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WO2015074747A1 - Procédé et dispositif d'épuration de gaz de procédé provenant de la déshydrogénisation oxydative d'hydrocarbures - Google Patents

Procédé et dispositif d'épuration de gaz de procédé provenant de la déshydrogénisation oxydative d'hydrocarbures Download PDF

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Publication number
WO2015074747A1
WO2015074747A1 PCT/EP2014/003060 EP2014003060W WO2015074747A1 WO 2015074747 A1 WO2015074747 A1 WO 2015074747A1 EP 2014003060 W EP2014003060 W EP 2014003060W WO 2015074747 A1 WO2015074747 A1 WO 2015074747A1
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WO
WIPO (PCT)
Prior art keywords
process gas
scrubber
carbon dioxide
gas
aldehydes
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
PCT/EP2014/003060
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German (de)
English (en)
Inventor
Oliver Noll
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
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Filing date
Publication date
Application filed by ThyssenKrupp Industrial Solutions AG filed Critical ThyssenKrupp Industrial Solutions AG
Publication of WO2015074747A1 publication Critical patent/WO2015074747A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/42—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor
    • C07C5/48—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
    • 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
    • B01D53/1406—Multiple stage absorption
    • 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
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/202—Alcohols or their derivatives
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20436—Cyclic amines
    • B01D2252/20447—Cyclic amines containing a piperazine-ring
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20478—Alkanolamines
    • B01D2252/20484—Alkanolamines with one hydroxyl group
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • B01D2257/702—Hydrocarbons
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • 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
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • 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
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the present invention relates to a process for the purification of process gases obtained in the oxidative dehydrogenation of hydrocarbons.
  • the process can be carried out by means of a device which is suitable for retrofitting existing plants but can also be installed in new plants.
  • ODH catalytic oxidative dehydrogenation
  • catalytic ODH processes can be operated from alkanes to olefins with reduced costs, lower greenhouse gas emissions, and lower energy input.
  • An essential economic reason for the construction of an ODH plant is also the demand for propylene, which is currently rising faster than the demand for ethylene.
  • Low molecular weight alkenes such as ethene and propene can also be formed by non-oxidative dehydrogenation of the corresponding alkanes.
  • Non-oxidative dehydrogenation reactions are endothermic and result in the simultaneous formation of carbon dioxide and lower molecular weight alkanes. Both side reactions lead to reduced yields of olefins.
  • the ODH of light alkanes affords the possibility of an attractive route to alkenes, since the reaction is exothermic and the thermodynamic boundary conditions of non-oxidative routes through formation of water
  • CONFIRMATION COPY be avoided as a by-product.
  • ODH ODH by the STAR method, selective hydrogen combustion and dehydrogenation occur simultaneously; in the
  • Oxyreaktor therefore run two main reactions.
  • the deposition of carbon during ODH is reduced, which has a stabilizing effect on the catalytic activity.
  • the yield of alkenes by the ODH is limited by the fact that most catalysts promote combustion of the alkene to CO and CO 2 .
  • alkanes such as propane
  • propane dehydrogenation for example, propene is formed as
  • ODH ODH
  • STAR STeam Active Reforming
  • Water vapor partially converted to hydrogen and alkene Water vapor partially converted to hydrogen and alkene.
  • the heat supply in this implementation is generally carried out by an indirect heating, for example in a reformer.
  • the process gas is added from the first reactor with oxygen and the hydrogen contained in the process gas is partially oxidized to water, whereby the equilibrium in the direction of
  • Alkene formation is postponed.
  • the STAR technology is preferred for
  • lower alkenes for example propene from propane or from Isobutene from isobutane, used.
  • the STAR process uses a precious metal catalyst supported on a zinc-calcium aluminate.
  • alkane to alkene e.g., alkene
  • alkane to alkene is sequentially catalytically oxidized in an alloteric reformer and autothermal oxyreactor.
  • Propane to propene, dehydrated, with one of the by-products 2-4% carbon dioxide is formed.
  • the carbon dioxide has to be removed from the process gas in order to minimize propene losses through subsequent low-temperature treatment.
  • the crude gas loaded with CO 2 enters the bottom of an absorber, usually an absorption column, and flows upward through it.
  • Clean detergent is added to the absorption column via beds and trickles down in countercurrent to the gas to be purified.
