WO2013092844A2 - Dispositif et procédé pour traiter un flux de matières contenant de l'hydrogène et du méthane - Google Patents

Dispositif et procédé pour traiter un flux de matières contenant de l'hydrogène et du méthane Download PDF

Info

Publication number
WO2013092844A2
WO2013092844A2 PCT/EP2012/076360 EP2012076360W WO2013092844A2 WO 2013092844 A2 WO2013092844 A2 WO 2013092844A2 EP 2012076360 W EP2012076360 W EP 2012076360W WO 2013092844 A2 WO2013092844 A2 WO 2013092844A2
Authority
WO
WIPO (PCT)
Prior art keywords
methane
hydrogen
material stream
rich
stream
Prior art date
Application number
PCT/EP2012/076360
Other languages
German (de)
English (en)
Other versions
WO2013092844A3 (fr
Inventor
Werner Peschel
Michael Jaeger
Uwe Stabel
Eberhardt Gaffron
Original Assignee
Basf Se
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 Basf Se filed Critical Basf Se
Publication of WO2013092844A2 publication Critical patent/WO2013092844A2/fr
Publication of WO2013092844A3 publication Critical patent/WO2013092844A3/fr

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/062—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • C01B3/506—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification at low temperatures
    • 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
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0635—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/065—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 4 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0655—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of hydrogen
    • 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
    • C01B2203/042—Purification by adsorption on solids
    • 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
    • C01B2203/046—Purification by cryogenic separation
    • 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
    • C01B2203/048—Composition of the impurity the impurity being an organic compound
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/12—Refinery or petrochemical off-gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/02—Separating impurities in general from the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/80—Quasi-closed internal or closed external carbon dioxide refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/44—Particular materials used, e.g. copper, steel or alloys thereof or surface treatments used, e.g. enhanced surface

