WO2013100304A1 - 이산화탄소의 처리 모듈 및 그 처리 방법 - Google Patents
이산화탄소의 처리 모듈 및 그 처리 방법 Download PDFInfo
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- WO2013100304A1 WO2013100304A1 PCT/KR2012/006660 KR2012006660W WO2013100304A1 WO 2013100304 A1 WO2013100304 A1 WO 2013100304A1 KR 2012006660 W KR2012006660 W KR 2012006660W WO 2013100304 A1 WO2013100304 A1 WO 2013100304A1
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- carbon dioxide
- gas
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- discharged
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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
- F25J3/0228—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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- 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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- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0027—Oxides of carbon, e.g. CO2
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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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- 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
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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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
- 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
- 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
- F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
- F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/02—Internal refrigeration with liquid vaporising loop
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/08—Internal refrigeration by flash gas recovery loop
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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
- F25J2280/00—Control of the process or apparatus
- F25J2280/40—Control of freezing of components
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
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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 present invention relates to a carbon dioxide treatment module and a method of operating the carbon dioxide, and more particularly, can be supplied at a temperature and state conditions suitable for the demand of cryogenic liquid carbon dioxide, such as for transporting ships, storing and collecting carbon dioxide, or promoting oil recovery.
- the present invention relates to a treatment module for carbon dioxide and a treatment method thereof.
- Natural gas can be divided into sweet gas, which contains high methane, carbon dioxide and hydrogen sulfide, and sour gas, which is corrosive and toxic.In recent years, the number of gas wells capable of producing sweet gas has gradually decreased. It is a trend.
- the present invention has been invented to improve the above problems, the carbon dioxide of the carbon dioxide to be supplied at a temperature and state conditions suitable for the demand of cryogenic liquid carbon dioxide, such as for the transport of ships, storage and capture of carbon dioxide, or oil recovery promotion. It is to provide a processing module and a processing method thereof.
- the present invention discharges methane in the upper side, a controlled freezing zone (CFZ) is formed in the middle, and generated from a stranded gas well in the lower side.
- a separation unit for discharging carbon dioxide contained in sour gas a gas-liquid separator connected to the separation unit to separate carbon dioxide into gas and liquid, and a liquid carbon dioxide mounted between the separation unit and the gas-liquid separator and discharged from the separation unit It is possible to provide a processing module for carbon dioxide, comprising an expansion valve for expanding the pressure reduction by throttling.
- the inlet side temperature of the expansion valve is preferably higher than the gas outlet side and liquid outlet side temperatures of the gas-liquid separator.
- the gas-liquid separator discharges gaseous carbon dioxide upward and discharges liquid carbon dioxide downward.
- the gas-liquid separator is equipped with a liquid discharge pipe for discharging liquid carbon dioxide to a saturated liquid state at -55 ° C. to -20 ° C. to the lower side, and is mounted at the end of the liquid discharge pipe so that the ship transport or carbon dioxide capture and storage (CCS) is carried out. It is preferable to further include a flow control valve for controlling the supply amount of the liquid carbon dioxide supplied for) or for enhanced oil recovery (EOR).
- the gas-liquid separator further includes a gas discharge pipe for discharging the gas carbon dioxide upwards, and a pressure control valve mounted on the gas discharge pipe.
- the present invention is a separation unit for separating and discharging carbon dioxide from the sour gas generated in the limit gas well, an expansion valve for throttling and expanding the liquid carbon dioxide supplied from the separation unit, the gas and liquid two-phase of the carbon dioxide passed through the expansion valve
- a process module for carbon dioxide may be provided that includes a gas-liquid separator that separates gas and liquid carbon dioxide from a two phase fluid.
- the present invention discharges methane in the upper side, a controlled freezing zone (CFZ) is formed in the middle, sour gas (sour gas) generated from the stranded gas well on the lower side
- a controlled freezing zone CTZ
- sour gas sour gas
- the further cooling is preferably accomplished by throttling and expanding the liquid carbon dioxide discharged from the separation unit.
- the additional cooling is achieved by throttling and expanding the liquid carbon dioxide discharged from the separation unit, and separating the axially reduced gas and liquid carbon dioxide two-phase fluid through a gas-liquid separator into gaseous carbon dioxide and liquid carbon dioxide. desirable.
- the present invention may provide a method for treating carbon dioxide, characterized in that the liquid carbon dioxide separated from the sour gas swelling under reduced pressure, and gas-liquid separation at low temperature to supply for ship transport or oil recovery enhancement.
- a method for treating carbon dioxide characterized in that the liquid carbon dioxide separated from the sour gas swelling under reduced pressure, and gas-liquid separation at low temperature to supply for ship transport or oil recovery enhancement.
- the separation unit for discharging the methane in the upper side, the controlled freezing zone (CFZ) is formed in the middle, the carbon dioxide contained in the sour gas in the lower side; And cooling the liquid carbon dioxide discharged from the separation unit by using the methane discharged from the separation unit as a refrigerant, and providing a processing module for carbon dioxide, characterized in that it comprises a heat exchanger mounted on a pipe from which the liquid carbon dioxide is discharged from the separation unit. Can be.
- a pressure reducing valve on the pipe interconnecting the separation unit and the heat exchanger to reduce the pressure to a pressure suitable for ship transportation.
