2738results about "Cold treatment separation" patented technology

The invention relates to a facility for producing liquid CO2 and biomethane, comprising: —a unit for producing biogas; —at least one unit for the membrane separation of biogas to produce biomethane and a gaseous mixture M1 mainly comprising carbon dioxide; —a unit for cryogenically distilling the gaseous mixture M1 to produce liquid CO2 and a gaseous mixture M2 comprising carbon dioxide, methane, oxygen and hydrogen; —one or more membranes located in the flow of the gaseous mixture M2 to separate the methane from the oxygen-hydrogen mixture

The invention discloses a carbon capture and energy storage and thermal power generation coupled energy comprehensive utilization system, which comprises a thermal power generation system, an energy storage system and a carbon capture system, and is characterized in that a compression energy storage unit of the energy storage system is coupled to a feed water heat regeneration unit of the thermal power generation system; an expansion energy release unit of the energy storage system is coupled to a steam turbine generator set of the thermal power generation system, and a steam-water cycle working medium in the thermal power generation system serves as a heat storage and cold storage medium of the carbon dioxide energy storage system. The carbon capture system is coupled between the thermal power generation system and the carbon dioxide energy storage system, captures carbon dioxide gas in the flue gas, inputs the carbon dioxide gas into the carbon dioxide energy storage system to serve as a circulating working medium, and heats the circulating working medium in the expansion energy release unit through waste heat of the flue gas. According to the scheme, the operation efficiency of the thermal power generation system and the operation efficiency of the carbon dioxide energy storage system can be improved, the overall energy utilization efficiency of the system can be improved, and meanwhile the emission amount of gas pollutants is reduced.

A feed gas including neon, nitrogen, and helium is cooled in a heat exchange system to a first temperature to produce a two-phase mixture that is introduced into a first phase separator and separated into a nitrogen-rich liquid and a first gaseous crude neon stream. The pressure is reduced in at least a portion of the nitrogen-rich liquid, which is vaporized in the heat exchange system to generate a portion of the refrigeration therein. The first gaseous crude neon stream is introduced into a first adsorber that removes impurities such as nitrogen. The gaseous crude neon stream is further cooled to a second temperature. A portion of the cooling duty may come from the heat exchange system and another portion may come from a cryocooler to produce a two-phase stream. The two-phase stream is separated in a second phase separator into a crude helium vapor stream and a crude neon liquid stream with the latter being introduced into a distillation column to produce a vent stream containing a helium impurity and a pure liquid neon product. The pure liquid neon product is vaporized in the heat exchange system to generate refrigeration and produce the pure gaseous neon product.

A system and method for liquefying a hydrogen gas feed stream uses a pre-cooling refrigerant for pre-cooling the feed stream, where the pre-cooling refrigerant is compressed, cooled and then separated to provide high pressure mixed refrigerant vapor and liquid streams. The high pressure vapor stream is cooled and directed to a cold vapor separator where cold separator liquid and vapor streams are formed. The cold separator vapor stream is cooled and expanded to provide a pre-cool refrigeration stream in a heat exchanger system. The high pressure pre-cooling refrigerant liquid and cold separator liquid streams are cooled and expanded and directed to the pre-cool refrigeration stream. A high pressure primary refrigerant steam, after compression and cooling, is further cooled in the heat exchanger system and then expanded using warm and cold expanders, with the resulting expanded primary refrigerant streams used to liquefy the pre-cooled hydrogen feed stream via heat exchange in the heat exchanger system.

The invention provides a liquid air energy storage system and method for coupling LNG and an air separation device, and relates to the technical field of energy storage. The liquid air energy storage system coupling the LNG and the air separation device comprises an LNG tank body, an air compression device, a main heat exchanger, a nitrogen circulation device, a liquid air storage tank, a rectification device and a power generation device. Circulating nitrogen is adopted as a heat exchange intermediate medium, so that the temperature zones of the liquefied natural gas vaporization process and the compressed air cooling process are matched, the liquefied natural gas is isolated from the compressed air, and the safety of the system is guaranteed. By adjusting the system flow, on the premise that the vaporization process of the liquefied natural gas is not affected, the air separation subsystem can absorb the cold energy of the liquefied natural gas in the peak period, a cold storage unit of the LNG-LAES is omitted, and the oxygen production energy consumption is effectively reduced. By adjusting the operation load of the air separation subsystem, the multi-cogeneration system can effectively cope with seasonal fluctuation of the vaporization amount of the liquefied natural gas, and the peak regulation capacity of the system is enhanced.

