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EP2736626A1 - Récupération de chaleur au cours de processus d'absorption et de désorption avec une surface d'échange thermique réduite - Google Patents

Récupération de chaleur au cours de processus d'absorption et de désorption avec une surface d'échange thermique réduite

Info

Publication number
EP2736626A1
EP2736626A1 EP12735090.8A EP12735090A EP2736626A1 EP 2736626 A1 EP2736626 A1 EP 2736626A1 EP 12735090 A EP12735090 A EP 12735090A EP 2736626 A1 EP2736626 A1 EP 2736626A1
Authority
EP
European Patent Office
Prior art keywords
desorption
heat transfer
absorption
solution
transfer section
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.)
Ceased
Application number
EP12735090.8A
Other languages
German (de)
English (en)
Inventor
Johannes Menzel
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
ThyssenKrupp Industrial Solutions AG
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 ThyssenKrupp Industrial Solutions AG filed Critical ThyssenKrupp Industrial Solutions AG
Publication of EP2736626A1 publication Critical patent/EP2736626A1/fr
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • 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
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/541—Absorption of impurities during preparation or upgrading of a fuel
    • 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

Definitions

  • the present invention relates to an economical process for removing components to be separated from industrial gases by means of absorption and desorption processes.
  • the technical gases are usually natural gas or synthesis gas, wherein the synthesis gas is obtained from fossil fuels such as petroleum or coal and from biological raw materials.
  • Natural gas and synthesis gas contain in addition to the useful valuable gases and interfering components such as sulfur compounds, especially sulfur dioxide, carbon dioxide and other components to be separated, as well as hydrogen cyanide and water vapor.
  • flue gases from a combustion of fossil fuels belong to the group of technical gases from which also disturbing components, such. Carbon dioxide are removed.
  • the components to be separated can also be useful gases which are to be separated for a specific purpose.
  • Both physical and chemical absorbents can be used for absorption.
  • Chemically acting absorbents are z.
  • As aqueous amine solutions, alkali salt solutions, etc. Selexol, propylene carbonate, N-methyl-pyrrolidone, Mophysorb, methanol, etc. belong to the physical absorbents.
  • the components to be separated are absorbed by the liquid absorbent. While the solvent-insoluble gas leaves the absorption device at the head, the components to be separated remain dissolved in the liquid absorbent and leave the absorption device at the bottom.
  • the loaded solution is usually preheated by heat exchange with the hot, desorbed solution, thereby recovering a portion of the energy needed for desorption in the desorption apparatus.
  • a reboiler located at the bottom of the desorption is generated by means of a heating medium vapor by partial evaporation of the solvent at the bottom within the desorption.
  • the steam thus produced acts as a stripping medium to expel the components to be separated from the loaded solution.
  • the loaded solution is freed with the stripping medium from the absorbed components to be separated off.
  • the expelled, separated components leave the desorption over the head, the vapor content of the stripping medium is condensed in a top condenser and the desorption is fed back.
  • the of The desorbed solution freed from the components to be separated leaves the desorption device at the sump, with the solution usually being cooled and returned to the head of the absorption device after heat exchange has taken place. This completes the cycle of absorption and desorption processes.
  • an absorption temperature of 20 ° C up to 70 ° C proved to be favorable to remove the components to be separated from the technical gas.
  • the required temperature for desorption in a desorption device is generally higher than that in the absorption device.
  • the desorption is operated at a temperature of 80 ° C up to 140 ° C and at an absolute pressure of 0.2 to 3 bar.
  • An energy saving can be achieved by efficiently utilizing the waste heat from the streams passing through the absorption and desorption process.
  • the loaded solution emanating from the absorption device is introduced into the desorption apparatus for regeneration, e.g. preheated the charged solution by means of the hot solution leaving the desorption device to bring the temperature of the loaded solution closer to the temperature required for desorption.
  • the separated components from the desorption apparatus are cooled in order to recover the stripping vapors as condensate and to process them further. This has hitherto been done in practice by a capacitor.
  • EP 1 569 739 B1 the brimstone vapor rising after stripping is cooled by a condenser in the desorption column by means of cooling water containing hydrogen sulfide.
  • the regenerated solution leaves the desorption at the bottom usually with at least a temperature of 100 ° C.
  • the solution Before the regenerated solution can then be returned to the absorption device, the solution must be cooled to a temperature of 20 ° C to 70 ° C. Heat is removed from the heat exchanger regenerated solution transferred to the cold, loaded solution.
  • the highest possible temperature approximation between the entering into the heat exchanger, hot, regenerated solution and the heat exchanger leaving, preheated, loaded solution allows a correspondingly large recovery, this is achieved in the Desorptionsvornchtung abandoned regenerated solution flow contained heat. In general, this temperature approximation is about 10 K.
  • Such a high temperature approach requires a correspondingly large heat exchange surface, which is associated with correspondingly high costs. Therefore, a temperature approach of less than 10 K for recovering the heat level from the desorption is no longer economically acceptable.
  • EP 1 606 041 B1 discloses a method for the selective removal of sour gas components from natural gas or synthesis gas, wherein the sour gas component is selectively removed within two absorption stages to allow an economical operation.
  • the invention is therefore based on the problem to provide an economically improved process with heat recovery by reduced heat exchange surface over the prior art, which is realized for the removal of components to be separated from industrial gases by absorption and desorption processes.
