WO2014064172A2 - Procédé pour la récupération de molécules légères à partir d'un courant d'alimentation oléfinique - Google Patents

Procédé pour la récupération de molécules légères à partir d'un courant d'alimentation oléfinique Download PDF

Info

Publication number
WO2014064172A2
WO2014064172A2 PCT/EP2013/072212 EP2013072212W WO2014064172A2 WO 2014064172 A2 WO2014064172 A2 WO 2014064172A2 EP 2013072212 W EP2013072212 W EP 2013072212W WO 2014064172 A2 WO2014064172 A2 WO 2014064172A2
Authority
WO
WIPO (PCT)
Prior art keywords
stream
gaseous
liquid
gaseous stream
liquid stream
Prior art date
Application number
PCT/EP2013/072212
Other languages
English (en)
Other versions
WO2014064172A3 (fr
Inventor
Laurent LEMINEUR
Dominique Pascal
Wolfgang Garcia
Sylvain GOURVIL
Original Assignee
Total Research & Technology Feluy
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 Total Research & Technology Feluy filed Critical Total Research & Technology Feluy
Publication of WO2014064172A2 publication Critical patent/WO2014064172A2/fr
Publication of WO2014064172A3 publication Critical patent/WO2014064172A3/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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • 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
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • 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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream 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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins
    • 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
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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
    • F25J2210/04—Mixing or blending of fluids with 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • At least part of the condensed liquid effluent stream is contacted with a liquid water-containing stream in a liquid-liquid contacting device to at least partly separate said condensed liquid effluent stream, or portion thereof, into an aqueous phase rich in said at least one oxygenate and an organic phase rich in said C5+ hydrocarbons.
  • MTO effluents also contain significant amount of light molecules such as hydrogen and methane that required to be separated. Separation of those light molecules can be performed in a demethanizer.
  • Typical purification scheme including demethanizer of steam cracker effluent can for instance be found in the Kirk-Othmer encyclopaedia of Chemical Technology 5 th edition Vol. 10 p 611 -613. In this usual design, effluent purification is performed in a demethanizer.
  • FR 2957931 relates to the treatment of a stream originating from a steam cracker (and not of the treatment of a stream originating from a MTO process), involving a demethanizer to remove methane and hydrogen.
  • the process described involves different separation and washing steps of the olefinic stream before entering the demethanizer. It can be noted that the separation and washing steps are conducted at a temperature below -90°C. For example, it describes a stream being introduced in an ethylene adsorption column, said stream having previously been cooled to a temperature between -1 10°C to -120°C.
  • N2O3 may combine and react with poly-unsaturated olefins, such as butadiene present in an olefin-containing stream, to form highly unstable gum compounds.
  • poly-unsaturated olefins such as butadiene present in an olefin-containing stream
  • Such compounds are a major safety and operability concern, as they may cause runaway reactions and even explosions.
  • a solution is given by US 2010/0105973 which replace said traditional methods involving a succession of separation/ distillation steps at cryogenic temperature by distillation using hydrocarbons absorbents.
  • the solvent used comprises hydrocarbons C2 to C4.
  • the inlet stream can contain nitrogen oxides, the extractive distillation is run under conditions avoiding the formation of N203 from nitrogen oxides. Formation of N203 is avoided when temperature are above -100°C.
  • step d) conducting a distillation on the second liquid stream (E) and/or the third liquid stream (G) to recover a fourth gaseous stream (H) and a fourth liquid stream (I) comprising hydrocarbons with at least two carbon atoms the process being remarkable in that stream (A) is produced by a methanol to olefin process, in that the operating temperature of the second gaseous stream (D) is greater than -90°C and in that the separation of the second gaseous stream (D) in step c) is conducted by washing said second gaseous stream (D) by a solvent.
