CA2771558A1 - Method and device for treating a carbon dioxide-containing gas stream - Google Patents
Method and device for treating a carbon dioxide-containing gas stream Download PDFInfo
- Publication number
- CA2771558A1 CA2771558A1 CA2771558A CA2771558A CA2771558A1 CA 2771558 A1 CA2771558 A1 CA 2771558A1 CA 2771558 A CA2771558 A CA 2771558A CA 2771558 A CA2771558 A CA 2771558A CA 2771558 A1 CA2771558 A1 CA 2771558A1
- Authority
- CA
- Canada
- Prior art keywords
- carbon dioxide
- gas stream
- dioxide content
- liquid
- stream
- Prior art date
- Legal status (The legal status 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 status listed.)
- Abandoned
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F15—FLUID-PRESSURE ACTUATORS; HYDRAULICS OR PNEUMATICS IN GENERAL
- F15B—SYSTEMS ACTING BY MEANS OF FLUIDS IN GENERAL; FLUID-PRESSURE ACTUATORS, e.g. SERVOMOTORS; DETAILS OF FLUID-PRESSURE SYSTEMS, NOT OTHERWISE PROVIDED FOR
- F15B15/00—Fluid-actuated devices for displacing a member from one position to another; Gearing associated therewith
- F15B15/08—Characterised by the construction of the motor unit
- F15B15/10—Characterised by the construction of the motor unit the motor being of diaphragm type
-
- 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
-
- 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
- F25J2215/04—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
- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/32—Compression of the product 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/80—Processes or apparatus involving steps for increasing the pressure of gaseous 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
- 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
- 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
- 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/62—Details of storing a fluid in a tank
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Thermal Sciences (AREA)
- Fluid Mechanics (AREA)
- Carbon And Carbon Compounds (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a method and an apparatus for treating a carbon dioxide-containing gas stream. Precompressed raw gas stream (1) is partially liquefied in a cryogenic carbon dioxide purification stage (2, 3, 4). Part of the resultant liquid is used to obtain a gas stream having an elevated carbon dioxide content (7). From the non--liquefied raw gas, a gas stream having a reduced carbon dioxide content is obtained.
This vent gas stream is expanded and the refrigeration generated is recovered for cooling the raw gas stream. The carbon dioxide gas stream is compressed (8) to a final pressure and fed to further utilization and/or storage. Another part of the liquid from the cryogenic carbon dioxide purification stage is fed in a liquid phase (9) to further utilization and/or storage (10).
This vent gas stream is expanded and the refrigeration generated is recovered for cooling the raw gas stream. The carbon dioxide gas stream is compressed (8) to a final pressure and fed to further utilization and/or storage. Another part of the liquid from the cryogenic carbon dioxide purification stage is fed in a liquid phase (9) to further utilization and/or storage (10).
Description
METHOD AND DEVICE FOR TREATING A CARBON DIOXIDE-CONTAINING GAS
STREAM
Summary of the Invention The invention relates to a method for treating a carbon dioxide-containing gas stream (raw gas stream), in particular a carbon dioxide-containing gas from a large-scale furnace plant. The precompressed raw gas stream is partially liquefied in a cryogenic carbon dioxide purification stage, and the liquid is separated off from which a gas stream having an elevated carbon dioxide content (carbon dioxide gas stream) is obtained by reevaporation. In addition, a gas stream having a reduced carbon dioxide content (vent gas stream) is obtained from the non-liquefied raw gas. This vent gas stream is expanded in at least one expansion turbine and the refrigeration generated in this process is recovered for cooling the raw gas stream. The carbon dioxide gas stream is compressed to a final pressure and fed to further utilization and/or storage.
The invention also relates to an apparatus for carrying out the above-described method.
Carbon dioxide-containing gas streams are produced in all large-scale furnace plants which are operated with fossil fuels such as coal, oil or natural gas.
These include, in particular, power plants, but also industrial furnaces, steam kettles and similar large-scale thermal plants for power and/or heat generation. In addition, carbon dioxide-containing gas streams are also formed in process plants of the chemical or petrochemical industry, such as cracking furnaces of olefin plants or steam reformers of synthesis gas plants. Owing to the harmful climatic effect of carbon dioxide gas, solutions are being sought in order to decrease the emissions of carbon dioxide-containing exhaust gases into the atmosphere.
Very recently, novel power plant concepts are proposed in which the fossil fuel, e.g. coal, is burnt with an oxygen-rich combustion gas, in particular with technically pure oxygen, or with oxygen-enriched air (oxygen combustion gas method). The oxygen fraction of this combustion gas is, e.g., 95 to 99.9% by volume. The resultant exhaust gas, which is also termed flue gas, contains principally carbon dioxide (C02) at a fraction
STREAM
Summary of the Invention The invention relates to a method for treating a carbon dioxide-containing gas stream (raw gas stream), in particular a carbon dioxide-containing gas from a large-scale furnace plant. The precompressed raw gas stream is partially liquefied in a cryogenic carbon dioxide purification stage, and the liquid is separated off from which a gas stream having an elevated carbon dioxide content (carbon dioxide gas stream) is obtained by reevaporation. In addition, a gas stream having a reduced carbon dioxide content (vent gas stream) is obtained from the non-liquefied raw gas. This vent gas stream is expanded in at least one expansion turbine and the refrigeration generated in this process is recovered for cooling the raw gas stream. The carbon dioxide gas stream is compressed to a final pressure and fed to further utilization and/or storage.
The invention also relates to an apparatus for carrying out the above-described method.
Carbon dioxide-containing gas streams are produced in all large-scale furnace plants which are operated with fossil fuels such as coal, oil or natural gas.