- the pressure reducing valve may be installed on the heat exchanger outlet side pipe.
- the liquid carbon dioxide passed through the heat exchanger and the pressure reducing valve may be shipped to the vessel and transported for carbon dioxide capture and storage (CCS) or enhanced oil recovery (EOR).
- CCS carbon dioxide capture and storage
- EOR enhanced oil recovery
- the present invention is a refrigerant to the methane discharged from the separation unit to the heat exchanger mounted on the pipe forming a flow path of the liquid carbon dioxide discharged from the separation unit for separating and discharging the carbon dioxide from the sour gas produced in the stranded gas well It is possible to provide a processing module for carbon dioxide, characterized in that for cooling the liquid carbon dioxide passing through the heat exchanger.
- the present invention is characterized by cooling the liquid carbon dioxide by passing the methane generated from the limit gas well as a refrigerant through the liquid carbon dioxide separated from the sour gas produced in the stranded gas well (sour gas) as a refrigerant. It is also possible to provide a treatment method.
- the present invention also provides a first step of supplying sour gas to a separation unit that is connected to a stranded gas well and forms a controlled freezing zone (CFZ) and sour gas. Distilling from the separation unit to discharge methane to the upper side of the separation unit and liquid carbon dioxide to the lower side of the separation unit; and passing the methane as a refrigerant through a heat exchanger mounted on the liquid carbon dioxide discharge pipe of the separation unit.
- CCS carbon dioxide capture and storage
- EOR enhanced oil recovery
- it may also provide a method for treating carbon dioxide, comprising the fourth step.
- the second step preferably further includes the step of depressurizing the liquid carbon dioxide discharged from the separation unit via a pressure reducing valve mounted between the separation unit and the heat exchanger or on the pipe at the outlet side of the heat exchanger.
- the present invention discharges methane in the upper side, a controlled freezing zone (CFZ) is formed in the middle, sour gas generated from the strandes gas well in the lower side
- a separation unit for discharging the included carbon dioxide A heat exchanger cooling the liquid carbon dioxide discharged from the separation unit using methane discharged from the separation unit as a refrigerant, and mounted on a pipe through which liquid carbon dioxide is discharged from the separation unit; And a gas-liquid separator connected to the heat exchanger to separate carbon dioxide into a gas and a saturated liquid state at -55 ° C to -20 ° C.
- the gas-liquid separator discharges gaseous carbon dioxide to the upper side, and discharges liquid carbon dioxide to the lower side.
- an expansion valve is mounted on the pipe connecting the separation unit and the heat exchanger or on the pipe at the outlet side of the heat exchanger.
- the present invention also provides a first step of supplying sour gas to a separation unit that is connected to a stranded gas well and forms a controlled freezing zone; A second step of cooling the methane as a refrigerant through a heat exchanger mounted on a pipe for discharging liquid carbon dioxide of the separation unit; A third step of separating heat-cooled liquid carbon dioxide into a gas and a liquid through a gas-liquid separator connected to the heat exchanger; And a fourth step of shipping the liquid carbon dioxide having passed through the gas-liquid separator to the vessel and transporting the carbon dioxide for carbon dioxide capture and storage (CCS) or enhanced oil recovery (EOR).
- CCS carbon dioxide capture and storage
- EOR enhanced oil recovery
- the present invention is equipped with an expansion valve between the separation unit and the gas-liquid separator to axially decompress and expand the liquid carbon dioxide discharged from the separation unit by low temperature separation into gaseous carbon dioxide and liquid carbon dioxide to transport liquid carbon dioxide for CCS or to sell for EOR You could do it.
- the present invention significantly reduces the cooling load of liquid carbon dioxide by distilling the sour gas produced from the limit gas well in a separation module forming a controlled freezing region, and using methane discharged as a refrigerant. May be shipped for CCS or sold for EOR.
- the present invention when there is no carbon dioxide storage in the vicinity when processing a large amount of carbon dioxide generated as a by-product when producing natural gas using CFZ technology in the existing limit gas well without a carbon dioxide treatment facility, it is transported to a ship The cost required to construct and construct a treatment facility for liquefaction for transportation can be greatly reduced, which is economically efficient.
- the present invention can significantly reduce the amount of gaseous carbon dioxide generated from the separation module that forms the installed and constructed controlled freezing zone (CFZ) and is released into the atmosphere, thereby being environmentally friendly and further strengthening in the future. It will also comply with the expected CO2 emission standards.
- FIG. 1 is a conceptual diagram showing a processing module of carbon dioxide according to an embodiment of the present invention
- FIG. 2 is a block diagram showing a method of treating carbon dioxide according to an embodiment of the present invention.
- FIG. 3 is a conceptual diagram showing a processing module of carbon dioxide according to another embodiment of the present invention.
- FIG. 4 is a block diagram showing a method of treating carbon dioxide according to another embodiment of the present invention.
- FIG. 5 is a conceptual diagram showing a processing module of carbon dioxide according to another embodiment of the present invention.
- FIG. 6 is a block diagram showing a method of treating carbon dioxide according to another embodiment of the present invention.
- FIG. 1 is a conceptual diagram showing an additional cooling module of carbon dioxide according to an embodiment of the present invention.
- the separation unit 100 for separating and discharging carbon dioxide from the sour gas generated in the stranded gas well 900 and the expansion of the liquid carbon dioxide supplied from the separation unit 100 by axial expansion under reduced pressure.
