WO2011002277A1 - Procédé d'élimination du dioxyde de carbone présent dans un flux de fluide et ensemble séparateur pour fluides - Google Patents

Procédé d'élimination du dioxyde de carbone présent dans un flux de fluide et ensemble séparateur pour fluides Download PDF

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Publication number
WO2011002277A1
WO2011002277A1 PCT/NL2009/050388 NL2009050388W WO2011002277A1 WO 2011002277 A1 WO2011002277 A1 WO 2011002277A1 NL 2009050388 W NL2009050388 W NL 2009050388W WO 2011002277 A1 WO2011002277 A1 WO 2011002277A1
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WO
WIPO (PCT)
Prior art keywords
fluid
carbon dioxide
outlet
section
fluid stream
Prior art date
Application number
PCT/NL2009/050388
Other languages
English (en)
Inventor
Bart Prast
Jakob Arie Cornelis Langerak
Marco Betting
Cornelis Antonie Tjeenk Willink
Original Assignee
Twister B.V.
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 Twister B.V. filed Critical Twister B.V.
Priority to PCT/NL2009/050388 priority Critical patent/WO2011002277A1/fr
Priority to CA2748128A priority patent/CA2748128C/fr
Priority to PCT/NL2009/050781 priority patent/WO2010074565A1/fr
Priority to CN200980156303.XA priority patent/CN102307642B/zh
Priority to EA201170870A priority patent/EA020177B1/ru
Priority to MYPI2011002936A priority patent/MY155298A/en
Priority to US13/141,408 priority patent/US20120017638A1/en
Priority to AU2009330799A priority patent/AU2009330799B2/en
Publication of WO2011002277A1 publication Critical patent/WO2011002277A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/061—Natural gas or substitute natural gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
    • B01D45/16—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by the winding course of the gas stream, the centrifugal forces being generated solely or partly by mechanical means, e.g. fixed swirl vanes
    • 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
    • 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
    • B01D53/24—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 centrifugal force
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0635—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/10—Processes or apparatus using other separation and/or other processing means using combined expansion and separation, e.g. in a vortex tube, "Ranque tube" or a "cyclonic fluid separator", i.e. combination of an isentropic nozzle and a cyclonic separator; Centrifugal separation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/50—Arrangement of multiple equipments fulfilling the same process step in parallel
    • 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 of removing carbon dioxide from a fluid stream.
  • embodiments of the present invention relate to a method of removing carbon dioxide from a natural gas stream.
  • the invention further relates to a fluid separation assembly.
  • Natural gas from storage or production reservoirs typically contains carbon dioxide (CO 2 ). Such a natural gas is denoted as a “sour” gas. Another species denoted as “sour” in a fluid stream is hydrogen sulphide (H 2 S). A fluid stream without any of
  • aforementioned sour species is denoted as a "sweet" fluid.
  • CO 2 promotes corrosion within pipelines. Furthermore, in some jurisdictions, legal and commercial requirements with respect to a maximum concentration of CO 2 in a fluid stream may be in force. Therefore, it is desirable to remove CO 2 from a sour fluid stream.
  • Fluid sweetening processes i.e. a process to remove a sour species like carbon dioxide from a fluid stream
  • processes typically include at least one of chemical absorption, physical absorption, adsorption, low temperature distillation, also referred to as cryogenic separation, and membrane separation.
  • an embodiment of the invention provides a method of removing carbon dioxide from a fluid stream by a fluid separation assembly comprising: a cyclonic fluid separator comprising a throat portion arranged between a converging fluid inlet section and a diverging fluid outlet section and a swirl creating device configured to create a swirling motion of the carbon dioxide containing fluid within at least part of the cyclonic fluid separator, the converging fluid inlet section comprising a first inlet for fluid components and the diverging fluid outlet section comprising a first outlet for carbon dioxide depleted fluid and a second outlet for carbon dioxide enriched fluid;
  • a separation vessel having a first section in connection with a collecting tank, the first section being provided with a second inlet connected to the second outlet of the cyclonic fluid separator, and the collecting tank being provided with a third outlet for solidified carbon dioxide, wherein said separation vessel is operated at a pressure and temperature combination that is at or in the vicinity of the phase boundary between a vapour/liquid/solid coexistence region (IVb) and the vapour/solid coexistence region (IVa);
  • the invention further relates to a fluid separation assembly for removing carbon dioxide from a fluid stream, the fluid separation assembly
  • a cyclonic fluid separator comprising a throat portion arranged between a converging fluid inlet section and a diverging fluid outlet section and a swirl creating device configured to create a swirling motion of the carbon dioxide containing fluid within at least part of the separator, the converging fluid inlet section comprising a first inlet for fluid components and the diverging fluid outlet section comprising a first outlet for carbon dioxide depleted fluid and a second outlet for carbon dioxide enriched fluid;
  • a separation vessel having a first section in connection with a collecting tank, the section being provided with a second inlet connected to the second outlet of the cyclonic fluid separator, and the collecting tank being provided with a third outlet for solidified carbon dioxide, wherein said separation vessel is operated at a pressure and temperature combination that is at or in the vicinity of the phase boundary between a vapour/liquid/solid coexistence region (IVb) and the vapour/solid coexistence region (IVa);
  • fluid separation assembly is arranged to:
  • fluid is used. This term is used to refer to liquid and/or gas.
