EP1809587A1 - Procede de deshydratation catalytique de propane pour former du propylene - Google Patents

Procede de deshydratation catalytique de propane pour former du propylene

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Publication number
EP1809587A1
EP1809587A1 EP05810736A EP05810736A EP1809587A1 EP 1809587 A1 EP1809587 A1 EP 1809587A1 EP 05810736 A EP05810736 A EP 05810736A EP 05810736 A EP05810736 A EP 05810736A EP 1809587 A1 EP1809587 A1 EP 1809587A1
Authority
EP
European Patent Office
Prior art keywords
oxygen
hydrogen
propane
gas mixture
water vapor
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Withdrawn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
EP05810736A
Other languages
German (de)
English (en)
Inventor
Max Heinritz-Adrian
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
Uhde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Uhde GmbH filed Critical Uhde GmbH
Publication of EP1809587A1 publication Critical patent/EP1809587A1/fr
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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
    • C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
    • C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
    • C07C5/333—Catalytic processes

Definitions

  • the invention relates to a process for the catalytic dehydrogenation of propane to propylene according to the following formula: C 3 H 8 ⁇ C 3 H 6 + H 2 (1) from various sources of propane, which may also contain other gas constituents.
  • the chemical reaction (1) which is usually carried out in the gas phase at a temperature between 540 0 C and 820 0 C, is a strongly endothermic equilibrium reaction whose conversion is thermodynamically limited and depend on the respective partial pressures and the temperature .
  • the dehydrogenation reaction is favored by low partial pressures of the hydrocarbons and by high temperatures. Side reactions form cracking products which deposit as carbon deposits on the catalyst and lead to the deactivation of the catalyst, so that the catalyst has to be cyclically regenerated in technical operation.
  • the temperature decreases over the length of the catalyst bed due to the endothermic reaction.
  • the conversion in the catalyst bed is thus limited, so that several catalyst beds are necessary for the desired high conversions and a renewed heating must take place behind each catalyst bed.
  • the catalytic dehydrogenation of paraffins to olefins can also be carried out in a heated or isothermal catalyst bed.
  • US Pat. No. 5,235,121 describes a process in which a feed mixture which consists of light paraffins and steam is introduced into a tube reactor which is fired from the outside, ie the catalyst bed is a heated fixed bed.
  • the catalyst used is such that no steam reforming process, ie a reaction of the hydrocarbons with water vapor to form CO, CO 2 and H 2 , can be established in the presence of the water vapor.
  • the catalyst is regenerated cyclically.
  • a similar method is also described in DE 198 58 747 A1.
  • An advantage of the described procedure in the presence of steam is that it reduces the partial pressure of the hydrocarbons and thus increases the conversion. Furthermore, part of the carbon deposits on the catalyst is converted into CO 2 by the use of steam and the cycle times between the regenerations can be extended.
  • the addition to large amounts of steam is disadvantageous because it leads to a large increase in volume of the gas stream, which leads to additional investment costs and burdened the economics of the process. Furthermore, the risk of steam reforming of hydrocarbons increases, which results in product loss or yield reduction.
  • the amount of steam that can be added without the problems described above being dependent on the absolute pressure at which the reaction is run and the dehydrogenation catalyst used.
  • thermodynamic limitation of the equilibrium weight conversion is that, due to the supply of oxygen, part of the hydrogen formed in the dehydrogenation is selectively burned - the abbreviation "SHC" for "Selective Hydrogen combustion "used - and thus the equilibrium of the dehydrogenation is shifted in the direction of higher Um ⁇ rates.
  • EP 0 799 169 B1 describes a reactor for such a dehydrogenation process with SHC, in which a paraffin-oxygen mixture is passed over a first catalyst which oxidizes both dehydrogenated and also selectively hydrogenated resulting in a further addition of Oxygen in a Zwi ⁇ space of the reactor and a subsequent second catalyst, which also oxidizes both dehydrogenated and hydrogen formed selectively.
  • the process of EP 0 799 169 B1 is carried out autothermally, the strongly exothermic reaction of the hydrogen with the oxygen supplies the energy for carrying out the endothermic dehydrogenation reaction (1).
  • WO 96/33150 describes a process in which the Pa ⁇ raffingemisch is first dehydrogenated in a first stage, then oxygen is added, wherein in at least a second stage, this oxygen with the liberated in the dehydrogenation hydrogen to water vapor responding. At least a partial stream of the obtained product is subjected to post-dehydration to obtain unreacted paraffins are still to be dehydrogenated, and it is also proposed to recycle a partial stream into the first stage.
