WO2017021003A1 - Verfahren zum abtrennen von kohlendioxid aus einer kohlenwasserstoff-reichen fraktion - Google Patents
Verfahren zum abtrennen von kohlendioxid aus einer kohlenwasserstoff-reichen fraktion Download PDFInfo
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- WO2017021003A1 WO2017021003A1 PCT/EP2016/001330 EP2016001330W WO2017021003A1 WO 2017021003 A1 WO2017021003 A1 WO 2017021003A1 EP 2016001330 W EP2016001330 W EP 2016001330W WO 2017021003 A1 WO2017021003 A1 WO 2017021003A1
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- 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
- F25J3/0209—Natural gas or substitute natural gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
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- 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
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- 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
- F25J3/0266—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 carbon dioxide
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
- B01D2256/245—Methane
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2259/00—Type of treatment
- B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/06—Heat exchange, direct or indirect
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/46—Compressors or pumps
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/48—Expanders, e.g. throttles or flash tanks
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/545—Washing, scrubbing, stripping, scavenging for separating fractions, components or impurities during preparation or upgrading of a fuel
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/548—Membrane- or permeation-treatment for separating fractions, components or impurities during preparation or upgrading of a fuel
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- 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
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- 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
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- F25J2205/00—Processes or apparatus using other separation and/or other processing means
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- F25J2205/80—Processes or apparatus using other separation and/or other processing means using membrane, i.e. including a permeation step
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
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- 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
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- 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
- F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
- F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
Definitions
- the invention relates to a method for separating a C0 2 -rich liquid fraction from a hydrocarbon-rich, C0 2 -containing gas fraction.
- Natural gas and associated gases contain acid gases - mainly C0 2 , in addition H 2 S and other sulfur compounds, such as COS and mercaptans - in various concentrations; these sour gases are usually removed by washing (eg.
- membranes preferably polymer membranes, used to reduce the C0 2 content of the feed gas before amine washing to about 2 to 10 mol%, so that they can be optimally operated again.
- Cryogenic decomposition is basically suitable for solving this problem.
- Object of the present invention is to provide a generic method for separating a C0 2 -rich liquid fraction from a hydrocarbon-rich gas fraction, which makes it possible C0 2 in technically pure form - here below is a C0 2 -rich fraction having a C0 2 Content of at least 98 mol%, to be understood - and in the liquid state from a hydrocarbon-rich
- the hydrocarbon-rich, C0 2 -containing gas fraction is permeatively separated into a C0 2 -arm gas fraction and a C0 2 -rich gas fraction, b) the C0 2 -rich gas fraction to a pressure which is at least 10% above the critical pressure the C0 2 -rich gas fraction is compressed,
- the relaxed C0 2 -rich fraction is separated by means of a stripping process into a C0 2 -depleted gas fraction and a C ⁇ 2 -rich liquid fraction, and
- Hydrocarbon-rich, C0 2 -containing gas fraction is supplied.
- Separation of a C0 2 -rich liquid fraction from a hydrocarbon-rich, C0 2 -containing gas fraction are characterized in that the stripping process is operated such 'that the C0 2 liquid fraction rich in a C0 2 content of at least 98 mol%, preferably at least 99.5 mol%, the hydrocarbon-rich, C0 2 -containing gas fraction 10-85 Mol% C0 2 , preferably between 25 and 60 mol% C0 2 , the C0 2 -arm gas fraction contains at most 15 mol% C0 2 , preferably at most 10 mol% GQ 2 ⁇ - for the permeative separation (process step a) used membrane has a selectivity between C0 2 and CH 4 of at least 2, preferably at least 3, in the permeative separation (step a), the pressure on the permeate side by a factor of 4 to 10, preferably 5 to 8 lower than the pressure on the feed side, provided that the compression of the C0 2 -rich gas fraction takes place at least
- the hydrocarbon-rich, C0 2 -containing gas fraction having a C0 2 content between 10 and 85 mol% and which under a pressure of 30 to 70 bar, preferably 40 to 60 bar is present, if necessary, first fed to a pretreatment in which C 5+ hydrocarbons and water are separated. If desired, these components can be dispensed together with the retentate to be described later.
- a pretreatment in which C 5+ hydrocarbons and water are separated. If desired, these components can be dispensed together with the retentate to be described later.
- Hydrocarbon-rich gas fraction is permeatively separated into a C0 2 -arm gas fraction (retentate) and a C0 2 -rich gas fraction (permeate).
- This separation is preferably carried out by means of a polymer membrane.
