EP3056481A1 - Procédé et système de fabrication d'hydrocarbures - Google Patents

Procédé et système de fabrication d'hydrocarbures Download PDF

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Publication number
EP3056481A1
EP3056481A1 EP15155244.5A EP15155244A EP3056481A1 EP 3056481 A1 EP3056481 A1 EP 3056481A1 EP 15155244 A EP15155244 A EP 15155244A EP 3056481 A1 EP3056481 A1 EP 3056481A1
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EP
European Patent Office
Prior art keywords
effluent
fluid
separation
separation effluent
hydrocarbons
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.)
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EP15155244.5A
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German (de)
English (en)
Inventor
Heinz Zimmermann
Ernst Haidegger
Rainer Kemper
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Linde GmbH
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Linde GmbH
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Publication date
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Priority to EP15155244.5A priority Critical patent/EP3056481A1/fr
Priority to PCT/EP2016/053287 priority patent/WO2016131837A1/fr
Publication of EP3056481A1 publication Critical patent/EP3056481A1/fr
Withdrawn legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts

Definitions

  • the invention relates to a process and a plant for the production of hydrocarbons according to the preambles of the independent claims.
  • Steam cracking processes are carried out on a commercial scale almost exclusively in heated tubular reactors.
  • steam-slicing processes produce gas mixtures which, in addition to the actual target compounds, may contain by-products.
  • larger quantities of methane and hydrogen are typically formed in steam cracking processes.
  • These components of the so-called Schugasfrtress are conventionally used individually or jointly as heating gas for heating said tubular reactors.
  • Oxidative methane coupling involves the direct conversion of methane to higher hydrocarbons in an oxidative, heterogeneously catalyzed process. Corresponding processes appear to be particularly promising for the production of ethylene. For further details of the oxidative methane coupling should be at this point on relevant literature, for example Zavyalova, U.
  • the heating gas fraction can also be converted to synthesis gas.
  • the synthesis gas can be converted into higher hydrocarbons in subsequent further steps, for example by Fischer-Tropsch synthesis or via oxygenates such as methanol as intermediates.
  • An attractive target product here is dimethyl ether (DME), the synthesis of synthesis gas, for example in the DME Handbook of the Japan DME Forum, Tokyo 2007: Ohmsha, ISBN 978-4-9903839-0-9, especially Chapter 4, "DME Production Technologies
  • dimethyl ether can be converted into further compounds, for example to olefins in known DTO (ie DME to olefins) and especially to propylene in known DTP processes (DME to propylene).
  • the use of the fuel gas fraction in corresponding upgrading reactions is energetically and economically more favorable than its combustion for heating.
  • the heating must be ensured in this case, however, due to the elimination of the heating gas fraction by other energy sources.
  • the present invention therefore has as its object to improve corresponding processes and plants for the production of hydrocarbons and in particular to enable the complete utilization of the heating gas fraction for upgrading reactions.
  • steam cracking processes are, as mentioned, carried out on a commercial scale almost exclusively in tubular reactors in which individual reaction tubes (in the form of coils, so-called coils) or groups of corresponding Reaction tubes can be operated at different clearance conditions.
  • a cracking furnace in the language used here is thus a structural unit used for the vapor cracking, which equates to a furnace insert or exposes it to comparable cracking conditions.
  • a steam cracking plant (also referred to as "olefin plant”) may comprise one or more such cracking furnaces.
  • furnace insert refers to one or more liquid and / or gaseous streams which are fed to one or more cracking furnaces. Also, streams obtained by a corresponding steam cracking process, as explained below, may be recycled to one or more cracking furnaces and reused as furnace feed.
  • a furnace insert is a variety of hydrocarbons and hydrocarbon mixtures of ethane to gas oil up to a boiling point of typically 600 ° C.
  • a furnace insert may consist of a so-called "fresh use”, ie an insert which is provided externally and obtained, for example, from one or more mineral oil fractions, natural gas and / or natural gas condensates.
  • a furnace insert can also consist of one or more so-called “recycle streams”, ie streams that are generated in the plant itself and returned to a corresponding cracking furnace.
  • a furnace insert may also consist of a mixture of one or more fresh feeds with one or more recycle streams.