  • a disadvantage of these two methods is that very high temperatures can be produced by the addition of the oxygen and the exothermic selective hydrogen oxidation, by which the selectivity of the catalytic dehydrogenation is reduced.
  • the temperature setting by indirect cooling is disadvantageous because it requires fixed heat exchanger installations, which does not allow targeted temperature control in the regeneration of the catalyst bed, or makes an installation for a temporary extraction of the heat exchanger required, such as one by additional fittings such as valves lockable bypass. The latter would be in view of the large tube cross-sections and the high operating temperatures of about 500-650 0 C, which brings the dehydration, with extremely high cost ver ⁇ tied.
  • the direct cooling by inert gases is disadvantageous because they must be separated from the product in the subsequent product processing by consuming process stages.
  • the direct cooling with steam is disadvantageous because steam in the reaction, as described above, is not inert and is set by the cooling a certain steam to hydrocarbon ratio as a function of the cooling. As a result, the amount of steam increases considerably with heavy cooling, which adversely affects the process.
  • WO 2004/039920 furthermore describes a process in which both water and steam are added for this reason.
  • all of these methods are not able to use such propane sources that are contaminated by oxygen or other gas components without a prior treatment of the propane stream from such a propane source fürge leads, otherwise in the heating of both propane as also oxygen already contained a non-catalytic and thus non-selective reaction of the oxygen with propane, which would lead to the loss of product yield.
  • the object of the invention is therefore to provide a process for De hydrogenation with optional hydrogen oxidation available, which allows to use a propane source which is contaminated with oxygen and may also contain other gas components.
  • a further object of the invention is to remove the hydrogen which is produced by the dehydrogenation largely or even completely by oxidation from the product, without thereby reducing the propylene selectivity. As a result, a complicated separation of hydrogen can be avoided.
  • the invention solves the problem according to the main claim by
  • a further gas mixture containing propane and oxygen which may also contain ammonia, and in which the propane content predominates over the oxygen content, is passed into the same reaction apparatus where it reacts with the first gas mixture to form propylene, water vapor and Hydrogen reacts,
  • oxygen free oxygen is understood here as a gas that meets the usual specifications and its oxygen content, especially its content of molecular oxygen O 2 , is below 100 ppm.
  • Commercially available propane which is obtained from the petroleum / natural gas production, is usually technically sau ⁇ free for the purposes of this invention.
  • superheated steam is supplied to the first gas mixture before it is passed into the reaction apparatus.
  • the energy balance can be regulated via the reaction device when the colder, propane and oxygen-containing gas mixture compared to the warmer propane, water vapor and hydrogen-containing gas mixture has a high propane content, without the latter at too high temperatures, ie higher than 550 0 C, must be heated, as this would result in a non-selective reaction of propane with water vapor.
  • At least part of the gas mixture containing propylene, propane, water vapor and hydrogen is fed to a gas mixture with which it forms the first propane, water vapor and hydrogen-containing gas mixture, which together with a temperature of at least 400 0 C is passed into the reaction apparatus. This is a recycling because the dehydrogenation due to the adjusting chemical equilibrium is only incomplete.
  • the Itemssvorrich ⁇ device is formed by 2 series-connected catalyst beds, each of the Katalysatorbet ⁇ th with the other, propane and oxygen-containing gas mixture individually beauf ⁇ beat and the amount of oxygen supplied is compared to that each added hydrogen substoichiometrically in relation to the reaction of the oxygen with the hydrogen to hydrogen vapor.
  • the Letsvorrich ⁇ device of 3 series-connected catalyst beds is formed, wherein the first two of the catalyst beds with the other, propane and oxygen-containing Gasge ⁇ mixture are applied individually, and the amount of oxygen supplied ge ⁇ compared to the supplied hydrogen in the first two of the catalyst beds each stoichiometrically in relation to the reaction of the oxygen with the hydrogen to hydrogen vapor, and the third catalyst bed with an oxygen-containing gas, which also contains the further, propane and Oxygen-containing gas mixture may be or may contain this, and the amount of oxygen supplied to the supplied hydrogen in the third catalyst bed stöchio- Metric with respect to the reaction of the oxygen with the hydrogen to Wasser ⁇ vapor.