  • the detergent loads in the direction of thermodynamic equilibrium with the carbon dioxide to be washed out of the gas, so that the gas leaves the wash column with reduced carbon dioxide content; the detergent, however, leaves the
  • wash column loaded with carbon dioxide state Before being used again as a low-carbon laundry detergent for leaching it must be freed from its own carbon dioxide loading.
  • the regeneration of the detergent preferably takes place at elevated temperature in a desorber in which, for reasons of energy optimization, a first heat exchanger, the loaded detergent heated and at the same time the warm, regenerated and thus low-carbon dioxide detergent cools.
  • a further heating of the absorbent can take place in a heater before the desorber or in another apparatus which is located at the bottom of the desorber usually designed as a regenerating column. The heated detergent trickles down in the desorber over the bed, with part of the
  • Carbon dioxide goes back into the gas phase and rises in the desorber upwards. At the top of the desorber, the carbon dioxide is cooled to condense evaporated detergent and to be able to return it to the process. Water introduced into the process with the raw gas can be discharged here. Desorption by pressure reduction can be arranged with the help of a head desorber
  • Vacuum pump to be performed An example of a regeneration of an amine-containing washing solution resulting from the purification of gases can be found in DE 10 2007 048 565 B3.
  • the carbon dioxide can be expelled from the detergent through a stripping gas stream.
  • the low-carbon detergent from the bottom of the regenerating column can now be loaded again in the absorber. For this it is to cool to absorber temperature, which is e.g. can be done by treatment in a detergent countercurrent and / or in a cooled with cooling water heat exchanger.
  • Suitable bases are primary alkanolamines, e.g. Monoethanolamine (MEA) or diglycolamine (DGA, chemical: 2- (2-aminoethoxy) ethanol), or secondary alkanolamines, e.g. Diethanolamine (DEA) or diisopropanolamine (DIPA); or tertiary alkanolamines, e.g. Triethanolamine (TEA) or methyldiethanolamine (MDEA).
  • MEA or DEA can lead to a significant improvement in the activity of tertiary alkanoalamines.
  • activated MDEA aMDEA
  • aMDEA activated MDEA which has been activated with the addition of monomethyl MEA or piperazine has been found to be particularly beneficial.
  • alkanolamines In addition to the above basic types of alkanolamines, there are still commercially available various tailor-made alkanolamine blends with various additives (activators, corrosion inhibitors and antifoams). These include, for example, the Cansolv amine from Cansolv Technology Inc.
  • Another class of amines are the so-called sterically hindered amines.
  • the reaction between carbon dioxide and amine can be controlled and thus a higher selectivity can be generated.
  • KS series detergents from Mitsubishi Heavy Industries and Kansai Electric Power Company belong to this group.
  • Process gas remains gaseous. Thereafter, the process gas is subjected to gas scrubbing to remove the carbon dioxide. Surprisingly, it has been found that by prior increased deposition of aldehydes from the
  • One possible technical approach to solving the problem would be to change the type of wash solution in the gas scrub to remove carbon dioxide.
  • the aMDEA process could be replaced by other carbon dioxide removal processes.
  • a solvent would have to be found which does not react with the aldehydes.
  • this procedure has the consequence that either other residual contents of carbon dioxide in the process gas are to be accepted after the absorber or apparatuses have to be replaced by the scrubber recovery.
  • the change in the washing solution means that the tolerance limits for the carbon dioxide content in the purified process gas can no longer be complied with and that additional measures for gas scrubbing must be taken.
  • Aldehydes acetaldehyde and acrolein in the downstream absorber in the aMDEA wash react with the activator piperazine to form a solid. This means that even the smallest amounts of these aldehydes lead in the long term to a solid accumulation in the absorber and consequently also to a clogging.
  • One approach to remedying the problems in the aMDEA wash would be to scrub the process gas with water directly from the absorber inlet. If the water of a pure water wash is not continuously regenerated, the aldehydes will accumulate and after some time, this pure water wash becomes useless because of a physical phase equilibrium between process gas and wash water. However, a regeneration can also be replaced by an ejection.
  • Reaction zone can not be avoided in the short term.
  • the approach proposed by the present invention contemplates to utilize the reactivity of selected chemicals in a prewash to achieve the desired performance
  • a scrubber upstream of the scrubber (hereinafter also referred to as "scavenger") which adds water to small amounts of aldehyde-reactive chemicals such as piperazine or the like, preferably contains primary or secondary amines, removes the unwanted aldehydes and the gas scrubbing can be operated unchanged as planned.
  • the present invention therefore relates to an improved process for removing carbon dioxide from the process gas of an oxyreactor comprising the following
  • the alcohols, amines and amino alcohols used in the pre-scrubber react with the aldehydes in the process gas. This results in a known manner hemiacetals, acetals, imines or enamines.
