EP2539307A1 - Procédé de production de méthanol - Google Patents

Procédé de production de méthanol

Info

Publication number
EP2539307A1
EP2539307A1 EP11702934A EP11702934A EP2539307A1 EP 2539307 A1 EP2539307 A1 EP 2539307A1 EP 11702934 A EP11702934 A EP 11702934A EP 11702934 A EP11702934 A EP 11702934A EP 2539307 A1 EP2539307 A1 EP 2539307A1
Authority
EP
European Patent Office
Prior art keywords
synthesis gas
catalyst
reaction
methanol
synthesis
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Withdrawn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
EP11702934A
Other languages
German (de)
English (en)
Inventor
Holger Schlichting
Philipp Marius Hackel
Thomas Wurzel
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.)
Air Liquide Global E&C Solutions Germany GmbH
Original Assignee
Lurgi 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 Lurgi GmbH filed Critical Lurgi GmbH
Publication of EP2539307A1 publication Critical patent/EP2539307A1/fr
Withdrawn legal-status Critical Current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
    • B01J8/04—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
    • B01J8/0457—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 placed in separate reactors
    • 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
    • C07C29/1512—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 reaction conditions
    • 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
    • C07C29/153—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 catalyst used
    • C07C29/154—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 catalyst used containing copper, silver, gold, or compounds thereof
    • 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
    • B01J2208/00265—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
    • 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
    • B01J2208/00628—Controlling the composition of the reactive mixture
    • 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
    • B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
    • B01J2208/023—Details
    • B01J2208/024—Particulate material
    • B01J2208/025—Two or more types of catalyst
    • 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
    • B01J2219/00002—Chemical plants
    • B01J2219/00027—Process aspects
    • B01J2219/0004—Processes in series
    • 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
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T29/00—Metal working
    • Y10T29/49—Method of mechanical manufacture
    • Y10T29/49716—Converting