  • the furnace insert is at least partially reacted in the respective cracking furnace and leaves the cracking furnace as a so-called "raw gas", which can be subjected to post-treatment steps.
  • post-treatment steps comprise first a treatment of the raw gas, for example by quenching, cooling and drying, whereby a so-called “cracking gas” is obtained.
  • the raw gas is already referred to as cracking gas.
  • steam gap feed stream As a general term for a component mixture supplied to one or more cracking furnaces, that is to say one or more furnace inserts as explained above hereinafter also the term “steam gap feed stream”, as a general term for a gas mixture taken from one or more cracking furnaces, the term “steam cracking effluent” is also used below.
  • a corresponding Dampfspaltabstrom is, as mentioned, a hydrocarbon mixture containing by-products in addition to the desired target compounds.
  • a steam crack effluent is therefore typically at least partially separated into fractions. This can be done by means of differently designed separation sequences to which a steam gap effluent is subjected, for example, after a so-called crude gas compression and further treatment steps. Corresponding separation sequences are also mentioned in the article " Ethylene "in Ullmann's Encyclopedia of Industrial Chemistry explained.
  • Corresponding separation sequences for steam sludge effluents which originate from the reaction of liquid or at least partially liquid steam column feed streams, such as naphtha initially comprise the so-called primary fractionation.
  • the steam cracking effluent at typically about 230 ° C in a so-called oil column in ascending direction is first brought into contact with a finely divided stream of pyrolysis oil and then with a finely divided stream of heavy pyrolysis gas oil (see below).
  • the steam cracking effluent is cooled in direct contact with water to about ambient temperature.
  • the heavy pyrolysis gas oil which is returned to the oil column.
  • the pyrolysis oil accumulates, which is partly relinquished to the oil column and partly carried out of this.
  • the pyrolysis oil is thus formed in the illustrated primary fractionation in the form of a single fraction, which consists predominantly of hydrocarbons having a boiling point of more than 200 ° C.
  • two fractions can be formed, namely pyrolysis gas oil (Pyrolysis Gasoil, PGO) predominantly hydrocarbons having boiling points of 200 to 400 ° C, and pyrolysis fuel oil (English Pyrolysis Fuel Oil, PFO) with hydrocarbons higher Boiling points.
  • pyrolysis oil is a hydrocarbon mixture of hydrocarbons which are obtained from a steam cracking effluent and which at least predominantly, ie at least 75%, 80%, 90% or 95%, has a boiling point of more have 200 ° C.
  • Pyrolysis oil may include pyrolysis gas oil and / or pyrolysis fuel oil.
  • pyrolysis gasoline (Pyrolysis Gasoline, Pygas), like pyrolysis oil or pyrolysis gas oil and pyrolysis fuel oil, is familiar to the person skilled in the art of the steam cracking process. As in the mentioned article “ Ethylene “in Ullmann's Encyclopedia of Industrial Chemistry In particular, this is a fraction of hydrocarbons having five to ten, depending on the definition also five to twelve, carbon atoms. Pyrolysis gasoline is rich in aromatic compounds, which are typically obtained as valuable products. Also included acetylenes and dienes are typically hydrogenated prior to recovery of the aromatic compounds. In the context of the present invention, it is possible in particular to use compounds remaining after the hydrogenation and the extraction of the aromatics.
  • the present invention may include the use of any boiling cuts of pyrolysis gasoline, for example, a boiling cut having a boiling range of about 25 to about 70 ° C, the so-called benzene cut having a boiling range of about 70 to about 90 ° C, the so-called toluene cut with a boiling range of about 90 to about 115 ° C, the so-called C8 cut with a boiling range of about 115 to about 145 ° C and a boiling cut with heavier compounds and a boiling range of about 145 to about 230 or 240 ° C.
  • the transition to the pyrolysis oil or pyrolysis gas oil is fluid.
  • several corresponding cuts can be used in combination.
  • Pyrolysis gasoline or any of the mentioned boiling cuts may also be treated with pyrolysis oil, i. Pyrolysis gas oil and / or pyrolysis fuel combined used.
  • separation effluent any stream formed in and downstream of the primary fractionation using fluid from a vapor column effluent, especially a stream containing components of the pyrolysis gasoline and / or pyrolysis oil fraction and the heating gas fraction.
  • a separation effluent may also be formed from a plurality of streams obtained in a corresponding separation, for example, from a residue of a pyrolysis benzine fraction or one or more boiling cuts after hydrogenation and separation of aromatic compounds and part of a pyrolysis oil fraction. If, in the following, the term "fluid" of a flow (in particular of a separation effluent) is used for specific purposes, this may include the use of the entire flow or only a part thereof or else only certain components.