  • FIG. 1 schematically depicts a longitudinal sectional view of a cyclonic fluid separator that may be used in embodiments
  • Figure 2 schematically depicts a cross-sectional view of a separation vessel that may be used in embodiments
  • Figures 3 a, 3b depict an exemplary phase diagram of a natural gas containing carbon dioxide in which schematically different embodiments of the method are visualised
  • FIG. 4 5,6, 7, 8a and 8b schematically depict further embodiments.
  • Figure 1 schematically depicts a longitudinal sectional view of a cyclonic fluid separator 1 that may be used in embodiments of the invention.
  • a cyclonic fluid separator is described in more detail in international patent application WO03/029739. It must be understood that, in embodiments of the invention, also cyclonic fluid separators of a different type may be used, e.g. a cyclonic fluid separator as described in WO99/01194, WO2006/070019 and WO00/23757.
  • the cyclonic fluid separator 1 comprises a converging fluid inlet section 3, a diverging fluid outlet section 5 and a tubular throat portion 4 arranged in between the converging fluid inlet section 3 and diverging fluid outlet section 5.
  • the cyclonic fluid separator 1 further comprises a swirl creating device, e.g. a number of swirl imparting vanes 2, configured to create a swirling motion of the fluid within at least part of the cyclonic fluid separator 1.
  • the cyclonic fluid separator 1 comprises a pear-shaped central body 11 on which the swirl imparting vanes 2 are mounted and which is arranged coaxial to a central axis I of the cyclonic separator 1 and inside the cyclonic separator such that an annular flow path is created between the central body 1 and separator housing 20.
  • the width of the annulus is designed such that the cross-sectional area of the annulus gradually decreases downstream of the swirl imparting vanes 2 such that in use the fluid velocity in the annulus gradually increases and reaches a supersonic speed at a location downstream of the swirl imparting vanes 2.
  • the cyclonic separator 1 further comprises a tubular throat portion 4 from which, in use, the swirling fluid stream is discharged into a diverging fluid separation chamber 5 which is equipped with a central primary outlet conduit 6 for gaseous components and with an outer secondary outlet conduit 7 for condensables enriched fluid components.
  • the central body 1 has a substantially cylindrical elongated tail section 8 on which an assembly of flow straightening blades 19 is mounted.
  • the central body 11 has a largest outer width or diameter 2R 0 max which is larger than the smallest inner width or diameter 2R n mm of the tubular throat portion 4.
  • the tubular throat portion 4 comprises the part of the annulus 3 having the smallest cross-sectional area.
  • the maximum diameter of the central body 1 is larger than the minimum diameter of the tubular throat portion 4.
  • the converging fluid inlet section 3 comprises a first inlet 10.
  • the diverging fluid outlet section 5 comprises a first outlet 6 and a second outlet 7.
  • cyclonic fluid separator 1 The function of the various components of the cyclonic fluid separator 1 will now be explained with respect to a case in which the cyclonic fluid separator 1 is used to separate carbon dioxide from a fluid stream comprising carbon dioxide in accordance with an embodiment of the invention.
  • the fluid stream comprising carbon dioxide is fed through the first inlet 10 in the converging fluid inlet section 3.
  • the fluid stream comprises a mole percentage carbon dioxide larger than 10%.
  • the swirl imparting vanes 2 create a circulation in the fluid stream and are oriented at an angle ⁇ relative to the central axis of the cyclonic fluid separator l,i.e. the axis around which the cyclonic fluid separator 1 is about rotationally symmetric.
  • the swirling fluid stream is then expanded to high velocities.
  • the number of swirl imparting vanes 2 is positioned in the throat portion 4.
  • the number of swirl imparting vanes 2 is positioned in the converging fluid inlet section 3.
  • the central body 11 has a largest outer width or diameter 2R 0 max which is larger than the smallest inner width or diameter 2R n min of the tubular throat portion 4.
  • the swirling fluid stream has a transonic velocity. In other embodiments of the invention, the swirling fluid stream may reach a supersonic velocity.
  • the expansion is performed rapidly. With respect to an expansion two time scales may be defined.
  • the first time scale is related to a mass transfer time t eq , i.e. a time associated with return to equilibrium conditions.
  • the t eq depends on the interfacial area density in a two-phase system, the diffusion coefficient between the two phases and the magnitude of the departure from equilibrium.
  • the t eq for a liquid-to-solid transition is typically two orders of magnitude larger than for a vapour-to-liquid transition.
  • the second time scale is related to an expansion residence time t res of the fluid in the device.
  • the t res relates to the average speed of the fluid in the device and the axial length of the device along which the fluid travels.
  • An expansion is denoted as 'rapid' when ⁇ > l .
  • the swirling fluid stream may reach a temperature below 200 K and a pressure below 50% of a pressure at the first inlet 10 of the converging inlet section 3.
  • carbon dioxide components are formed in a meta-stable state within the fluid stream.
  • the fluid stream at the inlet section 3 is a gas stream
  • the carbon dioxide components will be formed as liquefied carbon dioxide components.
  • the fluid stream at the inlet section 3 is a liquid stream
  • hydrocarbon vapours will be formed whilst the majority of carbon dioxide components remain in liquid form.
  • the fluid stream may be induced to further expand to higher velocity or be kept at a substantially constant speed.
