WO2011113225A1 - Extraction d'un composant d'une composition en utilisant un fluide supercritique - Google Patents

Extraction d'un composant d'une composition en utilisant un fluide supercritique Download PDF

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Publication number
WO2011113225A1
WO2011113225A1 PCT/CN2010/073183 CN2010073183W WO2011113225A1 WO 2011113225 A1 WO2011113225 A1 WO 2011113225A1 CN 2010073183 W CN2010073183 W CN 2010073183W WO 2011113225 A1 WO2011113225 A1 WO 2011113225A1
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WO
WIPO (PCT)
Prior art keywords
fluid
component
supercritical
supercritical fluid
composition
Prior art date
Application number
PCT/CN2010/073183
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English (en)
Inventor
Hao Wang
Chen Zhao
Original Assignee
Peking University
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 Peking University filed Critical Peking University
Publication of WO2011113225A1 publication Critical patent/WO2011113225A1/fr

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Classifications

    • 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/04—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction
    • C10G1/045—Separation of insoluble materials
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/02—Solvent extraction of solids
    • B01D11/0203—Solvent extraction of solids with a supercritical fluid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/02—Solvent extraction of solids
    • B01D11/0292—Treatment of the solvent
    • B01D11/0296—Condensation of solvent vapours
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/04—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1033—Oil well production fluids
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/208—Sediments, e.g. bottom sediment and water or BSW
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/44—Solvents