  • the present invention is based on a process for producing hydrocarbons in which one or more hydrocarbon-containing vapor column feed streams are subjected to a steam cracking process to obtain one or more steam cracking effluents. From fluid of the steam or the effluent effluent streams, as just explained, a first separation effluent predominantly or exclusively hydrocarbons having a boiling point of more than 25 ° C, ie a stream containing predominantly or exclusively components of the Pyrolysebenzin- and / or the pyrolysis oil fraction , and a second separation effluent, which contains at least methane and in particular is low in hydrocarbons having two or more carbon atoms formed.
  • the second separation effluent may be a conventional fuel gas stream or a corresponding fuel gas fraction and thus also contain hydrogen in addition to methane and thus predominantly or exclusively comprise methane and hydrogen.
  • the separate separation of methane and hydrogen is possible.
  • the second separation effluent contains predominantly or exclusively methane.
  • the present invention makes it possible to at least partially subject the second separation effluent to a reaction process in which a reaction effluent containing organic compounds having at least two carbon atoms is formed. This is possible because the second separation effluent is not or not exclusively used for heat recovery for the steam cracking process.
  • the reaction effluent contains organic compounds having at least two carbon atoms, hydrocarbons which are typical among these organic compounds, in particular olefins, but also other compounds such as oxygenates, in particular alcohols, such as methanol and ethanol, and Ether understood as dimethyl ether.
  • the organic compounds having at least two carbon atoms contain carbon atoms derived from the methane of the second separation effluent. However, it is not explicitly required that methane be subjected directly to reactions in which corresponding compounds are formed. Rather, it is also possible first to form synthesis gas from the methane and optionally from hydrogen contained in the second separation effluent and then to subject this synthesis gas to further reaction steps, as explained.
  • the second separation effluent is not or not exclusively used for heat recovery in the steam cracking process. Rather, the steam cracking process is performed at least intermittently using heat energy derived from fluid of the first separation effluent.
  • the present invention therefore proposes to supply components of the pyrolysis gasoline and / or pyrolysis oil fraction instead of the heating gas fraction to thermal utilization in the steam cracking process.
  • the direct thermal utilization of components of the pyrolysis oil fraction may possibly lead to increased cleaning and increased nitrogen oxide emissions. Therefore, a particularly advantageous embodiment of the invention provides an indirect heating.
  • the fluid of the first Trennabstroms is first used to generate electrical energy, which is then converted into the heat energy. It is advantageous if, upon combustion of the fluid of the first separation effluent, a vapor stream is generated and at least partially used for obtaining the electrical energy.
  • the invention can in this way resort to known steam turbine technology. By providing steam at different pressure levels, exergy losses can be reduced. By spatially decoupling the combustion from the steam cracking process, the combustion can better respond to combustion targets, i. particular low emissions and / or reduced soot formation, to be adjusted. In the case of direct combustion in a steam cracking furnace, however, this is not readily possible.
  • One or more steam cracking furnaces used in the steam cracking process are thus at least partially electrically heated.
  • the steam cracking process can additionally also, as also explained below, using further or additional heat energy is generated, which is not generated from electrical energy and / or using other energy sources.
  • the present invention by at least partially heating the vapor cracking process by means of energy obtained using fluid of the first separation effluent, allows predominantly or fully to supply methane contained in the second separation effluent to the above-described upgrading reactions.
  • the naphtha steam cracking is based on a methane yield of about 15%, this results, for example, in the use of oxidative methane coupling in a selectivity of 60%, an increase in the ethylene yield of 9% based on use or by 30%. relative (increase in naphtha cracking from 31 to 40% ethylene yield).
  • a plant capable of producing one million metric tons per year can produce an additional 300 kilotons of ethylene per year. This equates to an increase of $ 300 million in profits, assuming a price difference between fuel gas and ethylene at $ 1,000 per tonne.
