US20120137728A1 - Auto-refrigerated gas separation system for carbon dioxide capture and compression - Google Patents

Auto-refrigerated gas separation system for carbon dioxide capture and compression Download PDF

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Publication number
US20120137728A1
US20120137728A1 US13/389,909 US201013389909A US2012137728A1 US 20120137728 A1 US20120137728 A1 US 20120137728A1 US 201013389909 A US201013389909 A US 201013389909A US 2012137728 A1 US2012137728 A1 US 2012137728A1
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stream
liquid
carbon dioxide
gas stream
passing
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Kourosh Zanganeh
Ahmed Shafeen
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Canada Minister of Natural Resources
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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
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • 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
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/70—Flue or combustion exhaust gas
    • 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
    • F25J2215/02—Mixing or blending of fluids to yield a certain product
    • 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
    • F25J2215/80—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
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/80—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/90—Hot gas waste turbine of an indirect heated gas for power generation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • 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
    • F25J2280/10—Control for or during start-up and cooling down of the installation
    • 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 systems for capturing and separating carbon dioxide from mixed gas streams.
  • the invention relates to an auto-refrigerated system and method for separating carbon dioxide using multiple compression, intercooling and condensates separation stages, and selective gas recycling.
  • the objective of carbon dioxide capture is to address the increasing problem of the effects of the emission of carbon dioxide (a greenhouse gas) into the atmosphere, by separating carbon dioxide from gaseous products of various processes, and deliver the separated carbon dioxide for further use, processing, and storage.
  • carbon dioxide a greenhouse gas
  • Oxy-fuel combustion provides an advantageous approach to carbon dioxide capture, whereby combustion takes place in an oxygen-enriched environment, thus producing a flue gas stream which is rich in carbon dioxide, and thus can readily be captured and compressed using non-solvent based processes, such as low-temperature gas separation, for pipeline transport.
  • non-solvent based processes such as low-temperature gas separation, for pipeline transport.
  • a typical capture plant consists of a pre-cleaning stage, a compression stage and a liquefaction stage. In the pre-cleaning stage the inlet gas stream is cleaned of solid particles and/or impurities such as mercury, SO x , etc., and then is passed through an initial demister unit before entering the compression stage.
  • the gas stream is compressed, cooled (which may be in multiple stages and forms condensates that can be removed in condensate separator vessels), and then passed through a drier, to further dry the gas stream.
  • the gas stream is further cooled for liquefying the carbon dioxide and separating it from non-condensable gases to form the carbon dioxide product stream.
  • the non-condensable gases such as argon and oxygen or nitrogen, are vented along with a small percentage of carbon dioxide in gaseous form to the atmosphere. Some systems partially vent non-condensable gases through the dryer to assist regeneration of the dryer material.
  • the carbon dioxide may be sent to insulated storage tanks, used directly, or transported in a pipeline or other means of transportation for underground storage.
  • the present invention provides a system of carbon dioxide capture from a mixed gas stream input, and methods of operating the system, and provides various configurations and options for the system and methods.
  • the carbon dioxide rich feed gas is sent to a low temperature separation unit of the invention, and carbon dioxide is liquefied and separated as the primary product, while non-condensable impurities are separated as a vent and sent for further processing or to the atmosphere.
  • the incoming carbon dioxide-rich gas stream is preferably pretreated as necessary to remove specifically targeted solid particles and/or impurities such as particulates, mercury, and SO x .
  • the incoming gas stream is preferably also dried after compression and before recovery of the carbon dioxide, in the process which includes compression and cooling at different stages with removal of condensates, and subsequent liquefaction and separation of the carbon dioxide as the product stream, while using the energy from the compressed gas stream to provide cooling to earlier stages, and recycling of part of the compressed gas stream, without the need for any external cooling, thus providing significant commercial and technical advantage over the prior art.
  • the system of the present invention is capable of handling a feed gas stream with a carbon dioxide concentration at least as low as 30%, and preferably higher, up to and exceeding 90%. It has been found that for carbon dioxide concentrations of the feed gas stream anywhere between 30% and 90%, the carbon dioxide purity in the product stream remains at least 94%, more specifically in some cases greater than 97%, and more specifically in few cases greater than 99%.