  • suitable alcohols are aliphatic alcohols having one to six carbon atoms and preferably one hydroxy group, for example methanol, ethanol, propanol, isopropanol, butanols, pentanols and hexanols.
  • Suitable amines are primary aliphatic or aromatic amines having one to seven carbon atoms and one to two amino groups, such as methylamine,
  • Amino groups e.g. the N-methyl or N-ethyl derivatives of the above primary amines; or secondary cycloaliphatic amines having four to five
  • Ring carbon atoms and one to two ring nitrogen atoms such as pyrrolidine, piperidine or piperazine.
  • Suitable amino alcohols are primary alkanolamines having one to six carbon atoms and having one or two amino groups and having one
  • Hydroxyl group such as MEA or DGA, or secondary alkanolamines having two to seven carbon atoms and having one or two amino groups and one to two
  • Hydroxyl groups such as DEA or DIPA, or tertiary alkanolamines having three to eight carbon atoms and having one or two amino groups and one to three
  • Hydroxyl groups such as TEA or MDEA.
  • the content of alcohol, amine and / or aminoalcohol in the aqueous solution intended for use in the pre-scrubber is typically between 1 and 50% by weight, in particular between 2 and 25% by weight, and very particularly preferably between 3 and 15% by weight, in each case based on the total amount of the aqueous solution.
  • the pre-scrubber can be formed by the reaction with the aldehydes solids, which can lead to clogging of the pre-scrubber. It may therefore be necessary to occasionally remove the solid deposits or the
  • the pre-scrubber could therefore be realized in duplicate or preferably be equipped with a bypass. Solids which are formed in the scrubber are preferably removed by suitable, redundant filter systems, in particular in one circulation.
  • at least one small discharge of deposits from the pre-scrubber is provided, which is effected by a supply of fresh aqueous scrubbing solution, preferably an amine-containing scrubbing solution.
  • the wash water used in the pre-scrubber does not need to be cleaned because it is not used to remove carbon dioxide.
  • carbon dioxide dissolves to saturation, but according to our laboratory tests it has no negative influence on the formation of solids or the reaction of the aldehydes with the chemicals used. It is irrelevant for the formation of solids or for the reaction of the aldehydes with the chemicals used, whether loaded with carbon dioxide or unloaded wash water comes into contact with the process gas.
  • the reactive dissolved chemical e.g. The amine reacts with the aldehyde and must be replenished from time to time.
  • a pack washer is used. This is preferably similar to the pack scrubber which is used in the downstream stage for Kohledioxidentfernung. In this embodiment, there is the risk that uses an uncontrollable foaming in this scrubber. Possible countermeasures in addition to the addition of anti-foaming agents in combination with a filtration is the setting of a suitable concentration of the aldehyde-reacting Chemikaiie in the washing solution. It should also be noted that the circulation rates can be significantly reduced so that low relative fluid velocity does not necessarily mean large cross sections. If necessary, a trickle bed reactor can also be used at low fluid velocities.
  • a bubble column reactor is used to ensure intimate contact of the process gas with the wash water.
  • the process gas occurs at the bottom of the bubble column reactor, for example, through nozzles or a frit finely distributed in a standing
  • the solid which forms can be removed by discontinuous replacement of the wash water solution.
  • a circulation of the reacting with aldehyde chemicals can be added
  • Gas scrubbing is the complete use of the previous process concept for the treatment of partially reacted process gases from oxyreactors, for example, from the oxyreactor of STAR propane dehydrogenation, without the existing
  • Equipment needs to be changed. Although the washing solution in the pre-scrubber does not need to be regenerated, it should be cleaned from time to time. Because the chemicals present in the wash solution react, they must be added continuously or discontinuously.
  • the pre-wash selectively removes those components which cause foaming and solid accumulation in the downstream gas scrub to remove the carbon dioxide. If the downstream gas scrubber is operated with aMDEA to remove the carbon dioxide, it is best to pre-wash with an aqueous piperazine solution, so that contamination of the aMDEA with another amine is not possible. Alternatively, a little volatile amine can advantageously be used here.
  • the inventive idea is to observe the observed solids formation
  • the regeneration of the detergent takes place at elevated temperature in a desorber.
  • the invention also relates to a device suitable for carrying out the method described above. This is characterized by the presence of the following features:
  • a reaction of saturated hydrocarbons in the presence of steam to form olefinically unsaturated hydrocarbons and simultaneous conversion of hydrogen with oxygen to water preferably takes place in the oxy reactor A), resulting in a process gas containing saturated hydrocarbons, olefins, aldehydes and carbon dioxide.
  • the pre-scrubber is a pack scrubber, a trickle bed reactor, a bubble column reactor or, in particular, a spray scrubber.

