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EP2496518A1 - Réacteur chimique à prélèvement de chaleur - Google Patents

Réacteur chimique à prélèvement de chaleur

Info

Publication number
EP2496518A1
EP2496518A1 EP10770820A EP10770820A EP2496518A1 EP 2496518 A1 EP2496518 A1 EP 2496518A1 EP 10770820 A EP10770820 A EP 10770820A EP 10770820 A EP10770820 A EP 10770820A EP 2496518 A1 EP2496518 A1 EP 2496518A1
Authority
EP
European Patent Office
Prior art keywords
gas
reactor
water
heat exchanger
chemical reactor
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Withdrawn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
EP10770820A
Other languages
German (de)
English (en)
Inventor
Roland Birley
Frank Hannemann
Daniel Hofmann
Nicolas Vortmeyer
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.)
Siemens AG
Original Assignee
Siemens AG
Siemens Corp
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 Siemens AG, Siemens Corp filed Critical Siemens AG
Publication of EP2496518A1 publication Critical patent/EP2496518A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
    • 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
    • B01J2219/24—Stationary reactors without moving elements inside
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1005—Arrangement or shape of catalyst
    • C01B2203/1035—Catalyst coated on equipment surfaces, e.g. reactor walls
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • C01B2203/84—Energy production
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F05—INDEXING SCHEMES RELATING TO ENGINES OR PUMPS IN VARIOUS SUBCLASSES OF CLASSES F01-F04
    • F05D—INDEXING SCHEME FOR ASPECTS RELATING TO NON-POSITIVE-DISPLACEMENT MACHINES OR ENGINES, GAS-TURBINES OR JET-PROPULSION PLANTS
    • F05D2220/00—Application
    • F05D2220/70—Application in combination with
    • F05D2220/72—Application in combination with a steam turbine
    • F05D2220/722—Application in combination with a steam turbine as part of an integrated gasification combined cycle
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the invention relates to a chemical reactor with continuous heat extraction.
  • IGCC Integrated Gasification Combined Cycle
  • the CO2 is then separated by an additional wash, compacted and transported to the storage sites.
  • the synthesis gas from other pollutants such as dust and Sweden ⁇ feltagenen is cleaned demands of air pollution control and technical requirements in the gas turbine to genü-
  • the remaining hydrogen is diluted with nitrogen and water vapor and burned in a gas turbine.
  • the resulting hot exhaust gases are used to generate steam;
  • the steam is used for further power generation in a steam turbine.
  • the task is to further develop the shift reactor and the CO shift process so that improved plant efficiency is achieved.
  • the catalytically active surfaces would be on the swept by the raw gas heat exchanger outer surfaces and the heat can be delivered directly to a suitable medium. It is expedient if the surface of the réelletau ⁇ shear surfaces catalyzes or effects a conversion of carbon monoxide and water into hydrogen and carbon dioxide.
  • the gas-tight wall also has a catalytically active surface. Thus, the catalytically active surface can be increased while maintaining a low pressure loss.
  • the feed means for the second fluid are arranged distributed in the direction of a longitudinal axis of the Gaska ⁇ nals in the gas channel, the second fluid is admiffleßi ⁇ wise water, which must be fed to the shift process.
  • the gradual addition of water has the advantage of being able to use a small amount of additional water (just as much as necessary for the process) to achieve the highest possible efficiency.
  • the gas duct is designed in a horizontal construction and can be flowed through in a substantially horizontal direction by gas, the heat exchanger surfaces being evaporator heating surfaces or economizer heating surfaces.
  • the heat generated during the conversion can be used directly in the power plant process.
  • the reactor is integrated in a power plant with a gas turbine, a steam turbine ⁇ ne and a gas turbine upstream BrennstoffVerga ⁇ solution, wherein it is connected between the BrennstoffVergasung and the gas turbine.
  • the object is achieved in that a carbon monoxide-containing gas over several heat exchanger surfaces with kata- lytically effective surface is passed and water in the flow direction of the gas is distributed to the gas supplied.
  • the heat exchanger surfaces are formed by tubes through which water is passed, wel ⁇ ches thereby heated and can be used elsewhere in the power plant process.
  • the previously split in stages shift reaction is transferred into a quasi-continuous reaction and heat removal process.
  • the inventive chemical reactor offers large catalyst surfaces and lower pressure losses than the usual catalyst bed.
  • the technology is not limited to IGCC applications, but could also be used in other reactions, such as the production of synthetic natural gas or substitute natural gas (SNG), a natural gas substitute based on coal , especially Lignite, or biomass (Bio-SNG or Biome ⁇ than) is produced via synthesis gas.