- the structure includes a valve 200 and a gas-liquid separator 300 that separates gas and liquid carbon dioxide from the gas and liquid two-phase fluid of carbon dioxide passing through the expansion valve 200.
- the separation unit 100 discharges methane (CH4, sweet gas) to the upper side, and a controlled freezing zone (CFZ) is formed in the middle, and the limit gas well ( Carbon dioxide contained in the sour gas generated from 900 is to be discharged.
- methane CH4, sweet gas
- CFZ controlled freezing zone
- the separation unit 100 distills and separates each component such as carbon dioxide, hydrogen sulfide, and methane contained in the sour gas generated from the limit gas well.
- the separation unit 100 has an upper side of the separation tank 110 as an upper distillation zone (UDS, Upper Distillation Sector) to discharge methane (CH4), and a lower side of the separation tank 110 as a lower distillation zone ( LDS, Lower Distillation Sector (CO2) is emitted.
- UDS Upper Distillation Sector
- LDS Lower Distillation Sector
- the separation tank 110 is connected to the limit gas well 900, and the sour gas supplied from the limit gas well 900 is cooled to a temperature suitable for distillation in the separation tank 110, and the limit gas well may be expanded under reduced pressure.
- Cooling 120 and gas expansion valve 130 are sequentially mounted on the pipe interconnecting the 900 and the separation tank 110, respectively, and is expanded under reduced pressure.
- the lower side of the separation tank 110 is equipped with a reheater 160 is heated to discharge the liquid carbon dioxide discharged to some of the separation tank 110 and the rest is discharged, the upper side of the separation tank 110, the condenser ( 140 is mounted to condense the sweet gas (CH4) in the heated sour gas vapor is accommodated in the temporary storage tank 150, and then supplied to the demand of natural gas through the gas discharge pipe (142).
- a reheater 160 is heated to discharge the liquid carbon dioxide discharged to some of the separation tank 110 and the rest is discharged
- the condenser ( 140 is mounted to condense the sweet gas (CH4) in the heated sour gas vapor is accommodated in the temporary storage tank 150, and then supplied to the demand of natural gas through the gas discharge pipe (142).
- the liquid gas in which carbon dioxide or the like is mixed is stored in the temporary storage tank 170, and the separation tank 110 is provided through the injection pipe 190 mounted at each end of the nozzle 180 through the pump 180. Injecting to the inside to reduce the load caused by the separation of the sweet gas (CH4).
- CH4 sweet gas
- the expansion valve 200 is connected to the separation unit 100, that is, the discharge tank 400 connected to the lower side of the separation tank 110 to discharge the liquid carbon dioxide, thereby cooling and cooling the liquid carbon dioxide while expanding under reduced pressure. Let's do it.
- Gas-liquid separator 300 is connected to the end of the discharge pipe 400 serves to separate carbon dioxide into gas and liquid.
- the inlet side temperature of the expansion valve 200 is about 1 to 5 ° C., usually about 2.2 ° C., and the gas outlet side and liquid outlet side temperatures of the gas-liquid separator 300 passing through the expansion valve 200 are approximately. -55 to -20 ° C.
- CCS carbon dioxide capture and storage
- EOR enhanced oil recovery
- the gas-liquid separator 300 discharges gaseous carbon dioxide to the upper side, and discharges liquid carbon dioxide to the lower side.
- the gas-liquid separator 300 may apply a structure including a liquid discharge pipe 310 for discharging liquid carbon dioxide downward and a flow control valve 320 mounted at an end of the liquid discharge pipe 310 as shown. There will be.
- the flow control valve 320 serves to control the amount of liquid carbon dioxide supplied for transport for carbon dioxide capture and storage (CCS) or for enhanced oil recovery (EOR). do.
- the gas-liquid separator 300 is mounted on the gas discharge pipe 330 and the gas discharge pipe 330 for discharging gas carbon dioxide to the upper side to discharge the gas carbon dioxide when the pressure inside the gas-liquid separator 300 is higher than the set pressure. It is preferable to further include a pressure control valve 340 to open and close.
- FIG. 2 is a block diagram illustrating a method of treating carbon dioxide according to an exemplary embodiment of the present invention, and reference numerals of the drawings not shown in FIG. 2 refer to FIG. 1.
- the present invention can be understood that the embodiment in which the liquid carbon dioxide separated from the sour gas is throttled and expanded under reduced pressure, and gas-liquid separation is carried out at low temperature to supply the vessel for transportation or oil recovery.
- the liquid carbon dioxide discharged from the separation unit 100 is further cooled to a low temperature to make and supply a temperature and pressure condition suitable for ship transportation.
- the additional cooling is achieved by throttling and expanding the liquid carbon dioxide discharged from the separation unit 100 while passing through the expansion valve 200.
- the additional cooling is achieved by passing the axially reduced gas and liquid carbon dioxide two-phase fluid through the gas-liquid separator 300 to separate gaseous carbon dioxide and liquid carbon dioxide.
- liquid carbon dioxide discharged from the separation unit 100 at a temperature of about 2.2 ° C. becomes liquid carbon dioxide at about ⁇ 55 to ⁇ 20 ° C. through the expansion valve 200 and the gas-liquid separator 300, and may be shipped to the carbon dioxide transport ship. have.
