EP1572342A1 - Procede de fabrication d'oxide d'ethylene - Google Patents

Procede de fabrication d'oxide d'ethylene

Info

Publication number
EP1572342A1
EP1572342A1 EP03782582A EP03782582A EP1572342A1 EP 1572342 A1 EP1572342 A1 EP 1572342A1 EP 03782582 A EP03782582 A EP 03782582A EP 03782582 A EP03782582 A EP 03782582A EP 1572342 A1 EP1572342 A1 EP 1572342A1
Authority
EP
European Patent Office
Prior art keywords
tubes
reaction
outlet
inlet
process according
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Withdrawn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
EP03782582A
Other languages
German (de)
English (en)
Inventor
Mathias Mauvezin
Christine Poulain
Mehdi Rghioui
Hassan Taheri
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.)
PetroIneos Europe Ltd
Ineos USA LLC
Original Assignee
BP Chemicals Ltd
Ineos Europe Ltd
BP Corp North America Inc
Innovene USA LLC
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 BP Chemicals Ltd, Ineos Europe Ltd, BP Corp North America Inc, Innovene USA LLC filed Critical BP Chemicals Ltd
Publication of EP1572342A1 publication Critical patent/EP1572342A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
    • F28F13/06—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media
    • F28F13/08—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media by varying the cross-section of the flow channels
    • 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
    • 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
    • B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling the reactor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
    • 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
    • B01J2208/00212—Plates; Jackets; Cylinders