  • SNG synthetic natural gas or substitute natural gas
  • Bio-SNG or Biome ⁇ than is produced via synthesis gas.
  • Figure 2 is a schematic synthesis gas temperature profile over the reactor according to the invention.
  • Figure 3 is a schematic synthesis gas temperature profile over prior art reactors.
  • the arrangement in Figure 1 has two main components: the gasification reactor 1 and the chemical reactor 2 according to the invention for the conversion of carbon monoxide.
  • the conversion of the feedstock 3 (which are fossil or renewable fuels and residues, such as natural gas, Erd ⁇ olfr hopeen, coal, biomass or waste) takes place in the gasification reactor 1 in a flame reaction.
  • the amongst other things resulting hot raw gas 4 flows from the gasification reactor 1 through various stations, such as a waste heat ⁇ unit 19 for cooling the raw gas from the gasification Tempe ⁇ temperature to about 700 ° C to 900 ° C at which ideally high ⁇ pressure steam
  • the aim of the quench is an increase in the proportion of water vapor in the raw gas for the subsequent water gas shift reaction in the chemical reactor 2, and / or a quench unit 20.
  • the gas channel 5 of the chemical reactor 2 comprises heat exchanger surfaces 6 constructed from tubes. These can be arranged in the gas channel 5 or can also form the surrounding wall 7 of the gas channel 5.
  • the steam generator tubes which are not illustrated in more detail, are gas-tightly welded to one another at their longitudinal sides via webs or so-called fins. A plurality of mutually adjacent tubes is combined in this way to a heat exchanger surface 6.
  • the inlet ends 8 of the tubes forming a heat exchanger surface 6 at the downstream end 9 of the chemical reactor 2 are supplied, for example, with feed water via a common inlet collector (not shown). In this case, the heat exchanger surface 6 is used as the economizer heating surface 10.
  • the feed water heated in the tubes of the economizer heating surface 10 as a result of the heating by the synthesis gas flows via a common outlet collector (not shown) and is subsequently fed to an evaporator unit.
  • the evaporator ⁇ unit 11 may also in the chemical reactor 2, ⁇ example, in the direction of flow of the synthesis gas upstream of the economizer 10 may be disposed.
  • the water preheated by the economizer 10 can also be supplied to the heat exchanger surfaces 6 in the evaporator 11 via an inlet header. In the evaporator unit 11, the preheated water is evaporated to low, medium or high pressure steam and, likewise via corresponding collector, for example, a superheat purity ⁇ 12 supplied.
  • the heat exchange surfaces 6 can also embritthit- for wetting of the effluent 13 from a first turbine stage of a steam turbine, partially relaxed flow medium into ⁇ sets, so that the flow medium then again the next stage of the steam turbine is fed to heated.
  • heat transfer to the flow medium flowing through the heat exchanger surfaces 6 heat of the synthesis gas flowing in the gas channel 5 is continuously removed as the flow path progresses. However, heat is generated again as a result of the water gas shift reaction. To control this reaction, and thus the temperature of the synthesis gas What ⁇ ser is distributed at various points and in the longitudinal direction of the gas channel 5 introduced into the synthesis gas stream.
  • the What ⁇ serein technischevortechnischevorraum 14.
  • the nozzles of the Eindüsevorraum are adjusted and oriented such that the smallest possible water quantity (even as much as for the process necessary) is provided to the highest possible system efficiency to Errei ⁇ chen.
  • the heating surfaces of the economizer and the evaporator and, if necessary, superheater are provided with a catalyst layer for the water ⁇ gas shift reaction. Through the catalyst material, the activation energy for the shift reaction in which carbon monoxide and water into carbon dioxide and hydrogen are converted, lowered and thus changed ⁇ changed their kinetics.
  • FIG. 2 shows schematically the temperature profile of the synthesis ⁇ gas from the reactor inlet 15 to the reactor outlet 9.
  • this temperature profile is not necessarily horizontal (A), but according to the Equil ⁇ weight of the water gas shift reaction tend to fall towards the end of the gas channel 5 (B) to take into account the fact that at higher temperature but a fast kinetics there is an unfavorable chemical equilibrium and at lower temperatures the equilibrium is stronger on the right side of the reaction equation, but the kinetics decrease.
  • the temperature profile does not have to be linear.
  • Figure 3 shows the temperature profile, as in the prior art when using a high-temperature 16 and a
  • Low-temperature shift stage 17 with interposed heat ⁇ exchanger 18 would look like.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Industrial Gases (AREA)