- FIG. 3 is a conceptual diagram illustrating a processing module of carbon dioxide according to another embodiment of the present invention.
- the present invention is mounted on the pipe 400 to form a flow path of the liquid carbon dioxide discharged from the separation unit 100 for separating and discharging carbon dioxide from the sour gas produced in the stranded gas well (900) as shown
- the heat exchanger 500 By passing the methane discharged from the separation unit 100 to the heat exchanger 500 as a refrigerant, it can be seen that the structure to cool the liquid carbon dioxide passing through the heat exchanger 500.
- the separation unit 100 discharges methane (CH4) on the upper side, and a controlled freezing zone (CFZ) is formed in the middle, and from the limit gas well 900 on the lower side. It emits carbon dioxide contained in the sour gas generated.
- CH4 methane
- CTZ controlled freezing zone
- the separation unit 100 distills and separates each component such as carbon dioxide, hydrogen sulfide, and methane contained in the sour gas generated from the limit gas well.
- the separation unit 100 has an upper side of the separation tank 110 as an upper distillation zone (UDS, Upper Distillation Sector) to discharge methane, and a lower side of the separation tank 110 as a lower distillation zone (LDS, Lower). It becomes a distillation sector and carbon dioxide is emitted.
- UDS Upper Distillation Sector
- LDS Lower distillation zone
- the separation tank 110 is connected to the limit gas well 900, and the sour gas supplied from the limit gas well 900 is cooled to a temperature suitable for distillation in the separation tank 110, and the limit gas well may be expanded under reduced pressure.
- Cooling 120 and gas expansion valve 130 are sequentially mounted on the pipe interconnecting the 900 and the separation tank 110, respectively, and is expanded under reduced pressure.
- the lower side of the separation tank 110 is equipped with a reheater 160 is heated to discharge the liquid carbon dioxide discharged to some of the separation tank 110 and the rest is discharged, the upper side of the separation tank 110, the condenser ( 140 is mounted and condensed methane in the heated sour gas vapor is accommodated in the temporary storage tank 150 and then supplied to the demand of natural gas through the gas discharge pipe 142.
- the liquid gas in which carbon dioxide or the like is mixed is stored in the temporary storage tank 170, and the separation tank 110 is provided through the injection pipe 190 mounted at each end of the nozzle 180 through the pump 180. Inward injection reduces the load due to methane separation.
- the heat exchanger 500 is mounted on the pipe 400 through which the liquid carbon dioxide is discharged from the separation unit 100, and is discharged from the separation unit 100 using methane discharged from the separation unit 100 as a refrigerant. It is for cooling liquid carbon dioxide.
- the above-described gas discharge pipe 142 communicates with the heat exchanger 500, and the liquid carbon dioxide flowing through the pipe 400 is supplied to the inside of the heat exchanger 500 through the gas discharge pipe 142. 90 to -80 ° C).
- the temperature at the inlet side of the heat exchanger 500 is about 1 to 5 ° C., usually about 2.2 ° C., and the temperature of the liquid carbon dioxide passing through the heat exchanger 500 is about ⁇ 55 to ⁇ 20 ° C.
- liquid carbon dioxide is cooled to a temperature suitable for ship transport and shipped to the ship and then transported for carbon dioxide capture and storage (CCS) or enhanced oil recovery (EOR).
- CCS carbon dioxide capture and storage
- EOR enhanced oil recovery
- the pressure reducing valve 600 is mounted on the pipe 400 connecting the separation unit 100 and the heat exchanger 500 or on the outlet pipe 400 of the heat exchanger 500.
- the pressure reducing valve 600 is connected to the separation unit 100, that is, the lower side of the separation tank 110, and is mounted on the pipe 400 through which the liquid carbon dioxide is discharged to lower the pressure of the liquid carbon dioxide to reduce the pressure to a pressure suitable for ship transportation. Can be.
- the liquid carbon dioxide separated through the separation unit 100 is in a high pressure state of about 37 bar, the liquid carbon dioxide may be decompressed to a saturation pressure of 5.5 bar to 19.7 bar at -55 degrees to -20 ° C through the pressure reducing valve 600.
- saturated carbon dioxide of -50 to -30 ° C is considered to be a carbon dioxide state suitable for ship transport, it is preferable to reduce the pressure to 6.8 bar ⁇ 14.3 bar through the pressure reducing valve 600.
- FIG. 4 is a block diagram illustrating a method of treating carbon dioxide according to an embodiment of the present invention, and reference numerals of the drawings not shown in FIG. 4 refer to FIG. 3.
- the present invention is applicable to the embodiment of cooling the liquid carbon dioxide by passing the methane generated from the limit gas well as a refrigerant through the liquid carbon dioxide separated from the sour gas generated from the stranded gas well (sour gas) as a refrigerant I can figure it out.
- the present invention is to further supply the liquid carbon dioxide discharged from the separation unit 100 to a low temperature to supply a state suitable for ship transport.
- methane production by distillation is carried out in a separation unit 100 connected to a stranded gas well and forming a controlled freezing zone (CFZ).
- a separation unit 100 connected to a stranded gas well and forming a controlled freezing zone (CFZ).
- CFZ controlled freezing zone
- sour gas sour gas
- the sour gas is distilled from the separation unit 100 to discharge methane above the separation unit 100 and to discharge liquid carbon dioxide below the separation unit 500.