These include, in particular, power plants, but also industrial furnaces, steam kettles and similar large-scale thermal plants for power and/or heat generation. In addition, carbon dioxide-containing gas streams are also formed in process plants of the chemical or petrochemical industry, such as cracking furnaces of olefin plants or steam reformers of synthesis gas plants. Owing to the harmful climatic effect of carbon dioxide gas, solutions are being sought in order to decrease the emissions of carbon dioxide-containing exhaust gases into the atmosphere.
Very recently, novel power plant concepts are proposed in which the fossil fuel, e.g. coal, is burnt with an oxygen-rich combustion gas, in particular with technically pure oxygen, or with oxygen-enriched air (oxygen combustion gas method). The oxygen fraction of this combustion gas is, e.g., 95 to 99.9% by volume. The resultant exhaust gas, which is also termed flue gas, contains principally carbon dioxide (C02) at a fraction
2 of approximately 70 to 85% by volume. The purpose of these novel concepts is to inject the carbon dioxide formed in the combustion of the fossil fuels and present in concentrated form in the flue gas into suitable repositories, in particular into certain rock strata or salt water-bearing strata, and thereby to limit the emission of carbon dioxide into the atmosphere. The harmful climatic effect of greenhouse gases such as carbon dioxide is thereby reduced. Such power plants are termed in the specialist field "oxyfuel"
power plants.
In the concepts known to date, a dedusting, denitrification and desuiphurization of the flue gas proceed in sequential steps. Subsequently to this flue gas purification, the carbon dioxide-rich exhaust gas thus treated is compressed and fed to a carbon dioxide purification stage. There, typically, a gas substream having a reduced carbon dioxide content and another gas substream having an elevated carbon dioxide content are generated by way of a cryogenic separation method. The gas substream having an elevated carbon dioxide content is the desired carbon dioxide product stream, which is produced having a carbon dioxide content of, e.g., greater than 95% by volume and is provided for further use, in particular for transport to repositories. The gas substream having a reduced carbon dioxide content is produced as a subsidiary stream (what is termed vent gas) at 15 to 30 bar, preferably 18 to 25 bar, and contains predominantly the components not intended for the injection, in particular inert gases such as nitrogen (N2) and argon (Ar) and oxygen (02). However, in this gas substream, fractions of carbon dioxide are also still present at a concentration of approximately 25 to 35% by volume. This vent gas is currently blown off into the atmosphere.
Usually, the raw gas stream is precompressed to a desired pressure in upstream plant parts and dried, e.g., in adsorber stations. This means that the vent gas also is first still present in the compressed state. At present this pressure level is reduced by expansion valves.
In EP 1952874 Al and EP 1953486 Al (Air Products) it has already been proposed, after warming the vent gas and further heating by means of waste heat from the compression, to carry out a turbine expansion of the vent gas stream.
However, utilization of the energy liberated in the turbine expansion, in particular of the
power plants.
In the concepts known to date, a dedusting, denitrification and desuiphurization of the flue gas proceed in sequential steps. Subsequently to this flue gas purification, the carbon dioxide-rich exhaust gas thus treated is compressed and fed to a carbon dioxide purification stage. There, typically, a gas substream having a reduced carbon dioxide content and another gas substream having an elevated carbon dioxide content are generated by way of a cryogenic separation method. The gas substream having an elevated carbon dioxide content is the desired carbon dioxide product stream, which is produced having a carbon dioxide content of, e.g., greater than 95% by volume and is provided for further use, in particular for transport to repositories. The gas substream having a reduced carbon dioxide content is produced as a subsidiary stream (what is termed vent gas) at 15 to 30 bar, preferably 18 to 25 bar, and contains predominantly the components not intended for the injection, in particular inert gases such as nitrogen (N2) and argon (Ar) and oxygen (02). However, in this gas substream, fractions of carbon dioxide are also still present at a concentration of approximately 25 to 35% by volume. This vent gas is currently blown off into the atmosphere.
Usually, the raw gas stream is precompressed to a desired pressure in upstream plant parts and dried, e.g., in adsorber stations. This means that the vent gas also is first still present in the compressed state. At present this pressure level is reduced by expansion valves.
In EP 1952874 Al and EP 1953486 Al (Air Products) it has already been proposed, after warming the vent gas and further heating by means of waste heat from the compression, to carry out a turbine expansion of the vent gas stream.
However, utilization of the energy liberated in the turbine expansion, in particular of the
3 refrigeration capacity produced in the expansion process, is not envisaged in this case.
In DE 102009039898 Al (Linde), for improving the energy efficiency, it is proposed that the vent gas stream is expanded in at least one expansion turbine and both the resultant kinetic energy and also the refrigeration generated are utilized for energy recovery. For utilizing the kinetic energy, the expansion turbine can be coupled to a compressor (booster) which compresses the raw gas stream and/or the carbon dioxide gas stream. For utilizing the refrigeration generated in the expansion, the at least partially expanded vent gas stream can be brought into heat exchange with process streams that are to be cooled, e.g. the raw gas stream and/or the carbon dioxide gas stream.
The carbon dioxide gas stream is usually compressed by way of a final compressor to the required final pressure of above 80 bar (preferably 120 to 150 bar) for transport and subsequent sequestration.
Alternatively, for the carbon dioxide gas stream compression, liquefaction of the separated-off carbon dioxide-rich gas with subsequent pressure elevation by way of pumps is also possible. Here, however, the use of refrigerant is necessary.
When external refrigeration from a refrigeration plant is used, a liquid carbon dioxide pure product is already present after the cryogenic separation, which liquid carbon dioxide pure product can be brought to the necessary final pressure by way of a pump.
However, the use of a refrigeration plant (external refrigeration) increases the necessary energy consumption.
