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DE19948585A1 - Process and plant for the production of methanol - Google Patents

Process and plant for the production of methanol

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Publication number
DE19948585A1
DE19948585A1 DE19948585A DE19948585A DE19948585A1 DE 19948585 A1 DE19948585 A1 DE 19948585A1 DE 19948585 A DE19948585 A DE 19948585A DE 19948585 A DE19948585 A DE 19948585A DE 19948585 A1 DE19948585 A1 DE 19948585A1
Authority
DE
Germany
Prior art keywords
methanol
heater
trimer
synthesis
gas
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Withdrawn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
DE19948585A
Other languages
German (de)
Inventor
Hans-Joachim Baehnisch
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.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
Krupp Uhde GmbH
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 Krupp Uhde GmbH filed Critical Krupp Uhde GmbH
Priority to DE19948585A priority Critical patent/DE19948585A1/en
Priority to US10/070,407 priority patent/US6686398B1/en
Priority to PCT/EP2000/008486 priority patent/WO2001017936A2/en
Priority to EP00964071A priority patent/EP1210309B1/en
Priority to JP2001521683A priority patent/JP4837213B2/en
Priority to AT00964071T priority patent/ATE255552T1/en
Priority to DE50004668T priority patent/DE50004668D1/en
Priority to ES00964071T priority patent/ES2211610T3/en
Priority to DK00964071T priority patent/DK1210309T3/en
Priority to CNB008125058A priority patent/CN1181023C/en
Publication of DE19948585A1 publication Critical patent/DE19948585A1/en
Withdrawn legal-status Critical Current

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
    • B01J8/06—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
    • 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
    • B01J8/0285—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/1516—Multisteps
    • C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
    • 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
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00044—Temperature measurement
    • B01J2208/00061—Temperature measurement of the reactants
    • 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
    • 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
    • B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from 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
    • 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
    • B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
    • B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
    • 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

Landscapes

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

Abstract

The invention relates to a method for the methanol synthesis from hydrogen, carbon monoxide and carbon dioxide under pressure. The inventive method comprises at least one synthesis stage that comprises at least one methanol reactor which is filled with catalyst. At least one stage is provided with a compressor when there are several stages. The invention also relates to an arrangement for carrying out said method. The aim of the invention is to overcome the mentioned disadvantages, especially to give the possibility to reduce the heat exchanger surface and/or to increase the yield while particularly taking into account the changing catalyst activity. According to the invention, the gas mixture which is designed for the use in a methanol reactor being filled with catalyst is heated in an additional trimmer heater in at least one synthesis stage just before said gas mixture is added to the methanol reactor. A corresponding arrangement is characterised in that a trimmer heater (5) is provided in at least one synthesis stage for heating the gas mixture that directly impinges upon the methanol reactor (10).

Description

Die Erfindung bezieht sich auf ein Verfahren zur Methanol­ synthese aus Wasserstoff, Kohlenmonoxid und Kohlendioxid unter Druck mit wenigstens einer Synthesestufe der im Ober­ begriff des Anspruches 1 angegebenen Gattung sowie auf eine entsprechende Anlage.The invention relates to a method for methanol synthesis from hydrogen, carbon monoxide and carbon dioxide under pressure with at least one synthesis step in the upper Concept of claim 1 specified genus and a corresponding facility.

Es sind eine Reihe von Anlagen bzw. Verfahren zur katalyti­ schen Methanolsynthese bekannt, wobei für die Fülle der Lö­ sungen hier als Beispiel die DE 21 17 060, DE 25 29 591, DE 32 20 995, DE 35 18 362, US 29 04 575 und vor allem die DE 41 00 632 genannt seien.There are a number of systems and processes for catalytic known methanol synthesis, the abundance of Lö here are examples of DE 21 17 060, DE 25 29 591, DE 32 20 995, DE 35 18 362, US 29 04 575 and especially the DE 41 00 632 may be mentioned.