  • further heat energy used to carry out the steam cracking process is generated at least temporarily by combustion of fluid of at least one further combustible stream.
  • fluid of the first one Trennausstroms generated heat energy is not sufficient, at least one other combustible electricity can be used to support.
  • the second separation effluent, which contains at least methane is temporarily present in excess or the reaction process, to which the second separation effluent is at least temporarily subjected, is rendered inoperative.
  • the fluid of the at least one further combustible stream can be used first for generating electrical energy, which is then converted into the further heat energy.
  • the generation of this electrical energy can be done together with or separate from the generation of electrical energy from the first separation effluent.
  • a particularly advantageous embodiment of the present invention comprises that the steam cracking process is performed at least temporarily using additional heat energy derived from external electrical energy.
  • external electrical energy is meant in particular electrical network energy, which is taken from an electrical power network of an energy supplier.
  • external electrical energy can also be electrical energy that is generated in other plants or using other energy sources in a corresponding plant park.
  • a particularly preferred embodiment of the present invention may include providing a first and a second mode of operation, the steam gap method in the first and second modes of operation using different proportions of thermal energy derived from the fluid of the first separator effluent Heat energy from the or the other combustible streams and / or the additional heat energy from the external electrical energy is performed.
  • the electrical energy used to obtain the thermal energy predominantly or exclusively comprises external electrical energy in the first operating mode and in the second operating mode predominantly or exclusively the electrical energy obtained using at least a portion of the first separating effluent.
  • the method according to the invention may also comprise, in the first operating mode, the first separation effluent, ie the components of the pyrolysis oil and / or pyrolysis benzine fraction, temporarily stored, so that the present method simultaneously represents a method for intermediate storage and recovery of electrical energy.
  • the components which can be used in the context of the present invention have already been explained in the definition of pyrolysis oil and pyrolysis gasoline.
  • the first separation effluent predominantly or exclusively hydrocarbons having a boiling point between 25 and 70 ° C, between 70 and 90 ° C, between 90 and 115 ° C, between 115 and 145 ° C, between 145 and 230 ° C, between 145 and 240 ° C, between 200 and 400 ° C and / or between 400 and 600 ° C.
  • any combinations of corresponding boiling ranges are possible.
  • the selection of the components to be used thermally depends in particular on their occurrence in a corresponding process and their other utilisability or their commercial value. In particular, the selection may also be based on the formation of corresponding components in the inserts used for the steam cracking process and / or the conditions used there.
  • the reaction process to which the second separation effluent is at least partially subjected may comprise the production of synthesis gas.
  • a second separation effluent is used which comprises methane and hydrogen or it is the second separation effluent, if it consists exclusively of methane, additional hydrogen fed.
  • hydrocarbons and / or oxygenates are advantageously prepared from at least part of the synthesis gas.
  • Oxygenates are typically understood as meaning ethers and alcohols.
  • methyl tert-butyl ether MTBE, English methyl tertiary butyl ether
  • TAEE tert-amyl ethyl ether
  • ETBE ethyl tert-butyl ether
  • DIPE Diisopropyl ether
  • oxygenates include, in particular, dimethyl ether (DME, dimethyl ether).
  • DME dimethyl ether
  • oxygenates are compounds which have at least one alkyl group covalently bonded to an oxygen atom.
  • the at least one alkyl group may have up to five, up to four or up to three carbon atoms.
  • the oxygenates of interest in the present invention have alkyl groups with one or two carbon atoms, in particular they are methyl groups.
  • they are monohydric alcohols and dialkyl ethers such as methanol and dimethyl ether or corresponding mixtures.
  • the present invention also extends to a plant for producing hydrocarbons. It comprises means adapted to subject one or more hydrocarbon-containing vapor column feed streams to a vapor cracking process to obtain one or more vapor column effluents, and fluid from the vapor column or effluent effluents to a first separation effluent predominantly hydrocarbons having a boiling point greater than 25 ° C and a second separation effluent containing at least methane.