Definitions

  • the present invention relates to a process for manufacturing ethylene oxide by the catalytic oxidation reaction of ethylene.
  • the catalytic oxidation reaction of ethylene by molecular oxygen leading to the formation of ethylene oxide is known to be strongly exothermic. It is often carried out in a tube reactor, in particular a vertical multitubular shell exchanger type reactor or a vertical shell-and-tube exchanger type reactor.
  • the tube reactor comprises three successive and adjacent chambers traversed by a reactive gas current comprising ethylene and molecular oxygen: an inlet chamber of the reactive gas current, then a central chamber where the ethylene oxide is formed in a gas current resulting from the catalytic oxidation reaction and an outlet chamber of the resulting gas current.
  • the central chamber comprises generally a bundle of reaction tubes immersed in a heat exchange fluid and filled with a solid silver-based catalyst.
  • the reactive gas current passes to the interior of the reaction tubes and, by contact with the catalyst, leads to the formation of ethylene oxide in the gas current resulting from the reaction.
  • Each reaction tube comprises an inlet issuing into the inlet chamber and an outlet issuing into the outlet chamber.
  • three successive zones from the inlet to the outlet of the tubes are generally found, that is to say in the flow direction of the gas current, namely a pre-heating zone situated towards the inlet of the tubes, then a reaction zone and a quenching or cooling, zone situated towards the outlet of the tubes.
  • the desired product of the catalytic oxidation reaction of ethylene is ethylene oxide.
  • the reaction tubes have an internal cross-section whose area decreases between the inlet and the outlet of the tubes. They may, in addition, have a wall whose thickness is constant, or on the contrary varies, for example decreases or increases from the inlet up to the outlet of the tubes (in the flow direction of the reactive gas current). It is possible in particular to use reaction tubes of cylindrical shape which have an internal diameter (Di) which decreases from the inlet up to the outlet of the tubes, for example continuously or discontinuously, in particular by stages, as described previously according to the invention, and which may, in addition, have an external diameter (De) which is constant between the inlet and the outlet of the tubes and equal in particular to the external diameter (Die) at the inlet of said tubes. In this case, it was found in a remarkable manner that the resulting enlargement of the wall of the reaction tubes from the inlet up to the outlet of the tubes does not affect, or only in an insignificant manner, the effects sought by the process of the invention.
  • the heat exchange fluid may also be water superheated under pressure, in particular used at a relative pressure of from 1500 to 8000 kPa. In thisicase, the superheated water may be used according to a process and a heat exchange apparatus as described in American patent US 5,292,904.
  • the temperature of the heat exchange fluid at the outlet of the tube reactor generally lies between 210 and 300 °C, preferably between 220 and 280 °C, more particularly between 210 and 280 °C.
  • the temperature of the heat exchange fluid at the inlet of the tube reactor generally lies between 120 and 250 °C, preferably between 130 and 240 °C, more particularly between 130 and 230 °C.
  • Example 3 (comparative) Exactly the same procedure was adopted as in Example 1 , except that the tube reactor comprised a bundle of 4750 cylindrical reaction tubes (5), identical and parallel to one another, and that each tube (5) had a conventional shape and possesses in particular an internal diameter (Di) which was constant between the inlet (6) and the outlet (7) of the tubes and which was equal to 38.7 mm, and a length (L) of 12 m.
  • the reaction tubes were filled with the silver-based catalyst, as in Example 1, in an equal manner between them and over almost the whole (96 %) of their length.
  • the total volume of catalyst introduced into the reaction tubes of the reactor was substantially identical to that of Example 1.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Epoxy Compounds (AREA)
  • Catalysts (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne un procédé de fabrication d'oxyde d'éthylène par une réaction d'oxydation catalytique d'éthylène au moyen d'oxygène moléculaire dans un réacteur à tubes. Ledit réacteur comprend un faisceau de tubes de réaction (5) qui sont immergés dans un fluide d'échange de chaleur et remplis d'un catalyseur solide à base d'argent (8) et qui sont traversés par un courant de gaz réactifs contenant de l'éthylène et de l'oxygène moléculaire, lesquels forment de l'oxyde d'éthylène lorsqu'ils sont en contact avec le catalyseur. La surface de la section interne des tubes de réaction (5) diminue entre l'entrée (1) et la sortie (3) des tubes sur au moins une partie de la longueur de ceux-ci et reste constante sur les autres parties. Ce procédé permet d'accroître la sélectivité de la réaction vis-à-vis de l'oxyde d'éthylène pour une production donnée d'oxyde d'éthylène. Il permet également d'utiliser une charge maximale de catalyseur actif par unité de volume de tube interne disponible dans le réacteur, en particulier grâce à un échange de chaleur optimal permettant plus particulièrement de fournir un profil de températures de réaction relativement stable sur toute la longueur des tubes de réaction et d'empêcher en particulier des emballements de réaction.
EP03782582A 2002-12-19 2003-12-03 Procede de fabrication d'oxide d'ethylene Withdrawn EP1572342A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR0216145A FR2849031A1 (fr) 2002-12-19 2002-12-19 Procede de fabrication d'oxyde d'ethylene
FR0216145 2002-12-19
PCT/GB2003/005203 WO2004056463A1 (fr) 2002-12-19 2003-12-03 Procede de fabrication d'oxide d'ethylene

Publications (1)

Publication Number Publication Date
EP1572342A1 true EP1572342A1 (fr) 2005-09-14

Family

ID=32406186

Family Applications (1)

Application Number Title Priority Date Filing Date
EP03782582A Withdrawn EP1572342A1 (fr) 2002-12-19 2003-12-03 Procede de fabrication d'oxide d'ethylene

Country Status (7)

Country Link
US (1) US20060054314A1 (fr)
EP (1) EP1572342A1 (fr)
CN (1) CN1747782A (fr)
AU (1) AU2003290219A1 (fr)
FR (1) FR2849031A1 (fr)
NO (1) NO20053400L (fr)
WO (1) WO2004056463A1 (fr)