Definitions

  • the invention relates to a device for processing a hydrogen and methane-containing material stream, wherein the device comprises at least one heat exchanger, at least one separation unit, at least one cooling unit and at least one cryogenic gas separation unit.
  • the invention further relates to a method for preparing a material stream and the use of the device or the method for processing a extracted from a Hydrodealkly istsstrom material flow.
  • aromatic hydrocarbons in particular benzene, toluene, xylene and ethylbenzene (also called BTXE-cut), which are the raw materials for plastics and other bulk chemicals.
  • aromatic hydrocarbons are found in petroleum and a majority of technically important compounds are synthesized through petrochemical processes such as steam cracking. This long-chain hydrocarbons are cracked at residence times in the millisecond range and temperatures between 800 and 850 ° C in the presence of water vapor. The aim here is to obtain short-chain alkenes, such as ethylene or propylene. Aromatic hydrocarbons are initially obtained as a by-product and separated by complicated separation processes into the individual components, such as benzene or toluene.
  • An essential conversion process is the hydrodealkylation in addition to isomerization.
  • an aromatic hydrocarbon such as toluene
  • a simpler aromatic hydrocarbon such as benzene.
  • This chemical process is described, for example, in WO 2007/051851 and is generally carried out at high temperatures, under high pressure or in the presence of a catalyst.
  • a high excess of hydrogen must be used, which places high demands on the hydrogen recycling and in particular on the separation of the hydrogen from the resulting product gas mixture.
  • a cryogenic separation in which condensable impurities are separated from the product gas mixture in various cooling stages in a so-called cryogenic gas separation unit.
  • DE 20 55 507 A1 discloses a process for purifying a feed gas from crude hydrogen, in which a raw hydrogen feed gas containing condensable impurities is subjected to a stepwise cooling. To this end, the feed is passed through various stages of cooling, the condensate is separated from the feed after passing through each stage of cooling, each condensate is decompressed and then passed in a return stream through each preceding cooling stage for autogenous cooling. In order to maintain the correct heat balance of the process, heat is released to the outside in the last cooling stage, which allows temperatures of up to -165 ° C to be achieved. Hydrogen with a purity of more than 90% can be obtained with this cryogenic cleaning plant.
  • No. 3,371,126 describes a process for the preparation of benzene and heating gas, after which a dealkylation unit is used to purify a stream of hydrogen and methane-rich material within a cryogenic purification zone.
  • the material stream leaving the dealkylation unit is first decomposed into a benzene-rich fraction and a hydrogen- and methane-rich fraction.
  • the hydrogen and methane-rich fraction contains, for example, 55.6 mol% of hydrogen, about 40.7 mol% of methane and about 4 mol% of ethane.
  • a hydrogen-rich material stream is provided which contains more than 80% by volume of hydrogen.
  • the object of the present invention is to provide an apparatus and a method to simplify the treatment of product gas mixtures and at high purity of the treated hydrogen to create a cost-effective alternative that meets high safety standards.
  • a device for processing a hydrogen and methane-containing material stream which comprises the following components: (i) at least one heat exchanger for cooling a material stream to be treated;
  • At least one cryogenic gas separation unit for separating the hydrogen and methane-rich stream into at least one hydrogen-rich stream and at least one methane-rich stream.
  • the object is further achieved by a method for processing a hydrogen and methane-containing material stream comprising the following steps:
  • the invention makes it possible to recover in a simple manner hydrogen and methane in high purity and to recycle.
  • simple and robust designed components can be used, which increase the life of the device and minimize the monitoring and maintenance costs.
  • the heat exchanger for precooling the material stream to be reprocessed can be made simple and robust, since with the device according to the invention or the method according to the invention the demands on its efficiency are lower than in the systems known from the prior art.
  • sensitive components such as the cryogenic gas separation unit, can be adequately protected from damage by separating corrosive and freezable fractions from the material stream. By separating impurities, hydrogen and methane are thus recovered with high purity, which facilitates the subsequent operation.
  • the invention provides a two-stage cooling of the reprocessed material flow with the heat exchanger and the cooling unit in a first stage and the cryogenic gas separation unit in a second stage, which increases the stability of the processing process.
  • a substantially constant temperature level comprises temperature fluctuations in the range of +/- 2 ° C.
  • indications in% by volume are a measure of the proportion of a substance in a substance mixture based on the total volume of the substance mixture.
  • ppm based on the total volume of the substance mixture, means one part by volume in one million.
  • ppt in relation to the total volume of the substance mixture denotes a volume part in a trillion.
  • Nm 3 / h refers to standard cubic meters per hour, the standard volume for a pressure of 1 bar and a temperature of 20 ° C is specified.
  • the apparatus of the invention finds use in treating a stream taken from a dealkylation of alkyl-substituted aromatic hydrocarbons.
  • the device according to the invention can be connected downstream of a plant for dealkylation of alkyl-substituted aromatic hydrocarbons.
  • the individual components of the system are arranged in the order mentioned above and, accordingly, the steps of the method according to the invention are also carried out in the order mentioned.
  • non-aromatic hydrocarbons having six or more carbon atoms are aromatized in a first step, for example in the presence of water vapor and a catalyst.
  • a second step at least a portion of the resulting product stream containing alkyl-substituted aromatic hydrocarbons is reacted with the aid of hydrogen, optionally in the presence of a catalyst, by dealkylating the alkyl-substituted aromatic hydrocarbons.
  • the reaction product is rich in hydrogen, impurities and dealkylated aromatic hydrocarbons such as benzene or toluene.
  • dealkylated aromatic hydrocarbons such as benzene or toluene.
  • the formed dealkylated aromatic hydrocarbons and a hydrogen-containing gas phase can be separated by conventional methods.
  • the reaction product of dealkylation may be passed from the reactor to a heat exchanger and cooled there, preferably to 20 to 100 ° C. It is expedient to integrate the heat released in the process in order to For example, to heat the feed stream of the dealkylation or other currents to be heated, for example, an evaporator of a column.
  • a liquid phase and a hydrogen-containing gas phase are formed in the heat exchanger.