  • the object is achieved by a method for removing components to be separated from industrial gases by implementing the method by means of absorption and desorption processes which use liquid absorbents, wherein at least one absorption device (20) is provided which at least comprising a mass transfer section in which the components to be separated are taken up by the liquid absorbent and at least one desorption device (22) is provided, the desorption device (22) comprising at least one heat transfer section (22a), a stripping section (22b) and a reboiler (8) at the sump, wherein the heat transfer section (22a) is located above the stripping section (22b) and the temperature in the desorption device (22) is higher than the temperature in the absorption device (20).
  • the laden with components to be separated solution is heated by a heat exchanger before this solution of Desorptionsvornchtung (22) is supplied.
  • the remainder of the energy required for desorption is provided by the reboiler (8) in the bottom of the desorption apparatus (22).
  • the components to be separated by the stripping medium leave the head of the stripping section (22b) as vapors which are introduced into the heat transfer section (22a), cooled accordingly, and leave the desorption device (22) over the head.
  • the solution freed from the components to be separated after desorption leaves the desorption device (22) at the sump and, after heat exchange and cooling, is returned to the top of the absorption device (20).
  • At least part of the absorbent device (20) leaving laden solution is diverted before being heated by a heat exchanger and applied to the head of the heat transfer section (22a).
  • This loaded partial stream is warmed up by the heat rising from the lower part of the desorption device (22b) by heat exchange in the heat transfer section (22a).
  • the residual flow of the cold, laden solution leaving the absorption device (20) is preheated by heat exchange by means of the hot, regenerated solution leaving the desorption device (22), the heat exchange being designed such that the total requirement of the heat exchange surface for the absorption and desorption process is reduced becomes.
  • the absorbent device (20) leaving laden solutions can be abandoned without branching all the way to the head of the heat transfer section (22a) for heating.
  • the heating by the heat transfer section (22a) may be a direct or indirect heat transfer.
  • the vapor from the stripping section (22b) releases its heat to the laden solution to be heated.
  • the heat transfer section (22a) has a mass transfer section equipped with mass transfer elements wherein direct heat transfer is performed, the mass transfer elements structuring in-column internals used for heat and mass transfer, such as packing Packings, soils (bells, valves, sieve plates) etc. are meant.
  • the trickled down solution absorbs the heat from the rising vapor, the vapor is cooled accordingly.
  • the heat transfer section (22a) may be configured with a condenser in which indirect heat transfer is performed. By the condenser, on the one hand, the ascending vapor is cooled as required, on the other hand, the laden solution to be heated is warmed up as desired.
  • the preheated substream is further fed into the stripping section (22b) or the preheated substream is withdrawn below the heat transfer section (22a) leaving with the absorber (20), cold residual stream (5a, 5b) brought together by a heat exchanger (21) by means of the desorption device (22) leaving hot, regenerated solution further warmed, then fed to the stripping section (22b).
  • a further advantageous embodiment is: the preheated partial stream is withdrawn below the heat transfer section (22a), combined with the preheated residual stream of the solution, and further heated by a further heat exchanger by means of the desorption device (22) leaving, hot, regenerated solution, then to the Stripping section (22b) abandoned.
  • a physically or a chemically acting absorbent can be used.
  • the process can be used to remove acid gas components from industrial gases.
  • Fig. 1 illustrates the prior art.
  • Fig. 3 represents an alternative of the procedure according to the invention, wherein the preheated in the heat transfer section (22a) current is completely guided to the head of the stripping section (22b).
  • the desorption (22) at least one heat transfer section (22 a) Mass transfer element / condenser, a stripping section (22b), and at the sump comprises a reboiler (8).
  • the stripping medium at the sump heats up the stripping medium in order to expel the components to be separated from the loaded solution in the stripping section (22b).
  • the absorption device leaving cold, laden solution (3) is branched off before warming, a part (4) is placed on the head of the heat transfer section (22a), the rest (5a) is merged with the preheated partial flow and through a heat exchanger (21) further warmed up.
  • the cold, charged solution stream (4) applied to the heat transfer section (22a) leads to cooling and condensation of the stripping vapor rising from the sump. In this case, virtually all of the existing in the stripping steam to the heat from the head down trickling solution directly or indirectly transmitted.
  • the cooled vapor (13) with the components to be separated leaves the head of the desorption device at approximately a temperature at which the loaded solution (4) enters the heat transfer section (22a).
  • a high temperature approach between the overhead vapor (13) and the abandoned laden solution (4) is made possible by the direct / indirect heat and mass exchange in the heat transfer section (22a).
  • the preheated solution (4a) is withdrawn below the heat transfer section (22a), merged with the residual stream (5a) and fed to the heat exchanger (21) to further warm the so-merged stream.
  • the already regenerated solution (9, 10) flows through the same heat exchanger (21) and is thereby cooled.
  • FIG. 3 another variant is illustrated. The difference from FIG. 2 is that the stream preheated via the heat transfer section (22a) is no longer drawn out of the desorption device but is fed further to the top of the stripping section (22b).
  • the heat exchangers are all considered as shell and tube heat exchangers.
  • WT heat exchanger Table 1: Total exchange area for a prior art absorption and desorption processes.
  • Table 2 Total exchange surface for an absorption and desorption processes according to the method of the invention with carrying out the preheated in the heat transfer section (22a) solution stream.
  • Table 3 Total exchange surface for an absorption and desorption processes according to the invention, wherein the solution stream preheated in the heat transfer section (22a) is led completely to the top of the stripping section (22b).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Gas Separation By Absorption (AREA)
  • Treating Waste Gases (AREA)