  • the system is operated with a maximum pressure not exceeding about 35 to 45 bar absolute, for the purpose of energy savings and overall efficiency, and in some cases preferably 25 bar to 35 bar absolute.
  • the invention therefore seeks to provide a method for separating carbon dioxide from a mixed gas stream, the method comprising the steps of:
  • step (j) throttling selected portions of the separated liquid carbon dioxide stream from step (d) and/or step (e) to provide cooling to the processing structure;
  • the method further comprises a start-up operation wherein step (e) further comprises diverting a selected portion of the mixed liquid carbon dioxide stream through a second mixer and a second one of the heat exchangers before removing the diverted portion from the processing structure in step (f).
  • the method can further comprise prior to step (c) the step of (b.1) pre-treating the mixed gas stream by removing at least one of water, particulate matter, mercury and other heavy metals, hydrogen chloride, hydrogen fluoride, nitrogen oxides, sulphur oxides and other sulphur derivatives from the mixed gas stream.
  • the invention seeks to provide a method for separating carbon dioxide from a mixed gas stream, the method comprising the steps of:
  • the method further comprises after step (o) the step of:
  • the method further comprises after step (o) the step of:
  • the method further comprises after step (b), the step of:
  • the method further comprises a start-up operation comprising the steps of
  • the start-up operation further comprises after step (B.2) the step of:
  • the method further comprises matching the pressure of the first pressurized product stream and the second pressurized product stream.
  • the invention seeks to provide a method for separating carbon dioxide from a mixed gas stream, the method comprising the steps of:
  • the method further comprises after step (q) the step of:
  • the method further comprises after step (q) the steps of:
  • the method further comprises after step (b), the step of:
  • the method further comprises after step (s) the step of:
  • the method further comprises prior to step (b) the step of:
  • the method further comprises after step (m) the step of:
  • the method further comprises a start-up operation comprising the steps of
  • start-up operation further comprises after step (s) the step of:
  • step (t.1) raising the pressure of the second product stream to a higher set pressure to form a second pressurized product stream; and after step (B.2) the step of:
  • the method can further comprise selectively removing oxygen from selected ones of each of the product streams before removing the selected product stream from the processing structure.
  • the pressurizing means preferably comprises a pump.
  • the fourth gas stream can be expanded in a vent stream turbo-expander to recover energy and to form a vent stream comprising impurities and residual carbon dioxide.
  • vent stream can be split into a first vent stream branch and a second vent stream branch; preferably the first vent stream branch is passed through the first heat exchanger to use the residual cooling capacity of the said stream, the compressed gas stream is passed through a first additional heat exchanger, the first vent stream branch is passed through the first additional heat exchanger, and the second gas stream branch and the second vent stream branch are each passed through a second additional heat exchanger.
  • the second gas stream branch can be expanded in a main turbo-expander to recover energy, and to produce the third two-phase flow.
  • this expanding can be performed in sequence through a Joule-Thompson throttle valve and a chiller.
  • the methods further comprise raising the pressure of the product stream to higher set pressure to form a pressurized product stream.
  • the invention seeks to provide a system for separating carbon dioxide from a mixed gas stream, the system comprising a processing structure including:
  • the system further comprises a second mixer means for receiving and transferring a selected portion of the mixed liquid carbon dioxide stream in a start-up operation.
  • the system further comprises at least one pre-treatment means for removing from the mixed gas stream at least one of water, particulate matter, mercury and other heavy metals, hydrogen chloride, hydrogen fluoride, nitrogen oxides, sulphur oxides and other sulphur derivatives from the mixed gas stream.
  • at least one pre-treatment means for removing from the mixed gas stream at least one of water, particulate matter, mercury and other heavy metals, hydrogen chloride, hydrogen fluoride, nitrogen oxides, sulphur oxides and other sulphur derivatives from the mixed gas stream.
  • the system further comprises oxygen removal means for selectively removing oxygen from at least one carbon dioxide stream.
  • FIG. 1 is a schematic representation of a first embodiment of the invention
  • FIGS. 2 and 3 are schematic representations showing further features of the embodiment of FIG. 1 ;
  • FIG. 4 is a schematic representation of a second embodiment of the. invention.
  • FIGS. 5 and 6 are schematic representations showing further features of the embodiment of FIG. 4 ;
  • FIGS. 7 to 10 are schematic representations showing further features of embodiments of the invention.