  • the stream (A) is produced by a methanol to olefin process, or by a methanol to olefin process with at least part of the effluent of the methanol to olefin process being treated in an olefin cracking process. Therefore, advantageously, the stream (A) comprises up to 20 %mol of methane and hydrogen relative to the total molar content of stream (A) preferably up to 10%mol, and/or the stream (B) comprises up to 70%mol of methane and hydrogen relative to the total molar content of stream (B) preferably up to 60% mol.
  • the step a) of separating the gaseous stream (A) into a first gaseous stream (B) and a first liquid stream (C), and/or the step b) of separating the first gaseous stream (B) into a second gaseous stream (D) and a second liquid stream (E) comprises the steps of cooling the gaseous stream (A) and/or (B) and separating the liquid fraction obtained from the remaining gaseous fraction to produce a gaseous stream and a liquid stream, with preference said stream (A) and/or (B) is cooled to a temperature ranging from - 30°C to - 90°C
  • the first liquid stream (C) is further subjected to a step of distillation to recover a gaseous stream, and a liquid stream with at least with two carbon atoms, preferably the distillation step of the first liquid stream (C) is conducted together with the step d) of conducting a distillation on the second liquid stream (E) and/or the third liquid stream (G) to recover a fourth gaseous stream (H) and a fourth liquid stream (I) comprising hydrocarbons with at least two carbon atoms.
  • the fourth liquid stream (I) comprising hydrocarbons with at least two carbon atoms are further subjected to a step of recovering hydrocarbons comprising:
  • the solvent of step c) used to wash the second gaseous stream (D) is ethane, preferably the ethane used is originated from saturated hydrocarbon stream (N).
  • the fourth gaseous stream (H) is recycled into gaseous stream (A), preferably before the step of removal of contaminants from the gaseous stream (A) according to the previously mentioned embodiment.
  • the operating temperature of one or more of the second and third liquid stream (E) and (G) and of the third gaseous stream (F) is greater than -90°C.
  • the oxygenated contaminants consist of alcohols, ethers, carboxylic acids, aldehydes or any combination.
  • a first separator unit to separate a incoming gaseous stream (A) into a first gaseous stream (B) and a first liquid stream (C);
  • the first and second separation unit comprising at least one cooler device followed by a gas/liquid separator
  • the third separator unit is an absorption column (9).
  • the installation is remarkable in that it further comprises distillation means (8) to separate hydrocarbon with at least two carbon atoms from hydrogen and methane, preferably said distillation means are a demethaniser (8), preferably it further comprises means to convey one or more of the first liquid stream (c), the second liquid stream (E) and the third liquid stream (G) said distillation means (8), more preferably at least two of the first liquid stream (c), the second liquid stream (E) and the third liquid stream (G) are conveyed to the same distillation means (8).
  • the installation is preferably characterized in that it further comprises means to collect the overhead stream (H) exiting the distillation means (8) and to convey said stream (H) to expanding means (10) in order to cool said stream (H), and means to convey said cool stream (H) in the cooling device of the first or second separation unit.
  • the main stream (A) originates from a methanol to olefins (MTO) process or a MTO process with at least part of the effluent of MTO process being treated in an olefin cracking process (OCP).
  • MTO methanol to olefins
  • OCP olefin cracking process
  • the main stream (A) being at a temperature of about 50°C, is firstly compressed in a compression means (1 ) like for instance a compressor.
  • a step of removal of the contaminants comprising a purification in an oxygen removal unit (2) to remove the oxygenated contaminants by a stripping step, and the removal of C02 and H2S in the C02 removal unit (3) by implementation of a caustic washing step using for instance a caustic wash tower.
  • the temperature is then adapted in a cooler device like for instance the heat exchanger (4) to reach at most -30°C.
  • the temperature is maintained at a temperature greater than -90°C.
  • a liquid and a gaseous fraction are then produced and separated using a gas/liquid separator like the splitter (5) to form a first gaseous stream (B) and a first liquid stream (C).