- the heat exchanger 500 mounted on the liquid carbon dioxide discharge pipe 400 of the separation unit 100 is discharged through the gas discharge pipe 142 connected to the separation unit 100. Cooling is accomplished by passing methane through the refrigerant.
- the liquid carbon dioxide that has passed through the heat exchanger 500 is shipped to the vessel for carbon dioxide capture and storage (CCS) or enhanced oil recovery (EOR). This is done by transporting the goods to the site.
- CCS carbon dioxide capture and storage
- EOR enhanced oil recovery
- the liquid carbon dioxide is transported to the vessel via the pressure reducing valve 600 mounted between the separation unit 100 and the heat exchanger 500 or on the pipe 400 on the outlet side of the heat exchanger 500. It is preferable to further carry out the process of reducing the pressure to a pressure suitable for.
- the liquid carbon dioxide discharged from the separation unit 100 at a temperature of about 2.2 ° C is -55 to -20 ° C, more preferably -50 ° C to -30 ° C through the pressure reducing valve 600 and the heat exchanger 500. It can be internal and external liquid carbon dioxide and shipped to carbon dioxide carriers.
- the pressure is 5.5 bar to 19.7 bar, more preferably 14.3 bar of liquid carbon dioxide can be shipped to the carbon dioxide transport ship.
- FIG. 5 is a conceptual diagram illustrating a carbon dioxide treatment module according to another embodiment of the present invention.
- a separation unit 100 separating and discharging carbon dioxide from sour gas generated in a stranded gas well (900) and a pipe forming a flow path of liquid carbon dioxide discharged from the separation unit 100 is shown.
- a heat exchanger 500 mounted on the 400 and a gas-liquid separator 300 for separating gas and liquid carbon dioxide from a gas and a liquid two-phase fluid of carbon dioxide that have passed through the heat exchanger 500. You can see that it is a structure.
- the separation unit 100 discharges methane to the upper side, and a controlled freezing zone (CFZ) is formed in the middle, and is included in the sour gas generated from the limit gas well 900 at the lower side. To emit carbon dioxide.
- CFZ controlled freezing zone
- the separation unit 100 is substantially the same as the previous embodiment, and detailed description thereof will be omitted.
- the heat exchanger 500 cools liquid carbon dioxide discharged from the separation unit 100 using methane discharged from the separation unit 100 as a refrigerant, and is mounted on a pipe through which liquid carbon dioxide is discharged from the separation unit 100. .
- the gas discharge pipe 142 is connected to the heat exchanger 500, and the liquid carbon dioxide flowing in the pipe 400 is supplied to the inside of the heat exchanger 500 through the gas discharge pipe 142 (about ⁇ 90 ° C.). To about -80 ° C).
- the gas-liquid separator 300 is connected to the heat exchanger 500 to separate carbon dioxide into a gas and a saturated liquid state of ⁇ 55 ° C. to ⁇ 20 ° C., thereby discharging gaseous carbon dioxide upward and discharging liquid carbon dioxide downward. .
- the gas-liquid separator 300 is connected to the end of the discharge pipe 400 to separate carbon dioxide into gas and liquid.
- an expansion valve 200 is mounted on the pipe connecting the separation unit 100 and the heat exchanger 500 or on the pipe at the outlet side of the heat exchanger 500 to cool the liquid carbon dioxide while throttling and expanding the liquid carbon dioxide.
- the inlet side temperature of the expansion valve 200 is about 1 to 5 ° C, usually about 2.2 ° C, and the gas outlet side and liquid outlet side temperature of the gas-liquid separator 300 passing through the expansion valve 200 is approximately- 55 to -20 ° C.
- CCS carbon dioxide capture and storage
- EOR enhanced oil recovery
- FIG. 6 is a block diagram illustrating a method of treating carbon dioxide according to another embodiment of the present invention, and reference numerals not shown in FIG. 6 refer to FIG. 5.
- the present invention uses the methane generated from the bound gas well as a refrigerant, the carbon dioxide that is also separated and discharged from the limited gas well through the heat exchanger (500) to cool the refrigerant of the methane, the gas in the gas-liquid separator (300) And it can be seen that the embodiment of separating into a liquid can be applied.
- a sour gas is supplied to the separation unit 100 connected to a stranded gas well and forming a controlled freezing zone. The work is done.
- step (S2) is performed to pass the methane as a refrigerant to the heat exchanger 500 mounted on the liquid carbon dioxide discharge pipe of the separation unit 100 to cool.
- step (S3) is performed to separate the liquid carbon dioxide cooled by heat exchange into gas and liquid through the gas-liquid separator 300 connected to the heat exchanger 500.
- the liquid carbon dioxide that has passed through the gas-liquid separator 300 is shipped to the vessel and transported for carbon dioxide capture and storage (CCS) or enhanced oil recovery (EOR). Work is done.
- CCS carbon dioxide capture and storage
- EOR enhanced oil recovery
- liquid carbon dioxide discharged from the separation unit 100 at a temperature of about 2.2 ° C is -55 to -20 ° C through the pressure reducing valve 600 and the heat exchanger 500, more preferably at about -30 ° C liquid carbon dioxide Can be shipped to a carbon dioxide carrier.