  • FIG. 11 is a schematic representation of a start-up feature in a third embodiment of the invention.
  • FIG. 12 is a schematic representation of a fourth embodiment of the invention.
  • FIG. 13 is a schematic representation of a fifth embodiment of the invention.
  • FIGS. 1 to 3 a first embodiment of the method and system of the invention is shown schematically, FIGS. 2 and 3 showing variants of the pathways depicted in FIG. 1 .
  • the inlet carbon dioxide rich gas stream enters the process structure as inlet feed gas in path 1 , and is compressed in compressor module CM 1 , and substantially dehydrated in dryer module D 1 .
  • the compressor block must consist of a minimum of two compression stages, preferably three or four, with intercoolers and condensate separators.
  • Dryer module D 1 can comprise any suitable dryer system, such as a molecular sieve, where the process gas will not be contaminated but only be dried, to achieve a water dew point temperature equal to or lower than the gas stream temperature in path 9 . In the event that this dew point temperature is not practical for any reason, based on factors such as cost or equipment, the next acceptable temperature to be used is the dew point temperature at path 21 .
  • the gas stream proceeds in path 3 to the heat exchanger E 1 , where it is cooled, leading to a two-phase flow in path 4 , from heat exchanger E 1 to separator S 1 , where the two phases are separated.
  • the gas stream leaving separator S 1 passes in path 5 to splitter SP 1 , where it is split into two branches as follows.
  • the first branch flows in path 23 to and through heat exchanger E 2 , leaving in path 6 as a two phase flow, into separator S 2 .
  • the gas stream leaving separator S 2 consists of non-condensable gas phase impurities, such as argon, nitrogen, oxygen, and possibly NO x and SO x , and residual carbon dioxide, which have remained in the gaseous state.
  • This stream flows in path 7 to and through heat exchanger E 2 , and from heat exchanger E 2 in path 14 to heat exchanger E 1 and flows therefrom in path 15 to be exhausted to atmosphere by any suitable means (not shown) through a vent with or without a silencer in path 15 .
  • the liquid stream leaving separator S 2 flows in path 8 to and through heat exchanger E 2 to mixer M 2 , where it is mixed with flow in path 18 a, discussed below, and the mixed stream flows in path 9 through throttle valve TV 2 , back through heat exchanger E 2 , and flows in path 10 to heat exchanger E 1 , and leaves the system as in path 11 as a product stream.
  • the second branch from splitter S 1 flows in path 19 to and through expander module EM 1 , and as the gas passes through expander module EM 1 it cools resulting in a two phase flow to separator S 3 .
  • expander module EM 1 allows for the production of necessary cooling for liquefaction in the system, and also for additional shaft output work, thereby enhancing the overall energy balance and improving the efficiency of the process.
  • separator S 3 the gas and liquid phases are separated.
  • the gas stream leaving separator S 3 flows in path 21 through heat exchanger E 1 , leaving heat exchanger E 1 in path 22 , and is recycled back to an appropriate selected location in the compressor module CM 1 . This location must be subsequent to the inlet of path 1 into the compressor module CM 1 , i.e. the gas stream in path 22 must be returned to one of the intermediate compression stages within compressor module CM 1 .
  • the liquid stream from separator S 3 flows in path 20 to pump P 1 , where its pressure is raised to match that of the liquid stream leaving separator S 1 in path 12 .
  • the liquid stream in path 12 and the liquid stream leaving pump P 1 in path 20 are combined in mixer M 1 .
  • the combined liquid streams flow from mixer M 1 in path 18 a to mixer M 2 , to be mixed with the flow in path 8 from separator S 2 and heat exchanger E 2 , to flow in path 9 as described above. This diversion which takes place in path 18 a allows for the maximum cooling effect from the throttling process occurring in path 9 .
  • This configuration provides only one product stream, i.e. the flow in path 11 , from the overall process, which allows for simplification of the carbon dioxide product piping, and of the multi-pass design for heat exchanger E 1 .
  • FIG. 2 is a schematic representation of a high purity configuration as a variant of the configuration of FIG. 1 .
  • an additional separator Sb is added to path 9 down stream of throttle valve TV 2 .
  • the liquid stream from the separator Sb is a highly pure carbon dioxide product stream, which flows in paths 10 and 11 , as in the configuration shown in FIG. 1 .