  • the fluid stream is kept at substantially constant speed, carbon dioxide component formation is about to stop after a defined relaxation time.
  • the centrifugal action causes the carbon dioxide particles to drift to the outer circumference of the flow area adjacent to the inner wall of the housing of the cyclonic fluid separator 1 so as to form an outward fluid stream.
  • the outward fluid stream is a stream of a carbon dioxide enriched fluid, the carbon dioxide components therein being liquefied and/or partly solidified.
  • the outward fluid stream comprising the components of carbon dioxide in aforementioned meta-stable state is extracted from the cyclonic fluid separator 1 through the second outlet 7 of the cyclonic fluid separator 1.
  • Other components within the fluid stream not being part of aforementioned outward fluid stream are extracted from the cyclonic fluid separator 1 through first outlet 6 of the cyclonic fluid separator 1.
  • FIG. 2 schematically depicts a cross-sectional view of a separation vessel 21 that may be used in embodiments of the invention.
  • the separation vessel 21 has a first section, further referred to as tubular section 22, with, in use, a substantially vertical orientation positioned on and in connection with a collecting tank 23.
  • the collecting tank 23 is provided with a third outlet 28 and a fourth outlet 26.
  • the tubular section 22 is provided with a second inlet 25 and a fifth outlet 29.
  • the second inlet 25 is connected to the second outlet 7 of the cyclonic fluid separator 1.
  • the second inlet 25 is arranged to provide a tangential fluid stream into the separation vessel 21, e.g. the second inlet 25 is arranged tangent to the circumference of the separation vessel 21.
  • the separation vessel 21 further comprises a cooling arrangement, in Figure 2 schematically represented by reference number 31, and a separation arrangement, in Figure 2 schematically represented by reference number 33.
  • a cooling arrangement in Figure 2 schematically represented by reference number 31, and a separation arrangement, in Figure 2 schematically represented by reference number 33.
  • the function of the various components of the separation vessel 21 will now be explained with respect to a case in which the separation vessel 21 is used in a method of removing carbon dioxide from a fluid stream in accordance with an embodiment of the invention.
  • the cooling arrangement 31 is configured to provide a predetermined
  • the temperature condition in the separation vessel 21 is such that it enables solidification of the carbon dioxide enriched fluid, which enters the separation vessel 21 through the second inlet 25 as a mixture.
  • the temperature within the separation vessel 21 should remain below the solidification temperature of carbon dioxide, the latter being dependent on the pressure conditions in the separation vessel 21.
  • a mixture comprising carbon dioxide originating from the second outlet 7 of the cyclonic fluid separator 1 is split in at least three fractions. These fractions are a first fraction of gaseous components, a second fraction of hydrocarbon, predominantly in a liquid state, and a third fraction of carbon dioxide, predominantly in a solid state.
  • the first fraction is formed by gaseous components which are dragged along with the liquids exiting the second outlet 7.
  • the cooling arrangement 31 is configured to keep the temperature within the separation vessel 21 below the solidification temperature of the fluid.
  • the gaseous components do not contain much carbon dioxide as most carbon dioxide will be dissolved in the mixture liquid, as will be explained in more detail with reference to Figure 3.
  • the carbon dioxide depleted gaseous components may leave the separation vessel 21 through the fifth outlet 29.
  • the vessel 21 may be equipped with one or more inlets 25 which are positioned tangent to the perimeter of the vertical section 22, such that a rotational flow in section 22 results. Furthermore the top gas outlet 29 may extent as a vertical pipe in said vertical section 22 as to form a so-called vortex finder. The edge of said vortex finder is at a vertical lower position compared to the vertical position of the inlet(s) 25. This is explained in more detail below with reference to Fig. 7.
  • the edge of the vortex finder i.e. lowest part of the gas outlet 29
  • the edge of the vortex finder is below the inlet 25 to allow the components that enter through the inlet 25 to separate before reaching the edge of the vortex finder. So this distance is provided to prevent liquids and solids from entering the vortex finder. The liquids and solids will be forced to the outer perimeter due to the rotational forces and will not enter the gas outlet 29.
  • the sections 22 and 23 of vessel 21 may be physically separated by a conical shaped vortex breaker of which the outer perimeter has a clearance C with respect to the inner perimeter of the vertical section 22.
  • This clearance C can range typically from 0.05 to 0.3 times the inner diameter of section 22. This is explained in more detail below with reference to Fig. 7.
  • the mixture may be split in a liquid component containing hydrocarbon and a solid component of carbon dioxide by means of a separation arrangement 33.
  • Possible separation arrangements 33 include a gravity separator, a centrifuge and a hydro cyclone. In case a gravity separator is used, it preferably comprises a number of stacked plates. In case a centrifuge is used, it preferably comprises a stacked disc bowl.
  • the separation arrangement 33 in the separation vessel 21 is configured to enable carbon dioxide enriched hydrocarbon liquid components to leave the separation vessel 21 through the fourth outlet 26, and to enable solidified carbon dioxide to leave the separation vessel 21 through the third outlet 28.
  • the fluid separation assembly further comprises a screw conveyor or scroll type discharger 35 in connection with the third outlet 28.
  • the scroll type discharger 35 is configured to extract the solidified carbon dioxide from the separation vessel 21.