Abstract

L'invention concerne un réacteur chimique (2) dans une installation technique, en particulier une centrale électrique, qui comprend une paroi étanche aux gaz formant un conduit de gaz (5). Selon l'invention, on place dans le conduit de gaz (5) des surfaces d'échange thermique dans lesquelles un premier fluide peut s'écouler et qui présentent au moins en partie une surface catalytiquement active. L'invention concerne également un procédé de conversion de CO à l'aide d'un tel réacteur.
EP10770820A 2009-11-04 2010-10-26 Réacteur chimique à prélèvement de chaleur Withdrawn EP2496518A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102009051938A DE102009051938A1 (de) 2009-11-04 2009-11-04 Chemischer Reaktor mit Wärmeauskopplung
PCT/EP2010/066140 WO2011054698A1 (fr) 2009-11-04 2010-10-26 Réacteur chimique à prélèvement de chaleur

Publications (1)

Publication Number Publication Date
EP2496518A1 true EP2496518A1 (fr) 2012-09-12

Family

ID=43413654

Family Applications (1)

Application Number Title Priority Date Filing Date
EP10770820A Withdrawn EP2496518A1 (fr) 2009-11-04 2010-10-26 Réacteur chimique à prélèvement de chaleur

Country Status (6)

Country Link
US (1) US20120216501A1 (fr)
EP (1) EP2496518A1 (fr)
KR (1) KR20120093259A (fr)
CN (1) CN102639434A (fr)
DE (1) DE102009051938A1 (fr)
WO (1) WO2011054698A1 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP6128932B2 (ja) * 2013-04-22 2017-05-17 株式会社神戸製鋼所 処理装置及び処理方法
US10076739B1 (en) 2014-07-22 2018-09-18 Precision Combustion, Inc. Chemical reactor for use with overly reactive chemicals
DE102015219391A1 (de) 2015-10-07 2017-04-13 Siemens Aktiengesellschaft Verfahren zum Betreiben eines Gas-und-Dampf-Kombinationskraftwerks

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2465235A (en) * 1949-03-22 Production of hydrogen
DE1964810C3 (de) * 1969-12-24 1979-04-05 Siemens Ag, 1000 Berlin Und 8000 Muenchen Vorrichtung zur Gewinnung von Wasserstoff
DE2709768A1 (de) * 1977-03-07 1978-09-21 Metallgesellschaft Ag Verfahren zum katalytischen konvertieren von rohgas aus der vergasung fester brennstoffe
CA2405927A1 (fr) * 2000-04-17 2001-10-25 Shell Internationale Research Maatschappij B.V. Processeur de combustible
US20040148862A1 (en) * 2003-01-31 2004-08-05 Yu Paul Taichiang WGS reactor incorporated with catalyzed heat exchanger for WGS reactor volume reduction
ES2319285T3 (es) * 2004-08-05 2009-05-06 Saudi Basic Industries Corporation Proceso con un intercambiador de calor recubierto con un catalizador.
US20070072949A1 (en) * 2005-09-28 2007-03-29 General Electric Company Methods and apparatus for hydrogen gas production

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2011054698A1 *

Also Published As

Publication number Publication date
DE102009051938A1 (de) 2011-05-26
CN102639434A (zh) 2012-08-15
WO2011054698A1 (fr) 2011-05-12
KR20120093259A (ko) 2012-08-22
US20120216501A1 (en) 2012-08-30

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