  • the gaseous stream leaving separator Sb is recycled back in path 25 to the compressor module CM 1 .
  • FIG. 3 is a schematic representation of a high purity configuration as a further variant of the configuration of FIG. 1 .
  • an additional separator Sb is provided to path 9 down stream of throttle valve TV 2 in the same way as in FIG. 2 , and the liquid stream from the separator Sb flows in paths 10 and 11 as in the configurations shown in FIGS. 1 and 2 .
  • the gaseous stream from separator Sb flows in path 25 to an additional compressor, compressor module CMb, where it is further compressed.
  • the compressed stream leaving compressor module CMb flows to mixer M 4 , where it is combined with the outlet stream flowing in path 3 from dryer module D 1 , and the mixed flow passes from mixer M 4 into heat exchanger E 1 .
  • the configuration of FIG. 3 produces the same high purity of carbon dioxide in the product stream in path 11 as in the configuration of FIG. 2 , but the configuration of FIG. 3 provides more flexibility to the overall operation of the high purity variant processes.
  • FIGS. 4 to 6 a second embodiment of the method and system of the invention is shown schematically, FIGS. 5 and 6 showing variants of the pathways depicted in FIG. 4 .
  • the flow from mixer M 1 in path 18 a is diverted to mixer M 2 , as in the configuration shown in FIGS. 1 to 3 .
  • the combined stream leaving mixer M 2 in path 8 flows to splitter SP 2 , where it is divided into two streams, flowing in paths 9 and 27 respectively.
  • the stream in path 9 follows the same path as in the embodiment shown in FIGS. 1 to 3 , to generate the carbon dioxide product stream in paths 10 and 11 .
  • the stream flowing from splitter SP 2 in path 27 passes through throttle valve TVc, and provides cooling energy to heat exchanger E 1 , before exiting the process as a second carbon dioxide product stream in path 13 .
  • FIG. 5 is a schematic representation of a variant of the configuration of FIG. 4 , in which two separators, Sc and Sd are added to the down stream flows in paths 9 and 27 , respectively.
  • the liquid stream from separator Sc flows in path 10 as a highly pure carbon dioxide product stream; similarly the liquid stream flowing from separator Sd in paths 28 and 13 is a highly pure carbon dioxide product streams.
  • the gaseous streams (Stream 26 and Stream 29 ) from each of separators Sc and Sd in paths 26 and 29 , respectively, are recycled back to the compressor module CM 1 , again at an intermediate stage, via mixer M 5 .
  • FIG. 6 is a schematic representation of a variant of the configuration of FIG. 5 , in which the gaseous streams in paths 26 and 29 from the separators Sc and Sd, respectively, are compressed by an additional compressor module CMc.
  • the compressed stream from compressor module CMc flows in path 30 to be combined with the outlet stream flowing in path 3 from dryer module DM 1 in mixer M 6 , before entering into heat exchanger E 1 .
  • This option provides the same purity of carbon dioxide in the product streams in paths 11 and 13 , but provides more flexibility to the overall operation of the high purity variant processes.
  • FIGS. 1 to 6 Various options can be provided to the configurations shown in each of FIGS. 1 to 6 . These are illustrated by the schematic representations of FIGS. 7 to 10 .
  • a second expander module EM 2 is added to path 15 on the down stream side of heat exchanger E 1 , to harness more cooling energy and shaft output work, which reduces the overall energy demand and hence increases the overall efficiency of the process.
  • the stream leaving the dryer module D 1 in path 3 can be further cooled by the stream from second expander module EM 2 in path 16 , by the addition of heat exchanger E 1 a.
  • FIG. 7 Also shown in FIG. 7 is the addition of a second compressor module CM 2 to the streams in paths 11 and 13 to increase the pressure of the carbon dioxide product streams in those paths to a level required for e.g. pipeline transportation. Further, considerable heating energy can also be harnessed from the inter-stage cooling of compressor module CM 2 for use in another integrated energy conversion system with which the system of the present invention might be connected.
  • the stream leaving splitter SP 1 in path 19 can be further cooled by the stream in path 16 by the addition of heat exchanger E 2 a.
  • the main features of this option are:
  • splitter SP 2 can be adjusted from 0 to 100% between the streams in paths 16 a and 16 b as desired.