- This advantageously has a selectivity between C0 2 and CH 4 of at least 2, preferably at least 3. Furthermore, the pressure on the permeate side is a factor of 4 to 10,
- the C0 2 -rich gas fraction is compressed to a pressure which is at least 10% above the critical pressure of this C0 2 -rich gas fraction.
- the compression of the C0 2 -rich gas fraction takes place in two or more stages.
- compressed C0 2 -rich gas fraction is preferably interim or post-cooled against cooling water and / or air.
- the compressed C0 2 -rich gas fraction is cooled by means of a suitable refrigeration system and then relaxed. Here it is cooled to a temperature at which the formation of a solid, C0 2 -rich phase can be safely avoided after the relaxation; As a rule, a cooling takes place to a temperature which is at least 5 ° C, preferably
- the relaxed C0 2 -rich fraction is separated by means of a stripping process into a C0 2 -depleted gas fraction and a C0 2 -rich liquid fraction. Since the liquid content of the relaxed C0 2 -rich fraction usually too rich
- Hydrocarbons, in particular of methane is, in order to meet the requirements for the C0 2 - purity, the C0 2 - rich fraction fed to the stripping process or stripping column is purged of methane by boiling until the C0 withdrawn from the bottom of the stripping column 2 -rich liquid fraction - which represents the product stream - having the desired composition.
- this C0 2 -rich liquid fraction has a C0 2 content of at least 98 mol%, preferably at least 99.5 mol%.
- the pressure of the stripping process is advantageously selected such that the bottom temperature is at least 10 ° C., preferably at least 15 ° C is below the process temperature achievable during the intercooling of the C0 2 - rich gas fraction; As a rule, a pressure between 30 and 60 bar is therefore chosen.
- Stripping column evaporating methane used at least partially to the
- the C0 2 -depleted gas fraction obtained at the top of the stripping column is fed to the hydrocarbon-rich gas fraction to be separated permeatively.
- the C0 2 -depleted gas fraction is preheated to ambient temperature. Normally, no additional compression is required before admixture.
- the hydrocarbon-rich, C0 2 -containing gas fraction 1 which has a C0 2 content between 10 and 85 mol% and is usually present under a pressure of 30 to 70 bar, is a pretreatment P, shown only in the black box the C 5+ hydrocarbons and / or water are separated, fed. If a separation of C 5+ hydrocarbons and / or water is not required, this pre-treatment P can be omitted.
- the optionally pretreated hydrocarbon-rich gas fraction 1 ' is now separated permeatively M into a low-C0 2 gas fraction 2 and a ⁇ C0 2 -rich gas fraction 3. This separation is preferably carried out by means of a polymer membrane.
- the C0 2 -rich gas fraction 3 is compressed in the compressor stages C1, C2 and C3 to a pressure which is at least 10% above the critical pressure of the CQ 2 -rich gas fraction.
- the intercooling of the Intermediate pressures of compressed C0 2 -rich gas fraction 4 and 5 takes place in the
- the compressed in the compressor C3 to the desired final pressure C0 2 -rich gas fraction 6 is in
- Heat exchanger E5 cooled against cooling water or air.
- the compressed C0 2 - rich gas fraction 6 is in the heat exchanger E6 against a suitable refrigeration system R, which is shown in Figure 1 only as a black box, cooled; this is the
- Refrigeration system R is coupled via the refrigeration circuit 12 to the heat exchanger E6. Subsequently, the cooled C0 2 -rich gas fraction 6 is expanded in the valve V1 and fed to the top of the stripping column T1.
- the compressed C0 2 -rich gas fraction 6 is cooled down to a temperature in the heat exchanger E6, _ beräer after the relaxation in the valve V1, the formation of a solid, C0 2 -rich phase can be safely avoided. For this reason, it is cooled down to a temperature which is at least 5 ° C, preferably at least 10 ° C above the fixed point of carbon dioxide.
- the T1 of the stripping column supplied C0 2 -rich fraction is separated C0 2 -depleted gas fraction 7 and a C0 2 -rich liquid fraction 8 in a.
- the latter is delivered via the control valve V2. Since the liquid fraction of the relaxed C0 2 -rich fraction is generally too rich in hydrocarbons, in particular methane, to meet the requirements for the C0 2 purity of the C0 2 -rich liquid fraction 8, the C0 2 fed to the stripping column is rich fraction by boiling so far from methane purified until the C0 2 liquid fraction 8 has the desired purity, ie a C0 2 content of at least 98 mol%, preferably at least 99.5 mol%.
- Partial stream 9 is heated in the heat exchangers E2 and E4 against the compressed and cooled C0 2 -rich gas fraction, at least partially vaporized and fed together with the warmed in the refrigeration system R and at least partially vaporized substream 9 'of the stripping column T1 as a stripping vapor.