  • the forming liquid phase which contains the dealkylated aromatic hydrocarbon, such as benzene, and excess water of the reactions is fed to a phase separator and the organic phase separated from the water phase.
  • the organic phase containing the dealkylated aromatic hydrocarbon may optionally be further purified, for example by distillation. The products obtained during the distillation may optionally be recycled to the reaction steps.
  • the hydrogen-containing gas phase Before the hydrogen-containing gas phase is fed to the device according to the invention, it can be passed, for example, to a separator or a stripping column where heavy-boiling hydrocarbons, preferably hydrocarbons having 4 or more carbon atoms and more preferably hydrocarbons having 6 or more carbon atoms are separated off.
  • This step may, for example, be carried out in a phase separator by adiabatic relaxation.
  • the resulting bottom fraction, containing high-boiling hydrocarbons, in particular hydrocarbons having 6 or more carbon atoms, may optionally be recycled to the dealkylation process.
  • the resulting overhead fraction forms the material stream to be treated, which essentially contains hydrogen and methane and, in the apparatus according to the invention, is separated, apart from minor impurities, into at least one hydrogen-rich and at least one methane-rich material stream.
  • the stream to be treated preferably contains at least 40% by volume of hydrogen and at least 15% by volume of methane. More preferably, the material stream to be treated contains 45 to 75% by volume, more preferably 50 to 70% by volume of hydrogen and 15 to 45% by volume, particularly preferably 20 to 40% by volume of methane.
  • the material stream to be treated may contain up to 10% by volume impurities. As impurities, 1 to 5% by volume of ethane, 0.2 to 2% by volume of nitrogen and 0 to 7% by volume of hydrocarbons, for example 0.3 to 4% by volume of hydrocarbons having 6 or more carbon atoms, in particular aromatic hydrocarbons, and up to 2 vol.% C to C 5 hydrocarbons.
  • the material stream to be treated is fed to the device according to the invention at a pressure of up to 100 bar, preferably up to 70 bar and particularly preferably up to 60 bar.
  • the volume flow of the material stream to be supplied and processed is up to 50,000 Nm 3 / h, preferably up to 40,000 Nm 3 / h and particularly preferably up to 35,000 Nm 3 / h.
  • the temperature of the material stream to be treated can be up to 100 ° C. and is preferably in the range from 20 to 50 ° C.
  • the material stream to be treated has a temperature in the range from 30 to 40.degree.
  • the device according to the invention initially provides a first cooling stage for the preparation of the material stream to be reprocessed.
  • This comprises at least one heat exchanger which comprises at least one supply line for supplying a material stream to be cooled, and at least one outlet for discharging a cooled material stream to be treated.
  • the heat withdrawn from the material stream to be cooled and treated is used in the preparation process by heating at least one stream of material to be heated before leaving the device. In this way, in particular treated material streams can be heated before leaving the device and thus be recycled directly in process steps, for example for dealkylation or for heating.
  • the heat exchanger can be designed as a plate, spiral or tube bundle heat exchanger.
  • the guidance of the material stream to be cooled and processed with respect to the material stream to be heated can be carried out in cocurrent, countercurrent, crosscurrent or crosscurrent.
  • cross countercurrent refers to a guide, in which the substances flow in an accommodating manner past each other, but intersect at least once on their way.
  • DC cross-flow designates a guide in which rectified currents intersect at least once.
  • An embodiment of the guide is preferably in countercurrent.
  • the heat transfer capacity of the heat exchanger can be between 100 and 600 kW, preferably between 200 and 500 kW and particularly preferably between 250 and 450 kW.
  • the heat transfer performance of the heat exchanger depends largely on the heat transfer coefficient of the provided transfer surface, the volume flow of the material flows and the desired average temperature difference between the cooled, reprocessed material flow and the material flow to be heated.
  • the heat transfer coefficient is determined inter alia by the thermal conductivity of the material used. This has a high thermal conductivity of the used material on the heat transfer performance.
  • the heat exchanger or at least the surfaces involved in the heat transfer can be made of metals, preferably steel, such as unalloyed or low-alloy, ferritic steel, in particular stainless steel, copper, aluminum, as well as glass, plastic, enamel, silicon carbide or combinations thereof.
  • increased transmission area results in better heat transfer performance.
  • the plates of a plate heat exchanger or tubes of a shell and tube heat exchanger may have ribs to provide increased heat transfer performance in the smallest possible space.
  • the heat exchanger is designed such that the average temperature difference between the cooled material stream to be treated and the stream to be heated is 0.5 to 10 ° C., preferably 1 to 9 ° C., particularly preferably 2 to 8 ° C is.
  • the material stream to be reprocessed can be cooled from an inlet temperature of, for example, 35 ° C. to an outlet temperature of, for example, 5 ° C.
  • the at least one material stream to be heated, in particular at least one prepared material stream can be heated from, for example, 0 ° C. to 40 ° C.
  • a heat exchanger having an average heat transfer performance may be sufficient.
  • a plate heat exchanger made of stainless steel is used.
  • a heat exchanger made of, for example, aluminum may be used, which has a higher thermal conductivity than stainless steel.
  • a smaller transfer area may suffice compared to a stainless steel heat exchanger, but aluminum is more susceptible to corrosion due to, for example, ammonia- or sulfur-containing residues in the material stream to be reprocessed.
  • materials such as aluminum larger heat exchanger surfaces can be realized more cost-effectively than in the case of stainless steel.
  • the material stream to be treated is fed to a first cooling stage for cooling.
  • the material stream to be treated is first cooled by a heat exchanger of the type described above.
  • the material stream to be reprocessed is from an inlet temperature of at most 100 ° C., preferably in the range from 20 to 50 ° C. and more preferably in the range from 30 to 40 ° C., to a maximum temperature of 15 ° C. , preferably in the range of -5 to 10 ° C, and more preferably in the range of 0 to 7 ° C cooled.
  • At least one material stream to be heated in particular at least one recycled material stream, can be warmed from, for example, 0 ° C. to 40 ° C.
  • a separation unit to the heat exchanger in order to separate off corrosive and high-boiling fractions from the material stream to be treated.
  • ammonia-containing substances, substances containing sulfur, in particular hydrogen sulfide, or both substance components in the ppm range which may damage the downstream components, in particular the cryogenic gas separation unit, may be present in the material stream to be reprocessed.