Definitions

  • the invention relates to a process for the catalytic production of methanol, in which the economy is significantly improved by optimized selection of the catalysts used compared to a known from the prior art.
  • the invention relates to a process for optimized methanol synthesis in a multi-stage process.
  • the invention further relates to a process for the conversion of an existing plant for the production of methanol.
  • the synthesis gas is preheated by indirect heat exchange before it enters the water-cooled methanol synthesis reactor.
  • the same copper-based methanol synthesis catalysts are used in both synthesis reactors.
  • the water cooled reactor is typically operated at a higher synthesis gas inlet temperature than a water cooled reactor in a one step methanol synthesis process to provide higher pressure steam. Furthermore, this reactor is charged with not yet reacted synthesis gas. Due to the high exothermicity of the methanol synthesis, therefore, a very good temperature control of the reactor is necessary to avoid overheating of the catalyst, which would lead to its premature deactivation by loss of active metal surface due to coagulation of the metal crystallites, the so-called sintering.
  • the object of the present invention is therefore to avoid the abovementioned disadvantages and to provide a new, robust, economically advantageous and industrially easy to carry out process for the production of methanol while retaining the advantages of the multistage mode of operation.
  • a preferred embodiment of the invention it is provided to use in a process for methanol synthesis with more than two reaction stages, at least one further, third catalyst with average activity.
  • an optimal adaptation of the catalysts used to the prevailing in the respective reaction stage sharpness of the reaction conditions is achieved.
  • An alternative embodiment of the invention envisages using only two different catalysts with different activity in a process for methanol synthesis with more than two reaction stages. Although in this way a slight Fügig worse adaptation of the catalysts used to the prevailing in the respective reaction stage sharpness of the reaction conditions achieved as in the embodiment described above; however, the restriction to two different types of catalysts leads to logistical advantages and thus to an improved economy of the process.
  • all catalysts used are copper-based.
  • Methanol synthesis catalysts of the type Cu / Zn / Al 2 O 3 are used in virtually all currently operated industrial plants for the synthesis of methanol and are held by the trade with different copper dispersions and therefore different degrees of activity.
  • the at least two reaction stages are integrated into a cycle for unreacted synthesis gas. Even with the highly active catalysts for methanol synthesis available today, only one partial conversion of the synthesis gas to methanol is achieved per pass through a reaction stage, so that the recycling of unreacted synthesis gas to the reaction stages is economically sensible and necessary.
  • the circulation method also serves in a conventional manner for temperature control in the reaction stages due to the highly exothermic reaction.
  • At least one further, catalyst-containing reaction stage is arranged upstream of the synthesis loop as a pre-reactor for the partial conversion of synthesis gas to methanol, wherein the catalyst has a lower activity than the first reaction stage fluid within the synthesis gas cycle.
  • the process according to the invention is further developed in that, downstream of the synthesis gas cycle, at least one further reaction stage containing catalyst is arranged as a post-reactor for the partial conversion of synthesis gas to methanol, the catalyst having a higher activity than the last reaction stage within the synthesis gas cycle. Since the synthesis gas entering the secondary reactor has already largely reacted, the higher activity of the catalyst can be optimally utilized here.
  • the high activity of the methanol synthesis catalyst can advantageously be exploited by introducing the synthesis gas before it enters the postreactor in comparison to the last methanol synthesis reactor within the synthesis loop lower temperatures must be heated, which improves the energy balance of the overall process.
  • a catalyst of lesser activity is not commercially obtained, but such a catalyst is provided by using a partially de-activated methanol synthesis catalyst already used in a process for catalytic methanol synthesis as a catalyst of lesser activity in the process according to the invention.
  • a particular embodiment of this development provides for removal of the partially deactivated catalyst from the last reaction stage of the reaction, filling this reaction stage with fresh, highly active catalyst and using the previously removed, partially deactivated catalyst in an upstream, for example the first reaction stage.
  • this procedure only fresh, highly active catalyst is obtained from the market, whose period of use can be extended according to the invention, resulting in further economic advantages and the amount of catalyst to be disposed of deactivated, is reduced.
  • two reaction stages are present within the synthesis gas cycle, wherein the reaction of the synthesis gas takes place first in a water-cooled reactor and then in a gas-cooled reactor.