- the pressure within the stripping column T1 is selected so that its bottom temperature is at least 10 ° C, preferably at least 15 ° C below the process temperature, which can be achieved in the intermediate cooling of the compressed C0 2 -rich gas fraction in the heat exchangers E1 and E3 is. Therefore, the pressure within the stripping column T1 is usually 30 to 60 bar. through This procedure, the cooling capacity of the stripping column T1
- vaporizing methane are at least partially used to the
- FIGS. 2 to 4 show three different embodiments of the refrigeration system R, which is shown in FIG. 1 only as a black box, and serves to cool the compressed CO 2 -rich gas fraction 6.
- Heat exchanger E2 deducted, increased by an additional compressor C4 in the pressure and then in the heat exchanger E7 against cooling water or air and in the
- Liquid fraction 8 cooled. Subsequently, the cooled partial flow 21 in a expansion turbine X1, which is coupled to the above-described compressor C4, work expanded; the mechanical power of the expansion turbine X1 is used to drive the compressor C4. If necessary, this relaxation can also be carried out in several stages, possibly with an intermediate heating.
- the additional heat exchanger E8 is analogous to the heat exchangers E2 and E4 to the,
- the heat exchanger system E6 shown in FIG. 1 is divided into two heat exchangers E6 and E6 'arranged in parallel with the aim of optimizing the use of so-called wound heat exchangers. While the cooled C0 2 -rich gas fraction 6 is guided on the tube side due to their comparatively high pressure, the cold streams 7 and 21 are guided on the shell side. The warmed in the heat exchanger E6 ', as a refrigerant used partial stream 22 is the C0 2 -rich gas fraction 3 mixed before their compression.
- Hydrocarbons from the group C to C 5 (methane, ethylene, ethane, propylene, propane, butane and pentane) consists.
- the compressed in the compressor C4 refrigerant 31 is completely condensed in the heat exchangers E7 and E8 against cooling water or air or against the partial flow 9 of the C0 2 -rich liquid fraction 8.
- the container D1 serves to store liquid refrigerant to enable various operating conditions.
- the withdrawn from the container D1 refrigerant mixture 32 is in the heat exchanger E6 'subcooled, relaxed in the expansion valve V3, at
- the cooling of the compressed C0 2 -rich gas fraction 6 by means of a pure refrigerant is carried out on at least two pressure stages in the heat exchangers E6 'and E6 " the refrigerant 43 withdrawn from the container D1 is first fed to the heat exchanger E6 'via the expansion valve V3, a portion of the refrigerant is vaporized therein and fed via line 40 to the intermediate stage of the compressor C4, while the remaining refrigerant partial stream is fed via the control valve V4 into the heat exchanger E6 " is relaxed.
- the refrigerants for such a refrigerant refrigeration cycle are all substances that can be liquefied at ambient temperature, including but not limited to propane, propylene, R22, R134a and at low ambient temperatures also ethane as well as carbon dioxide.
- the inventive method for separating a C0 2 -rich liquid fraction from a hydrocarbon-rich, C0 2 -containing gas fraction allows liquid C0 2 in technically pure form, ie with a C0 2 content of at least 98 mol%, from a raw gas with a wide range of C0 2 concentration to separate.
- the C0 2 content of C0 2 low-gas fraction can be reduced to less than 10 mol%.