Wie in der DE 41 00 632 beschrieben, ist es dabei besonders vorteilhaft, mehrere Synthesestufen mit Reaktoren einzu­ setzen, deren erzeugtes Methanol auszukondensieren, vom Syn­ thesegas abzuscheiden, und nach jedem einzelnen Reaktor als separaten Methanol-Produktstrom abzuziehen. Bei der Abküh­ lung des die Reaktoren verlassenden Methanol-Synthesegas-Ge­ misches ist es wirtschaftlich, die abzugebende Wärme wenigs­ tens zum Teil dazu zu nutzen, die Eintrittsströme in die je­ weiligen Reaktoren mittels Gas/Gas-Wärmetauschern zuvor auf­ zuwärmen.As described in DE 41 00 632, it is special advantageous to use several synthesis stages with reactors set, to condense out the generated methanol, from Syn to separate thesegas, and after each reactor as separate methanol product stream. When cooling development of the methanol synthesis gas Ge leaving the reactors it is economical to mix the heat to be released at least partly to use the entry streams in each previously reactors using gas / gas heat exchangers warm up.

Als nachteilig stellte sich im langjährigen Betrieb jedoch heraus, daß sich das üblicherweise in den Methanolreaktoren eingesetzte Katalysatormaterial in seiner Aktivität im Laufe der Zeit derart verändert, daß immer höhere Reaktortempera­ turen erforderlich werden, um eine optimale Ausbeute zu er­ reichen und wobei allerdings in den Zonen nach den Gasein­ trittsbereichen der Reaktoren solche höheren Reaktortempera­ turen nach einiger Zeit nicht mehr erreichbar sind. Aufgrund des verringerten Reaktionsumsatzes wird sowohl weniger Methanol als auch weniger Dampf produziert, der bei der Küh­ lung der Methanolreaktoren üblicherweise als Koppelprodukt anfällt.However, it turned out to be disadvantageous in long-term operation  out that this is usually in the methanol reactors used catalyst material in its activity in the course the time changed in such a way that ever higher reactor temperatures structures are necessary to obtain an optimal yield range and although in the zones after the gas tread areas of the reactors such higher reactor temperatures doors can no longer be reached after some time. Because of the reduced reaction turnover is both less Methanol also produces less steam, which is used in the cooling development of the methanol reactors usually as a co-product arises.

Aufgabe der Erfindung ist es, die genannten Nachteile zu überwinden und insbesondere die Ausbeute unter besonderer Berücksichtigung der veränderlichen Katalysatoraktivität zu erhöhen.The object of the invention is to overcome the disadvantages mentioned overcome and especially the yield under special Taking into account the changing catalyst activity increase.

Mit einem Verfahren der eingangs bezeichneten Art wird diese Aufgabe gemäß der Erfindung durch die kennzeichnenden Merk­ male des Anspruches 1 gelöst. Dabei ist vorgesehen, daß in zumindest einer Synthesestufe das für den Einsatz in einem katalysatorgefüllten Methanolreaktor bestimmte Gasgemisch direkt vor Zugabe in besagten Methanolreaktor in einem zu­ sätzlichen Trimerhitzer aufgeheizt wird.This is done using a method of the type described at the beginning Object according to the invention by the characterizing note male of claim 1 solved. It is provided that in at least one synthesis step for use in one catalyst-filled methanol reactor certain gas mixture immediately before adding to said methanol reactor in one additional trimer heater is heated.

Ausgestaltungen der Erfindung bestehen u. a. darin, daß
Embodiments of the invention include that

  • - die Temperatur des für den Einsatz in den katalysatorge­ füllten Reaktoren bestimmten Gasgemisches nach seiner Er­ hitzung durch den zusätzlichen Trimerhitzer gemessen wird, die Wärmezufuhr des zusätzlichen Trimerhitzers geregelt werden kann, und- The temperature of the for use in the catalyst filled reactors of certain gas mixture after its Er heating is measured by the additional trimer heater, the heat supply of the additional trimer heater is regulated can be, and
  • - der zusätzliche Trimerhitzer mit einem Fremdmedium, z. B. Dampf, beheizt wird.- The additional trimer heater with a foreign medium, e.g. B. Steam being heated.

Der Hauptvorteil einer solchen Vorgehensweise liegt darin, daß bei nachlassender Katalysatoraktivität eine Nachregelung der Reaktoreintrittstemperatur möglich ist und daher stets eine optimale Ausbeute erreicht werden kann. Überraschender­ weise zeigte sich auch, daß der Gas/Gas-Wärmetauscher, der den austretenden Strom aus dem Reaktor gegen den eintreten­ den Strom abkühlt, deutlich kleiner dimensioniert werden kann, weil die erforderliche Sicherheitsreserve dem Trimer­ hitzer zugerechnet werden kann.The main advantage of doing this is that readjustment when the catalyst activity decreases the reactor inlet temperature is possible and therefore always an optimal yield can be achieved. More surprising also showed that the gas / gas heat exchanger, the the emerging stream from the reactor against the entering the electricity cools down, can be dimensioned significantly smaller can because of the required safety margin the trimer heat can be attributed.