  • interior surfaces of elements of the fluid separation assembly being exposed to the fluid i.e. cyclonic fluid separator 1, separation vessel 21 and the one or more tubes or the like connecting the second outlet 7 of the cyclonic fluid separator 1 and the second inlet 25 of the separation vessel 21, are provided with a non-adhesive coating.
  • the non-adhesive coating prevents adhesion of solidified fluid components, i.e. carbon dioxide, on aforementioned interior surfaces. Such adhesion would decrease the efficiency of the fluid separation assembly.
  • FIGS 3 a, 3b show an exemplary phase diagram of a natural gas containing carbon dioxide in which schematically different embodiments of the method according to the invention are visualised.
  • the phases are represented as a function of pressure in bar and temperature in degrees Celsius.
  • the natural gas contains 71 mol% CO 2 .
  • the natural gas contains 0.5 mol% nitrogen (N 2 ), 0.5 mol% hydrogen sulphide (H 2 S), 27 mol% Cl, i.e. hydrocarbons with a single carbon atom therein, and 1 mol% C2, i.e. hydrocarbons with two carbon atoms therein.
  • the condition of the fluid stream at the first inlet 10 of the cyclonic fluid separator 1 schematically depicted in Figure 1 corresponds to the coordinate of 80 bar and -40 0 C , denoted by [START] in the diagram of figure 3a.
  • the isentropic trajectory along arrow A is in the liquid region (II)
  • the isentropic trajectory along arrow B is in the vapour/liquid coexistence region (III).
  • a meta-stable state in the liquid/vapour regime may be reached while following arrow B, until phase transition occurs at a certain super saturated condition.
  • the resulting evaporation process will then restore equilibrium conditions.
  • the fluid stream may be separated by a cyclonic fluid separator, e.g. a cyclonic fluid separator as described in International patent application
  • WO2006/070019 in a carbon dioxide enriched fluid stream and a carbon dioxide depleted fluid stream at the end of the expansion trajectory denoted by arrow C.
  • the separated, carbon dioxide enriched fluid is in a state of non-equilibrium, which will only last for a limited period of time, in the order of 10 milliseconds. Therefore the carbon dioxide enriched fluid is recompressed in the second outlet 7 of the diverging outlet section 5 of the cyclonic fluid separator 1 and discharged via the second outlet 7 to the separation vessel 21, preferably within said time period that the meta-stable state exists.
  • a breakdown of said meta-stable state results in solid formation which in practice means that dissolved carbon dioxide in the liquid solidifies.
  • the separated, carbon dioxide enriched fluid entering the separation vessel 21 may be cooled in order to ensure that the fluid remains in the vapour/solid or vapour/liquid/solid coexistence region. Said process of cooling and recompressing the carbon dioxide enriched fluid is denoted by arrow D.
  • the process of further solidification takes place in the separation vessel 21.
  • the state of the fluid at a newly developed equilibrium within the separation vessel 21 is denoted as [END].
  • Solidified carbon dioxide is removed through the third outlet 28 as described above.
  • the condition of the fluid stream at the first inlet 10 of the cyclonic fluid separator 1 schematically depicted in Figure 1 corresponds to the coordinate of about 85 bar and about 18 0 C , denoted by [START] in the diagram of figure 3b.
  • the isentropic trajectory along arrow A' is in the vapour region (I)
  • the isentropic trajectory along arrow B' is in the vapour/liquid coexistence region (III).
  • a meta-stable state in the liquid/vapour regime may be reached while following arrow B', until phase transition occurs at a certain super-cooled condition.
  • the resulting condensation process will then restore equilibrium conditions.
  • the fluid stream is separated by the cyclonic fluid separator 1 in a carbon dioxide enriched fluid stream and a carbon dioxide depleted fluid stream at the end of the expansion trajectory denoted by arrow C, a process described above with reference to Figure 1.
  • the separated, carbon dioxide enriched fluid is in a state of non-equilibrium, which will only last for a limited period of time, in the order of 10 milliseconds. Therefore the carbon dioxide enriched fluid is recompressed in the diverging outlet section 5 of the cyclonic fluid separator 1 and discharged via the second outlet 7 to the separation vessel 21, preferably within said time period that the meta-stable state exists. A breakdown of said meta-stable state results in solid carbon dioxide formation from the liquefied part of the fluid stream. As a result of the solidification of carbon dioxide, latent heat is released causing the temperature of the fluid to rise.
  • the separated, carbon dioxide enriched fluid entering the separation vessel 21, may be cooled in order to ensure that the fluid remains in the vapour/solid or vapour/liquid/solid coexistence region. Said process of cooling and recompressing the carbon dioxide enriched fluid is denoted by arrow D'.
  • the process of solidification takes place in the separation vessel 21.
  • the state of the fluid at a newly developed equilibrium within the separation vessel 21 is denoted as [END].
  • solidified carbon dioxide is removed through the third outlet 28 as described above.
  • the maximum carbon dioxide solid fraction for a given temperature T is obtained at a pressure P intersecting the phase boundary between regions LVC (IVb) and VC (Iva).
  • the function of the separation vessel 21 is to remove a maximum amount of carbon dioxide in the solid phase. Therefore, according to an embodiment, the separation vessel 21 is operated at a pressure P and a temperature T at or close to the phase boundary between regions LVC (IVb) and VC (IVa). This phase boundary is shown in Fig.'s 3a and 3b.