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

Abstract

L'invention concerne un procédé permettant d'éliminer le dioxyde de carbone présent dans le gaz de procédé d'un réacteur d'oxydation, comprenant les étapes suivantes : i) l'introduction dans un pré-laveur d'un gaz de procédé provenant d'un réacteur d'oxydation et contenant des oléfines, des aldéhydes et du dioxyde de carbone; ii) le traitement du gaz de procédé dans le pré-laveur au moyen d'une solution aqueuse qui contient des alcools, des amines et/ou des aminoalcools, pour éliminer les aldéhydes présents dans le gaz de procédé; iii) l'introduction du gaz de procédé débarrassé des aldéhydes dans un absorbeur d'un système de lavage de gaz monté en aval du pré-laveur, afin d'éliminer le dioxyde de carbone présent dans le gaz de procédé; iv) et le traitement du gaz de procédé dans l'absorbeur au moyen d'une solution aqueuse contenant une amine et/ou un aminoalcool, et élimination du dioxyde de carbone présent dans le gaz de procédé. Le procédé constitue une amélioration des procédés connus du fait qu'il permet de réduire nettement la formation de mousse dans l'absorbeur du système de lavage de gaz.
PCT/EP2014/003060 2013-11-19 2014-11-14 Procédé et dispositif d'épuration de gaz de procédé provenant de la déshydrogénisation oxydative d'hydrocarbures Ceased WO2015074747A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102013019357.5 2013-11-19
DE102013019357.5A DE102013019357A1 (de) 2013-11-19 2013-11-19 Verfahren und Vorrichtung zur Reinigung von Prozessgasen aus der oxidativen Dehydrogenierung von Kohlenwasserstoffen

Publications (1)

Publication Number Publication Date
WO2015074747A1 true WO2015074747A1 (fr) 2015-05-28

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PCT/EP2014/003060 Ceased WO2015074747A1 (fr) 2013-11-19 2014-11-14 Procédé et dispositif d'épuration de gaz de procédé provenant de la déshydrogénisation oxydative d'hydrocarbures

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AR (1) AR098434A1 (fr)
DE (1) DE102013019357A1 (fr)
TW (1) TW201522302A (fr)
WO (1) WO2015074747A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113842659A (zh) * 2021-11-29 2021-12-28 东营威联化学有限公司 一种节能型二甲苯生产用分馏装置