An object of the present invention is to design a method of the type mentioned at the outset and also an apparatus for carrying out the method in such a manner that the energy efficiency can be further improved.
Upon further study of the specification and appended claims, other objects and advantages of the invention will become apparent.
These objects are achieved in terms of the method in that, from some of the
In DE 102009039898 Al (Linde), for improving the energy efficiency, it is proposed that the vent gas stream is expanded in at least one expansion turbine and both the resultant kinetic energy and also the refrigeration generated are utilized for energy recovery. For utilizing the kinetic energy, the expansion turbine can be coupled to a compressor (booster) which compresses the raw gas stream and/or the carbon dioxide gas stream. For utilizing the refrigeration generated in the expansion, the at least partially expanded vent gas stream can be brought into heat exchange with process streams that are to be cooled, e.g. the raw gas stream and/or the carbon dioxide gas stream.
The carbon dioxide gas stream is usually compressed by way of a final compressor to the required final pressure of above 80 bar (preferably 120 to 150 bar) for transport and subsequent sequestration.
Alternatively, for the carbon dioxide gas stream compression, liquefaction of the separated-off carbon dioxide-rich gas with subsequent pressure elevation by way of pumps is also possible. Here, however, the use of refrigerant is necessary.
When external refrigeration from a refrigeration plant is used, a liquid carbon dioxide pure product is already present after the cryogenic separation, which liquid carbon dioxide pure product can be brought to the necessary final pressure by way of a pump.
However, the use of a refrigeration plant (external refrigeration) increases the necessary energy consumption.
An object of the present invention is to design a method of the type mentioned at the outset and also an apparatus for carrying out the method in such a manner that the energy efficiency can be further improved.
Upon further study of the specification and appended claims, other objects and advantages of the invention will become apparent.
These objects are achieved in terms of the method in that, from some of the
4 liquid that is separated off in the cryogenic carbon dioxide purification stage, a liquid stream having an elevated carbon dioxide content (carbon dioxide liquid stream) is obtained which is fed in a liquid phase to further utilization and/or storage.
Using the invention, an energy-sparing operation of the carbon dioxide purification stage is made possible without using external refrigeration from an external refrigeration plant. The refrigeration necessary for cooling and partial condensation of the raw gas stream can be provided via heat exchange with the evaporating liquid forming the carbon dioxide gas stream and also by heat exchange with the vent gas stream that is cooled by expansion in the expansion turbine. By branching off a carbon dioxide liquid stream, the final compression of the carbon dioxide gas stream can be relieved, whereby, in total, an improvement of the energy efficiency is achieved.
Furthermore, in this manner an additional liquid carbon dioxide product can be provided without further energy consumption.
It has proved in this case that operation of the carbon dioxide purification stage without an external refrigeration plant is expedient when the carbon dioxide liquid stream amounts to 5 to 25%, preferably 10 to 15%, of the total liquid that is separated off in the cryogenic carbon dioxide purification stage.
According to a particularly advantageous embodiment of the invention, the carbon dioxide liquid stream is fed to the carbon dioxide gas stream after compression thereof to the final pressure. In this case the carbon dioxide liquid stream is expediently compressed to the final pressure by way of a liquid pump before it is fed to the carbon dioxide gas stream.
Another variant of the invention provides that the carbon dioxide liquid stream is temporarily stored in a liquid gas tank for further use, in particular in the food industry.
Customers' wants can thereby be met by an additional liquid carbon dioxide product without additional energy expenditure and without the use of an external refrigeration plant.
A further possibility of use is in the use of the carbon dioxide liquid stream, after evaporation, as transport medium for the pneumatic transport (i.e., entrainment of solid particles, such as coal dust, by a gas stream) or as a lock gas of feedstocks, in particular coal dust, in large-scale furnace plants. For example, during preparation of combustible material (coal/lignite) for coal fired power plants, contact with oxygen has to be
Using the invention, an energy-sparing operation of the carbon dioxide purification stage is made possible without using external refrigeration from an external refrigeration plant. The refrigeration necessary for cooling and partial condensation of the raw gas stream can be provided via heat exchange with the evaporating liquid forming the carbon dioxide gas stream and also by heat exchange with the vent gas stream that is cooled by expansion in the expansion turbine. By branching off a carbon dioxide liquid stream, the final compression of the carbon dioxide gas stream can be relieved, whereby, in total, an improvement of the energy efficiency is achieved.
Furthermore, in this manner an additional liquid carbon dioxide product can be provided without further energy consumption.
It has proved in this case that operation of the carbon dioxide purification stage without an external refrigeration plant is expedient when the carbon dioxide liquid stream amounts to 5 to 25%, preferably 10 to 15%, of the total liquid that is separated off in the cryogenic carbon dioxide purification stage.
According to a particularly advantageous embodiment of the invention, the carbon dioxide liquid stream is fed to the carbon dioxide gas stream after compression thereof to the final pressure. In this case the carbon dioxide liquid stream is expediently compressed to the final pressure by way of a liquid pump before it is fed to the carbon dioxide gas stream.
Another variant of the invention provides that the carbon dioxide liquid stream is temporarily stored in a liquid gas tank for further use, in particular in the food industry.
Customers' wants can thereby be met by an additional liquid carbon dioxide product without additional energy expenditure and without the use of an external refrigeration plant.
A further possibility of use is in the use of the carbon dioxide liquid stream, after evaporation, as transport medium for the pneumatic transport (i.e., entrainment of solid particles, such as coal dust, by a gas stream) or as a lock gas of feedstocks, in particular coal dust, in large-scale furnace plants. For example, during preparation of combustible material (coal/lignite) for coal fired power plants, contact with oxygen has to be
5 minimized. Carbon dioxide is possible gas to use for displacing air, thereby acting as a lock gas.