  • the term "close to the phase boundary" is used to indicate a margin in the temperature of ⁇ 5°C with respect to the indicated phase boundary and a margin in the pressure of ⁇ 2 or ⁇ 5bar or a margin of 10% or 20% with respect to the indicated phase boundary.
  • the separation vessel 21 is operated at a pressure P within 5 bar and at a temperature T within 5°C within the phase boundary between regions LVC (IVb) and VC (IVa).
  • This conditions may be controlled by controlling the pressure and temperature within the separation vessel 21.
  • the temperature in the separation vessel 21 may be controlled by using cooling arrangement 31.
  • the pressure in the separation vessel 21 may be controlled by a pressure regulating valve which is located in the gas outlet stream 29.
  • the separation vessel 21 is operated at a pressure and temperature combination that is at or in the vicinity of the phase boundary between the vapour/liquid/solid coexistence region (IVb) and the vapour/solid coexistence region (IVa).
  • the separation vessel 21 may be operated at a pressure in the range of 5 - 25 bar.
  • the proposed temperate range for these examples is in the range of -70 0 C to -90 0 C.
  • Fig.' s 4, 5 and 6 schematically depict a further embodiment, in which the screw conveyor or scroll type discharger 35 is replaced with a perforated screen 40.
  • Fig. 4 shows a side-view of such a perforated screen 40
  • Fig. 5 shows a top view of such a perforated screen according to a possible embodiment.
  • Fig. 6 schematically depicts such a perforated screen 40 in combination with separation vessel 21.
  • the solidified carbon dioxide is removed from the separation vessel 21 by means of a perforated screen 40 comprising tapered
  • the perforated screen 41 may be heated and a pressure difference may be maintained between a feed side 42 and a collection side 43, such that the pressure at the feed side is always higher than or equal to the pressure at the collection side.
  • the perforated screen 40 may be provided with a plurality of perforations or openings 41.
  • the openings 41 may be rectangular openings, openings formed as slots, or may be circular openings as shown in Fig. 5.
  • the solidified carbon dioxide particles that leave the separation vessel 21 through the third outlet 28 are transported to the feed side 42 of the perforated screen 40, as shown in Fig. 4.
  • the solidified carbon dioxide particles are transported through the openings 41 from the feed side 42 to the collection side 43 of the perforated screen 40.
  • the size and shape of the openings 41 are such that, in use, the solidified carbon dioxide particles fill the openings 41 and form a layer of solidified carbon dioxide, thereby preventing transport of gases and liquids from the collection side 43 to the feed side 42.
  • the openings 41 may be provided with a tapered shape or conical shape, i.e. the openings 41 are provided with a cross section at the feed side 41 that is larger than a cross section of the opening 41 at the collection side 43. This is shown in Fig. 4.
  • An angle of convergence ⁇ of these openings 41 can be in the range of 5° and 30° with respect to a longitudinal axis 44 of the opening 41. According to a further embodiment, the angle of convergence ⁇ of the openings 41 is in the range of 10° and 20°.
  • the typical inlet size D42 of the opening 41 (e.g. the diameter for circular openings 41) at the feed side 42 of the perforated screen 40 may be at least 2 times the typical grain size of the solidified carbon dioxide.
  • the typical outlet size D43 of the opening 41 (e.g. the diameter for circular openings 41) at the collection side 43 may be approximately equal to the mean grain size of the solidified carbon dioxide. However, according to a further embodiment, the typical outlet size D43 of the opening 41 at the collection side 43 is substantially smaller than the mean grain size of the solidified carbon dioxide.
  • the diameter D43 of a circular opening 41 at the outlet side can range from 0.5 to 5 mm though is preferably between 1 and 3 mm.
  • the depth D41 of the openings 41 measured in the direction of longitudinal axis 44 may typically be two times the inlet size D42 of the opening 41. However, the depth D41 of the openings 41 may also be more than two times the inlet size D42 of the opening 41. Preferably the depth D41 is less than 5 times the inlet size D42.
  • the tapered shape and dimensions of the openings 41 allow a dense packing of solidified carbon dioxide particles to form in and possibly above the openings 41.
  • the solidified carbon dioxide particles will be present in the openings 41 and on top of the perforated screen 40.
  • the dense packing of solidified carbon dioxide particles have a relatively low porosity and ensure that no leak paths are present for gases or liquids to seep through from the feed side 42 towards the collection side 43.
  • Furthermore blocking said leak paths in order to obtain an impermeable layer of solidified carbon dioxide at the perforated screen 40 may be established by providing means to apply static head to the solidified carbon dioxide grains.
  • head is used to refer to a column or layer of liquid and solids which result in pressure on the dsolids on the perforated screen 40.
  • the solidified carbon dioxide particles are melted from the collection side 43. This may be accomplished by maintaining a suitable temperature T43 at the collection side 43 and/or maintaining a suitable pressure P43 at the collection side 43.
  • the collection pressure P43 at the collection side 43 is controlled at a pressure which is typically 2 bar lower than a pressure P42 at the feed side 42 and in the separation vessel 21. So, in case the separation vessel 21 is operated at a pressure of 20 bar, the pressure P42 at the feed side is approximately equal to 20 bar and the pressure P43 at the collection side may be controlled to be approximately 10 - 18 bar.