  • the invention further relates to a process for the conversion of an existing plant for the production of methanol from synthesis gas, wherein at least two catalyst-containing reaction stages are used with different reaction conditions, in which each synthesis gas is at least partially converted to methanol, wherein the severity of the reaction conditions, as measured the reaction temperature and / or the concentration of carbon monoxide in the synthesis gas decreases from the first to the last reaction stage in the flow direction, which is characterized in that the catalyst is removed in the first reaction stage through which the synthesis gas flows and exchanged for a catalyst with low activity.
  • An alternative embodiment of this method provides, in the regular decommissioning of a method for methanol synthesis with water and gas-cooled reactor according to the prior art to leave the aged, partially deactivated catalyst in the water-cooled reactor and the likewise aged, partially deactivated catalyst in the gas-cooled reactor against fresh to replace highly active catalyst.
  • FIGURE 1 shows schematically a plant for the production of methanol by the process according to the invention.
  • a synthesis gas stream containing hydrogen and carbon oxides is fed via line 1 to a compressor 2 and brought therefrom to the reaction pressure of typically 5 to 10 MPa.
  • the compressed synthesis gas stream is fed via line 3 to a heat exchanger 4 and in this brought to the reaction temperature, wherein usually the heat exchange takes place against the hot product gas stream from the last synthesis reactor (not shown in Fig. 1).
  • the preheated synthesis gas stream enters via line 5 in the gas-cooled synthesis reactor 6, but is not yet chemically reacted here, but initially serves as a cooling gas for receiving the released in reactor 6 heat of reaction.
  • the cooling gas is heated to the reaction temperature to a temperature of 220 to 280 ° C and then enters via line 7 in the water-cooled synthesis reactor 8 a.
  • the partial reaction of hydrogen with carbon oxides on a methanol synthesis catalyst wherein a product mixture is obtained which contains methanol vapor, water vapor and unreacted synthesis gas.
  • the product mixture is removed from the water-cooled synthesis reactor 8 and fed to the gas-cooled synthesis reactor 6, wherein in the conduction path of the line 9 optionally another heat exchanger (not shown in Fig. 1) for adjusting the temperature of the entering into the gas-cooled reactor synthesis gas stream be attached can.
  • a product mixture is obtained, which in turn contains methanol vapor, water vapor and unreacted synthesis gas.
  • a methanol synthesis catalyst of normal activity is used (hereinafter also referred to as the standard type)
  • a highly active and for lower reaction temperatures optimized methanol synthesis catalyst is used.
  • the reaction temperature in the second, gas-cooled synthesis reactor is therefore significantly lower than that in the first, water-cooled synthesis reactor in order to minimize the deactivation rate of the highly active methanol synthesis catalyst.
  • the CO content of the synthesis gas has been lowered sufficiently strongly by reaction in the first, water-cooled synthesis reactor.
  • the space velocity is typically 5000 to 30000 m 3 / (m 3 h) both in the water-cooled and in the gas-cooled synthesis reactor.
  • the released reaction heat serves, as explained above, the heating of the synthesis gas to the reaction temperature, as well as the generation of steam in the water-cooled reactor.
  • the "pro- Duktgasgemisch leaves the gas-cooled synthesis reactor via line 10.
  • the product gas mixture passes via line 12 into the separator 13, where methanol is separated as crude methanol and fed via line 14 to the further product processing.
  • This can be done in a known per se, but not shown in the figure by distillation or rectification.
  • the gas product obtained in the separator is discharged via line 15 and into a purge stream, which is discharged via line 16, and a circuit Ström, which is supplied via line 17 to the cycle compressor 18, separated. Inert components are discharged from the process via the purge stream.
  • the recycle Ström is returned to the synthesis reactor 6, being introduced via line 20 fresh synthesis gas and combined with the circulating stream.
  • the ratio of cycle stream to fresh synthesis gas stream is called the cycle ratio.
  • the invention thus proposes an economical process for the production of methanol, which is characterized by the fact that existing multistage plants for the synthesis of methanol can be reused without conversions.
  • the lower market price of methanol synthesis reactors of lower activity gives rise to economic advantages of the process according to the invention.
  • partial-deactivated methanol synthesis catalysts can advantageously be used further with the process according to the invention. This increases the useful life of the catalysts. Furthermore, the amount of catalyst to be disposed of is reduced, which results in advantages with regard to the environmental compatibility of the process according to the invention.
  • the comparative test was carried out with synthesis gas of the composition indicated below.
  • Inlet temperature 230 ° C (270 ° C between 630 and 700 h)
  • the CO conversions for catalyst types A and B are at a comparable level of 70% and 68%, respectively, after a running time of 120 hours. After 440 h running time the difference between the measured CO sales is already 9%, after 760 h running time even 12%. It should be noted that the reaction temperature was increased from 230 to 270 ° C between 630 and 700 h. Obviously, catalyst type B (optimized for high activity at lower temperatures) tends to more rapidly lose activity under the reaction conditions chosen here, which are typical for methanol synthesis with standard type methanol synthesis catalysts.