For utilization of the kinetic energy, the expansion turbine can also be coupled to at least one compressor (booster), in such a manner that the expansion turbine compresses the raw gas stream and/or the carbon dioxide product stream during the at least partial expansion of the vent gas stream. For utilization of the refrigeration generated in the expansion, the at least partially expanded vent gas stream is preferably brought into heat exchange with process streams that are to be cooled, e.g.
the raw gas stream and/or the carbon dioxide product stream. By expansion of the vent gas, process-internal refrigeration output can be provided and external refrigeration can thereby be spared.
The invention further relates to an apparatus for treating a carbon dioxide-containing gas stream (raw gas stream), in particular from a large-scale furnace plant, having a carbon dioxide purification appliance that is charged with the precompressed raw gas stream. The carbon dioxide purification appliance comprises an outlet line for a gas stream having an elevated carbon dioxide content (carbon dioxide gas stream) and an outlet line for a gas stream having a reduced carbon dioxide content (vent gas stream). The outlet line for the carbon dioxide gas stream is connected via a final compressor to a utilization appliance and/or repository, whereas the outlet line for the vent gas stream is connected to at least one expansion turbine which comprises an outlet line for the at least partially expanded vent gas stream. The outlet line for the at least partially expanded vent gas stream is connected to a heat-exchange appliance which is chargeable with the precompressed raw gas stream, the carbon dioxide gas stream and the vent gas stream.
The objects are achieved in terms of the apparatus in that the carbon dioxide purification appliance additionally comprises an outlet line for a liquid stream having an
For utilization of the kinetic energy, the expansion turbine can also be coupled to at least one compressor (booster), in such a manner that the expansion turbine compresses the raw gas stream and/or the carbon dioxide product stream during the at least partial expansion of the vent gas stream. For utilization of the refrigeration generated in the expansion, the at least partially expanded vent gas stream is preferably brought into heat exchange with process streams that are to be cooled, e.g.
the raw gas stream and/or the carbon dioxide product stream. By expansion of the vent gas, process-internal refrigeration output can be provided and external refrigeration can thereby be spared.
The invention further relates to an apparatus for treating a carbon dioxide-containing gas stream (raw gas stream), in particular from a large-scale furnace plant, having a carbon dioxide purification appliance that is charged with the precompressed raw gas stream. The carbon dioxide purification appliance comprises an outlet line for a gas stream having an elevated carbon dioxide content (carbon dioxide gas stream) and an outlet line for a gas stream having a reduced carbon dioxide content (vent gas stream). The outlet line for the carbon dioxide gas stream is connected via a final compressor to a utilization appliance and/or repository, whereas the outlet line for the vent gas stream is connected to at least one expansion turbine which comprises an outlet line for the at least partially expanded vent gas stream. The outlet line for the at least partially expanded vent gas stream is connected to a heat-exchange appliance which is chargeable with the precompressed raw gas stream, the carbon dioxide gas stream and the vent gas stream.
The objects are achieved in terms of the apparatus in that the carbon dioxide purification appliance additionally comprises an outlet line for a liquid stream having an
6 elevated carbon dioxide content (carbon dioxide liquid stream). This outlet line bypasses the heat-exchange appliance and the final compressor and is connected directly to a utilization appliance and/or storage appliance for liquid having an elevated carbon dioxide content.
Preferably, the outlet line for the carbon dioxide liquid stream comprises a liquid pump and, downstream of the final compressor, the carbon dioxide liquid stream is introduced into the outlet line for the carbon dioxide gas stream.
The invention is suitable for all conceivable large-scale furnace plants in which carbon dioxide-containing gas streams are produced. These include, e.g., fossil-fuel-fired power plants, industrial furnaces, steam kettles and similar large-scale thermal plants for power and/or heat generation. The invention can be used particularly advantageously in large-scale furnace plants which are supplied with technically pure oxygen or oxygen-enriched air as combustion gas and in which, accordingly, exhaust gas streams having high carbon dioxide concentrations are produced. In particular, the invention is suitable for what are termed low-CO2 coal power plants which are operated with oxygen as combustion gas ("oxyfuel" power plants) and in which the carbon dioxide that is present in the exhaust gas in high concentration is separated off and injected below ground ("CO2 capture technology").
The invention is associated with a large number of advantages.
The final compressor for the carbon dioxide gas stream is relieved, which leads to energy savings and also to a reduction of capital costs. The demands on the operation of the final compressor are reduced so, for example, a smaller compressor can be used thereby reducing capital costs. In addition, the energy balance at the heat-exchange appliance is optimally utilized. In some circumstances, the intake temperature at the final compressor can be adjusted in such a manner that simpler materials (no high-alloy steels) can be used. Furthermore, a prepurified liquid carbon dioxide product can be provided from the system which can be utilized, for example, for treatment to give a food-specific carbon dioxide product (external utilization) or else also as liquid store in a tank system.
Preferably, the outlet line for the carbon dioxide liquid stream comprises a liquid pump and, downstream of the final compressor, the carbon dioxide liquid stream is introduced into the outlet line for the carbon dioxide gas stream.
The invention is suitable for all conceivable large-scale furnace plants in which carbon dioxide-containing gas streams are produced. These include, e.g., fossil-fuel-fired power plants, industrial furnaces, steam kettles and similar large-scale thermal plants for power and/or heat generation. The invention can be used particularly advantageously in large-scale furnace plants which are supplied with technically pure oxygen or oxygen-enriched air as combustion gas and in which, accordingly, exhaust gas streams having high carbon dioxide concentrations are produced. In particular, the invention is suitable for what are termed low-CO2 coal power plants which are operated with oxygen as combustion gas ("oxyfuel" power plants) and in which the carbon dioxide that is present in the exhaust gas in high concentration is separated off and injected below ground ("CO2 capture technology").