  • high boiling levels such as water, hydrocarbons having 4 or more carbon atoms, can freeze at temperatures below-100 ° C in the catalytic gas separation unit and damage the cryogenic gas separation unit by ice formation.
  • the separation unit can be made in one or more parts.
  • the separation unit comprises at least one phase separator and / or at least one gas purification unit.
  • At least one phase separator can be connected downstream of the heat exchanger.
  • the condensed fraction of the gas to be treated can be separated from the gas phase of the material stream to be treated, for example by adiabatic expansion after cooling by the heat exchanger.
  • high-boiling components in particular high-boiling hydrocarbons, preferably hydrocarbons having 4 or more carbon atoms, particularly preferably hydrocarbons having 5 or more carbon atoms and very particularly preferably hydrocarbons having 6 or more carbon atoms, and corrosive fractions, in particular ammonia-containing substances and sulfuric containing substances, are removed from the reprocessed stream.
  • a washing liquid which binds constituents of the material stream to be treated can be fed to the material stream to be treated before it enters the heat exchanger.
  • the passing components of the material stream to be treated may be solid, liquid and gaseous components.
  • washing liquid which absorbs in particular corrosive fractions of the material stream to be treated, a pure solvent, such as water or steam, or a suspension, such as calcium hydroxide solution Ca (HO) 2 , can be used.
  • a gas cleaning unit may be provided within the separation unit. This is used for high-boiling constituents, in particular high-boiling hydrocarbons, preferably hydrocarbons having 4 or more carbon atoms, for example toluene, and corrosive constituents, such as water separate off the material stream to be treated.
  • the gas purification unit can be configured as an adsorptive gas purification unit.
  • the adsorptive gas cleaning unit can be designed as a temperature or pressure swing adsorption. In contrast to the temperature change adsorption, in which the regeneration of the adsorber (desorption) takes place by a temperature increase, the regeneration takes place in the pressure swing adsorption at a reduced pressure.
  • the adsorptive separation process quadsi
  • at least two adsorbers operated in parallel can be provided, of which at least one is in the adsorption phase and at least one in the regeneration phase.
  • the gas purification unit can be designed as an adsorptive gas purification unit, which is designed in particular for carrying out a continuous change in temperature of the adsorption.
  • adsorptive in the thermal cycling process are water, hydrogen sulfide and / or hydrocarbons, in particular hydrocarbons having 4 or more carbon atoms.
  • Adsorbers may be molecular sieves, in particular zeolites, silica gel and / or alumina, wherein different molecular sieves can be combined depending on the application.
  • a separation unit is connected downstream of the heat exchanger for cooling the material stream to be treated in order to obtain a hydrogen and methane-rich material stream.
  • corrosive fractions and / or high-boiling fractions can be separated from the material stream to be treated in the separation unit.
  • the separation of corrosive fractions and / or high-boiling fractions can be carried out as described above in one or more steps.
  • at least one phase separator and / or at least one gas cleaning unit can be used for the separation of corrosive fractions and / or high-boiling fractions.
  • high-boiling components in particular high-boiling hydrocarbons, preferably hydrocarbons having 4 or more carbon atoms, particularly preferably hydrocarbons having 5 or more carbon atoms and very particularly preferably hydrocarbons having 6 or more carbon atoms, can be removed from the stream to be treated.
  • high-boiling hydrocarbons preferably hydrocarbons having 4 or more carbon atoms, particularly preferably hydrocarbons having 5 or more carbon atoms and very particularly preferably hydrocarbons having 6 or more carbon atoms
  • corrosive fractions in the material stream to be treated such as ammonia-containing substances and sulfur-containing substances, may be bound by the introduction of a washing liquid before entering the heat exchanger become. Subsequently, the corrosive fractions of the cooled after passing through the heat exchanger to be processed material flow can be separated in a phase separator.
  • a continuously operated temperature swing adsorption can be used, for example, to separate water vapor from the material stream to be treated.
  • adsorption operated in the thermal cycling process for example, water, hydrogen sulfide and / or hydrocarbons, in particular hydrocarbons having 4 or more carbon atoms, are removed by adsorption, with molecular sieves, in particular zeolites, silica gel and / or aluminum oxide being used as the adsorber.
  • the hydrogen and methane-rich material stream extracted from the separation unit is preferably substantially free of corrosive fractions and / or high-boiling fractions, such as high-boiling hydrocarbons, in particular hydrocarbons having 4 or more carbon atoms, ammonia-containing substances, sulfur-containing substances and water, the Hydrogen- and methane-rich material stream contains only traces of a few ppm of corrosive and freezing contaminants.
  • the cooling unit comprises at least one refrigeration system.
  • the refrigeration system In the refrigeration system, an indirect cooling of the reprocessed material flow takes place, wherein the refrigeration system absorbs heat below the ambient temperature and releases it at a higher temperature.
  • compression and / or sorption refrigeration machines are typically used, to which the required energy is supplied completely as mechanical work or in the form of heat. Even electrically operated refrigeration systems are conceivable.
  • the cooling unit may have a cooling capacity of 10 to 500 kW, preferably 50 to 300 kW, particularly preferably 80 to 200 kW.
  • the already pre-cooled in the heat exchanger hydrogen and methane-rich material flow which may have a temperature in the range of 0 to 15 ° C after passing through the separation unit to a constant temperature level in the range of -10 to 5 ° C are cooled.
  • the constant temperature level includes small deviations of less than 2 ° C.
  • the cooling unit of the cryogenic gas separation unit is connected immediately upstream. This is particularly advantageous since the first cooling stage ensures a substantially constant temperature level before entry into the cryogenic gas separation unit and thus stabilizes the process of cryogenic gas separation.
  • a simple design medium power cooling unit sufficient to stabilize the process.
  • the refrigeration system comprises a compression refrigeration machine which is equipped with at least one compression element, at least one expansion element and at least two heat exchangers.
  • the compression element can be realized by a mechanical compressor, for example a compressor.
  • the expansion element can be configured as a throttle element, for example as an expansion valve.
  • a compression and an expansion element and two heat exchangers can be interconnected in a circuit such that the heat exchangers are connected on both sides between the compression and expansion element.