- the pressure is 5.5 bar to 19.7 bar, more preferably 14.3 bar of liquid carbon dioxide can be shipped to the carbon dioxide transport ship.
- the present invention is a cryogenic liquid, such as for carbon dioxide storage and collection or oil recovery promotion. It can be seen that the basic technical idea is to provide a carbon dioxide treatment module and a method of treating the carbon dioxide that can be supplied at a temperature and state conditions suitable for the demand of carbon dioxide.
Abstract
Description
Claims (22)
- 상측으로는 메탄을 배출하고, 중간에는 제어된 동결 영역(Controlled Freezing Zone; CFZ)이 형성되며, 하측으로는 한계가스정(stranded gas well)로부터 발생하는 사워 가스(sour gas)에 포함된 이산화탄소를 배출하는 분리 유닛;상기 분리 유닛과 연결되어 상기 이산화탄소를 기체 및 액체로 분리하는 기액 분리기; 및상기 분리 유닛과 상기 기액 분리기 사이에 장착되어 상기 분리 유닛으로부터 배출되는 액체 이산화탄소를 교축(絞縮) 감압 팽창시키는 팽창밸브;를 포함하는 것을 특징으로 하는 액화 이산화탄소의 추가 냉각 모듈.
- 청구항 1에 있어서,상기 팽창밸브의 입구측 온도는 상기 기액 분리기의 기체 출구측 및 액체 출구측 온도보다 높은 것을 특징으로 하는 액화 이산화탄소의 추가 냉각 모듈.
- 청구항 1에 있어서,상기 기액 분리기는,상측으로 기체 이산화탄소를 배출시키고, 하측으로 액체 이산화탄소를 배출시키는 것을 특징으로 하는 액화 이산화탄소의 추가 냉각 모듈.
- 청구항 1에 있어서,상기 기액 분리기는,하측으로 액체 이산화탄소를 -55℃~-20℃의 포화 액체상태로 배출시키는 액체 배출관과,상기 액체 배출관의 단부에 장착되어 이산화탄소 포집 및 저장(Carbon dioxide Capture and Storage; CCS)용 또는 석유 회수증진(Enhanced Oil Recovery; EOR)용으로 운송하기 위한 상기 액체 이산화탄소의 공급량을 조절하는 유량 조절 밸브를 더 포함하는 것을 특징으로 하는 액화 이산화탄소의 추가 냉각 모듈.
- 청구항 1에 있어서,상기 기액 분리기는,상측으로 기체 이산화탄소를 배출시키는 기체 배출관과,상기 기체 배출관 상에 장착되는 압력제어 밸브를 더 포함하는 것을 특징으로 하는 액화 이산화탄소의 추가 냉각 모듈.
- 한계가스정에서 발생되는 사워 가스로부터 이산화탄소를 분리 배출하는 분리 유닛과, 상기 분리 유닛으로부터 공급받은 액체 이산화탄소를 교축 감압 팽창시키는 팽창 밸브와, 상기 팽창 밸브를 통과한 이산화탄소의 기체 및 액체 2상 유체(2phase fluid)로부터 기체 및 액체 이산화탄소를 분리하는 기액 분리기를 포함하는 것을 특징으로 하는 액화 이산화탄소의 추가 냉각 모듈.
- 상측으로는 메탄을 배출하고, 중간에는 제어된 동결 영역(Controlled Freezing Zone; CFZ)이 형성되며, 하측으로는 한계가스정(stranded gas well)로부터 발생하는 사워 가스(sour gas)에 포함된 이산화탄소를 배출하는 분리 유닛으로부터 생산되는 액체 이산화탄소를 -55℃~-20℃의 포화 액체상태 로 추가 냉각시켜 선박 운송용으로 공급하는 것을 특징으로 하는 액화 이산화탄소의 추가 냉각 방법.
- 청구항 7에 있어서,상기 추가 냉각은,상기 분리 유닛으로부터 배출되는 액체 이산화탄소를 교축 감압 팽창시켜 이루어지는 것을 특징으로 하는 액화 이산화탄소의 추가 냉각 방법.
- 청구항 7에 있어서,상기 추가 냉각은,상기 분리 유닛으로부터 배출되는 액체 이산화탄소를 교축 감압 팽창시키고,교축 감압 팽창된 기체 및 액체의 이산화탄소 2상 유체(2phase fluid)를 기액 분리기를 통과시켜 기체 이산화탄소 및 액체 이산화탄소로 분리함으로써 이루어지는 것을 특징으로 하는 액화 이산화탄소의 추가 냉각 방법.
- 사워 가스(Sour Gas)로부터 분리된 액체 이산화탄소를 교축 감압 팽창시키고, 저온으로 기액 분리하여 선박 운송용으로 공급하는 것을 특징으로 하는 액화 이산화탄소의 추가 냉각 방법.
- 상측으로는 메탄을 배출하고, 중간에는 제어된 동결 영역(Controlled Freezing Zone; CFZ)이 형성되며, 하측으로는 사워 가스(sour gas)에 포함된 이산화탄소를 배출하는 분리 유닛; 및상기 분리 유닛으로부터 배출되는 상기 메탄을 냉매로 하여 상기 분리 유닛으로부터 배출되는 액체 이산화탄소를 냉각시키며, 상기 분리 유닛으로부터 액체 이산화탄소가 배출되는 배관 상에 장착되는 열교환기;를 포함하는 것을 특징으로 하는 이산화탄소의 처리 모듈.