  • the separator or splitter (5) makes a first separation of the fuel gas (i.e. methane and hydrogen) from the C2+.
  • the fuel gas (i.e. methane and hydrogen) are mainly contained in first gaseous stream (B), whereas the C2+ are mainly contained in the first liquid fraction (C).
  • the first liquid stream (C) is subjected to a step of distillation in a distillation means (8) being preferably a demethanizer/stripper (i.e. a distillation with a re-boiler on the bottom but no re-condenser on the top) to remove the remaining methane and hydrogen.
  • the fuel gas exits the distillation means (8) in a stream (H) as overhead flow and a purified stream (I) containing the C2+ is recovered as bottom flow.
  • the first gaseous stream (B) is cooled down to a temperature of about -85°C in a cooler device (6) being for instance a heat exchanger.
  • the cold used in this cooler device (6) comes advantageously from the decompressed flow ( ⁇ ') as described below.
  • This further cooling of the first gaseous stream (B) creates a liquid and a gaseous fraction.
  • the stream ( ⁇ ') obtained at the exit of the cooler device (6) is then sent to a gas/liquid separator (7) being for instance a splitter.
  • the liquid and the gaseous fractions are separated in this gas/liquid separator (7) to obtain a second liquid stream (E) and a second gaseous stream (D).
  • the gas/liquid separator (7) makes a second separation of the fuel gas from the C2+.
  • the fuel gas i.e. methane and hydrogen
  • the second gaseous stream (D) are mainly contained in second gaseous stream (D)
  • the C2+ are mainly contained in the second liquid fraction (E).
  • the second liquid stream (E) is subjected to a step of distillation in distillation means (8) to remove the remaining methane and hydrogen contained.
  • the fuel gas exit the distillation means (8) in a stream (H) as overhead flow and a purified stream (I) containing the C2+ is recovered as bottom flow.
  • the separation is conducted by washing stream (D) by a solvent on an absorption column (9).
  • the absorption column (9) finishes the separation started in the gas/liquid separator (5) and (7).
  • the absorption column (9) is fed with a solvent stream (L).
  • the solvent used is preferably ethane.
  • the ethane used as solvent is a product of the process that is recycled as it will be seen later.
  • a stream (F) containing purified fuel gas i.e. methane and hydrogen
  • the stream (D) exiting gas/liquid separator (7) has low ethylene content and is relatively small compared to stream (A). Indeed, the ratio of the flow rate of the second gaseous stream (D) to the gaseous stream (A) is at most 1/5, preferably at most 1/6. Consequently the requirements for the absorption column (9) are relatively low: the separation can be performed with a relatively small column and the absorbent flow (L) is also small. The capital expenditure (CAPEX) associated with the column remains therefore small and the stream (G) recycled to the distillation means (8) stays also small.
  • the stream (G) exiting the bottom of the absorption column (9) is subjected to a distillation step and therefore sent to the distillation means (8) to remove the remaining ethylene and methane and hydrogen contained.
  • the stream (H) obtained in the top of the distillation means (8) has a temperature of about - 30°C.
  • it is expanded in an expanding means being for instance a turbo expander (10) to obtain a cooled stream ( ⁇ ') at a temperature of about -95°C.
  • This temperature is obtained without the use of ethylene refrigeration cycle, thus lower capital expenditure (CAPEX) is required to set up the installation.
  • the interest of reaching such temperature is not in a separation step but to save energy by using this stream to cool stream (B) in a cooler device (6) being for instance a heat exchanger.
  • a stream (H") obtained at the exit of the cooler device (6) has a temperature of about -40°C.
  • Another advantage of this step of expanding is that it allows stream (H") to be recycled by being mixed with stream (A) at the beginning of the purifying process, as both stream will show similar pressure.
  • the stream (I) obtained at the bottom of the distillation means (8) is sent to a de- ethanizer (1 1 ) to recover a bottom stream (J) containing mainly C3+ and a top stream (K) containing mainly ethane and ethylene.
  • Stream (K) is further sent to a C2 splitter to separate ethylene on the top (stream (M)) from ethane on the bottom (stream (N) and (L)).