  • the temperature T43 at the collection side 43 of the perforated screen 40 may be chosen such that given the relevant pressure, the carbon dioxide is in a liquid phase. For instance for a pressure of typically 10 - 18 bar, a temperature may be chosen between approximately -55°C and 0 0 C.
  • the temperature at the collection side may be controlled by a temperature arrangement (not shown) or by an arrangement that heats the perforated screen to a desired temperature within the liquid phase of carbon dioxide to melt off liquid carbon dioxide from the perforated screen 40.
  • the above described embodiment provides an efficient way of separating carbon dioxide.
  • the carbon dioxide is separated from for instance methane (that would otherwise mix with carbon dioxide in liquid phase).
  • the carbon dioxide is available in liquid phase, allowing easy further transportation and processing.
  • a solid carbon dioxide barrier is provided between the feed side 42 and the collection side 43 allowing controlling the collection side and the separation side at different conditions (pressure/temperature).
  • Figure 7 shows a further embodiment.
  • the vessel 21 may be equipped with one or more inlets 25 which are positioned tangent to the perimeter of the vertical section 22, such that a rotational flow in section 22 results. Furthermore the top gas outlet 29 may extent as a vertical pipe in said vertical section 22 as to form a so-called vortex finder. The edge of said vortex finder is at a vertical lower position compared to the vertical position of the inlet(s) 25.
  • the sections 22 and 23 of vessel 21 may be physically separated by a conical shaped deflector plate or vortex breaker 30 of which the outer perimeter has a clearance C with respect to the inner perimeter of the vertical section 22.
  • This clearance C can range typically from 0.05 to 0.3 times the inner diameter of section 22.
  • the vortex breaker 30 breaks the rotational motion of the flow from the first section 22 to the collection tank 23, to prevent eddies to be formed in the collection tank 23.
  • the vortex breaker may prevent gaseous components to travel from the vertical section 22 into the collection tank 23 and deflects these gaseous components towards the top gas outlet 29.
  • the perforated screen 40 is now provided as part of the collection tank 23.
  • a layer of CO2 will form on top of the perforated screen 40.
  • An overflow wall 34 is formed to provide an overflow connection.
  • the overflow connection allows liquids that will typically form on top of the layer of CO2 to pass the overflow wall 34 and leave the collection tank 23 via fourth outlet 26.
  • Fig. 8a schematically depicts a further embodiment.
  • Fig. 8a depicts a vessel 21 and two cyclonic fluid separators 1 as described above. However, it will be understood that instead of two, any suitable number of cyclonic fluid separators 1 may be provided.
  • the fluid separation assembly further comprises a feedback conduit 81 that is on one side connected to the fourth outlet 26 and on the other side connected to a feedback inlet of the cyclonic fluid separator 1.
  • the feedback conduit 81 further comprises a pump PU.
  • the carbon dioxide enriched hydrocarbon liquid components that flow via the fourth outlet 26 are pumped by means of the pump PU through the feedback conduit 81 to the feedback inlet of the one or more cyclonic fluid separators 1.
  • the feedback inlet is upstream of the pear-shaped central body 11 and coincides with the 'normal' inlet 82 of the cyclonic fluid separators 1.
  • the feedback inlet may also be provided at another position, for instance halfway the cyclonic fluid separator 1.
  • a feedback conduit 81 By providing such a feedback conduit 81, it is possible to achieve partial or even complete solidification of the CO2, without the need of additional cooling in the vessel 21 where the temperature reaches its lowest value. Instead the carbon dioxide enriched hydrocarbon liquid stream is first pumped to the feed pressure and combined with the stream of conduit 82 to form a new feed stream transport indicated as the conduit 81+82, where after said combined feed stream may be cooled to a new temperature which is lower than the temperature in conduit 82 and higher than the temperature level present in the vessel 21. Typically the difference between the feed stream temperature in conduit 81+82 and the temperature in vessel 21, is 25 degrees C.
  • a cooling unit 85 may be provided in conduit 81+82, as shown in Fig. 8b.
  • the first outlets 6 of the cyclonic fluid separators 1 may be combined together with the fifth outlet 29 of the tubular section 22 to form an outlet 83.
  • the fluid through the inlet 81 of the cylonic fluid separator 1 may comprise approximately 70% CO 2 and 30%C x Hy, while the outlet 83 may comprise approximately 15% CO 2 and 85%C x H y .
  • a cyclonic fluid separator comprising a throat portion arranged between a converging fluid inlet section and a diverging fluid outlet section and a swirl creating device configured to create a swirling motion of the carbon dioxide containing fluid within at least part of the cyclonic fluid separator, the converging fluid inlet section comprising a first inlet for fluid components and the diverging fluid outlet section comprising a first outlet for carbon dioxide depleted fluid and a second outlet for carbon dioxide enriched fluid;
  • a separation vessel having a first section in connection with a collecting tank, said first section being provided with a second inlet connected to said second outlet of said cyclonic fluid separator, and said collecting tank being provided with a third outlet for solidified carbon dioxide;
  • the collection side 43 may be operated at a temperature and pressure combination for which carbon dioxide is liquid.
  • the feed side 42 may be operated at a first pressure and the collection side 43 may be operated at a second pressure, the second pressure being equal or lower than the first pressure.