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

Abstract

L'invention porte sur un procédé de production de méthanol à l'aide d'un procédé catalytique comportant plusieurs étages de synthèse disposés les uns derrière les autres, dans lesquels la sévérité des conditions de la réaction, mesurée par la température de la réaction et/ou par la concentration de monoxyde de carbone dans le gaz de synthèse, diminue dans le sens de l'écoulement, du premier au dernier étage de réaction. Dans le premier étage de réaction traversé par le gaz de synthèse, on utilise un premier catalyseur ayant une faible activité mais une stabilité élevée à long terme et, dans le dernier étage de réaction traversé par le gaz de synthèse, on utilise un deuxième catalyseur ayant une activité élevée mais une faible stabilité à long terme.
EP11702934A 2010-02-22 2011-01-28 Procédé de production de méthanol Withdrawn EP2539307A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102010008857A DE102010008857A1 (de) 2010-02-22 2010-02-22 Verfahren zur Herstellung von Methanol
PCT/EP2011/000378 WO2011101081A1 (fr) 2010-02-22 2011-01-28 Procédé de production de méthanol

Publications (1)

Publication Number Publication Date
EP2539307A1 true EP2539307A1 (fr) 2013-01-02

Family

ID=43779596

Family Applications (1)

Application Number Title Priority Date Filing Date
EP11702934A Withdrawn EP2539307A1 (fr) 2010-02-22 2011-01-28 Procédé de production de méthanol

Country Status (5)

Country Link
US (1) US20120322651A1 (fr)
EP (1) EP2539307A1 (fr)
CN (1) CN102770401B (fr)
DE (1) DE102010008857A1 (fr)
WO (1) WO2011101081A1 (fr)

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ES2444634T5 (es) † 2011-10-12 2017-07-25 Etogas Gmbh Procedimiento para la fabricación de un gas producto rico en metano, así como instalación apropiada para ello
PL2818458T3 (pl) 2013-06-27 2017-07-31 Haldor Topsøe A/S Sposób wytwarzania metanolu w reaktorach równoległych
CN106458804A (zh) * 2014-06-20 2017-02-22 托普索公司 串联甲醇反应器
DK3334704T3 (da) * 2015-08-12 2023-07-31 Topsoe As Hidtil ukendt fremgangsmåde til fremstilling af methanol fra syntesegas af lav kvalitet
CN105233762B (zh) * 2015-10-23 2018-06-26 湖南安淳高新技术有限公司 甲醇合成反应系统及甲醇合成反应方法
CN105218310B (zh) * 2015-10-23 2017-06-13 湖南安淳高新技术有限公司 甲醇合成反应装置及甲醇合成反应方法
BR112019013078B1 (pt) 2016-12-23 2024-01-02 Carbon Engineering Ltd Método e sistema para sintetizar combustível a partir de fonte de dióxido de carbono diluído
DE102017001520A1 (de) 2017-02-15 2018-08-16 Clariant International Ltd Reaktor und Verfahren zur Maximierung der Methanolausbeute durch Einsatz von Katalysatorschichten
FI3806992T3 (fi) * 2018-06-12 2023-11-20 Topsoe As Menetelmä ja laitos metanolin tuottamiseksi
MY205111A (en) 2018-06-12 2024-10-02 Haldor Topsoe As A process for methanol production using a low-iron catalyst
EP3782973B1 (fr) * 2019-08-19 2023-03-01 L'air Liquide, Société Anonyme Pour L'Étude Et L'exploitation Des Procédés Georges Claude Procédé et installation de fabrication de méthanol
EP3808724A1 (fr) 2019-10-16 2021-04-21 L'air Liquide, Société Anonyme Pour L'Étude Et L'exploitation Des Procédés Georges Claude Procédé de fabrication de méthanol par synthèse en plusieurs étapes
EP3808725A1 (fr) 2019-10-16 2021-04-21 L'air Liquide, Société Anonyme Pour L'Étude Et L'exploitation Des Procédés Georges Claude Procédé de fabrication en plusieurs étapes de méthanol
EP4015496B8 (fr) 2020-12-15 2023-06-07 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé et installation de production de méthanol à partir de gaz de synthèse substochiométrique

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Also Published As

Publication number Publication date
CN102770401A (zh) 2012-11-07
CN102770401B (zh) 2016-04-20
US20120322651A1 (en) 2012-12-20
DE102010008857A1 (de) 2011-08-25
WO2011101081A1 (fr) 2011-08-25

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