Abstract

L'invention concerne un procédé d'extraction de composants à séparer de gaz industriels au moyen de processus d'absorption et de désorption, par l'utilisation d'agents absorbants liquides. Selon ce procédé, au moins une partie de la solution chargée sortant de l'installation d'absorption (20) est dérivée avant son chauffage et introduite dans la tête de la section de transfert thermique (22a), et ce courant partiel chargé est réchauffé dans la section de transfert thermique (22a), par échange de chaleur avec la vapeur s'élevant depuis la partie inférieure de l'installation de désorption (22b), tandis que le courant restant de solution chargée froide sortant le l'installation d'absorption (20) est préchauffé par échange de chaleur avec la solution régénérée chaude sortant de l'installation de désorption (22), l'échange de chaleur étant réglé de manière à réduire la consommation d'énergie totale des processus d'absorption et de désorption.
EP12735090.8A 2011-07-25 2012-06-27 Récupération de chaleur au cours de processus d'absorption et de désorption avec une surface d'échange thermique réduite Ceased EP2736626A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102011108308A DE102011108308A1 (de) 2011-07-25 2011-07-25 Wärmerückgewinnung bei Absorptions- und Desorptionsprozessen bei reduzierter Wärmeaustauschfläche
PCT/EP2012/002690 WO2013013750A1 (fr) 2011-07-25 2012-06-27 Récupération de chaleur au cours de processus d'absorption et de désorption avec une surface d'échange thermique réduite