Example gas recovery systems include a source gas conditioning assembly configured to condition and compress the inlet source gas to provide a conditioned source gas, a first membrane assembly configured to separate the conditioned source gas into a hydrocarbon enriched stream and a recovery stream, a second membrane assembly fluidly coupled to the hydrocarbon enriched stream, and configured to separate the hydrocarbon enriched stream into a hydrocarbon product stream and a recycle stream, a carbon dioxide (CO2) plant assembly fluidly coupled to the recovery stream configured to provide a carbon dioxide product stream and an enriched recycle stream, a standalone membrane assembly configured to separate the enriched recycle stream into a hydrocarbon enriched recycle stream and an effluent stream, and wherein the source gas conditioning assembly is fluidly coupled to the recycle stream and the hydrocarbon enriched recycle stream.

The embodiment of the invention provides a liquid air energy storage system and a liquid air energy storage method.The liquid air energy storage system comprises an air compressor, a cooler set, an air throttling device, a gas-liquid separator, a liquid air storage tank, a first refrigeration compressor and a first refrigeration throttling device; the cooler set is provided with a first cooling channel, a second cooling channel, a third cooling channel and a first refrigerant channel, the input end of the third cooling channel is used for being connected with the output end of the cold storage medium cold tank, and the output end of the third cooling channel is used for being connected with the input end of the cold storage medium hot tank; the input end of the first refrigerant channel is connected to the output end of the first refrigeration throttling device, and the output end of the first refrigerant channel is connected to the input end of the first refrigeration compressor; the output end of the first refrigeration compressor is connected to the input end of the first refrigeration throttling device. According to the technical scheme, cold sources of the system can be more diversified, and stable operation of the system under different loads is facilitated.

The invention relates to the technical field of liquid air energy storage, and discloses a liquid air energy storage coupling system. The liquid air energy storage coupling system comprises a liquid air energy storage subsystem and a biomass gasification subsystem. The liquid air energy storage subsystem comprises a compressor unit, a heat storage unit, a cold storage unit and a turbine unit. And the biomass gasification subsystem comprises a biomass gasification furnace. And an air inlet of the heat storage unit is communicated with an air outlet of the air compressor unit. And the cold storage unit communicates with the heat storage unit. An air outlet of the heat storage unit communicates with an air inlet of the turbine unit and is used for conveying high-temperature air to the turbine unit, the high-temperature air enters the turbine unit to drive the power generator to generate power, and an air outlet of the turbine unit is used for discharging cooled air. And a gasifying agent inlet of the biomass gasifier is communicated with an air outlet of the turbine unit. Resource utilization of clean air at the outlet of the liquid air energy storage system can be achieved, and the system efficiency of the liquid air energy storage system is improved.

The utility model provides a carbon dioxide liquefaction system, a liquid cargo system and a carbon dioxide capture system, and belongs to the technical field of carbon capture. Wherein the liquefying system comprises a compression device, a liquefying device and a storage tank device, the storage tank device receives liquid carbon dioxide output by the liquefying device through a second liquid inlet end and outputs gaseous carbon dioxide in the storage tank device into the compression device, and the compression device recompresses the gaseous carbon dioxide output by the storage tank device and outputs the compressed gaseous carbon dioxide into the storage tank device. Then liquefying by the liquefying device, and inputting into the storage tank device for storage; the gaseous carbon dioxide in the storage tank device is compressed and liquefied into the liquid carbon dioxide again, and the problems that in the liquid carbon dioxide storage process of the storage tank, part of the liquid carbon dioxide in the storage tank is gasified into the gaseous carbon dioxide, loss of the liquid carbon dioxide is caused, and then the liquefaction efficiency of the carbon dioxide is reduced are solved; the loss of liquid carbon dioxide is avoided.

The present disclosure relates to a carbon dioxide capture apparatus and process combined with biogas upgrading, and there is provided the carbon dioxide capture apparatus combined with biogas upgrading for simultaneously obtaining high purity methane and carbon dioxide, and improving separation efficiency without an additional process by making use of gas streams after a liquefaction process, and recovering cold heat in the process.