  • the main advantageous features of this option in addition to those listed above in relation to FIGS. 7 and 8 , include the important features
  • the expander module EM 1 which receives the stream which flows in path 19 from splitter SP 1 , can be replaced by a Joule-Thompson Expansion Valve JT- 1 and a chiller CH 1 .
  • This option can be combined with the configurations of any of the options discussed above.
  • FIG. 11 A configuration exemplifying the start up procedure is shown schematically in FIG. 11 .
  • the pressure of the stream in path 20 is increased by any suitable pressure boosting device, such as pump P 1 , to match the pressure of the stream in path 12 , following which the streams from paths 12 and 20 can be combined in mixer M 1 .
  • the combined stream is then diverted proportionally, and the proportion can be varied between 0 and 100% as desired, so as to flow from mixer M 1 in the desired proportions in paths 18 and 18 a.
  • the stream in path 18 a is directed to mixer M 2 , and thence to heat exchanger E 2 throttle valve TV 2 , in path 9 .
  • the stream in path 18 flows from mixer M 1 to throttle valve TV 1 to heat exchanger E 1 and leaves as product in path 13 .
  • This diversion and subsequent throttling provides maximum cooling to produce enough liquid carbon dioxide required for throttling and stabilizing the overall process. Also, this diversion of the portion of the combined streams in paths 12 and 20 which flows in path 18 , balances the overall cooling load to the individual heat exchangers E 1 , E 2 .
  • FIG. 12 this is a schematic representation of a configuration of an embodiment of the invention in which the carbon dioxide purity in the product stream which flows in path 13 can be greater than 98% by volume.
  • an additional separator Sa is added after the throttle valve TV 1 . Liquid from the separator Sa is taken out as a highly pure carbon dioxide product stream in paths 13 or 18 , and the gaseous stream in path 24 is recycled back to the compressor module CM 1 at an intermediate stage of that module.
  • any of the additional optional features described above in relation to FIGS. 7 to 10 can be included in the configuration shown in FIG. 12 .
  • FIG. 13 a further embodiment is shown, in which the exemplary startup operation of FIG. 11 is shown in relation to the embodiment of FIG. 6 .
  • the combined stream in mixer M 1 is diverted proportionally between the stream which flows in path 18 a to mixer M 2 , as described in relation to FIG. 11 , and a second stream, which flows from mixer M 1 to throttle valve Tve, and thence to heat exchanger E 1 , to leave the system as a third product stream in path 11 a.
  • the embodiments described above thus provide for more efficient and cost-effective separation of carbon dioxide from carbon dioxide rich gas streams, by the use of the low-temperature gas separation processes of the invention, including the features described which provide for auto-refrigeration and gas recycling, by providing compression to the inlet gas streams in multiple stages with inter-stage cooling and condensate removal, while using the energy in the compressed gas to provide cooling to the incoming stream, and at the same time using an expansion stage before recycling a portion of the gas back to the compressor, at some intermediate stage within the multiple compression stages.
  • the invention enables the reduction of the overall energy demand and temperature of the process without the use of external refrigeration means, in a simple and compact system, without the disadvantages of known processes and systems, using the novel arrangement of process flow pathways, described above in relation to the exemplary and non-restrictive embodiments, and more fully defined in the appended claims.

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WO2016064267A1 (en) * 2014-10-20 2016-04-28 Haffmans B.V. A process installation for preparing a carbon dioxide (co2) end product from a gaseous carbon dioxide containing starting product
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JP7481698B1 (ja) 2024-02-20 2024-05-13 有限会社入交昭一郎 二酸化炭素分離装置、二酸化炭素分離方法、燃料合成装置および燃料合成方法

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US20160363368A1 (en) 2016-12-15
EP2713129A2 (de) 2014-04-02
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EP2478312A1 (de) 2012-07-25
US11635253B2 (en) 2023-04-25
US20200378680A1 (en) 2020-12-03
EP2478312A4 (de) 2012-12-12
CA2769687A1 (en) 2011-10-20
ES2378610A1 (es) 2012-04-16
WO2011127552A1 (en) 2011-10-20
CA2769687C (en) 2014-12-30
ES2378610B2 (es) 2012-11-06
EP2478312B1 (de) 2018-04-11
EP2713129B1 (de) 2020-10-14

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