  • Part of the ethane obtained in the bottom of the C2 splitter is used in the absorption column (9).
  • Other possible solvents that can be used in the absorption column (9) are saturated paraffins from C2 to C4.
  • the stream (K) exiting the de- ethanizer (1 1 ) is sent to a selective hydrogenation unit to convert the possible acetylene traces.
  • Acetylene being a poison for the polymerization catalysts, it is required to limit to a maximum level of 5ppmv its content in the ethylene stream.
  • Selective hydrogenation is an adequate option to purify an ethylene stream.
  • distillation means (8), the gas/liquid separator (7) and the absorption column (9) allow separating the fuel gas from the C2+ fraction with the same specifications as a usual industrial design of a steam cracker plant. Good heat balances are obtained with the process design of the present invention.
  • the MTO process has also been described in US 2006 0235251 , WO 2005 016856, US 2006 0063956, US 2006 0161035, US 6207872, US 2005 0096214, US 6953767 and US 7067095, the content of which is incorporated in the present application.
  • the C4+ olefins produced in the MTO process may also be cracked in an olefin cracking process.
  • EP1036133, EP92091 1 the content of which is incorporated in the present application.
  • the effluent produced by a MTO and Quench processes is a hydrocarbon stream comprising light molecules.
  • the composition of stream (A) consists of water, hydrogen (H2), methane, ethylene, ethane, propylene, propane and C3+ (i.e. hydrocarbons having at least three carbon atoms).
  • water is present in the stream with a concentration between 1 to 10% mol (molar percent), preferably between 2 and 8 % mol based upon total molar content of the stream (A).
  • Hydrogen (H2) is present in the stream with a concentration between 1 and 10 % mol, preferably between 2 and 8 % based upon total molar content of the stream (A).
  • Methane is present in the range of 1 to 5 % mol, preferably in the range of 2 to 4 % mol based upon total molar content of the stream (A).
  • the C2 molecules ethane + ethylene
  • the heavier molecules constitute the rest of the stream.
  • the effluent stream (A) coming from the MTO + Quench section or from the MTO + OCP + Quench section has a temperature in the range of 10 and 90°C, preferably in the range of 30 and 60°C and a pressure in the range of 10 4 Pa to 5 10 5 Pa (0.1 to 5 bara), preferably between 10 5 to 3 10 5 Pa (1 and 3 bara).
  • Ethylene and propylene are particularly desirable olefins but it has been found that their yields in the MTO process are reduced by the production of medium weight hydrocarbons such as C4, C5 and C6 olefins, as well as some heavier components. Methods are needed to alter the product distribution in the MTO process for making light olefins to provide processing flexibility. Methods are sought to reduce the production of C4, C5 and higher olefins from the MTO process relative to the production of ethylene and propylene. Therefore an olefin cracking process (OCP) is combined with the MTO process to crack the C4, C5 and higher olefins from the MTO process. Such yield improvements of ethylene and propylene significantly improve the economies of the methanol to olefins process.
  • OCP olefin cracking process
  • the OCP process As regards to the OCP process, it consists in selective cracking of olefin- rich stream. The process is selective toward the formation of light olefins. It enables improvements of the ethylene and propylene yields from the MTO unit. Details about the OCP catalyst and process can be found in the patent EP 1036139; EP 1036135; EP 1036133 and WO 99/29805, content of which is incorporated in the present application.
  • oxygenated contaminants one can cite alcohols such as methanol, ethanol, C3 alcohols; ethers such as dimethyl ether, diethylether and methyl ethyl ether; carboxylic acids such as acetic acid, propanoic acid and butyric acid; aldehydes such as acetaldehyde; ketones such as acetone; and esters such as methyl esters.
  • Particularly problematic oxygenate contaminants downstream the MTO process are dimethyl ether (DME) and acetaldehyde.
  • DME dimethyl ether
  • acetaldehyde acetaldehyde.
  • the presence and concentrations of these by-products may vary depending, for example, on the feedstock qualify, the type and size of reactor, the reaction conditions, and the type and condition of the catalyst used.
  • the patent US 7332639 consists in the separation of the gaseous fraction from the liquid fraction and washing the gaseous fraction with a liquid alcohol-containing stream and finally washing the gaseous fraction washed fraction obtained with a water containing stream.