Da ein beispielsweise dampfbeheizter Trimerhitzer vielfach bessere Wärmeübertragungseigenschaften als ein Gas/Gas-Wär­ metauscher besitzt, ergibt sich unter dem Strich sogar eine Einsparung an Investitionskosten. Außerdem zeigte sich, daß die im Trimerhitzer über die Katalysatorlebensdauer einzu­ setzende Dampfmenge kleiner ist als der Verlust an Koppel­ produkt für den Fall von Einbußen aufgrund verringerten Reaktionsumsatzes. Somit erhöht sich trotz des zusätzlichen Dampfbedarfs unter dem Strich die erzeugte Menge an Dampf. Außerdem zeigte sich, daß sich der Inbetriebnahmezeitraum einer solchen Anlage erheblich verkürzen läßt, wenn Trimer­ hitzer als Starterhitzer verwendet werden können.For example, a steam-heated trimer heater is often used better heat transfer properties than a gas / gas heat possesses metauscher, the bottom line is even one Saving on investment costs. It also turned out that which in the trimer heater over the catalyst life amount of steam is less than the loss of coupling product in case of loss due to reduced Reaction sales. Thus, despite the additional  The bottom line is the amount of steam generated. It was also shown that the commissioning period such a facility can be significantly shortened if trimer heater can be used as a starter heater.

Die oben angegebene Aufgabe wird mit einer Anlage der gat­ tungsgemäßen Art dadurch gelöst, daß in wenigstens einer Synthesestufe ein Trimerhitzer zur Erwärmung des den Metha­ nolreaktor unmittelbar beaufschlagenden Gasgemisches vorge­ sehen ist.The task specified above is carried out with a system from gat solved in accordance with the fact that in at least one Synthesis stage a trimer heater for heating the metha nolreactor pre-applied gas mixture see is.

Weitere Ausgestaltungen der Anlage ergeben sich aus den wei­ teren Anlageansprüchen, wobei die diesen Anlagen zuzuordnen­ den Vorteile mit den Vorteilen des entsprechenden Verfahrens übereinstimmen.Further refinements of the system result from the white other investment claims, whereby the assignments to these investments the advantages with the advantages of the corresponding procedure to match.

Weitere Vorteile, Einzelheiten und Merkmale der Erfindung ergeben sich aufgrund der nachfolgenden Beschreibung sowie anhand der Zeichnung. Diese zeigt in vereinfachter Darstel­ lung eine von ansonsten mehreren in der Regel identisch auf­ gebauten Stufen einer Methanolsyntheseanlage.Further advantages, details and features of the invention result from the following description as well based on the drawing. This shows in a simplified representation usually one of several otherwise identical built stages of a methanol synthesis plant.

Zur Verdichtung des mit 1 bezeichneten Einsatzgases ist ein Verdichter 2 vorgesehen, wobei im weiteren Gasweg ein Gas/Gas-Wärmetauscher 3 zur Vorwärmung des Einsatzgases vorgesehen ist. A compressor 2 is provided for compressing the feed gas designated 1, a gas / gas heat exchanger 3 being provided in the further gas path for preheating the feed gas.

Das so vorgewärmte Gas wird über die Leitung 4 einem Trimer­ hitzer 5 zugeführt, der das Einsatzgas 1 auf die gewünschte Temperatur erhitzt. Zur Messung der Temperatur ist in der Zuführleitung 6 eine Temperaturmess- und -regeleinrichtung 7 vorgesehen, wobei mittels eines Dampfregelventiles 8 die Dampfzufuhr 9 so geregelt wird, daß stets eine optimale Gas­ eintrittstemperatur im katalysatorgefüllten Methanolreaktor 10 eingestellt werden kann.The gas thus preheated is fed via line 4 to a trimer heater 5 , which heats the feed gas 1 to the desired temperature. To measure the temperature, a temperature measuring and regulating device 7 is provided in the feed line 6 , the steam feed 9 being regulated by means of a steam control valve 8 so that an optimal gas inlet temperature can always be set in the catalyst-filled methanol reactor 10 .