- 청구항 11에 있어서,상기 분리 유닛과 상기 열교환기를 상호 연결하는 상기 배관 상 또는 상기 열교환기 출구측의 상기 배관 상에 감압 밸브가 장착되는 것을 특징으로 하는 이산화탄소의 처리 모듈.
- 청구항 11에 있어서,상기 열교환기를 통과한 상기 액체 이산화탄소는 선박을 이용하여 이산화탄소 포집 및 저장(Carbon dioxide Capture and Storage; CCS)용 또는 석유 회수증진(Enhanced Oil Recovery; EOR)용으로 운송되는 것을 특징으로 하는 이산화탄소의 처리 모듈.
- 한계가스정(stranded gas well)에서 생산되는 사워 가스로부터 이산화탄소를 분리 배출하는 분리 유닛으로부터 배출되는 액체 이산화탄소의 유로를 형성하는 배관 상에 장착되는 열교환기에 상기 분리 유닛으로부터 배출되는 메탄을 냉매로 통과시켜 상기 열교환기를 통과하는 액체 이산화탄소를 냉각시키는 것을 특징으로 하는 이산화탄소의 처리 모듈.
- 한계가스정(stranded gaas well)에서 생산되는 사워 가스(sour gas)로부터 분리 배출되는 액체 이산화탄소에 상기 한계가스정으로부터 발생되는 메탄을 냉매로써 통과시켜 상기 액체 이산화탄소를 냉각시키는 것을 특징으로 하는 이산화탄소의 처리 방법.
- 한계가스정(stranded gas well)과 배관 연결되며 제어된 동결 영역(CFZ, Controlled Freezing Zone)을 형성하는 분리 유닛에 사워 가스(sour gas)를 공급하는 제1 단계;상기 사워 가스를 상기 분리 유닛에서 증류하여 상기 분리 유닛의 상측으로는 메탄을, 상기 분리 유닛의 하측으로는 액체 이산화탄소를 배출시키는 제2 단계;상기 분리 유닛의 액체 이산화탄소 배출용 배관 상에 장착된 열교환기에 상기 메탄을 냉매로 통과시켜 냉각시키는 제3 단계; 및상기 열교환기를 통과한 액체 이산화탄소를 선박에 선적하여 이산화탄소 포집 및 저장(Carbon dioxide Capture and Storage; CCS)용 또는 석유 회수증진(Enhanced Oil Recovery; EOR)용으로 운송하는 제4 단계;를 포함하는 것을 특징으로 하는 이산화탄소의 처리 방법.
- 청구항 16에 있어서,상기 제2 단계는,상기 분리 유닛으로부터 배출되는 액체 이산화탄소는 상기 분리 유닛과 상기 열교환기 사이의 상기 배관 상에 장착된 감압 밸브를 거쳐 감압되는 과정을 더 포함하는 것을 특징으로 하는 이산화탄소의 처리 방법.
- 청구항 16에 있어서,상기 제2 단계는,상기 분리 유닛으로부터 배출되는 액체 이산화탄소는 상기 열교환기 출구측의 상기 배관 상에 장착된 감압 밸브를 거쳐 감압되는 과정을 더 포함하는 것을 특징으로 하는 이산화탄소의 처리 방법.
- 상측으로는 메탄을 배출하고, 중간에는 제어된 동결 영역(Controlled Freezing Zone; CFZ)이 형성되며, 하측으로는 한계가스정(strandes gas well)으로부터 발생하는 사워 가스(sour gas)에 포함된 이산화탄소를 배출하는 분리 유닛;상기 분리 유닛으로부터 배출되는 상기 메탄을 냉매로 하여 상기 분리 유닛으로부터 배출되는 액체 이산화탄소를 냉각시키며, 상기 분리 유닛으로부터 액체 이산화탄소가 배출되는 배관 상에 장착되는 열교환기; 및상기 열교환기와 연결되어 상기 이산화탄소를 기체 및 -55℃~-20℃의 포화 액체상태로 분리하는 기액 분리기;를 포함하는 것을 특징으로 하는 액화 이산화탄소의 처리 모듈.
- 청구항 19에 있어서,상기 기액 분리기는,상측으로 기체 이산화탄소를 배출시키고, 하측으로 액체 이산화탄소를 배출시키는 것을 특징으로 하는 액화 이산화탄소의 처리 모듈.
- 청구항 19에 있어서,상기 분리 유닛과 상기 열교환기를 상호 연결하는 상기 배관 상 또는 상기 열교환기 출구측의 상기 배관 상에 팽창 밸브가 장착되는 것을 특징으로 하는 액화 이산화탄소의 처리 모듈.
- 한계가스정(stranded gas well)과 배관 연결되며 제어된 동결 영역(Controlled Freezing Zone)을 형성하는 분리 유닛에 사워 가스(sour gas)를 공급하는 제1 단계;상기 분리 유닛의 액체 이산화탄소 배출용 배관 상에 장착된 열교환기에 상기 메탄을 냉매로 통과시켜 냉각시키는 제2 단계;열교환되어 냉각된 상기 액체 이산화탄소를 상기 열교환기와 연결된 기액 분리기를 통하여 기체 및 액체로 분리하는 제3 단계; 및상기 기액 분리기를 통과한 액체 이산화탄소를 선박에 선적하여 이산화탄소 포집 및 저장(Carbon dioxide Capture and Storage; CCS)용 또는 석유 회수증진(Enhanced Oil Recovery; EOR)용으로 운송하는 제4 단계;를 포함하는 것을 특징으로 하는 이산화탄소의 처리 방법.