  • a refrigerant for the thermodynamic cycle for example, carbon dioxide (C0 2 ) or ammonia (NH 3 ) can be used.
  • a cooling unit of the type described above is used.
  • the hydrogen and methane-rich material flow can be cooled to a substantially constant temperature level.
  • a substantially constant temperature level denotes a temperature level of the material flow which is constant except for small deviations of less than 2 ° C. Cooling by the cooling unit preferably takes place immediately before the separation of the hydrogen- and methane-rich material stream in the cryogenic gas separation unit. In this way, the pre-cooled by the heat exchanger hydrogen and methane-rich material flow can be cooled by up to 30 ° C, preferably by 5 to 10 ° C, with a simple designed cooling unit with medium power can be used.
  • the first cooling stage ensures a substantially constant temperature level before entry into the cryogenic gas separation unit, which stabilizes the treatment process, in particular the cryogenic gas separation.
  • a compression refrigeration system For cooling the hydrogen and methane-rich material flow, a compression refrigeration system can preferably be used.
  • a refrigerant in the compression refrigeration system for example, carbon dioxide (C0 2 ) or ammonia (NH 3 ) can be used.
  • the separation into at least one hydrogen-rich and at least one methane-rich material stream takes place in the context of the present invention in the cryogenic gas separation unit.
  • the synthesis gas is cooled by means of expansion units and the indirect heat exchange against material flows to be heated so far that it comes to a partial condensation in which at least one form methane-rich liquid fraction and at least one hydrogen-rich gas fraction, which are then separated in a phase separator.
  • the methane-rich liquid fraction can also be re-vaporized and heated and removed in gaseous form from the cryogenic gas separation unit.
  • the cryogenic gas separation unit comprises a cascade of heat exchangers and / or expansion units enclosed by a thermally insulated housing.
  • the cascade of heat exchangers and / or expansion units necessary for carrying out the condensation process is usually arranged in a steel housing and insulated with perlite in order to minimize heat input.
  • the housing can be flushed inside with a stream of nitrogen at slightly elevated pressure continuously.
  • the kroygene gas separation unit is usually operated under cryogenic conditions and uses the Joule Thomson effect and freezing to separate hydrogen from methane.
  • the hydrogen and methane-rich Stoffström can be cooled in the cryogenic gas separation unit to cryogenic temperatures of less than -100 ° C, with cooling to -180 ° C, preferably between -150 and -165 ° C. can be.
  • cryogenic temperatures of less than -100 ° C, with cooling to -180 ° C, preferably between -150 and -165 ° C. can be.
  • methane condenses from the gaseous stream and the methane fraction can be removed in a phase separator as a liquid fraction.
  • multiple stages of expansions are provided in the cryogenic gas separation unit.
  • methane-rich material flows can arise, which have different pressures.
  • the methane-rich liquid fraction produced in the first expansion can be removed and then re-evaporated, warmed up and discharged in gaseous form from the gas separation unit.
  • This methane-rich material flow can have a pressure between 5 and 10 bar.
  • the hydrogen- and methane-rich material stream can be cooled to lower temperatures than in the first expansion stage.
  • the result is a second methane-rich material flow, which has a pressure in the range of 0 to 4 bar.
  • the gas fraction from both expansion stages is removed together and forms the hydrogen-rich material flow.
  • At least one hydrogen-rich and at least one methane-rich material stream result at the outlet of the cryogenic gas separation unit.
  • these streams are in the heat exchanger of the first cooling stage heated by the material to be treated. This allows the treated hydrogen-rich stream and the treated methane-rich stream to be heated before being recycled to processes such as dealkylation.
  • the methane-rich material stream contains at least 70% by volume, preferably between 75 and 95% by volume of methane.
  • a maximum of up to 10% by volume, preferably not more than 5% by volume, of hydrogen can be present in the methane-rich material stream.
  • impurities in particular ethane, ethene, propene, propane, nitrogen, oxygen and carbon monoxide may be present in a proportion of not more than 20% by volume, preferably not more than 15% by volume, in the methane-rich material stream.
  • methane-rich material streams which can have different pressures in the range from 0 to 20 bar and originate from in each case one of the several expansion stages of the cryogenic gas separation unit.
  • a methane-rich material stream with a pressure of 0 to 4 bar (low pressure stream) and a methane-rich material stream with a pressure of 5 to 10 bar (high pressure stream) can be generated.
  • the composition of the high pressure stream and the low pressure stream may differ in that the low pressure stream in the cryogenic gas separation unit is recovered from a condensate having a lower temperature.
  • the low pressure stream portions of gases, for example, oxygen, which condense in a temperature range, which is achieved, for example, only from the second expansion.
  • gases for example, oxygen
  • up to 10% by volume, preferably up to 8% by volume, of methane can be present in the hydrogen-rich material stream.
  • Further impurities, in particular nitrogen and carbon monoxide may be present in a proportion of not more than 5% by volume, preferably not more than 2% by volume, in the hydrogen-rich material stream.
  • the hydrogen-rich material flow can have an outlet pressure which corresponds to the inlet pressure before the cryogenic gas separation unit.
  • the pressure can consequently be up to 100 bar, preferably up to 70 bar and particularly preferably up to 60 bar.
  • the at least one methane-rich material stream can be used as a heating gas, for example for firing a steam cracking furnace.
  • the calorific value of the at least one methane-rich material stream may be 35,000 to 50,000 kJ / m 3 , preferably 40,000 to 45,000 kJ / m 3 .
  • the calorific value is a measure of the specific usable amount of heat of a fuel, without taking into account any condensation heat.
  • the at least one hydrogen-rich material stream typically has a lower calorific value of 10,000 to 20,000 kJ / m 3 and is preferably recycled in the hydrodealkylation of alkyl-substituted hydrocarbons.
  • An exemplary embodiment of the invention is shown as a process flow diagram in FIG.
  • the inventive method and the associated apparatus 100 for processing a stream are described in the present example using a product stream 1.1 from a Hydrodealkyl michsstrom.
  • the reaction product is typically rich in dealkylated aromatic hydrocarbons, hydrogen and methane.
  • the aromatic hydrocarbons and a circulating gas to be treated are first separated off.
  • the recycle gas 1 .1 to be treated can first be introduced into the apparatus 100 according to the invention with the addition of water 2.