Publications (1)

Publication Number Publication Date
EP2736626A1 true EP2736626A1 (fr) 2014-06-04

Family

ID=46508307

Family Applications (1)

Application Number Title Priority Date Filing Date
EP12735090.8A Ceased EP2736626A1 (fr) 2011-07-25 2012-06-27 Récupération de chaleur au cours de processus d'absorption et de désorption avec une surface d'échange thermique réduite

Country Status (6)

Country Link
US (1) US20150321137A1 (fr)
EP (1) EP2736626A1 (fr)
AU (1) AU2012289277A1 (fr)
CA (1) CA2842982A1 (fr)
DE (1) DE102011108308A1 (fr)
WO (1) WO2013013750A1 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3024563A4 (fr) * 2013-07-23 2017-08-16 Carbon Clean Solutions Pvt. Ltd. Système de ligne dédoublée, procédé et traitement pour récupération du co2
JP5863741B2 (ja) * 2013-10-15 2016-02-17 三菱重工業株式会社 Ｃｏ２回収装置

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010086039A1 (fr) * 2009-01-28 2010-08-05 Siemens Aktiengesellschaft Procédé et dispositif de séparation du dioxyde de carbone contenu dans un gaz d'échappement d'une centrale électrique à combustible fossile

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US4152217A (en) * 1978-06-30 1979-05-01 Exxon Research & Engineering Co. Amine regeneration process
DE19945326B4 (de) 1999-01-22 2008-03-27 Uhde Gmbh Verfahren zur Entfernung von Kohlendioxid, Schwefelverbindungen, Wasser und aromatischen und höheren aliphatischen Kohlenwasserstoffen aus technischen Gasen
DE10258067A1 (de) 2002-12-11 2004-07-01 Thyssenkrupp Encoke Gmbh Verfahren und Vorrichtung zur Kühlung von Brüdendämpfen in einer Desorptionskolonne
DE10313438A1 (de) 2003-03-26 2004-11-04 Uhde Gmbh Verfahren zur selektiven Entfernung von Schwefelwasserstoff und CO2 aus Rohgas
JP4690659B2 (ja) * 2004-03-15 2011-06-01 三菱重工業株式会社 Ｃｏ２回収装置
DE102005004948B3 (de) 2005-02-02 2006-03-02 Uhde Gmbh Verfahren zur Erhöhung der Selektivität von physikalisch wirkenden Lösungsmitteln bei einer Absorption von Gaskomponenten aus technischen Gasen
JP5021917B2 (ja) * 2005-09-01 2012-09-12 三菱重工業株式会社 Ｃｏ２回収装置及び方法
JP5230080B2 (ja) * 2006-06-06 2013-07-10 三菱重工業株式会社 吸収液、ｃｏ２の除去装置及び方法
CA2718386A1 (fr) * 2008-03-13 2009-09-17 Shell Internationale Research Maatschappij B.V. Procede pour l'elimination de dioxyde de carbone a partir d'un gaz

Patent Citations (1)

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Publication number Priority date Publication date Assignee Title
WO2010086039A1 (fr) * 2009-01-28 2010-08-05 Siemens Aktiengesellschaft Procédé et dispositif de séparation du dioxyde de carbone contenu dans un gaz d'échappement d'une centrale électrique à combustible fossile

Non-Patent Citations (1)

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Title
See also references of WO2013013750A1 *

Also Published As

Publication number Publication date
US20150321137A1 (en) 2015-11-12
CA2842982A1 (fr) 2013-01-31
WO2013013750A1 (fr) 2013-01-31
DE102011108308A1 (de) 2013-01-31
AU2012289277A1 (en) 2014-02-06

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