The invention is associated with a large number of advantages.
The final compressor for the carbon dioxide gas stream is relieved, which leads to energy savings and also to a reduction of capital costs. The demands on the operation of the final compressor are reduced so, for example, a smaller compressor can be used thereby reducing capital costs. In addition, the energy balance at the heat-exchange appliance is optimally utilized. In some circumstances, the intake temperature at the final compressor can be adjusted in such a manner that simpler materials (no high-alloy steels) can be used. Furthermore, a prepurified liquid carbon dioxide product can be provided from the system which can be utilized, for example, for treatment to give a food-specific carbon dioxide product (external utilization) or else also as liquid store in a tank system.
7 The carbon dioxide liquid stream can also be used for other applications (e.g.
treatment to give purified seal gas for the oxyfuel process, use as transport medium for the pneumatic transport of coal dust in the oxyfuel process, storage of liquid carbon dioxide for use as start-up gas or charge gas after evaporation).
When multistage compression is used to bring the pressure of the carbon dioxide gas stream to the required final pressure, the carbon dioxide liquid stream, after a supercritical compression of the carbon dioxide gas stream (> 72 bar), can be fed (in the supercritical state) upstream of the suction side of the next-following compressor stage (or pump). The temperature falls and the density increases thereby. Owing to the higher density, the energy requirement of the subsequent compressor stages/pumps for achieving the required final pressure falls.
Brief Description of the Drawings The invention and further embodiments of the invention are described in more detail hereinafter with reference to working examples shown schematically in the figures, in comparison with the previous prior art. Various other features and attendant advantages of the present invention will be more fully appreciated as the same becomes better understood when considered in conjunction with the accompanying drawings, in which like reference characters designate the same or similar parts throughout the several views, and wherein:
Figure 1 shows a block diagram of a carbon dioxide treatment plant with expansion of the vent gas via an expansion turbine as per the prior art according to EP 1952874 Al;
Figure 2 shows a block diagram of a carbon dioxide treatment plant with expansion of the vent gas via expansion turbines with energy recovery as per the prior art according to DE 102009039898 Al;
Figure 3 shows a block diagram of a carbon dioxide treatment plant with removal of a separate carbon dioxide liquid stream with subsequent
treatment to give purified seal gas for the oxyfuel process, use as transport medium for the pneumatic transport of coal dust in the oxyfuel process, storage of liquid carbon dioxide for use as start-up gas or charge gas after evaporation).
When multistage compression is used to bring the pressure of the carbon dioxide gas stream to the required final pressure, the carbon dioxide liquid stream, after a supercritical compression of the carbon dioxide gas stream (> 72 bar), can be fed (in the supercritical state) upstream of the suction side of the next-following compressor stage (or pump). The temperature falls and the density increases thereby. Owing to the higher density, the energy requirement of the subsequent compressor stages/pumps for achieving the required final pressure falls.
Brief Description of the Drawings The invention and further embodiments of the invention are described in more detail hereinafter with reference to working examples shown schematically in the figures, in comparison with the previous prior art. Various other features and attendant advantages of the present invention will be more fully appreciated as the same becomes better understood when considered in conjunction with the accompanying drawings, in which like reference characters designate the same or similar parts throughout the several views, and wherein:
Figure 1 shows a block diagram of a carbon dioxide treatment plant with expansion of the vent gas via an expansion turbine as per the prior art according to EP 1952874 Al;
Figure 2 shows a block diagram of a carbon dioxide treatment plant with expansion of the vent gas via expansion turbines with energy recovery as per the prior art according to DE 102009039898 Al;
Figure 3 shows a block diagram of a carbon dioxide treatment plant with removal of a separate carbon dioxide liquid stream with subsequent
8 compression by way of a liquid pump to the required final pressure for pipeline transport; and Figure 4 shows a block diagram of a carbon dioxide treatment plant with removal of a separate carbon dioxide liquid stream with subsequent temporary storage for external use.
Figure 1 shows a conventional treatment of a carbon dioxide-containing raw gas stream from a coal power plant as per the prior art according to EP 1952874 Al (Air Products). The raw gas stream, after compression in the raw gas compressor 1, is fed via a heat-exchange unit 2 to a primary separator 3 for separating off carbon dioxide.
The vent gas from the primary separator 3 is introduced into the heat-exchange unit 2 and then fed to a secondary separator 4. The carbon dioxide product stream is withdrawn, respectively, from the bottoms of primary carbon dioxide separator 3 and secondary separator 4, introduced into the central heat-exchange unit 2 (and in the case of the vent gas from the primary separator 3 additionally via a CO2 product compressor 7), and then subjected to a final compression 8 in order finally to be fed via a pipeline (carbon dioxide pipeline) 9, e.g. to an injection below ground. The vent gas of the secondary separator 4 is withdrawn from the top of the secondary separator 4, likewise introduced into the central heat-exchange unit 2 and finally, downstream of a further warming in the heat exchanger 5, expanded via a turbine 6 in order to be delivered to the atmosphere.