A turbine engine assembly includes a compressor section (26, 136) where an inlet airflow is compressed, a cryogenic fuel system (46) for generating flow of cryogenic fuel, an air separation system (66, 96) where an airflow is placed in thermal communication with a portion of the flow of cryogenic fuel for generating an enhanced oxygen flow (68). In a combustor section (28), the compressed inlet airflow and a portion of the enhanced oxygen flow (68) is mixed with fuel and ignited to generate an exhaust gas flow (44) that is communicated through a core flow path (C) to a turbine section (30, 140) where expansion of the exhaust gas flow (44) is utilized to generate a mechanical power output. Water is extracted from the exhaust gas flow (44) in condenser (58) transformed into a steam flow (56) for injection into the core flow path (C) in an evaporator system (54).

The invention relates to the technical field of carbon dioxide capture, and provides a carbon capture system and a carbon capture method.The carbon capture system comprises a denitration and desulfurization device, a compression device, a refrigeration device and a cold rectification device, and the inlet side of the denitration and desulfurization device is used for introducing carbon-containing waste gas; the denitration and desulfurization device, the compression device and the cold rectification device are sequentially connected through a pipeline, and the pipeline between the compression device and the cold rectification device is thermally conducted with the refrigeration end of the refrigeration device; the cold rectification device comprises a cold rectification tower, and at least one of the inlet side and the outlet side of the cold rectification tower is in thermal conduction with the refrigeration end of the refrigeration device. The problem that the energy utilization rate is low in carbon dioxide capture, utilization and storage can be solved.

A gas supply system for a high-pressure gas consuming appliance and a low-pressure gas consuming appliance of a floating structure including a tank containing the gas is disclosed. The supply system includes: a first supply circuit and a second supply circuit; a gas return line; and a first heat exchanger and a second heat exchanger configured to carry out a heat exchange between the gas of the first supply circuit and the gas circulating in the return line. The first supply circuit includes an additional pump.

The invention relates to a natural gas liquefaction process using supersonic velocity spray pipe precooling. The system comprises a pre-cooling unit, a deep cooling unit, a heat exchange unit and a natural gas liquefaction unit. The pre-cooling unit comprises a supersonic spray pipe and a throttle valve; the cryogenic unit comprises a throttle valve, a compressor, a cooler, a component distributor and a mixer; the heat exchange unit comprises a heat exchanger; the natural gas liquefaction unit comprises a throttle valve and a separator. According to the production process, the technical scheme of supersonic spray pipe precooling and mixed refrigerant circulating cryogenic cooling is adopted. Compared with other processes, the process has the advantages of low refrigerant consumption, low energy consumption, high natural gas liquefaction rate, low process complexity, low equipment investment, good environmental protection benefit and the like under the same condition, and can efficiently recover the natural gas condensate (NGL) while precooling.

The invention discloses a cryogenic reliquefaction device utilizing natural gas cold energy. The cryogenic reliquefaction device comprises a compressor, an expansion machine and a motor used for driving the compressor and the expansion machine to rotate. The compressor is sequentially connected with the water cooler, the backheating heat exchanger, the expansion machine and the supercooling heat exchanger through pipelines to form a cooling loop; a cooled loop is formed between the supercooling heat exchanger and the liquefied natural gas storage device; at least one refrigerant side inlet of the backheating heat exchanger is communicated with the liquefied natural gas storage device, and an outlet of the backheating heat exchanger is communicated with the boil-off gas collecting facility. When the reliquefaction device works, natural gas cold energy can be fully utilized, part of heat exchange loss of the heat exchanger is offset, the inlet and outlet temperature of the compressor is improved, the compression efficiency is greatly improved, meanwhile, the use amount of cooling water can be reduced, and therefore the comprehensive efficiency of the reliquefaction device is improved. And the device has high economic and practical values in occasions where natural gas is needed.