Im katalysatorgefüllten Methanolreaktor 10 reagiert das Ein­ satzgas unter Wärmeentwicklung, die Reaktionswärme wird ge­ nutzt, um Dampf 12 aus Speisewasser 11 zu erzeugen. Das heiße Produktgas 13 gibt einen Teil seiner Wärmeenergie im Gas/Gas-Wärmetauscher 3 ab, das im Reaktor erzeugte, gasför­ mige Methanol wird im Methanolkondensator 14 aus dem Synthe­ segas auskondensiert, im Kondensatabscheider 15 vom Synthe­ segas abgetrennt und als Produkt-Methanol 16 abgeführt. Das verbleibende Synthesegas 17 kann in der nachfolgenden Stufe weiterverwendet werden.In the catalyst-filled methanol reactor 10 , the feed gas reacts with the development of heat, the heat of reaction is used to generate steam 12 from feed water 11 . The hot product gas 13 gives off part of its thermal energy in the gas / gas heat exchanger 3 , the gas-generated methanol generated in the reactor is condensed in the methanol condenser 14 from the Synthe segas, separated in the condensate separator 15 from the Synthe segas and discharged as product methanol 16 . The remaining synthesis gas 17 can be used in the subsequent stage.

Natürlich ist das beschriebene Ausführungsbeispiel der Er­ findung noch in vielfacher Hinsicht abzuändern, ohne den Grundgedanken zu verlassen. So kann beispielsweise der Trimerhitzer ggf. zweistufig ausgebildet sein und dergl. mehr.Of course, the described embodiment is the Er change in many ways without the To leave basic ideas. For example, the Trimer heater may be of two stages and the like. more.

Claims (6)

1. Verfahren zur Methanolsynthese aus Wasserstoff, Kohlen­ monoxid und Kohlendioxid unter Druck mit wenigstens einer Synthesestufe, die wenigstens einen katalysatorgefüllten Methanolreaktor enthält, wobei bei mehreren Stufen wenig­ stens eine Stufe mit einem Verdichter ausgestattet ist und wobei alle Synthesestufen mit eigenem Produktabzug für Methanol und eigenem Gas/Gas-Wärmetauscher zur Übertragung von Wärmeenergie des den Methanolreaktor verlassenden Gas­ gemisches an das zum Einsatz im Methanolreaktor vorgesehene Gasgemisch ausgestattet sind, dadurch gekennzeichnet, daß in zumindest einer Synthesestufe das für den Einsatz in einem katalysatorgefüllten Methanolreaktor bestimmte Gasge­ misch direkt vor Zugabe in besagten Methanolreaktor in einem zusätzlichen Trimerhitzer aufgeheizt wird.1. A process for the synthesis of methanol from hydrogen, carbon monoxide and carbon dioxide under pressure with at least one synthesis stage which contains at least one catalyst-filled methanol reactor, in which case at least one stage is equipped with at least one compressor and all synthesis stages have their own product deduction for methanol and their own Gas / gas heat exchangers for the transfer of thermal energy of the gas leaving the methanol reactor to the gas mixture intended for use in the methanol reactor are equipped, characterized in that in at least one synthesis stage the gas mixture intended for use in a catalyst-filled methanol reactor is mixed directly before adding to said gas reactor Methanol reactor is heated in an additional trimer heater. 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Temperatur des für den Einsatz in einem katalysator­ gefüllten Methanolreaktor bestimmte Gasgemisch nach seiner Erhitzung durch den Trimerhitzer gemessen wird. 2. The method according to claim 1, characterized, that the temperature of the for use in a catalyst filled methanol reactor determined gas mixture according to its Heating is measured by the trimer heater.   3. Verfahren nach einem der vorangegangenen Ansprüche 1 und 2, dadurch gekennzeichnet, daß die Wärmezufuhr des Trimerhitzers geregelt werden kann.3. The method according to any one of the preceding claims 1 and 2, characterized, that the heat supply of the trimer heater can be regulated. 4. Verfahren nach einem der vorangegangenen Ansprüche 1 bis 3, dadurch gekennzeichnet, daß der Trimerhitzer mit einem Fremdmedium, vorzugsweise Dampf, beheizt wird.4. The method according to any one of the preceding claims 1 to 3, characterized, that the trimer heater with a foreign medium, preferably Steam being heated. 5. Anlage zur Methanolsynthese, insbesondere zur Durchführung des Verfahrens nach einem der vorangehenden Ansprüche, dadurch gekennzeichnet, daß in wenigstens einer Synthesestufe (Fig. 1) ein Trimer­ hitzer (5) zur Erwärmung des den Methanolreaktor (10) unmit­ telbar beaufschlagenden Gasgemisches vorgesehen ist.5. Plant for methanol synthesis, in particular for performing the method according to any one of the preceding claims, characterized in that in at least one synthesis stage ( Fig. 1) a trimer heater ( 5 ) for heating the methanol reactor ( 10 ) is immediately acting gas mixture is provided . 6. Anlage nach Anspruch 5, dadurch gekennzeichnet, daß dem Trimerhitzer (5) in der Zuführleitung (6) eine Temperaturmess- und -regeleinrichtung (7) nachgeordnet ist.6. Plant according to claim 5, characterized in that the trimer heater ( 5 ) in the feed line ( 6 ) is followed by a temperature measuring and control device ( 7 ).
DE19948585A 1999-09-07 1999-10-08 Process and plant for the production of methanol Withdrawn DE19948585A1 (en)