  • the carbon dioxide and to the H2S requires removal.
  • an olefin product specification may require removal of carbon dioxide from the methanol-to-olefins reactor effluent.
  • exposure of the carbon dioxide containing stream to below-sublimation temperatures may result in equipment damage and frozen piping.
  • Methods commonly known and used in the industry such as caustic solution treatment or amine absorption, may be used to remove C02 from the methanol-to-olefins reactor effluent.
  • the reactor effluent may be contacted with a caustic solution to separate at least a portion of the carbon dioxide present in the reactor effluent. If necessary, the reactor effluent may be additionally compressed prior to the carbon dioxide removal stage.
  • a molecular sieve dryer may be used for separating at least a portion of the water, drying the reactor effluent.
  • a chemical desiccant such as glycol may be used for drying the reactor effluent.
  • a portion of the water in the reactor effluent may be condensed and the remaining effluent may be dried.
  • Other dehydration techniques commonly known and used in the industry may also be used.
  • the MTO+Quench effluents effluent may be additionally compressed prior to the water removal stage.
  • the stream containing the oxygenated contaminants is burned and heat is recovered.
  • the distillation means being preferably demethanizer/stripper
  • the demethanizer/stripper is a conventional distillation column containing a plurality of vertically spaced trays, one or more packed beds, or some combination of trays and packing.
  • the demethanizer/stripper section also includes re-boilers on the bottom of the column (not represented) but it presents no condenser on the top of the column and no reflux.
  • the re-boiler on the bottom of the column heats and vaporizes a portion of the liquids flowing down the column to provide the stripping vapours which flow up the column to strip the liquid product.
  • the presence of a condenser on the top of the column would require an ethylene cryogenic cooling and there is no need of a reflux on the top of the column because of the presence of the adsorption column.
  • reflux can be used at various height of the column to improve the separation yield.
  • demethanizer/stripper processes can be found in EP 0980502; EP 1 137903 and WO 03/040633 which are incorporated thereby by reference.
  • the demethanizer/stripper of the present invention operates at temperature between 20 and 80°C on the bottom of the column and between -10 and -90°C on the top of the column.
  • the operating pressure of the demethanizer/stripper is between 2 10 6 to 35 10 6 Pa (20 and 35 bara).
  • the overhead stream exiting the demethanizer/stripper is essentially constituted of hydrogen, methane, ethylene and ethane.
  • Hydrogen concentration is in the range of 2 to 10 % mol based upon the total molar content of stream (H); methane concentration is in the range of 30 to 50 % based upon the total molar content of stream (H); and C2 (ethylene and ethane) in the range of 40 to 60% based upon the total molar content of stream (H).
  • Traces of C3+ may also be present.
  • the bottom stream exiting the demethanizer/stripper (stream (I)) is essentially constituted of C2+ (ethylene, ethane and C3+).
  • Ethylene and ethane are in the range of 30 to 50 % mol in the effluents based upon the total molar content of stream (I).
  • C3+ content is in the range of 50 to 70% mol based upon the total molar content of stream (I).
  • the absorption column conventional absorption systems can be used in this invention.
  • the absorption system uses packed columns, although plate absorption columns may also be used.
  • the absorption column has a liquid inlet located at a top portion of the absorption column.
  • the absorbent liquid is evenly distributed across the top of the column. Desirably, an even distribution of the absorbent liquid is accomplished by using a distributor plate or spray nozzles.
  • a gas inlet At the bottom of the absorption column is a gas inlet where the hydrocarbon stream, enters the absorption column.
  • the vapour components move up the column counter-current to the liquid absorbent moving down the column. This is known as counter-current absorption.
  • the packing or plates in the column provides a surface for intimate contact between the vapour and liquid components within the column.
  • the heat exchanger (6) transfers cold from stream ( ⁇ ') to stream (B).