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* Cited by examiner, † Cited by third party
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EP1621247A1 (fr) * 2004-07-30 2006-02-01 MAN DWE GmbH Exécutions de réactions exothermiques en phase gazeuse
KR20070112870A (ko) * 2005-03-22 2007-11-27 셀 인터나쵸나아레 레사아치 마아츠샤피 비이부이 반응기 시스템 및 에틸렌옥사이드의 제조방법
GB0509747D0 (en) * 2005-05-13 2005-06-22 Ashe Morris Ltd Variable volume heat exchangers
US7977391B2 (en) 2005-12-19 2011-07-12 Bp Exploration Operating Company Limited Process for producing condensed-phase product from one or more gas-phase reactants
US20080286159A1 (en) * 2006-09-15 2008-11-20 Grover Bhadra S Variable Tube Diameter For SMR
AR066573A1 (es) 2007-05-18 2009-08-26 Shell Int Research Un sistema reactor un absorbente y un proceso para la reaccion de una fuente
CA2709887C (fr) 2007-12-18 2016-10-18 Dow Technology Investments Llc Reacteur tube comportant un espace de tete d'entree a volume reduit
US20100139902A1 (en) * 2008-12-05 2010-06-10 Baylis Bobbye K Plastic heat exchanger
CN102022943B (zh) * 2010-12-15 2013-01-30 茂名重力石化机械制造有限公司 列管式换热器的换热管及其列管式换热器
CA2774566C (fr) * 2011-04-22 2014-08-05 Air Products And Chemicals, Inc. Reacteur tubulaire avec transfert calorifique par collision de jet
US11504814B2 (en) 2011-04-25 2022-11-22 Holtec International Air cooled condenser and related methods
US9786395B2 (en) * 2011-04-25 2017-10-10 Holtec International, Inc. Air-cooled heat exchanger and system and method of using the same to remove waste thermal energy from radioactive materials
CN102921355B (zh) * 2011-08-08 2016-03-30 中国石油化工股份有限公司 一种列管式固定床反应器和煤层气脱氧方法
CN102865694B (zh) * 2012-08-31 2015-03-11 大连葆光节能空调设备厂 污水源热泵专用换热器
CN102865758B (zh) * 2012-08-31 2015-03-11 大连葆光节能空调设备厂 污水源热泵专用换热器
CN102865757B (zh) * 2012-08-31 2015-03-11 大连葆光节能空调设备厂 污水源热泵专用换热器
US10512990B2 (en) 2012-12-03 2019-12-24 Holtec International, Inc. Brazing compositions and uses thereof
CN105705229B (zh) 2013-11-07 2018-05-01 株式会社日本触媒 反应管用填充物、反应管及使用了该反应管的反应方法
CN107107016A (zh) * 2014-11-14 2017-08-29 赛贝克环球科技公司 固定床反应器及其相关方法
AU2018218185B2 (en) * 2017-02-08 2022-08-25 Commonwealth Scientific And Industrial Research Organisation Isothermal reactor
GB2598579A (en) * 2020-09-02 2022-03-09 Unisa Tubular reactors
CN113028864B (zh) * 2021-02-26 2022-10-04 南通星球石墨股份有限公司 石墨浸渍四氟列管式换热器的制备方法
CN116726804B (zh) * 2023-06-28 2025-12-26 福州大学 一种圆筒式氨分解反应装置及系统
CN117380098A (zh) * 2023-09-21 2024-01-12 国家电投集团氢能科技发展有限公司 氨裂解反应堆装置

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2929300A1 (de) * 1979-07-19 1981-01-29 Linde Ag Reaktor zur durchfuehrung katalytischer endothermer oder exothermer reaktionen
US7316804B2 (en) * 2001-08-02 2008-01-08 Ineos Usa Llc Flow reactors for chemical conversions with heterogeneous catalysts

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2004056463A1 *

Also Published As

Publication number Publication date
NO20053400L (no) 2005-09-19
NO20053400D0 (no) 2005-07-13
WO2004056463A1 (fr) 2004-07-08
AU2003290219A1 (en) 2004-07-14
FR2849031A1 (fr) 2004-06-25
CN1747782A (zh) 2006-03-15
AU2003290219A8 (en) 2004-07-14
US20060054314A1 (en) 2006-03-16

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