanaux

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2007122090A2 *

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US20090270640A1 (en) 2009-10-29

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