  • Typical temperature of stream ( ⁇ ') ranges from to -1 10°C to -80°C, preferably from -90°C to -100°C.
  • the typical temperature of stream (H") ranges from -50 to -20°C, preferably from -40 to -30°C.
  • typical temperature from stream (B) is in the range from - 20 to -40°C, preferably from -30 to -40°C.
  • the temperature of stream ( ⁇ ') ranges from -105 to -85°C, preferably from -100 to -90°C.
  • any absorbing medium allowing good separation of the fuel gas from the C2+ can be used.
  • Hydrocarbons can be used. More preferably short chain hydrocarbons in C2-C4. Even more preferably ethane as it presents a low boiling point. Absorption being an exothermic process, part of the absorption heat can be released via ethane vaporization inside the absorption column. Thereby ethane vaporization advantageously limits the heat treatment outside the column.
  • the turbo expander it is well known by the person skilled as an apparatus used to expand a high pressure gas while recovering work. The work recovered can be used to drive a compressor or to produce electricity.
  • the turbo expander is driven by a high pressure gas source.
  • the high pressure gas source becomes reduced in pressure to a lower pressure gas source as a consequence of gas expansion that drives the turbo expander.
  • the energy recovered by the turbo expander can be either used to produce electricity with an alternator or it can be used to run a compressor.
  • the alternator or the compressor runs in the same shaft as the turbo expander.
  • the turbo expander (10) may be linked with the compressor (1 ) in order to improve the overall energy balance.
  • the de-ethanizer is a conventional distillation column containing a plurality of vertically spaced trays, one or more packed beds, or some combination of trays and packing.
  • the de-ethanizer section also includes reboilers or reflux (not represented) which heat and vaporize a portion of the liquids flowing down the column to provide the stripping vapours which flow up the column to strip the liquid product.
  • reflux can be used at various height of the column to improve the separation yield.
  • the ethylene splitter it is can also be referred to as a "fractionation tower” or a “distillation column”. It is a conventional separation unit used to separate ethane from ethylene well known in the art.
  • traces refers to a concentration in the range of 0.001 %wt to 0.1 %wt.
  • the term “essentially” refers to a composition containing at least 80 wt % of the said product, preferably between 85 wt % and 95 wt %, more preferably above 95 wt %.
  • Embodiment 1 the present invention is a process for purifying a gaseous stream
  • Embodiment 2 a process according to embodiment 1 wherein the stream (I) is sent to a de-ethanizer (1 1 ) to get a C3+ bottom flow (J) and an overhead (K) constituted mainly of ethane and ethylene and the flow (K) is sent to a C2 splitter (12) where ethylene is separated on the top and ethane on the bottom.
  • Embodiment 3 a process according to embodiment 2 wherein part of the ethane obtained in said C2 splitter (12) is used as absorbent in the absorption column (9).
  • Embodiment 4 a process according to any of the preceding embodiments wherein the said olefins stream (A) is produced by a methanol to olefins (MTO) process.
  • MTO methanol to olefins
  • Embodiment 5 a process according to any of the preceding embodiments wherein the said MTO process is based on methanol and dimethyl ether.
  • Embodiment 6 a process according to any of the preceding embodiments wherein the said olefins stream (A) is produced by an olefin cracking process.
  • Embodiment 7 a process according to embodiment 1 wherein the solvent used in said absorption column of step g) is ethane.
  • Embodiment 8 a process according to embodiment 2 wherein a acetylene selective hydrogenation is performed on stream (K).
  • Embodiment 9 a process according to embodiment 1 wherein the oxygenates contaminants (iii) consist of alcohols, ethers, carboxylic acids, aldehydes.
  • the energy consumption of the design of the invention was of 506 kcal/ kg light olefins (ethylene and propylene).
  • the design generally used (as described in the Kirk-Othmer encyclopaedia of Chemical Technology 5 edition Vol. 10 p 61 1 -612) was of 583 kcal/ kg light olefins (ethylene and propylene).
  • the present invention allows an improvement of the energy consumption. In both cases, the ethylene and propylene recovery were higher than 99.7%.
  • Table 1 clearly shows that the ratio of the flow rate of the stream (D) to the stream (A) is of about 0.12 which is less than 0.17 (i.e. 1/6).