In contrast to the method shown in Figure 1 for carbon dioxide treatment, the method according to DE 102009039898 Al (Linde), shown in Figure 2, offers the advantage of energy recovery in the expansion of the vent gas. In this method, as in the method shown in Figure 1, two carbon dioxide separators 3 and 4 and also a central heat-exchange unit 2 are provided. In contrast to the method as per Figure 1, however, simple expansion of the vent gas via a single turbine does not occur, but instead a stepwise expansion via two expansion turbines 5 and 6 is performed. By way of the stepwise expansion of the vent gas stream, the formation of solid carbon dioxide in the vent gas can be prevented. Downstream of the expansion in the first expansion turbine 5, the vent gas stream is warmed in the central heat-exchange unit 2 and then expanded further to close to atmospheric pressure in the second expansion turbine 6 and again
Figure 1 shows a conventional treatment of a carbon dioxide-containing raw gas stream from a coal power plant as per the prior art according to EP 1952874 Al (Air Products). The raw gas stream, after compression in the raw gas compressor 1, is fed via a heat-exchange unit 2 to a primary separator 3 for separating off carbon dioxide.
The vent gas from the primary separator 3 is introduced into the heat-exchange unit 2 and then fed to a secondary separator 4. The carbon dioxide product stream is withdrawn, respectively, from the bottoms of primary carbon dioxide separator 3 and secondary separator 4, introduced into the central heat-exchange unit 2 (and in the case of the vent gas from the primary separator 3 additionally via a CO2 product compressor 7), and then subjected to a final compression 8 in order finally to be fed via a pipeline (carbon dioxide pipeline) 9, e.g. to an injection below ground. The vent gas of the secondary separator 4 is withdrawn from the top of the secondary separator 4, likewise introduced into the central heat-exchange unit 2 and finally, downstream of a further warming in the heat exchanger 5, expanded via a turbine 6 in order to be delivered to the atmosphere.
In contrast to the method shown in Figure 1 for carbon dioxide treatment, the method according to DE 102009039898 Al (Linde), shown in Figure 2, offers the advantage of energy recovery in the expansion of the vent gas. In this method, as in the method shown in Figure 1, two carbon dioxide separators 3 and 4 and also a central heat-exchange unit 2 are provided. In contrast to the method as per Figure 1, however, simple expansion of the vent gas via a single turbine does not occur, but instead a stepwise expansion via two expansion turbines 5 and 6 is performed. By way of the stepwise expansion of the vent gas stream, the formation of solid carbon dioxide in the vent gas can be prevented. Downstream of the expansion in the first expansion turbine 5, the vent gas stream is warmed in the central heat-exchange unit 2 and then expanded further to close to atmospheric pressure in the second expansion turbine 6 and again
9 warmed in the central heat-exchange unit 2. The available pressure level of the vent gas can thereby be completely exploited. The vent gas that is cold after the expansion is warmed in the central heat-exchange unit 2 against the process streams that are to be cooled. The vent gas thereby provides some of the refrigeration capacity necessary in the process.
Figure 3 shows a carbon dioxide treatment according to the invention. The process procedure differs from that shown in Figure 2 in that some of the liquid carbon dioxide separated off in the primary separator 3 is branched off and fed via a carbon dioxide liquid pump 9 downstream of the final compressor 8 to the CO2 pipeline
Figure 3 shows a carbon dioxide treatment according to the invention. The process procedure differs from that shown in Figure 2 in that some of the liquid carbon dioxide separated off in the primary separator 3 is branched off and fed via a carbon dioxide liquid pump 9 downstream of the final compressor 8 to the CO2 pipeline
10. In this procedure the carbon dioxide liquid stream is brought to the required final pressure for the pipeline transport by way of the carbon dioxide liquid pump 9. Since this carbon dioxide liquid stream by passes the final compressor 8, the operational demands on the final compression 8 are reduced thereby increasing energy efficiency and reducing capital costs. The energy balance at the heat-exchange unit 12 can be used optimally.
The intake temperature at the final compressor 8 can be adjusted in such a manner that simpler materials (e.g. no high-alloy steels) can be used.
In the variant of the invention shown in Figure 4, the liquid carbon dioxide that is separated off from the primary separator 3 is first temporarily stored in a liquid carbon dioxide tank 11. The liquid carbon dioxide can be fed, as required, from tank
The intake temperature at the final compressor 8 can be adjusted in such a manner that simpler materials (e.g. no high-alloy steels) can be used.
In the variant of the invention shown in Figure 4, the liquid carbon dioxide that is separated off from the primary separator 3 is first temporarily stored in a liquid carbon dioxide tank 11. The liquid carbon dioxide can be fed, as required, from tank
11 via the liquid pump 9 to the CO2 pipeline 10 and/or loaded into a transport vehicle 12 for further external utilization (e.g. in the food industry) and/or evaporated in a CO2 evaporator 13 and provided for internal utilization (e.g. as start-up or feed gas).
The entire disclosure[s] of all applications, patents and publications, cited herein and of corresponding German Application No. 10 2011 014 678.4, filed March 22, 2011, are incorporated by reference herein.
The preceding examples can be repeated with similar success by substituting the generically or specifically described reactants and/or operating conditions of this invention for those used in the preceding examples.
The entire disclosure[s] of all applications, patents and publications, cited herein and of corresponding German Application No. 10 2011 014 678.4, filed March 22, 2011, are incorporated by reference herein.
The preceding examples can be repeated with similar success by substituting the generically or specifically described reactants and/or operating conditions of this invention for those used in the preceding examples.