Definitions

  • the systems and methods disclosed herein relate to the extraction of a component from a composition using supercritical fluid.
  • a system for extracting a component from a composition may have an extraction device configured to contain the composition and configured to receive a supercritical fluid.
  • the supercritical fluid extracts the component from the composition.
  • the system may also have a separation device configured to separate the component from the supercritical fluid.
  • the system may also have a feed pump that receives and pressurizes a fluid.
  • the component is resolvable to the fluid in a supercritical phase.
  • the system may also include a solar collector that receives the fluid from the feed pump and heats the fluid to a supercritical phase to form a supercritical fluid.
  • the extraction and separation device receives the supercritical fluid from the solar collector.
  • the system also may include a heat exchanger that receives the fluid from the extraction and separation device and cools the fluid for returning to the feed pump.
  • the extraction and separation device of the system may have a water bath; a high pressure cell in the water bath that contains the composition; a pump (for instance, a syringe pump or a diaphragm pump) that charges the supercritical fluid through the cell; a filter contained in the cell that filters the supercritical fluid out of the cell; and a separator that receives the supercritical fluid and separates the supercritical fluid from the component.
  • the extraction and separation device of the system may also have a pressure gauge in the water bath to control the pressure of the supercritical fluid.
  • the fluid of the system may be liquid carbon dioxide.
  • the fluid of the system may be water.
  • the component of the system may be oil, and the composition of the system may be oil sand.
  • the feed pump of the system may pressurize the fluid to about 20MPa.
  • the solar collector of the system may heat the fluid up to about 170°C. In order to obtain good extraction ability, the fluid should be heated by the solar collector to a temperature of about 70°C.
  • the supercritical fluid of the system may be separated from the component in the separator by decreasing the pressure of the supercritical fluid to change the fluid into a gaseous state. The pressure may be decreased to about 4.5MPa.
  • the heat exchanger of the system may include a first exchanger component that recycles the heat of the fluid; and a second exchanger component that cools the fluid into a liquid state.
  • the heat exchanger of the system may cool the fluid to about 20°C.
  • a method for extracting a component from a composition may include the steps of extracting the component from the composition with a supercritical fluid and separating the component from the supercritical fluid.
  • the method may also include the steps of pressurizing a fluid, wherein the component is resolvable to the fluid in a supercritical phase and heating the fluid to a supercritical phase to form a supercritical fluid.
  • the method may also include the step of cooling the fluid after the separating step.
  • the cooling step of the method may include the steps of recycling the heat of the fluid and cooling the fluid into a liquid state.
  • the cooling step of the method may include cooling said fluid to about 20°C.
  • Figure 1 is a diagram of a system for extracting a component from a composition using a fluid according to an embodiment disclosed herein.
  • Figure 2 is a diagram of an extraction and separation device according to an embodiment disclosed herein.
  • Figure 3 is a flow diagram of a method for extracting a component from a composition according to an embodiment disclosed herein.
  • Figure 4 is a flow diagram of a method for extracting a component from a composition according to another embodiment disclosed herein.
  • This disclosure is drawn, inter alia, to methods and systems related to the extraction of a component from a composition using supercritical fluid.
  • the extraction may be from a solid composition, liquid composition, or a mixture.
  • Such extractions may be used on all different scales. For instance, extraction on a small scale may be appropriate for analytical purposes, whereas extraction on a large scale may be appropriate for industrial applications.
  • this disclosure relates to a system and method involving placing fluid (for instance, by heating using solar energy), such as liquid carbon dioxide, in a supercritical phase. Then, the fluid in a supercritical phase can work as the extracting solvent to separate one component from another.
  • the system and method may be utilized to extract oil from oil sand.
  • the fluid to be placed in supercritical phase may be one or more fluid.
  • a supercritical fluid may be any substance at a temperature and pressure above its thermodynamic critical point.
  • Supercritical fluids combine properties of gases and liquids. For instance, supercritical fluids can diffuse through solids like a gas, and also dissolve materials like a liquid. Fluids such as supercritical carbon dioxide and water offer a range of unusual chemical possibilities in both synthetic and analytical chemistry. For example, supercritical fluids have solvent power similar to a light hydrocarbon for most solutes.
  • supercritical fluids may be mixed or combined with additional fluids. For instance, carbon dioxide may be modified with co-solvents. Suitable co-solvents include ethanol and/or methanol.
  • one or more possible fluids may be utilized, including, but not limited to carbon dioxide, water, methane, ethane, propane, ethylene, propylene, methanol, ethanol and acetone.
  • the supercritical fluid will contain no surface tension due to the absence of a liquid/gas phase boundary.
  • the properties may be "tuned" to be more liquid or more gas like.
  • Another property that may be considered is the solubility of the component to be extracted in the fluid. Solubility in a supercritical fluid tends to increase with density of the fluid (at constant temperature). Since density increases with pressure, then solubility also tends to increase with pressure. The relationship with temperature may also be considered. At constant density, solubility will increase with temperature. However, close to the critical point, the density can drop sharply with a slight increase in temperature. Therefore, close to the critical temperature, solubility often drops with increasing temperature, then rises again.