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Carbon And Carbon Compounds (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
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BR112018001717-5A BR112018001717B1 (pt) | 2015-08-04 | 2016-08-02 | Processo para separar dióxido de carbono de uma fração rica em hidrocarboneto |
AU2016304194A AU2016304194B2 (en) | 2015-08-04 | 2016-08-02 | Method for separating carbon dioxide from a hydrocarbon-rich fraction |
MYPI2018700384A MY194111A (en) | 2015-08-04 | 2016-08-02 | Method for separating carbon dioxide from a hydrocarbon-rich fraction |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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DE102015010164.1A DE102015010164A1 (de) | 2015-08-04 | 2015-08-04 | Verfahren zum Abtrennen von Kohlendioxid aus einer Kohlenwasserstoff-reichen Fraktion |
DE102015010164.1 | 2015-08-04 |
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WO2017021003A1 true WO2017021003A1 (de) | 2017-02-09 |
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PCT/EP2016/001330 WO2017021003A1 (de) | 2015-08-04 | 2016-08-02 | Verfahren zum abtrennen von kohlendioxid aus einer kohlenwasserstoff-reichen fraktion |
Country Status (4)
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AU (1) | AU2016304194B2 (de) |
DE (1) | DE102015010164A1 (de) |
MY (1) | MY194111A (de) |
WO (1) | WO2017021003A1 (de) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2021062397A1 (en) * | 2019-09-27 | 2021-04-01 | Wm Intellectual Property Holdings, L.L.C. | System and process for recovering methane and carbon dioxide from biogas and reducing greenhouse gas emissions |
Families Citing this family (1)
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EP4186583A1 (de) * | 2021-11-24 | 2023-05-31 | Linde GmbH | Verfahren und vorrichtung zur abtrennung von kohlendioxid aus einem kohlendioxidhaltigen zustrom |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5414190A (en) | 1992-11-06 | 1995-05-09 | Linde Aktiengesellschaft | Process to recover liquid methane |
US6301927B1 (en) * | 1998-01-08 | 2001-10-16 | Satish Reddy | Autorefrigeration separation of carbon dioxide |
US20050092594A1 (en) | 2003-10-30 | 2005-05-05 | Parro David L. | Membrane/distillation method and system for extracting CO2 from hydrocarbon gas |
FR2928720A1 (fr) * | 2008-03-13 | 2009-09-18 | Inst Francais Du Petrole | Procede de pretraitement d'un gaz naturel pour retirer le dioxyde de carbone |
US20110296867A1 (en) * | 2010-06-03 | 2011-12-08 | Ortloff Engineers, Ltd. | Hydrocarbon Gas Processing |
US20120111051A1 (en) * | 2010-10-06 | 2012-05-10 | L'air Liquide Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude | Carbon Dioxide Removal Process |
US20150013380A1 (en) * | 2013-07-11 | 2015-01-15 | Linde Aktiengesellschaft | Method for separating off acid gases from natural gas |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4639257A (en) * | 1983-12-16 | 1987-01-27 | Costain Petrocarbon Limited | Recovery of carbon dioxide from gas mixture |
JP5891848B2 (ja) * | 2012-02-27 | 2016-03-23 | ウシオ電機株式会社 | ガラス基板もしくは水晶基板からなるワークの貼り合わせ方法および装置 |
-
2015
- 2015-08-04 DE DE102015010164.1A patent/DE102015010164A1/de not_active Withdrawn
-
2016
- 2016-08-02 AU AU2016304194A patent/AU2016304194B2/en active Active
- 2016-08-02 MY MYPI2018700384A patent/MY194111A/en unknown
- 2016-08-02 WO PCT/EP2016/001330 patent/WO2017021003A1/de active Application Filing
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5414190A (en) | 1992-11-06 | 1995-05-09 | Linde Aktiengesellschaft | Process to recover liquid methane |
US6301927B1 (en) * | 1998-01-08 | 2001-10-16 | Satish Reddy | Autorefrigeration separation of carbon dioxide |
US20050092594A1 (en) | 2003-10-30 | 2005-05-05 | Parro David L. | Membrane/distillation method and system for extracting CO2 from hydrocarbon gas |
FR2928720A1 (fr) * | 2008-03-13 | 2009-09-18 | Inst Francais Du Petrole | Procede de pretraitement d'un gaz naturel pour retirer le dioxyde de carbone |
US20110296867A1 (en) * | 2010-06-03 | 2011-12-08 | Ortloff Engineers, Ltd. | Hydrocarbon Gas Processing |
US20120111051A1 (en) * | 2010-10-06 | 2012-05-10 | L'air Liquide Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude | Carbon Dioxide Removal Process |
US20150013380A1 (en) * | 2013-07-11 | 2015-01-15 | Linde Aktiengesellschaft | Method for separating off acid gases from natural gas |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2021062397A1 (en) * | 2019-09-27 | 2021-04-01 | Wm Intellectual Property Holdings, L.L.C. | System and process for recovering methane and carbon dioxide from biogas and reducing greenhouse gas emissions |
US10968151B1 (en) | 2019-09-27 | 2021-04-06 | Wm Intellectual Property Holdings, L.L.C. | System and process for recovering methane and carbon dioxide from biogas and reducing greenhouse gas emissions |
US11220470B2 (en) | 2019-09-27 | 2022-01-11 | Wm Intellectual Property Holdings, L.L.C. | System and process for recovering methane and carbon dioxide from biogas and reducing greenhouse gas emissions |
US11708313B2 (en) | 2019-09-27 | 2023-07-25 | Wm Intellectual Property Holdings, L.L.C. | System and process for recovering methane and carbon dioxide from biogas and reducing greenhouse gas emissions |
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Publication number | Publication date |
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MY194111A (en) | 2022-11-14 |
AU2016304194B2 (en) | 2021-10-28 |
AU2016304194A1 (en) | 2018-02-22 |
DE102015010164A1 (de) | 2017-02-09 |
BR112018001717A2 (pt) | 2018-09-18 |
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