  • the addition of water makes it possible to bind corrosive fractions, such as ammonia and sulfur-containing substances, in water and, after passing through a heat exchanger KS1, to separate them in a restrictor A1.
  • the device 100 is typically supplied with a volume flow of about 30,000 to 35,000 Nm 3 / h of recycle gas 1 .2 at a pressure of about 50 to 60 bar and a temperature of 30 to 40 ° C.
  • An exemplary composition of the recycle gas 1 .2 before entering the device 100 is shown in Table 1. This contains essentially hydrogen and methane as well as minor impurities of, for example, ethane, ethene, propane, C 4 and C 6 hydrocarbons (abbreviated to C 4 - or C 6 -KW in Table 1), oxygen, nitrogen and carbon monoxide.
  • the first cooling stage of the device 100 comprises a stainless steel plate heat exchanger KS1 with a transmission capacity of at least 300 kW in order to cool the recycle gas 1.2 to a temperature in the range of 3 to 7 ° C.
  • a subsequent throttle A1 condensed portions of the recycle gas 2 are separated by the cooling.
  • hydrocarbons having 4 or more carbon atoms, preferably 5 or more carbon atoms and more preferably 6 and more carbon atoms are condensed, which may optionally be recycled back to the process of dealkylation.
  • further purification stages A may follow, filtering out high-boiling components, such as water, from the cycle gas 4.
  • high-boiling components such as water
  • the drying of the circulation gas 4 takes place in an adsorption unit A2, A2 ', in which water is adsorbed with molecular sieves.
  • heavy-boiling hydrocarbons in particular hydrocarbons having 4 or more carbon atoms, are adsorbed in the adsorption unit A2, A2 'using further adsorbers known to the person skilled in the art.
  • the regeneration of the adsorber is achieved by desorption by means of hydrogen at elevated temperature.
  • the circulation gas 5 essentially contains hydrogen and methane with less than 10% by volume of other impurities.
  • the cooling of the cycle gas 5 is carried out by a refrigeration system KS2 to a temperature level in the range of 0 ° C and thus determines the inlet temperature of the cycle gas 6 for the cryogenic gas separation unit KS3. It can thereby be ensured that the temperature of the circulation gas 6 when entering the cryogenic gas separation unit KS3 is substantially constant and any temperature fluctuations due to, for example, the temperature change during regeneration of the adsorption unit A2 or A2 'can be prevented.
  • cryogenic gas separation unit KS3 which represents the second cooling stage of the treatment process according to the invention, the cryogenic separation of the cycle gas 6, which essentially comprises hydrogen and methane, takes place.
  • the recycle gas contains slightly more than 60% by volume of hydrogen and just over 35% by volume of methane.
  • the recycle gas 6 is cooled by cascades of heat exchangers and expansion stages to cryogenic temperatures in the range from -150 to -165 ° C., the dew point of methane being reached at these low temperatures.
  • cryogenic temperatures in the cryogenic gas separation unit KS3 will reach two expansions. Details of the cryogenic gas separation unit are not shown in FIG.
  • a first liquid fraction of methane is separated from the recycle gas 6 in a first expansion to cryogenic temperatures.
  • This first liquid fraction is heated again before exiting the cryogenic gas separation unit KS3 preferably against streams to be cooled in heat exchangers and fed back to the heat exchanger KS1 in the gaseous phase under a pressure between 5 and 10 bar, where a further warming against the input current to be cooled. 1 .2 takes place.
  • the gaseous fraction formed after the first expansion is further cooled in a second expansion in order to obtain even lower temperatures and to separate off further portions of methane from the gaseous fraction.
  • a second liquid fraction of essentially methane is formed again.
  • the second liquid fraction is also warmed up again before it leaves the cryogenic gas separation unit KS3 against flows to be cooled in the heat exchanger cascades of the cryogenic gas separation unit KS3.
  • the gaseous fraction formed after the second expansion essentially comprises hydrogen and thus forms the stream of recyclable clean gas 7, which is also warmed up before emerging from the cryogenic gas separation unit KS3 against streams to be cooled.
  • cryogenic gas separation unit KS3 From the cryogenic gas separation unit KS3 occur after the cryogenic separation thus a total of three treated streams: two methane-rich streams 9 and 8 at different pressure and a hydrogen-rich stream 7. These are in the gaseous phase and all have a temperature in the range of the inlet temperature of about 0th ° C as reached by the refrigeration system KS2 before entering the cryogenic gas separation unit KS3.
  • the treated methane-rich stream 9 resulting from the first expansion is typically under a pressure between 5 and 10 bar.
  • the treated methane-rich stream 8 originates from the second expansion and therefore has a lower pressure in the range from 0 to 4 bar.
  • Exemplary compositions of streams 8 and 9 are shown in Tables 2.1 and 2.2.
  • the treated methane-rich streams 8, 9 are recycled before recycling as heating gas in the heat exchanger KS1 and heated against the stream to be cooled 1 .2. Subsequently, the heated streams 12 and 13 are combined to form a total stream 15, the pressure ratios of the stream 13 being adapted to those of the stream 12.
  • Table 3 lists an exemplary composition of the hydrogen-rich stream 7 that forms the recyclable clean gas 7.
  • This stream has a temperature and a pressure which correspond to the conditions of the hydrogen-rich stream 6 before entering the cryogenic gas separation unit KS3.
  • this hydrogen-rich stream 6 has a pressure in the range of 40 to 80 bar.
  • the streams 7, 8, 9 are returned to the heat exchanger and against the stream to be cooled 1 .2. heated. Subsequently, the heated clean gas 11 is conducted in the total stream 14 into the plant for the dealkylation of alkyl-substituted aromatic hydrocarbons.
  • part of the recyclable clean gas 7 in the embodiment shown in FIG. 1 is branched off before heating in the heat exchanger KS1 and used for regeneration of the adsorption unit A2 or A2 '.
  • the partial flow 10.1 of the clean gas 7 is fed to a heater A3, for example an electric heater, and heated to a temperature of 150 to 350 ° C., preferably 200 to 260 ° C.
  • the partial flow of the recyclable clean gas can be diverted from the stream 1 1 after heating in the heat exchanger KS1 and fed to a heater.
  • the stream 10.2 is then passed into the adsorption unit A2 or A2 'to be regenerated. In addition, it may be provided to supply a portion of the stream 10.2 to the total flow of the heating gas 15. After regeneration, the stream 10.3 is fed to the heated stream of recyclable clean gas 11 and the total stream 14 is fed into the plant for dealkylation of alkyl-substituted aromatic hydrocarbons.
  • the inventive 100 are efficiently operated in the cycle, with as many resources as possible being recycled.
  • the hydrogen-rich material stream 11 can be recycled to the hyrodealkylation (not shown).
  • the two methane-rich material streams 12 and 13 can be used as a heating gas, for example for firing a steam cracking furnace (not shown).
  • A2 A2 'adsorptive separation unit