  • fluid pressure and temperature can be increased respectively by a pump and a solar collector, as illustrated in Figure 1.
  • carbon dioxide fluid can be heated and pressed into supercritical phase.
  • the critical temperature and pressure of carbon dioxide fluid is about 31°C and about 7.2MPa.
  • the addition of modifiers may slightly alter the temperature and pressure.
  • oil can be dissolved in the supercritical carbon dioxide fluid and extracted from the oil sands. Depressurization of the fluid separates the oil from the carbon dioxide because lowering the pressure reduces the solvent power of the supercritical fluid.
  • the heat of the fluid can be recycled.
  • Figure 1 illustrates a diagram of a system 10 according to one embodiment of this disclosure. Figure 1 will first be described as shown. Then, Figure 1 will be described using a specific example of extracting oil from oil sands with carbon dioxide.
  • a fluid flows from a feed pump 12 to a solar collector 14 to an extraction and separation device 16 to a heat exchanger 18.
  • the fluid flows into the feed pump 12, then out of the feed pump 12 into the solar collector 14, then out of the solar collector 14 into the extraction and separation device 16, and then out of the extraction and separation device 16 into the heat exchanger 18.
  • the fluid flows out of the heat exchanger 18 and back to the feed pump 12 so that the fluid flow is continuous.
  • the fluid may flow from one part of the system to the next through a pipe or any other means known to one of ordinary skill in the art.
  • a fluid flows in the feed pump 12 and is pressurized.
  • the feed pump 12 receives and pressurizes the fluid.
  • the fluid can be already in a liquid state.
  • the output of the heat exchanger 18 is a liquid.
  • the feed pump 12 may be a simple piston pump or any other conventional pump.
  • the pressurized fluid is heated by solar energy collected by the solar collector 14 to the point where the fluid becomes supercritical.
  • the solar collector 14 may be an evacuated solar collector.
  • the solar collector 14 may heat the fluid from about 20°C to about 170°C.
  • the supercritical fluid then flows through the extraction and separation device 16, which contains a composition.
  • the supercritical fluid extracts a desired component from the composition and carries the component away (not shown in Figure 1) from the rest of the composition.
  • the extraction and separation device 16 includes any structure capable of mixing the supercritical fluid with the composition and then performing a separation.
  • Figure 2 One example of an extraction and separation device is illustrated in Figure 2.
  • the extraction and separation device 16 may include a pump 20 (for example a syringe or a diaphragm pump), a water bath 22, and a separator 24.
  • the water bath 22 may contain a pressure gauge 26 and a cell 28 (for example, a high pressure cell) with a filter 30.
  • the composition is put in the cell 28.
  • the supercritical fluid is charged into the cell 28 through the pump 20.
  • the pressure gauge 26 may be used to control the pressure.
  • the cell 28 is put in the water bath 22.
  • the extraction portion of the extraction and separation device 16 can then maintain the temperature and pressure at a desired level.
  • the supercritical fluid with the component exits the cell 28 through a filter 30 and enters the separator 24.
  • the separator 24 decreases the pressure so that the supercritical fluid can be changed into a gaseous state and can be easily separated from the component. After the extraction and separation, the temperature of the fluid is maintained.
  • the heat exchanger 18 may include two exchanger components. If two exchanger components are used, the first exchanger component is used for recycling the heat of the high temperature fluid, and the second exchanger component is used for cooling the fluid into a liquid state for good pumping ability. With two exchanger components, they can be coupled in series and have the same or different internal structure. The heat exchanger 18 may alternatively have only one exchanger component as long as the high temperature fluid can be cooled.
  • working carbon dioxide flows from a feed pump 12 to a solar collector 14 to an extraction and separation device 16 to a heat exchanger 18.
  • the liquid carbon dioxide flows in the feed pump 12 and is pressurized.
  • the feed pump receives and pressurizes the liquid carbon dioxide.
  • the carbon dioxide fluid can be already in a liquid state and have a temperature around 20°C before the liquid carbon dioxide arrives at the feed pump 12.
  • the output of the heat exchanger 18 is liquid carbon dioxide.
  • the feed pump 12 may pressurize the carbon dioxide fluid from about 4.5MPa to about 20MPa.
  • the pressurized carbon dioxide fluid is heated by solar energy collected by the solar collector 14 to the point where the carbon dioxide fluid becomes supercritical.
  • the solar collector 14 may heat the carbon dioxide fluid from about 20°C to about 170°C.
  • the high pressure carbon dioxide fluid is heated by the solar collector 14 to a temperature of about 70°C.
  • the supercritical carbon dioxide fluid then flows through the extraction and separation device 16, which contains oil sands.
  • the supercritical fluid extracts oil from the oil sands and carries the oil away from the oil sands.
  • the extraction and separation device 16 is further illustrated in Figure 2.
  • the extraction and separation device 16 includes a pump 20, a water bath 22, and a separator 24.
  • the water bath 22 contains a pressure gauge 26 and a cell 28 (for example, a high pressure cell) with a filter 30.
  • the oil sands are put in the cell 28.
  • the supercritical carbon dioxide fluid is charged into the cell 28 through the pump 20.
  • the pressure gauge 26 is used to control the pressure.
  • the cell 28 is put in the water bath 22.
  • the extraction portion of the extraction and separation device 16 can then maintain the temperature at about 70°C and the pressure at about 20MPa.