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WO2003020670A1 (fr) * 2001-08-31 2003-03-13 Exxonmobil Chemical Patents Inc. Procede d'extraction des contaminants oxygenes d'un flux d'olefine
WO2007104600A1 (fr) 2006-03-14 2007-09-20 BSH Bosch und Siemens Hausgeräte GmbH Dispositif pour l'evacuation de l'eau de lavage dans une machine a laver
DE102007048565B3 (de) 2007-10-09 2009-01-22 Dge Dr.-Ing. Günther Engineering Gmbh Verfahren und Anlage zur Regeneration einer bei der Reinigung von Gasen anfallenden aminhaltigen Waschlösung
DE102008025224A1 (de) 2008-05-27 2009-12-03 Linde Ag Aminwäsche
DE102009056660A1 (de) 2009-12-02 2011-06-09 Mt-Biomethan Gmbh Verfahren und Anlage zur chemisorptiven Abtrennung von Kohlendioxid aus Bio- oder Klärgas mittels einer aminhaltigen Waschlösung und Regeneration der beladenen Waschlösung
DE102010017139A1 (de) 2010-05-28 2011-12-01 Fachhochschule Münster CO2-Absorptionsverfahren mittels Aminlösungen
DE102010017143A1 (de) 2010-05-28 2011-12-01 Fachhochschule Münster CO2-Absorptionsverfahren mittels wäßriger Amidinlösungen
WO2012117085A1 (fr) * 2011-03-03 2012-09-07 Basf Se Procédé pour traiter un flux de matière contenant du butène et/ou du butadiène
WO2013113743A1 (fr) * 2012-01-30 2013-08-08 Basf Se Procédé de production de butadiène et/ou de butènes à partir de n-butane

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EP1998870B2 (fr) 2006-03-16 2015-09-02 Basf Se Procede de mise en contact de deux phases dont le contact s'accompagne de formation de chaleur

Patent Citations (11)

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Publication number Priority date Publication date Assignee Title
US3728413A (en) * 1968-11-14 1973-04-17 Petro Tex Chem Corp Reduced fouling in oxidative dehydrogenation process
WO2003020670A1 (fr) * 2001-08-31 2003-03-13 Exxonmobil Chemical Patents Inc. Procede d'extraction des contaminants oxygenes d'un flux d'olefine
WO2007104600A1 (fr) 2006-03-14 2007-09-20 BSH Bosch und Siemens Hausgeräte GmbH Dispositif pour l'evacuation de l'eau de lavage dans une machine a laver
DE102007048565B3 (de) 2007-10-09 2009-01-22 Dge Dr.-Ing. Günther Engineering Gmbh Verfahren und Anlage zur Regeneration einer bei der Reinigung von Gasen anfallenden aminhaltigen Waschlösung
DE102008025224A1 (de) 2008-05-27 2009-12-03 Linde Ag Aminwäsche
WO2009143965A1 (fr) 2008-05-27 2009-12-03 Linde Aktiengesellschaft Lessive aminée
DE102009056660A1 (de) 2009-12-02 2011-06-09 Mt-Biomethan Gmbh Verfahren und Anlage zur chemisorptiven Abtrennung von Kohlendioxid aus Bio- oder Klärgas mittels einer aminhaltigen Waschlösung und Regeneration der beladenen Waschlösung
DE102010017139A1 (de) 2010-05-28 2011-12-01 Fachhochschule Münster CO2-Absorptionsverfahren mittels Aminlösungen
DE102010017143A1 (de) 2010-05-28 2011-12-01 Fachhochschule Münster CO2-Absorptionsverfahren mittels wäßriger Amidinlösungen
WO2012117085A1 (fr) * 2011-03-03 2012-09-07 Basf Se Procédé pour traiter un flux de matière contenant du butène et/ou du butadiène
WO2013113743A1 (fr) * 2012-01-30 2013-08-08 Basf Se Procédé de production de butadiène et/ou de butènes à partir de n-butane

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113842659A (zh) * 2021-11-29 2021-12-28 东营威联化学有限公司 一种节能型二甲苯生产用分馏装置
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