  • the two last embodiments differ mainly by the addition of the third stage. If a recycling is provided, the diversion of the product stream can take place either after the first or after the second catalyst bed. In the recycling of the reaction mixture obtained from the first or second stage, water vapor can easily be separated off by condensation.
  • the individual catalyst beds can also be divided in the same type of interconnection or distributed over several containers. Furthermore, it is possible to interconnect several small catalyst beds in parallel, which interact together like a single large catalyst bed.
  • catalyst bed used here is to be understood as meaning that in the case of such constructional variants, this is logically a catalyst bed in the sense of this invention.
  • H 2 O is supplied as water or water vapor or water / water vapor mixture between the first and the second series-connected catalyst bed.
  • a defined ratio of H 2 O - regardless of the state of aggregation - is usually given to hydrocarbons; this targeted adjustment of the ratio of H 2 O to hydrocarbons in the gas phase avoids a process-disadvantageous amount of steam, in particular a steam reforming or a Too much Gasvo ⁇ lumenstrom by too much steam or too high carbon deposition on the Kataly ⁇ capacitor by too little steam.
  • the reaction mixture Before entering the third catalyst bed, the reaction mixture must be cooled by direct or indirect heat exchange to reduce the temperature at which the oxidation of hydrogen is carried out. This avoids the risk of unselective hydrogen oxidation, by which the propylene yield is reduced. Therefore, in a further embodiment of the invention, a complete oxidation of the hydrogen at a temperature-temperature between 200 and 500 0 C in the third catalyst bed, preferably between 300 and 400 0 C is performed.
  • the propane and oxygen-containing gas mixture used as feedstock which may also contain ammonia, and in which the propane content is greater than the oxygen content, and which is conducted into the same reaction apparatus where it reacts with the first reaction gas
  • Gas mixture reacts to form propylene, water vapor and hydrogen, can be removed from conventional installations of the production of acrylonitrile or propylene oxide or acrolein or acrylic acid, where it is usually obtained.
  • customary dehydrogenation catalysts are used in an embodiment of the invention for all catalyst beds. These include e.g. Pt and Sn containing catalysts supported on Zn, Ca aluminate or hydrotalcite. Also, as catalyst in the catalyst beds of each stage, a conventional dehydrogenation catalyst alone or a specific catalyst for hydrogen oxidation can be used, which has a better selectivity than conventional dehydrogenation catalysts in the hydrogen oxidation, together with a conventional Dehydr michs ⁇ catalyst ,
  • 1 shows the process according to the invention with 2 oxydehydrogenation reactors for propylene and one oxidation reactor for hydrogen.
  • 2 shows the process according to the invention with an oxydehydrogenation reactor for propylene.
  • FIG. 1 From feed mixture 1, consisting of propane and smaller amounts of oxygen, carbon dioxide, methane, ethane and traces of further hydrocarbons, a first partial stream 2 is branched off and passed together with the cycle gas 3 into the first oxydehydrogenation reactor 4 where a part of the mixture reacts at a temperature of 500 to 600 0 C.
  • reaction gas 5 withdrawn from the first oxydehydrogenation reactor 4 is fed with a steam-water mixture 6, with the gas mixture 7 forming. Together with a second, branched off from the feed gas 1 substream 8, the gas mixture 7 is passed into the second Oxidehydrismesreaktor 9, where a further reaction takes place at a temperature of 500 to 600 0 C.
  • a portion of return gas 11 is branched off from the resulting propylene- and hydrogen-rich gas 10, which portion is cooled in the return gas cooler 12 and after removal of the gas.
  • Divorce of the resulting aqueous condensate 13 in Kondensatabschei ⁇ the 14 by means of the cycle gas compressor 15 again to the first Oxidehydr michsreak ⁇ tor 4 is promoted.
  • a mixture 17 of steam 18 and propane 19 is added to the circulating gas 16, after which the circulating gas 20 is heated in the reheater 21 to about 400 0 C before it is supplied as a circulating gas 3 to the first oxydehydrogenation reactor 4.
  • All oxydehydrogenation reactors contain at least one catalyst bed, and the catalyst used in all oxydehydrogenation reactors or dehydrogenation stages is a conventional dehydrogenation catalyst.
  • the feed mixture 1 consisting of propane and smaller proportions of oxygen, carbon dioxide, methane, ethane and traces of further hydrocarbons, is passed together with the cycle gas 3 into the oxydehydrogenation reactor 4, where part of the Mixture at a temperature of 500 to 600 0 C reacts.
  • the obtained propylene and hydrogen-rich gas 10, a portion of return gas 11 is branched off, which is cooled in the return gas cooler 12 and is conveyed after deposition of the resulting aqueous condensate 13 in the condensate 14 by means of the cycle gas compressor 15 again to the oxydehydrogenation reactor 4.