  • the supercritical fluid with the oil exits the cell 28 through a filter 30 and enters the separator 24.
  • the separator 24 decreases the pressure to about 4.5MPa so that the supercritical carbon dioxide fluid can be changed into a gaseous state and can be easily separated from the oil.
  • the temperature of the fluid is maintained at about 70°C.
  • the heat exchanger 18 may include two exchanger components. If two exchanger components are used, the first exchanger component is used for recycling the heat of the high temperature carbon dioxide fluid, and the second exchanger component is used for cooling the fluid into a liquid state for good pumping ability.
  • the temperature of the fluid may be about 35°C after the first exchanger component and about 20°C after the second exchanger component.
  • the pressure of the fluid is maintained at about 4.5MPa before and after entering the heat exchanger 18. With two exchanger components, they can be coupled in series and have the same or different internal structure.
  • the heat exchanger 18 may alternatively have only one exchanger component as long as the high temperature carbon dioxide fluid can be cooled down to about 20°C.
  • the heat exchanger 18 may be a carbon dioxide/water heat exchanger, which uses water pumps to recycle the water flow and gather the heat from water in a cooling tower.
  • a shell and tube design can be used for the heat exchanger components, with the tube side being for carbon dioxide and the shell side being for water, as an example.
  • the temperature of the water used to recover heat in the first exchanger component is determined by the temperature of the carbon dioxide fluid coming out of the extraction and separation device 16 and the cooling capacity of the cooling tower of the first exchanger component.
  • the temperature of the water used to recover heat in the low-temperature heat recovery system, i.e. the second exchanger component is about 10°C.
  • the method of this disclosure will now be more fully described with reference to Figures 1-4.
  • the method is for extracting a component from a composition.
  • one step is extracting a desired component from a composition with a supercritical fluid (step 110).
  • This step 110 may occur in an extraction and separation device, which contains the composition.
  • the supercritical fluid extracts a desired component from the composition and carries the component away from the rest of the composition.
  • the extracting step 110 may involve charging the supercritical fluid with a pump, such as a syringe pump or a diaphragm pump, through a high pressure cell in a water bath.
  • the cell contains the composition.
  • the extracting step 110 then may involve filtering the supercritical fluid out of the cell through a filter.
  • the extracting step 110 may also include controlling the pressure of the supercritical fluid with a pressure gauge in the water bath.
  • a further step of the method of Figure 3 is separating the component from the supercritical fluid (step 120).
  • This step 120 may also occur in the extraction and separation device.
  • the separating step 120 may involve separating the supercritical fluid from the component in a separator.
  • the separating step 120 may also include decreasing the pressure of the supercritical fluid to change the fluid into a gaseous state. For example, the pressure may be decreased to about 4.5MPa.
  • one step is pressurizing a fluid (step 210).
  • This step 210 may be done with a feed pump 12.
  • the component being extracted should be resolvable to this fluid when the fluid is in a supercritical phase.
  • the pressurizing step 210 may involve pressurizing the fluid to about 20MPa.
  • Another step is heating the high pressure fluid to a supercritical phase to form a supercritical fluid (step 220).
  • This step 220 may be done with a solar collector.
  • the heating step 220 may involve heating the fluid up to about 170°C. More particularly, the heating step 220 may involve heating the fluid to about 70°C.
  • step 230 another step is extracting the desired component from the composition with the supercritical fluid (step 230).
  • This step 230 may occur in an extraction and separation device, which contains the composition.
  • the supercritical fluid extracts a desired component from the composition and carries the component away from the rest of the composition.
  • the extracting step 230 may involve charging the supercritical fluid with a pump (such as a syringe pump or a diaphragm pump) through a high pressure cell in a water bath.
  • the cell contains the composition.
  • the extracting step 230 then may involve filtering the supercritical fluid out of the cell through a filter.
  • the extracting step 230 may also include controlling the pressure of the supercritical fluid with a pressure gauge in the water bath.
  • a further step of the method is separating the component from the supercritical fluid (step 240). This step 240 may also occur in the extraction and separation device.
  • the separating step 240 may involve separating the supercritical fluid from the component in a separator.
  • the separating step 240 may also include decreasing the pressure of the supercritical fluid to change the fluid into a gaseous state. For example, the pressure may be decreased to about 4.5MPa.
  • a further step of the method may include cooling the fluid (step 250).
  • This step 250 may occur in a heat exchanger.
  • the heat exchanger may include two exchanger components.
  • the cooling step may include recycling the heat of the fluid (step 252) and cooling the fluid into a liquid state (step 254).
  • the step 252 would be done with the first exchanger component, and the step 254 would be done with the second exchanger component.
  • the cooling step may involve cooling the fluid to about 20°C.
  • this method may be applied to extracting any component from any composition using a fluid as long as the component is resolvable to the fluid in a supercritical state.
  • the fluid may be liquid carbon dioxide and/or water.
  • the component may be oil when the composition is oil sand.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Extraction Or Liquid Replacement (AREA)