Claims (10)
1. A method for treating a carbon dioxide-containing gas stream comprising:
partially liquefying precompressed raw carbon dioxide-containing gas stream in a cryogenic carbon dioxide purification stage, removing from said cryogenic carbon dioxide purification stage a liquid stream having an elevated carbon dioxide content and a gas stream having a reduced carbon dioxide content, reevaporating a first portion of the liquid stream having an elevated carbon dioxide content to obtain a gas stream having an elevated carbon dioxide content, expanding the gas stream having a reduced carbon dioxide content in at least one expansion turbine and recovering the resultant refrigeration generated in this expansion for cooling the precompressed raw carbon dioxide-containing gas stream, compressing the gas stream having an elevated carbon dioxide content to a final pressure, and feeding the resultant compressed gas stream having an elevated carbon dioxide content to further utilization and/or storage, wherein a second portion of the liquid stream having an elevated carbon dioxide content removed from said cryogenic carbon dioxide purification stage is fed in a liquid phase to further utilization and/or storage.
partially liquefying precompressed raw carbon dioxide-containing gas stream in a cryogenic carbon dioxide purification stage, removing from said cryogenic carbon dioxide purification stage a liquid stream having an elevated carbon dioxide content and a gas stream having a reduced carbon dioxide content, reevaporating a first portion of the liquid stream having an elevated carbon dioxide content to obtain a gas stream having an elevated carbon dioxide content, expanding the gas stream having a reduced carbon dioxide content in at least one expansion turbine and recovering the resultant refrigeration generated in this expansion for cooling the precompressed raw carbon dioxide-containing gas stream, compressing the gas stream having an elevated carbon dioxide content to a final pressure, and feeding the resultant compressed gas stream having an elevated carbon dioxide content to further utilization and/or storage, wherein a second portion of the liquid stream having an elevated carbon dioxide content removed from said cryogenic carbon dioxide purification stage is fed in a liquid phase to further utilization and/or storage.
2. The method according to Claim 1, wherein said precompressed raw carbon dioxide-containing gas stream is a raw gas stream form a large-scale furnace plant.
3. The method according to Claim 1, wherein the second portion of the liquid stream having an elevated carbon dioxide content is 5 to 25% of the total liquid removed from the cryogenic carbon dioxide purification stage.
4. The method according to Claim 3, wherein the second portion of the liquid stream having an elevated carbon dioxide content is 10 to 15% of the total liquid removed from the cryogenic carbon dioxide purification stage.
5. The method according to anyone of Claims 1 to 4, wherein the second portion of the liquid stream having an elevated carbon dioxide content is introduced into the gas stream having an elevated carbon dioxide content after compression of the second portion of the liquid stream having an elevated carbon dioxide content to the final pressure.
6. The method according to Claim 5, wherein the second portion of the liquid stream is compressed to the final pressure by way of a liquid pump before it is introduced into the gas stream having an elevated carbon dioxide content.
7. The method according to any one of Claims 1 to 6, wherein said second portion of the liquid stream having an elevated carbon dioxide content is temporarily stored in a liquid gas tank for further use.
8. The method according to any one of Claims 3 to 7, said second portion of the liquid stream having an elevated carbon dioxide content is used as transport medium for the pneumatic transport of feedstocks.
9. An apparatus for treating a carbon dioxide-containing gas stream, said apparatus comprising:
a carbon dioxide purification appliance comprising an inlet for introducing a precompressed raw carbon dioxide-containing gas stream, an outlet line for removal of a gas stream having an elevated carbon dioxide content and another outlet line for removal of a gas stream having a reduced carbon dioxide content, said outlet line for removal of a gas stream having an elevated carbon dioxide content being connected via a final compressor to a utilization appliance and/or repository, said another outlet line for removal of a gas stream having a reduced carbon dioxide content being connected to at least one expansion turbine comprising an outlet line for removal of at least partially expanded gas stream having a reduced carbon dioxide content which is connected to an inlet of a heat-exchange appliance, and said heat exchange appliance further having inlets for introduction of said precompressed raw gas stream and said gas stream having an elevated carbon dioxide content, wherein said carbon dioxide purification appliance additionally comprises an outlet line for a liquid stream having an elevated carbon dioxide content, which bypasses said heat-exchange appliance and said final compressor, and is connected directly to a utilization appliance and/or storage appliance for liquid having an elevated carbon dioxide content.
a carbon dioxide purification appliance comprising an inlet for introducing a precompressed raw carbon dioxide-containing gas stream, an outlet line for removal of a gas stream having an elevated carbon dioxide content and another outlet line for removal of a gas stream having a reduced carbon dioxide content, said outlet line for removal of a gas stream having an elevated carbon dioxide content being connected via a final compressor to a utilization appliance and/or repository, said another outlet line for removal of a gas stream having a reduced carbon dioxide content being connected to at least one expansion turbine comprising an outlet line for removal of at least partially expanded gas stream having a reduced carbon dioxide content which is connected to an inlet of a heat-exchange appliance, and said heat exchange appliance further having inlets for introduction of said precompressed raw gas stream and said gas stream having an elevated carbon dioxide content, wherein said carbon dioxide purification appliance additionally comprises an outlet line for a liquid stream having an elevated carbon dioxide content, which bypasses said heat-exchange appliance and said final compressor, and is connected directly to a utilization appliance and/or storage appliance for liquid having an elevated carbon dioxide content.