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

Abstract

L'invention concerne un procédé permettant de produire du propylène, selon lequel un premier mélange gazeux, techniquement exempt d'oxygène, qui contient du propane, de la vapeur d'eau et de l'hydrogène et dont la température est d'au moins 400 °C, est guidé dans un dispositif de réaction présentant au moins un lit catalytique, ainsi que des conditions de déshydratation habituelles. Un autre mélange gazeux contenant du propane et de l'oxygène, qui peut également comprendre de l'ammoniac et dans lequel la teneur en propane est supérieure à celle de l'oxygène, est guidé dans le même dispositif de réaction, où il entre en réaction avec le premier mélange gazeux, ce qui donne lieu à la formation de propylène, de vapeur d'eau et d'hydrogène. Le mélange gazeux obtenu, contenant du propylène, du propane, de la vapeur d'eau et de l'hydrogène est extrait du dispositif de réaction.
EP05810736A 2004-11-11 2005-11-10 Procede de deshydratation catalytique de propane pour former du propylene Withdrawn EP1809587A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102004054657A DE102004054657A1 (de) 2004-11-11 2004-11-11 Verfahren zur katalytischen Dehydrierung von Propan zu Propylen
PCT/EP2005/012070 WO2006050957A1 (fr) 2004-11-11 2005-11-10 Procede de deshydratation catalytique de propane pour former du propylene

Publications (1)

Publication Number Publication Date
EP1809587A1 true EP1809587A1 (fr) 2007-07-25

Family

ID=35788038

Family Applications (1)

Application Number Title Priority Date Filing Date
EP05810736A Withdrawn EP1809587A1 (fr) 2004-11-11 2005-11-10 Procede de deshydratation catalytique de propane pour former du propylene

Country Status (9)

Country Link
US (1) US7678956B2 (fr)
EP (1) EP1809587A1 (fr)
JP (1) JP5442202B2 (fr)
DE (1) DE102004054657A1 (fr)
EA (1) EA010463B1 (fr)
EG (1) EG25078A (fr)
NO (1) NO20072980L (fr)
UA (1) UA92902C2 (fr)
WO (1) WO2006050957A1 (fr)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7582268B1 (en) * 2006-07-12 2009-09-01 Uop Llc Reactor system with interstage product removal
DE102006035718A1 (de) 2006-07-28 2008-01-31 Basf Ag Verfahren zum Langzeitbetrieb einer kontinuierlich betriebenen heterogen katalysierten partiellen Dehydrierung eines zu dehydrierenden Kohlenwasserstoffs
WO2008095860A2 (fr) * 2007-02-06 2008-08-14 Basf Se Procédé pour fournir un flux de gaz contenant de l'oxygène pour la réaction endothermique d'un flux de départ contenant un ou plusieurs hydrocarbures
DE102008010422A1 (de) * 2008-02-21 2009-09-03 Uhde Gmbh Fixiervorrichtung für Katalysatorpartikel
DE102008062782A1 (de) 2008-12-18 2010-07-01 Uhde Gmbh Variation der Zinnimprägnierung eines Katalysators zur Alkandehydrierung
JP2012512015A (ja) * 2008-12-18 2012-05-31 ティッセンクルップ ウーデ ゲゼルシャフト ミット ベシュレンクテル ハフツング アルカン脱水素化用触媒のスズ含浸の変形
DE102009056539A1 (de) 2009-12-03 2011-06-09 Uhde Gmbh Variation der Zinnimprägnierung eines Katalysators zur Alkandehydrierung
DE102009012452A1 (de) 2009-03-12 2010-09-16 Uhde Gmbh Verfahren zur Verminderung von Olefinverlusten bei der Entfernung von Kohlendioxid aus einem Olefinstrom aus Dehydrierungsreaktionen
CA2833822C (fr) * 2013-11-21 2020-08-04 Nova Chemicals Corporation Operation de deshydrogenation oxydante a securite intrinseque
JP2023539797A (ja) 2020-08-06 2023-09-20 エクソンモービル ケミカル パテンツ インコーポレイテッド アルカン及びアルキル芳香族炭化水素をアップグレードするためのプロセス
US12012557B2 (en) 2021-12-28 2024-06-18 Uop Llc Start-up method for contacting a feed stream with fluidized catalyst