  • Such a plant is characterized by means adapted to subject second separation effluent fluid to a reaction process in which a reaction effluent containing organic compounds having at least two carbon atoms is formed, and at least temporarily performing the steam cracking process using heat energy. which is obtained from fluid of the first separation effluent.
  • FIG. 1 a method according to a particularly preferred embodiment of the invention is shown in the form of a schematic flow chart and designated 100 in total.
  • a steam column feed stream a which may also include one or more recycle streams, is fed to one or more steam cracking furnaces 1 arranged to carry out a steam cracking process.
  • a separation effluent c (“first" separation effluent) is formed, typically predominantly hydrocarbons having a boiling point of more than 25 ° C, ie components of the pyrolysis gasoline and / or proline oil fraction comprises, typically in a primary fractionation.
  • a second separation effluent d is formed in the separation device 2, which contains at least methane, optionally also hydrogen, as explained above, and is low in higher hydrocarbons.
  • Further separation effluents are indicated by e to h. These include, for example, ethylene e, propylene f, a hydrocarbon fraction with hydrocarbons with four carbon atoms g and a separate pyrolysis benzine fraction h.
  • the first separation effluent c is supplied to a steam generating unit 3 in the illustrated example.
  • the pyrolysis oil and / or pyrolysis gas of the first separation effluent c is burned in the steam generation unit 3, optionally with at least one further combustible stream q and / or oxygen or an oxygen-rich stream.
  • a steam flow k is formed, which drives a generator unit 4 with one or more generators.
  • electrical energy as illustrated here with I
  • electrical energy m is, as denoted here by n
  • a heater 5 is operated, the heat energy, here illustrated with o, for the or the cracking furnaces 1 provides.
  • Further heat energy can be provided, for example, by means of a burner 6 from one or more further combustible streams p.
  • a control unit not shown, which is set up, for example, to set the proportions of the electrical energy I, the electrical energy m, of the other streams q or p and other parameters, in particular to carry out the first and second operating modes explained above.
  • the illustrated method 100 comprises at least partially subjecting the second separation effluent b in at least one reaction unit 6 to a reaction process in which a reaction effluent i is formed.
  • This contains organic compounds with two carbon atoms.
  • FIG. 2 a method according to a particularly preferred embodiment of the invention is shown in the form of a schematic flow chart and designated as 200 in total.
  • One or more steam cracking processes or steps to which a suitable insert A is supplied are designated 10 herein.
  • One or more steam gap effluents B are first fed to an oil and water wash 20, wherein, as mentioned, a (crude) pyrolysis oil stream C and a (crude) pyrolysis gasoline stream D are separated.
  • a vapor stream U may be returned to the vapor splitter 10 or processes.
  • the pyrolysis oil stream C and the pyrolysis gasoline stream D can be treated in any manner and separated into fractions, ultimately a separation effluent E ("first" separation effluent) is obtained, which is used to recover thermal energy at least temporarily in the or the steam cracking process 10 thermally.
  • There may be a direct recovery or recovery of electrical energy as explained above. Further heat energy can be provided at least temporarily but also via a further combustible stream F.
  • Portions of streams C and D may be discharged as products from process 200.
  • a remaining after the oil and water wash 20 stream G is subjected to a compression and drying 30, where again a Pyrolysebenzinstrom H may be incurred.
  • There remains a current I which can be supplied to a cryogenic separation 40.
  • a fuel gas stream K, an ethane stream L, an ethylene stream M and a stream N of hydrocarbons having three or more carbon atoms are obtained.
  • the stream N is subjected to a further separation 50 in which a further pyrolysis gasoline stream O, a propane stream P, a propylene stream Q and a stream R of hydrocarbons having four carbon atoms is obtained.
  • the fuel gas stream K, the ethane stream L and the propane stream P are conventionally recycled to the vapor cracking process (s), with the fuel gas stream K conventionally being fired.
  • an upgrading reaction 60 in the illustrated example a step for oxidative methane coupling, provided, it is advantageous to supply the methane of the fuel gas stream K this, as illustrated with stream S.
  • the same can also apply to the ethane stream L, as shown by stream T.
  • a reduction in the firing rate is compensated in the illustrated embodiment by the combustion of pyrolysis oil and / or pyrolysis gasoline or corresponding components.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP15155244.5A 2015-02-16 2015-02-16 Procédé et système de fabrication d'hydrocarbures Withdrawn EP3056481A1 (fr)