Landscapes

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

Abstract

La présente invention porte sur un procédé pour la purification d'effluents de procédé de conversion de méthanol en oléfines. Le procédé consiste à purifier les oléfines de valeur en les séparant du gaz combustible (c'est-à-dire le méthane et l'hydrogène) à l'aide d'étapes de séparation, d'étapes de distillation et d'un lavage final dans une colonne d'absorption de seulement une petite partie du gaz combustible extrait.
PCT/EP2013/072212 2012-10-24 2013-10-23 Procédé pour la récupération de molécules légères à partir d'un courant d'alimentation oléfinique WO2014064172A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP12189661 2012-10-24
EP12189661.7 2012-10-24

Publications (2)

Publication Number Publication Date
WO2014064172A2 true WO2014064172A2 (fr) 2014-05-01
WO2014064172A3 WO2014064172A3 (fr) 2015-11-26

Family

ID=47137579

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2013/072212 WO2014064172A2 (fr) 2012-10-24 2013-10-23 Procédé pour la récupération de molécules légères à partir d'un courant d'alimentation oléfinique

Country Status (1)

Country Link
WO (1) WO2014064172A2 (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3029402A1 (fr) * 2014-12-05 2016-06-08 Linde Aktiengesellschaft Procédé et système de traitement technique de séparation d'un courant de charge
EP3136028A1 (fr) 2015-08-28 2017-03-01 Linde Aktiengesellschaft Procede et installation de traitement technique de separation d'un melange de depart
DE102016200561A1 (de) 2016-01-18 2017-07-20 Linde Aktiengesellschaft Prozess zur Gewinnung von Ethylen aus Methan
DE102016200565A1 (de) 2016-01-18 2017-07-20 Linde Aktiengesellschaft Verfahren zur trenntechnischen Bearbeitung eines Gasgemischs
CN107285981A (zh) * 2016-03-31 2017-10-24 中国石化工程建设有限公司 一种脱甲烷塔换热系统及换热方法
WO2018211036A1 (fr) * 2017-05-18 2018-11-22 Technip France Procédé de récupération d'un courant d'hydrocarbures en c2+ dans un gaz résiduel de raffinerie et installation associée
TWI737680B (zh) * 2016-02-19 2021-09-01 德商林德股份有限公司 用於獲得超臨界狀態的乙烯產物的方法和裝置
CN114470812A (zh) * 2021-12-28 2022-05-13 万华化学集团股份有限公司 Tdi回收液中焦油粉末的分离装置及方法

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3220998A1 (de) * 1982-06-03 1983-12-08 Linde Ag, 6200 Wiesbaden Verfahren zur herstellung von niedermolekularen olefinen
US7294749B2 (en) * 2004-07-02 2007-11-13 Kellogg Brown & Root Llc Low pressure olefin recovery process
JP2009502915A (ja) * 2005-07-28 2009-01-29 イネオス ユーエスエイ リミテッド ライアビリティ カンパニー 自己熱分解反応装置流出物からエチレンを回収する方法
EP2212269B1 (fr) * 2007-10-01 2013-07-03 Lummus Technology Inc. Séparation de courants d'oléfines
EP2303807B1 (fr) * 2008-06-25 2019-08-07 Total Research & Technology Feluy Procédé pour la fabrication d'oléfines à partir de composés oxygénés
FR2957931B1 (fr) * 2010-03-29 2012-05-04 Technip France Procede de traitement d'un courant de gaz craque issu d'une installation de pyrolyse d'hydrocarbures et installation associee.