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US14/369,405 US9593883B2 (en) | 2011-12-27 | 2012-08-22 | Module for treatment of carbon dioxide and treatment method thereof |
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KR1020110143400A KR20130075152A (ko) | 2011-12-27 | 2011-12-27 | 액화 이산화탄소의 추가 냉각 모듈 및 방법 |
KR10-2011-0143401 | 2011-12-27 | ||
KR10-2011-0143400 | 2011-12-27 | ||
KR1020110143401A KR20130075153A (ko) | 2011-12-27 | 2011-12-27 | 이산화탄소의 처리 모듈 및 방법 |
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CN114963692A (zh) * | 2022-05-25 | 2022-08-30 | 崔静思 | 基于低温甲醇洗工艺低能耗捕集二氧化碳装置和方法 |
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HUE045214T2 (hu) * | 2012-11-14 | 2019-12-30 | Evonik Fibres Gmbh | Membrános gázelválasztó berendezés gáz összetételének szabályozása |
CN105157349B (zh) * | 2015-10-09 | 2017-05-10 | 易湘华 | 二氧化碳节能装置及利用其节能的方法 |
CN106440661B (zh) * | 2016-08-31 | 2020-03-31 | 惠生工程(中国)有限公司 | 一种制备高纯度液体二氧化碳的节能型装置和方法 |
DE102016011356A1 (de) * | 2016-09-20 | 2018-03-22 | Linde Aktiengesellschaft | Verfahren und Anlage zur Herstellung eines Erdgassubstituts und eines Kohlendioxidprodukts |
KR101919302B1 (ko) * | 2017-07-28 | 2018-11-19 | 한국전력공사 | 이산화탄소 분리막 플랜트 이상 감지 시스템 |
JP7434334B2 (ja) * | 2019-01-25 | 2024-02-20 | サウジ アラビアン オイル カンパニー | Co2回収を伴って水素を生成するための液体炭化水素およびco2輸送のためのプロセスおよび方法 |
CN115678628A (zh) * | 2022-10-13 | 2023-02-03 | 新疆敦华绿碳技术股份有限公司 | 二氧化碳驱油伴生气液二氧化碳回收装置、系统及方法 |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0618165A (ja) * | 1992-07-01 | 1994-01-25 | Nippon Sanso Kk | 低沸点不純物を含むガスの凝縮分離方法及び装置 |
KR100338881B1 (ko) * | 1997-07-01 | 2002-05-30 | 추후제출 | 하나 이상의 동결가능한 성분을 함유하는 천연 가스스트림의 액화 방법 |
KR20070083907A (ko) * | 2004-10-08 | 2007-08-24 | 유니온 엔지니어링 아/에스 | 가스로부터 이산화탄소를 회수하는 방법 |
KR20100074268A (ko) * | 2007-10-12 | 2010-07-01 | 유니온 엔지니어링 아/에스 | 공급가스로부터 이산화탄소의 제거 |
JP2011507680A (ja) * | 2007-12-21 | 2011-03-10 | エアパック・ホールディング・ベスローテン・フエンノートシャップ | サワーガスの分離方法 |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6070431A (en) * | 1999-02-02 | 2000-06-06 | Praxair Technology, Inc. | Distillation system for producing carbon dioxide |
GB0124617D0 (en) * | 2001-10-12 | 2001-12-05 | Alpha Thames Eng | Method and apparatus for collecting sand contained in production fluid and disposing of the collected sand |
GB0614250D0 (en) * | 2006-07-18 | 2006-08-30 | Ntnu Technology Transfer As | Apparatus and Methods for Natural Gas Transportation and Processing |
-
2012
- 2012-08-22 WO PCT/KR2012/006660 patent/WO2013100304A1/ko active Application Filing
- 2012-08-22 US US14/369,405 patent/US9593883B2/en not_active Expired - Fee Related
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0618165A (ja) * | 1992-07-01 | 1994-01-25 | Nippon Sanso Kk | 低沸点不純物を含むガスの凝縮分離方法及び装置 |
KR100338881B1 (ko) * | 1997-07-01 | 2002-05-30 | 추후제출 | 하나 이상의 동결가능한 성분을 함유하는 천연 가스스트림의 액화 방법 |
KR20070083907A (ko) * | 2004-10-08 | 2007-08-24 | 유니온 엔지니어링 아/에스 | 가스로부터 이산화탄소를 회수하는 방법 |
KR20100074268A (ko) * | 2007-10-12 | 2010-07-01 | 유니온 엔지니어링 아/에스 | 공급가스로부터 이산화탄소의 제거 |
JP2011507680A (ja) * | 2007-12-21 | 2011-03-10 | エアパック・ホールディング・ベスローテン・フエンノートシャップ | サワーガスの分離方法 |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN114963692A (zh) * | 2022-05-25 | 2022-08-30 | 崔静思 | 基于低温甲醇洗工艺低能耗捕集二氧化碳装置和方法 |
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US20140360226A1 (en) | 2014-12-11 |
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