Abstract

La présente invention concerne un système d'extraction d'un composant d'une composition et un procédé d'utilisation dudit système. Ledit système comprend un dispositif d'extraction et de séparation (16) contenant ladite composition et recevant un fluide supercritique, une pompe d'alimentation (12) qui reçoit un fluide et le met sous pression, un collecteur solaire (14) qui reçoit le fluide de la pompe d'alimentation (12) et chauffe le fluide à une phase supercritique pour former un fluide supercritique, et un échangeur thermique (18) qui reçoit le fluide du dispositif d'extraction et de séparation (16) et refroidit le fluide pour le renvoyer à la pompe d'alimentation (12). Ledit procédé comprend l'étape consistant à extraire un composant d'une composition avec un fluide supercritique.
PCT/CN2010/073183 2010-03-15 2010-05-25 Extraction d'un composant d'une composition en utilisant un fluide supercritique WO2011113225A1 (fr)

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Application Number Priority Date Filing Date Title
CA2696910A CA2696910C (fr) 2010-03-15 2010-03-15 Extraction d'un composant d'une composition par fluide supercritique
CA2,696,910 2010-03-15

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WO2011113225A1 true WO2011113225A1 (fr) 2011-09-22

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US10144874B2 (en) 2013-03-15 2018-12-04 Terrapower, Llc Method and system for performing thermochemical conversion of a carbonaceous feedstock to a reaction product
US10760004B2 (en) 2017-03-24 2020-09-01 Terrapower, Llc Method for recycling pyrolysis tail gas through conversion into formic acid
US10787610B2 (en) 2017-04-11 2020-09-29 Terrapower, Llc Flexible pyrolysis system and method

Citations (4)

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Publication number Priority date Publication date Assignee Title
CN1083513A (zh) * 1993-09-24 1994-03-09 中国石油化工总公司 一种分离石油重质油的方法
JPH08140695A (ja) * 1994-11-25 1996-06-04 Yaegaki Hakko Giken Kk 培養菌体からのアスタキサンチンの分離・精製方法
US20020127316A1 (en) * 2001-03-08 2002-09-12 Trout Richard B. Process and system for removing oil from foodstuffs using a membrane filter
CN101338248A (zh) * 2008-08-07 2009-01-07 安阳格林生物能源有限公司 用于提取和回收固体油料作物中油脂的超临界工艺

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1083513A (zh) * 1993-09-24 1994-03-09 中国石油化工总公司 一种分离石油重质油的方法
JPH08140695A (ja) * 1994-11-25 1996-06-04 Yaegaki Hakko Giken Kk 培養菌体からのアスタキサンチンの分離・精製方法
US20020127316A1 (en) * 2001-03-08 2002-09-12 Trout Richard B. Process and system for removing oil from foodstuffs using a membrane filter
CN101338248A (zh) * 2008-08-07 2009-01-07 安阳格林生物能源有限公司 用于提取和回收固体油料作物中油脂的超临界工艺

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CA2696910A1 (fr) 2011-09-15

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