10. The apparatus according to Claim 9, wherein said outlet line for a liquid stream having an elevated carbon dioxide content comprises a liquid pump and, downstream of said final compressor, outlet line for a liquid stream having an elevated carbon dioxide content communicates with said the outlet line for removal of a gas stream having an elevated carbon dioxide content being.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEDE102011014678.4 | 2011-03-22 | ||
| DE102011014678A DE102011014678A1 (en) | 2011-03-22 | 2011-03-22 | Process and apparatus for treating a carbon dioxide-containing gas stream |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2771558A1 true CA2771558A1 (en) | 2012-09-22 |
Family
ID=45877940
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2771558A Abandoned CA2771558A1 (en) | 2011-03-22 | 2012-03-16 | Method and device for treating a carbon dioxide-containing gas stream |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US20120240616A1 (en) |
| EP (1) | EP2503271A2 (en) |
| AU (1) | AU2012200908A1 (en) |
| CA (1) | CA2771558A1 (en) |
| DE (1) | DE102011014678A1 (en) |
| ZA (1) | ZA201202071B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20160028999A (en) | 2013-03-04 | 2016-03-14 | 에코진 파워 시스템스, 엘엘씨 | Heat engine systems with high net power supercritical carbon dioxide circuits |
| DE102013110163A1 (en) * | 2013-09-16 | 2015-03-19 | Universität Rostock | Carbon dioxide separator for an internal combustion engine |
| WO2016073252A1 (en) | 2014-11-03 | 2016-05-12 | Echogen Power Systems, L.L.C. | Active thrust management of a turbopump within a supercritical working fluid circuit in a heat engine system |
| US20170166503A1 (en) * | 2015-12-15 | 2017-06-15 | Swiss Liquid Future AG | Ecological and economic method and apparatus for providing hydrogen-based methanol |
| US10883388B2 (en) | 2018-06-27 | 2021-01-05 | Echogen Power Systems Llc | Systems and methods for generating electricity via a pumped thermal energy storage system |
| WO2021129925A1 (en) * | 2019-12-23 | 2021-07-01 | Kirchner Energietechnik GmbH | Turbo exhaust gas co2 capture |
| CN110987977B (en) * | 2019-12-31 | 2021-08-06 | 中国热带农业科学院农业机械研究所 | Intelligent servo cylinder type purification and separation control system and method |
| US11435120B2 (en) | 2020-05-05 | 2022-09-06 | Echogen Power Systems (Delaware), Inc. | Split expansion heat pump cycle |
| EP4259907A1 (en) | 2020-12-09 | 2023-10-18 | Supercritical Storage Company, Inc. | Three reservoir electric thermal energy storage system |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3976442A (en) * | 1974-12-18 | 1976-08-24 | Texaco Inc. | Synthesis gas from gaseous CO2 -solid carbonaceous fuel feeds |
| NL1018708C2 (en) * | 2001-08-03 | 2003-02-04 | Haffmans Bv | Processing device for the preparation of pure carbon dioxide (CO2) from a gaseous CO2-containing product. |
| US7819951B2 (en) | 2007-01-23 | 2010-10-26 | Air Products And Chemicals, Inc. | Purification of carbon dioxide |
| US8088196B2 (en) | 2007-01-23 | 2012-01-03 | Air Products And Chemicals, Inc. | Purification of carbon dioxide |
| DE102009039898A1 (en) | 2009-09-03 | 2011-03-10 | Linde-Kca-Dresden Gmbh | Process and apparatus for treating a carbon dioxide-containing gas stream |
| US8734569B2 (en) * | 2009-12-15 | 2014-05-27 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method of obtaining carbon dioxide from carbon dioxide-containing gas mixture |
| AU2011261670B2 (en) * | 2010-06-03 | 2014-08-21 | Uop Llc | Hydrocarbon gas processing |
-
2011
- 2011-03-22 DE DE102011014678A patent/DE102011014678A1/en not_active Withdrawn
-
2012
- 2012-02-16 AU AU2012200908A patent/AU2012200908A1/en not_active Abandoned
- 2012-03-01 EP EP12001383A patent/EP2503271A2/en not_active Withdrawn
- 2012-03-16 CA CA2771558A patent/CA2771558A1/en not_active Abandoned
- 2012-03-20 ZA ZA2012/02071A patent/ZA201202071B/en unknown
- 2012-03-21 US US13/425,567 patent/US20120240616A1/en not_active Abandoned
Also Published As
| Publication number | Publication date |
|---|---|
| DE102011014678A1 (en) | 2012-09-27 |
| AU2012200908A1 (en) | 2012-10-11 |
| US20120240616A1 (en) | 2012-09-27 |
| ZA201202071B (en) | 2012-11-28 |
| EP2503271A2 (en) | 2012-09-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US20120240616A1 (en) | Method and device for treating a carbon dioxide-containing gas stream | |
| US10746461B2 (en) | Cryogenic air separation method for producing oxygen at high pressures | |
| US9546814B2 (en) | Cryogenic air separation method and system | |
| US8080090B2 (en) | Process for feed gas cooling in reboiler during CO2 separation | |
| CA2775449C (en) | Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams | |
| KR101106195B1 (en) | Apparatus and method for purification and liquifaction of carbon dioxide | |
| US20120137728A1 (en) | Auto-refrigerated gas separation system for carbon dioxide capture and compression | |
| CN107108233B (en) | Production of low pressure liquid carbon dioxide from power generation systems and methods | |
| AU2010291532B2 (en) | Method and device for treating a carbon dioxide-containing gas flow, wherein the energy of the vent gas (work and cold due to expansion) is used | |
| WO2012174418A1 (en) | Process for removing carbon dioxide from a gas stream using desublimation | |
| EP2365265B1 (en) | Method and installation for separating carbon dioxide from flue gas of combustion plants | |
| WO2008099300A1 (en) | Process for vaporizing the product co2 at two different pressures during co2 separation | |
| EP2112989A1 (en) | Process for recycling of top gas during co2 separation | |
| Berdowska et al. | Technology of oxygen production in the membrane-cryogenic air separation system for a 600 MW oxy-type pulverized bed boiler | |
| WO2012114118A1 (en) | Process and apparatus for purification of carbon dioxide | |
| WO2012114119A1 (en) | Process and apparatus for purification of carbon dioxide | |
| US9995530B2 (en) | Method for the capture of carbon dioxide through cryogenically processing gaseous emissions from fossil-fuel power generation | |
| WO2012114120A1 (en) | Process and apparatus for purification of carbon dioxide |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FZDE | Discontinued |
Effective date: 20150317 |