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3029402A1 (fr) * 2014-12-05 2016-06-08 Linde Aktiengesellschaft Procédé et système de traitement technique de séparation d'un courant de charge
EP3136028A1 (fr) 2015-08-28 2017-03-01 Linde Aktiengesellschaft Procede et installation de traitement technique de separation d'un melange de depart
DE102016200561A1 (de) 2016-01-18 2017-07-20 Linde Aktiengesellschaft Prozess zur Gewinnung von Ethylen aus Methan
DE102016200565A1 (de) 2016-01-18 2017-07-20 Linde Aktiengesellschaft Verfahren zur trenntechnischen Bearbeitung eines Gasgemischs
WO2017125432A1 (fr) 2016-01-18 2017-07-27 Linde Aktiengesellschaft Processus de production d'éthylène à partir de méthane
WO2017125438A1 (fr) 2016-01-18 2017-07-27 Linde Aktiengesellschaft Procédé de traitement par séparation d'un mélange gazeux
TWI737680B (zh) * 2016-02-19 2021-09-01 德商林德股份有限公司 用於獲得超臨界狀態的乙烯產物的方法和裝置
CN107285981B (zh) * 2016-03-31 2020-08-04 中国石化工程建设有限公司 一种脱甲烷塔换热系统及换热方法
CN107285981A (zh) * 2016-03-31 2017-10-24 中国石化工程建设有限公司 一种脱甲烷塔换热系统及换热方法
FR3066491A1 (fr) * 2017-05-18 2018-11-23 Technip France Procede de recuperation d'un courant d'hydrocarbures en c2+ dans un gaz residuel de raffinerie et installation associee
CN110799478A (zh) * 2017-05-18 2020-02-14 泰克尼普法国公司 回收炼油残余气体中c2+烃流的方法和相关设备
WO2018211036A1 (fr) * 2017-05-18 2018-11-22 Technip France Procédé de récupération d'un courant d'hydrocarbures en c2+ dans un gaz résiduel de raffinerie et installation associée
RU2764176C2 (ru) * 2017-05-18 2022-01-14 Текнип Франс Способ извлечения потока с2+ углеводородов, содержащихся в нефтезаводском остаточном газе, и установка для его осуществления
CN110799478B (zh) * 2017-05-18 2022-12-06 泰克尼普法国公司 回收炼油残余气体中c2+烃流的方法和相关设备
US11629108B2 (en) 2017-05-18 2023-04-18 Technip Energies France Method for recovering a stream of C2+ hydrocarbons in a residual refinery gas and associated installation
CN114470812A (zh) * 2021-12-28 2022-05-13 万华化学集团股份有限公司 Tdi回收液中焦油粉末的分离装置及方法

Also Published As

Publication number Publication date
WO2014064172A3 (fr) 2015-11-26

Similar Documents

Publication Publication Date Title
WO2014064172A2 (fr) Procédé pour la récupération de molécules légères à partir d'un courant d'alimentation oléfinique
US10011541B2 (en) Recovery of ethylene from methanol to olefins process
US11255604B2 (en) Process for removing light components from an ethylene stream
CA2724146C (fr) Demethaniseur absorbeur utilisable pour la conversion du methanol en olefines
US8952211B2 (en) Absorber demethanizer for FCC process
US20130178683A1 (en) Process for removing oxygenated contaminants from an hydrocarbonstream
EP2736862A1 (fr) Procédé pour éliminer des contaminants oxygénés d'un flux d'éthylène
EP2729433B1 (fr) Procédé de production d'oléfines avec système de transfert de chaleur de l'unité de craquage à la vapeur à l'unité de déhydrogénation d'alcools.
US20130172655A1 (en) Process for removing oxygenated contaminants from an hydrocarbon stream
KR101971616B1 (ko) 약한 열 분해로부터 탄화수소의 분리 시퀀스
WO2017179009A1 (fr) Séparation de gaz d'échappement d'hydrocarbures c3 dans un procédé de déshydrogénation de propane
US10766836B2 (en) Methods and systems for separating olefins
CN112707786B (zh) 一种裂解气分离系统及分离方法
CN110156557B (zh) 一种石油化工产出气体的回收方法
CN112707787A (zh) 一种带净化的裂解气分离系统及利用方法
US20220064083A1 (en) Integrated process for producing acetylene
JP2017508038A (ja) オレフィンの製造方法
WO2007018509A1 (fr) Processus de fractionnement cryogénique
WO2018051214A1 (fr) Récupération et purification d'éthylène
CN112723974A (zh) 一种降低能耗的裂解气分离系统及分离方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 13782707

Country of ref document: EP

Kind code of ref document: A2

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 13782707

Country of ref document: EP

Kind code of ref document: A2