  • the temperature at the collection side 43 may be in the range of minus 55°C - 0 0 C, and higher than at feed side 42.
  • the openings 41 have an inlet size D42 at the feed side 42 that is greater than an outlet size D43 at the collection side 43.
  • the outlet size D43 may be approximately equal to or substantially smaller than the grain size of solidified carbon dioxide.

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Abstract

La présente invention concerne un procédé d'élimination du dioxyde de carbone présent dans un flux de fluide au moyen d'un ensemble séparateur pour fluides. L'ensemble séparateur pour fluides comporte un séparateur cyclonique pour fluides comportant une partie tubulaire haute disposée entre une partie d'alimentation en fluide convergente et une partie d'évacuation du fluide divergente, ainsi qu'un dispositif de tourbillonnement. Le récipient séparateur comporte une partie tubulaire située sur une cuve de collecte et en communication avec elle. Dans ce procédé, on utilise un flux de fluide contenant du gaz carbonique qui est soumis à un mouvement tourbillonnaire induisant un mouvement centrifuge. Le flux de fluide tourbillonnant est ensuite dilaté de façon à ce que les composants du dioxyde de carbone se retrouvent à l'état méta-stable au sein du flux de fluide. Par la suite, le flux de fluide centrifuge comportant les composants du dioxyde de carbone est extrait du séparateur cyclonique pour fluides et amené, sous la forme d'un mélange, jusqu'au récipient séparateur. Le mélange est ensuite acheminé à travers la partie tubulaire en direction de la cuve de collecte dans des conditions de traitement assurant la formation de dioxyde de carbone solide. Enfin, on procède à l'extraction du dioxyde de carbone solidifié.
PCT/NL2009/050388 2008-12-22 2009-07-01 Procédé d'élimination du dioxyde de carbone présent dans un flux de fluide et ensemble séparateur pour fluides WO2011002277A1 (fr)

Priority Applications (8)

Application Number Priority Date Filing Date Title
PCT/NL2009/050388 WO2011002277A1 (fr) 2009-07-01 2009-07-01 Procédé d'élimination du dioxyde de carbone présent dans un flux de fluide et ensemble séparateur pour fluides
CA2748128A CA2748128C (fr) 2008-12-22 2009-12-18 Procede d'elimination du dioxyde de carbone d'un flux de fluide et ensemble de separation de fluide
PCT/NL2009/050781 WO2010074565A1 (fr) 2008-12-22 2009-12-18 Procédé d'élimination du dioxyde de carbone d'un flux de fluide et ensemble de séparation de fluide
CN200980156303.XA CN102307642B (zh) 2008-12-22 2009-12-18 从流体流中去除二氧化碳的方法以及流体分离装置
EA201170870A EA020177B1 (ru) 2008-12-22 2009-12-18 Способ удаления диоксида углерода из потока текучей среды и устройство для разделения текучей среды
MYPI2011002936A MY155298A (en) 2008-12-22 2009-12-18 Method of removing carbon dioxide from a fluid stream and separation assembly
US13/141,408 US20120017638A1 (en) 2008-12-22 2009-12-18 Method of removing carbon dioxide from a fluid stream and fluid separation assembly
AU2009330799A AU2009330799B2 (en) 2008-12-22 2009-12-18 Method of removing carbon dioxide from a fluid stream and fluid separation assembly

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PCT/NL2009/050388 WO2011002277A1 (fr) 2009-07-01 2009-07-01 Procédé d'élimination du dioxyde de carbone présent dans un flux de fluide et ensemble séparateur pour fluides

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WO2013033425A1 (fr) 2011-08-31 2013-03-07 Alliant Techsystems Inc. Système d'extraction inertiel
EP3628951A1 (fr) * 2018-09-26 2020-04-01 Hysytech S.r.l. Séparateur flash pour le traitement d'un mélange liquide contenant du méthane liquéfié et du dioxyde de carbone de gaz et installation de production de biométhane ou de gaz naturel liquéfié comprenant un tel séparateur flash
US10987443B1 (en) 2020-07-03 2021-04-27 Chio Kang Medical, Inc. Container sterilization device and system, assembling method thereof, and use thereof
US11085016B1 (en) 2020-01-20 2021-08-10 Chio Kang Medical, Inc. Method for screening bacteria capable of degrading ethylene oxide
US11103829B1 (en) 2020-03-18 2021-08-31 Chio Kang Medical, Inc. Systems and methods for treating ethylene oxide waste gas
US11103608B1 (en) 2020-07-03 2021-08-31 Chio Kang Medical, Inc. Mobile pretreatment apparatus and an operating method thereof, and a mobile analysis apparatus and an operating method thereof
US11110390B1 (en) 2020-03-18 2021-09-07 Chio Kang Medical, Inc. Systems and methods for treating sterilization exhaust gas containing ethylene oxide
US11123680B1 (en) 2020-03-18 2021-09-21 Chio Kang Medical, Inc. Devices, systems, and methods for treating ethylene oxide waste gas