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un dispositif (100) servant à traiter un flux de matières (1.1) contenant de l'hydrogène et du méthane qui comprend les composants suivants : (i) au moins un échangeur de chaleur (KS1) pour refroidir un flux de matières (1.1) à traiter; (ii) au moins une unité de séparation (A, A1, A2, A2') pour purifier le flux de matières (3) à traiter afin d'obtenir un flux de matières (5) riche en hydrogène et en méthane; (iii) au moins une unité de refroidissement (KS2) pour refroidir le flux de matières (5) riche en hydrogène et en méthane; et (iv) au moins une unité de séparation de gaz (KS3) cryogénique pour séparer le flux de matières (6) riche en hydrogène et en méthane en au moins un flux de matières (7) riche en hydrogène et en au moins un flux de matières (8, 9) riche en méthane. L'invention concerne en outre un procédé servant à traiter un flux de matières.
PCT/EP2012/076360 2011-12-23 2012-12-20 Dispositif et procédé pour traiter un flux de matières contenant de l'hydrogène et du méthane WO2013092844A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP11195482 2011-12-23
EP11195482.2 2011-12-23

Publications (2)

Publication Number Publication Date
WO2013092844A2 true WO2013092844A2 (fr) 2013-06-27
WO2013092844A3 WO2013092844A3 (fr) 2014-05-22