Citations (2)

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EP0193310A1 (fr) * 1985-02-14 1986-09-03 Arco Chemical Technology, Inc. Procédé pour la préparation de nitriles non saturés à partir d'alcanes
WO2004020423A1 (fr) * 2002-08-30 2004-03-11 Basf Aktiengesellschaft Procede integre pour la synthese d'oxyde de propylene

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DE3461782D1 (en) * 1983-02-22 1987-02-05 Halcon Sd Group Inc Conversion of propane to acrylic acid
US4599471A (en) 1985-09-16 1986-07-08 Uop Inc. Method for oxygen addition to oxidative reheat zone of hydrocarbon dehydrogenation process
US4990632A (en) * 1988-03-23 1991-02-05 The Boc Group, Inc. Process for the production of oxides
US5233118A (en) * 1988-12-05 1993-08-03 Uop Steam dehydrogenation process
US5235121A (en) 1991-08-02 1993-08-10 Phillips Petroleum Company Method for reforming hydrocarbons
US5527979A (en) 1993-08-27 1996-06-18 Mobil Oil Corporation Process for the catalytic dehydrogenation of alkanes to alkenes with simultaneous combustion of hydrogen
NO300117B1 (no) 1994-12-22 1997-04-14 Norske Stats Oljeselskap Reaktor for dehydrogenering av hydrokarboner med selektiv oksidasjon av hydrogen
DE19858747A1 (de) 1998-12-18 2000-06-21 Linde Ag Verfahren und Katalysatorstation zur Dehydrierung von Alkanen
WO2004024666A1 (fr) 2002-09-10 2004-03-25 Arkema Procede de fabrication d'acide acrylique a partir de propane, en presence d'oxygene moleculaire
DE10251135B4 (de) 2002-10-31 2006-07-27 Uhde Gmbh Verfahren zur katalytischen Dehydrierung von leichten Paraffinen zu Olefinen

Patent Citations (2)

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Publication number Priority date Publication date Assignee Title
EP0193310A1 (fr) * 1985-02-14 1986-09-03 Arco Chemical Technology, Inc. Procédé pour la préparation de nitriles non saturés à partir d'alcanes
WO2004020423A1 (fr) * 2002-08-30 2004-03-11 Basf Aktiengesellschaft Procede integre pour la synthese d'oxyde de propylene

Non-Patent Citations (1)

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Title
See also references of WO2006050957A1 *

Also Published As

Publication number Publication date
US7678956B2 (en) 2010-03-16
US20080300440A1 (en) 2008-12-04
JP5442202B2 (ja) 2014-03-12
DE102004054657A1 (de) 2006-05-18
EG25078A (en) 2011-07-31
UA92902C2 (ru) 2010-12-27
WO2006050957A1 (fr) 2006-05-18
JP2008519792A (ja) 2008-06-12
NO20072980L (no) 2007-08-07
EA010463B1 (ru) 2008-08-29
EA200701037A1 (ru) 2007-10-26

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