US11123449B1 (en) 2020-07-03 2021-09-21 Chio Kang Medical, Inc. Mobile sterilization system, mobile execution system, and mobile analysis system
US11124438B2 (en) 2020-01-20 2021-09-21 Chio Kang Medical, Inc. Alcaligenes faecalis for degrading ethylene oxide
US11125498B1 (en) 2020-03-18 2021-09-21 Chio Kang Medical, Inc. Gas liquefaction separator, gas liquefaction recovery system, and method for separating and recovering ethylene oxide
US20210291105A1 (en) 2020-03-19 2021-09-23 Chio Kang Medical, Inc. Ethylene Oxide Adsorption Tower and Recovery System, and Method for Recovering Ethylene Oxide
WO2021184594A1 (fr) * 2020-03-18 2021-09-23 Qiaokang Biotech (Guangdong) Co., LTD. Séparateur de liquéfaction de gaz, système de récupération de liquéfaction de gaz et procédé de séparation et de récupération d'oxyde d'éthylène
US11130095B1 (en) 2020-03-18 2021-09-28 Chio Kang Medical, Inc. Sterilization exhaust gas treating system and method for treating ethylene oxide-containing sterilization exhaust gas by using the same
US11130939B2 (en) 2020-01-20 2021-09-28 Chio Kang Medical, Inc. Bacteria for degrading ethylene oxide and uses thereof
US11136253B1 (en) 2020-03-18 2021-10-05 Chio Kang Medical, Inc. Microbiological treatment system for ethylene oxide exhaust gas
US11220667B2 (en) 2020-01-20 2022-01-11 Chio Kang Medical, Inc. Bacteria for degrading ethylene oxide and applications thereof
CN114345017A (zh) * 2020-10-12 2022-04-15 北京星油科技有限公司 旋流式分离器
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

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US9283502B2 (en) 2011-08-31 2016-03-15 Orbital Atk, Inc. Inertial extraction system
WO2013033425A1 (fr) 2011-08-31 2013-03-07 Alliant Techsystems Inc. Système d'extraction inertiel
EP3628951A1 (fr) * 2018-09-26 2020-04-01 Hysytech S.r.l. Séparateur flash pour le traitement d'un mélange liquide contenant du méthane liquéfié et du dioxyde de carbone de gaz et installation de production de biométhane ou de gaz naturel liquéfié comprenant un tel séparateur flash
US11124438B2 (en) 2020-01-20 2021-09-21 Chio Kang Medical, Inc. Alcaligenes faecalis for degrading ethylene oxide
US11220667B2 (en) 2020-01-20 2022-01-11 Chio Kang Medical, Inc. Bacteria for degrading ethylene oxide and applications thereof
US11085016B1 (en) 2020-01-20 2021-08-10 Chio Kang Medical, Inc. Method for screening bacteria capable of degrading ethylene oxide
US11130939B2 (en) 2020-01-20 2021-09-28 Chio Kang Medical, Inc. Bacteria for degrading ethylene oxide and uses thereof
US11103829B1 (en) 2020-03-18 2021-08-31 Chio Kang Medical, Inc. Systems and methods for treating ethylene oxide waste gas
US11136253B1 (en) 2020-03-18 2021-10-05 Chio Kang Medical, Inc. Microbiological treatment system for ethylene oxide exhaust gas
US11123680B1 (en) 2020-03-18 2021-09-21 Chio Kang Medical, Inc. Devices, systems, and methods for treating ethylene oxide waste gas
US11110390B1 (en) 2020-03-18 2021-09-07 Chio Kang Medical, Inc. Systems and methods for treating sterilization exhaust gas containing ethylene oxide
US11125498B1 (en) 2020-03-18 2021-09-21 Chio Kang Medical, Inc. Gas liquefaction separator, gas liquefaction recovery system, and method for separating and recovering ethylene oxide
US11130095B1 (en) 2020-03-18 2021-09-28 Chio Kang Medical, Inc. Sterilization exhaust gas treating system and method for treating ethylene oxide-containing sterilization exhaust gas by using the same
WO2021184594A1 (fr) * 2020-03-18 2021-09-23 Qiaokang Biotech (Guangdong) Co., LTD. Séparateur de liquéfaction de gaz, système de récupération de liquéfaction de gaz et procédé de séparation et de récupération d'oxyde d'éthylène
US11129914B1 (en) 2020-03-19 2021-09-28 Chio Kang Medical, Inc. Ethylene oxide adsorption tower and recovery system, and method for recovering ethylene oxide
US20210291105A1 (en) 2020-03-19 2021-09-23 Chio Kang Medical, Inc. Ethylene Oxide Adsorption Tower and Recovery System, and Method for Recovering Ethylene Oxide
US11103608B1 (en) 2020-07-03 2021-08-31 Chio Kang Medical, Inc. Mobile pretreatment apparatus and an operating method thereof, and a mobile analysis apparatus and an operating method thereof
US11123449B1 (en) 2020-07-03 2021-09-21 Chio Kang Medical, Inc. Mobile sterilization system, mobile execution system, and mobile analysis system
US10987443B1 (en) 2020-07-03 2021-04-27 Chio Kang Medical, Inc. Container sterilization device and system, assembling method thereof, and use thereof
CN114345017A (zh) * 2020-10-12 2022-04-15 北京星油科技有限公司 旋流式分离器
CN114345017B (zh) * 2020-10-12 2023-02-07 北京星油科技有限公司 旋流式分离器
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
CN115678628B (zh) * 2022-10-13 2024-05-10 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

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