Priority Applications (2)

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EP15155244.5A EP3056481A1 (fr) 2015-02-16 2015-02-16 Procédé et système de fabrication d'hydrocarbures
PCT/EP2016/053287 WO2016131837A1 (fr) 2015-02-16 2016-02-16 Procédé de production d'hydrocarbures

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EP15155244.5A EP3056481A1 (fr) 2015-02-16 2015-02-16 Procédé et système de fabrication d'hydrocarbures

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US20230356171A1 (en) * 2020-10-02 2023-11-09 Basf Se Thermal integration of an electrically heated reactor

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5254781A (en) * 1991-12-31 1993-10-19 Amoco Corporation Olefins process which combines hydrocarbon cracking with coupling methane
US20060116543A1 (en) * 1999-07-07 2006-06-01 Naphtachimie S.A. & Bp Chemicals Limited Method and apparatus for steam cracking hydrocarbons
EP2711348A1 (fr) * 2012-09-20 2014-03-26 Linde Aktiengesellschaft Installation et procédé destinés à la fabrication d'éthylène

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5254781A (en) * 1991-12-31 1993-10-19 Amoco Corporation Olefins process which combines hydrocarbon cracking with coupling methane
US20060116543A1 (en) * 1999-07-07 2006-06-01 Naphtachimie S.A. & Bp Chemicals Limited Method and apparatus for steam cracking hydrocarbons
EP2711348A1 (fr) * 2012-09-20 2014-03-26 Linde Aktiengesellschaft Installation et procédé destinés à la fabrication d'éthylène

Non-Patent Citations (5)

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Title
"DME Handbook des Japan DME Forum, Tokyo", 2007, OHMSHA, article "DME Production Technologies"
"Ullmann's Encyclopedia of Industrial Chemistry erläutert", article "Ethylene"
"Ullmann's Encyclopedia of Industrial Chemistry", 15 April 2007, article "Ethylene"
"Ullmann's Encyclopedia of Industrial Chemistry", 15 April 2009, WILEY-VCH VERLAG GMBH & CO. KGAA, Weinheim, Germany, ISBN: 978-3-52-730673-2, article HEINZ ZIMMERMANN ET AL: "Ethylene", XP055007506, DOI: 10.1002/14356007.a10_045.pub3 *
ZAVYALOVA, U. ET AL.: "Statistical Analysis of Past Catalytic Data on Oxidative Methane Coupling for New Insights into the Composition of High-Performance Catalysts", CHEMCATCHEM, vol. 3, 2011, pages 1935 - 1947

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