Family

ID=47557084

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2012/076360 WO2013092844A2 (fr) 2011-12-23 2012-12-20 Dispositif et procédé pour traiter un flux de matières contenant de l'hydrogène et du méthane

Country Status (1)

Country Link
WO (1) WO2013092844A2 (fr)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3371126A (en) 1966-08-19 1968-02-27 Universal Oil Prod Co Hydrocarbon conversion process, naphtha to aromatics and town gas
DE2055507A1 (de) 1969-11-13 1971-05-19 Hydrocarbon Research Ine , New York, NY (VStA) Verfahren zur Reinigung eines Be schickungsgases aus Rohwasserstoff
WO2007051851A1 (fr) 2005-11-06 2007-05-10 Basf Se Procede de production de composes aromatiques, en particulier de benzene, par aromatisation de composes non aromatiques a la vapeur d'eau et desalkylation d'hydrocarbures aromatiques a substitution alkyle a l'hydrogene

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3626705A (en) * 1968-09-04 1971-12-14 Messer Griesheim Gmbh Low temperature separation of gaseous mixtures employing solidification
US4153428A (en) * 1977-08-30 1979-05-08 Union Carbide Corporation Prepurification of toluene dealkylation effluent gas

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3371126A (en) 1966-08-19 1968-02-27 Universal Oil Prod Co Hydrocarbon conversion process, naphtha to aromatics and town gas
DE2055507A1 (de) 1969-11-13 1971-05-19 Hydrocarbon Research Ine , New York, NY (VStA) Verfahren zur Reinigung eines Be schickungsgases aus Rohwasserstoff
WO2007051851A1 (fr) 2005-11-06 2007-05-10 Basf Se Procede de production de composes aromatiques, en particulier de benzene, par aromatisation de composes non aromatiques a la vapeur d'eau et desalkylation d'hydrocarbures aromatiques a substitution alkyle a l'hydrogene

Also Published As

Publication number Publication date
WO2013092844A3 (fr) 2014-05-22

Similar Documents

Publication Publication Date Title
DE60108835T2 (de) Verfahren und Anlage zur Rückgewinnung und Reinigung von Äthylen hergestellt durch Pyrolyse von Kohlenwasserstoff
DE3872255T2 (de) Behandlung stickstoffreicher, wasserstofffreier und olefinreicher gas mittels physikalischer lösungsmittel.
DE102007063347A1 (de) Verfahren zur Abtrennung von leichtsiedenden Komponenten aus einem Kohlenwasserstoffstrom
NZ212960A (en) Dehydrocyclodimerisation process for producing c 6 -c 8 aromatic hydrocarbons from c 3 and c 4 aliphatic hydrocarbons
EP3558912B1 (fr) Procédé et installation de production d'une oléfine
JP4117560B2 (ja) 炭化水素からノルマルパラフィンを分離する方法及び分離された炭化水素の用途
DE102012003741B4 (de) Verfahren zur Rückgewinnung von Kohlenwasserstoffen aus Polyolefinanlagen und dafür geeignete Vorrichtung
US9227854B2 (en) Process for purification of an aqueous phase containing polyaromatics
US4677235A (en) Production of aromatic hydrocarbons from natural gas
KR20200026945A (ko) 수소 및 메탄을 부분적으로 제거하는 두 가지 방법에서 프로판 탈수소화 및 증기 분해 방법을 예비-분리 단계와 결합하여 프로필렌을 생산하는 공정 및 플랜트
RU2697800C2 (ru) Способы и установки для извлечения этилена из углеводородов
WO2003106331A1 (fr) Installation et procede pour la decomposition et la purification de gaz de synthese
DE3244143A1 (de) Verfahren zur gaszerlegung
WO2013092844A2 (fr) Dispositif et procédé pour traiter un flux de matières contenant de l'hydrogène et du méthane
CN106350107A (zh) 用于处理含氢气和烃类的烃进料的方法
RU2757864C2 (ru) Способ и система для получения бензола
EP0733031A1 (fr) Procede et dispositif d'epuration du chlorure de vinyle
EP0683146B1 (fr) Procédé de séparation d'hydrocarbures en C2/C3 dans des unités de production d'éthylène
US8524046B2 (en) Distillation column pressure control
EP1519781B1 (fr) Dispositif de desorption de dioxyde de carbone a partir de methanol
DE1201857B (de) Verfahren zur Abtrennung niedrigsiedender Gase aus einem Gasgemisch
RU2501779C1 (ru) Способ выделения этилена полимеризационной чистоты из газов каталитического крекинга
DE2947239C2 (fr)
DE3544855A1 (de) Verfahren zur abtrennung von c(pfeil abwaerts)5(pfeil abwaerts)(pfeil abwaerts)+(pfeil abwaerts)-kohlenwasserstoffen aus einem gasstrom
DE69118427T2 (de) Verfahren zur Trennung von Gasgemischen aus Erdölraffinerien

Legal Events

Date Code Title Description
122 Ep: pct application non-entry in european phase

Ref document number: 12813841

Country of ref document: EP

Kind code of ref document: A2