Priority Applications (10)

Application Number Priority Date Filing Date Title
DE19948585A DE19948585A1 (en) 1999-09-07 1999-10-08 Process and plant for the production of methanol
US10/070,407 US6686398B1 (en) 1999-09-07 2000-08-31 Method and arrangement for producing methanol
PCT/EP2000/008486 WO2001017936A2 (en) 1999-09-07 2000-08-31 Method and arrangement for producing methanol
EP00964071A EP1210309B1 (en) 1999-09-07 2000-08-31 Method and arrangement for producing methanol
JP2001521683A JP4837213B2 (en) 1999-09-07 2000-08-31 Method and equipment for producing methanol
AT00964071T ATE255552T1 (en) 1999-09-07 2000-08-31 METHOD AND PLANT FOR PRODUCING METHANOL
DE50004668T DE50004668D1 (en) 1999-09-07 2000-08-31 METHOD AND PRODUCTION SYSTEM FOR METHANOL PRODUCTION
ES00964071T ES2211610T3 (en) 1999-09-07 2000-08-31 PROCEDURE FOR THE PRODUCTION OF METHANOL.
DK00964071T DK1210309T3 (en) 1999-09-07 2000-08-31 Methods and plants for methanol production
CNB008125058A CN1181023C (en) 1999-09-07 2000-08-31 Methanol synthesis process and equipment

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19942736 1999-09-07
DE19948585A DE19948585A1 (en) 1999-09-07 1999-10-08 Process and plant for the production of methanol

Publications (1)

Publication Number Publication Date
DE19948585A1 true DE19948585A1 (en) 2001-03-08

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DE19948585A Withdrawn DE19948585A1 (en) 1999-09-07 1999-10-08 Process and plant for the production of methanol
DE50004668T Expired - Fee Related DE50004668D1 (en) 1999-09-07 2000-08-31 METHOD AND PRODUCTION SYSTEM FOR METHANOL PRODUCTION

Family Applications After (1)

Application Number Title Priority Date Filing Date
DE50004668T Expired - Fee Related DE50004668D1 (en) 1999-09-07 2000-08-31 METHOD AND PRODUCTION SYSTEM FOR METHANOL PRODUCTION

Country Status (2)

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JP (1) JP4837213B2 (en)
DE (2) DE19948585A1 (en)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016008820A1 (en) * 2014-07-18 2016-01-21 Haldor Topsøe A/S A pseudo-isothermal reactor
WO2019174679A1 (en) * 2018-03-15 2019-09-19 Karl Bau Gmbh Method and arrangement for methanol synthesis
CN110603241A (en) * 2017-05-12 2019-12-20 乔治洛德方法研究和开发液化空气有限公司 Method for carrying out exothermic equilibrium reactions
DE102019124078A1 (en) * 2019-09-09 2021-03-11 Thyssenkrupp Ag Process for the synthesis of a substance

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4004862C2 (en) * 1990-02-16 1993-01-14 Uhde Gmbh, 4600 Dortmund, De
DE4028750C2 (en) * 1990-09-11 1993-06-17 Uhde Gmbh, 4600 Dortmund, De
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