The invention discloses a hydrogen low-temperature precooling device and method with oxygen liquefaction, relates to the technical field of low-temperature refrigeration and hydrogen energy liquefaction, and is particularly suitable for cooperative utilization of a hydrogen-oxygen co-production system in green hydrogen production. The device comprises a hydrogen pre-cooling cold box, a liquid oxygen cold box, a mixed refrigerant compression and heat exchange system, a nitrogen circulating refrigeration system and a trace oxygen analyzer arranged in a nitrogen loop. The raw material hydrogen is subjected to purification, precooling, adsorption and ortho-parahydrogen conversion treatment to obtain liquefiable precooled hydrogen; a liquid oxygen product is output after raw material oxygen is purified and liquefied through heat exchange. According to the device, cryogenic heat exchange is achieved through two-stage circulation of mixed refrigerants and nitrogen, a multi-temperature-zone segmented heat exchange network is constructed through multiple separation tanks and a throttling path, and the refrigeration efficiency and the heat recovery capacity are both considered. And liquid oxygen cooling can be dynamically regulated and controlled through a temperature-regulating nitrogen path to adapt to various working conditions of the electrolytic cell. The device is compact in structure, high in safety, excellent in energy efficiency and suitable for the hydrogen-oxygen synergistic liquefaction treatment scene in a water electrolysis hydrogen production device.

A method to control the cooldown of main heat exchangers in liquefied natural gas plant. The method provides for the automated control of a flow rate of a natural gas feed stream through a heat exchanger based on one or more process variables and set points. The flow rate of refrigerant streams through the heat exchanger is controlled by different process variables and set points, and is controlled independently of the flow rate of the natural gas feed stream.

The present invention improves the efficiency of liquefaction of a feed gas. This liquefaction device includes: a feed pipeline through which a feed gas flows; a feed-cooling part by which the feed gas being flowing in the feed pipeline is cooled with a refrigerant; a magnetic refrigeration part which is disposed downstream from the feed-cooling part along the feed-gas flow inside the feed pipeline and by which the cooled feed gas is cooled with a magnetic body to liquefy the feed gas; and a magnetic-body-cooling part in which the magnetic body that has cooled the feed gas is cooled with a refrigerant.

A combined cycle power generation and storage system is shown. A liquid air energy storage system uses excess power to liquefy air and stores it in a liquid state. A combustion engine produces power by combustion of a carbon-based fuel along with an exhaust stream containing carbon dioxide. A heat recovery system exchanges heat from the exhaust stream to air from the liquid air storage system, and thereby produce a cooled exhaust stream and heated air. An air expansion machine recovers power by expansion of heated air from the heat recovery system. A separation system separates carbon dioxide from ambient air prior to liquefaction during operation of the liquid air energy storage system, and separates carbon dioxide from the cooled exhaust stream during operation of the combustion engine prior to emission of the cooled exhaust stream to atmosphere.

A turbine engine assembly includes a compressor section where an inlet airflow is compressed, a cryogenic fuel system for generating flow of cryogenic fuel, an air separation system where an airflow is placed in thermal communication with a portion of the flow of cryogenic fuel for generating an enhanced oxygen flow. In a combustor section, the compressed inlet airflow and a portion of the enhanced oxygen flow is mixed with fuel and ignited to generate an exhaust gas flow that is communicated through a core flow path to a turbine section where expansion of the exhaust gas flow is utilized to generate a mechanical power output. Water is extracted from the exhaust gas flow in condenser transformed into a steam flow for injection into the core flow path in an evaporator system.

A liquefier device which may be a retrofit to an air separation plant or utilized as part of a new design. The flow needed for the liquefier comes from an air separation plant running in a maxim oxygen state, in a stable mode. The three gas flows are low pressure oxygen, low pressure nitrogen, and higher pressure nitrogen. All of the flows are found on the side of the main heat exchanger with a temperature of about 37 degrees Fahrenheit. All of the gases put into the liquefier come out as a subcooled liquid, for storage or return to the air separation plant. This new liquefier does not include a front end electrical compressor, and will take a self-produced liquid nitrogen, pump it up to a runnable 420 PSIG pressure, and with the use of turbines, condensers, flash pots, and multi pass heat exchangers. The liquefier will make liquid from a planned amount of any pure gas oxygen or nitrogen an air separation plant can produce.

A power supply and cooling system for a floating structure having a tank, includes a supply circuit having at least one compression device, the supply circuit being configured to supply gas to a gas-consuming device, and a cooling circuit having a heat exchanger configured to participate in managing the internal pressure of the tank, the cooling circuit being connected to the supply circuit on either side of the compression device. The compression device includes two compression stages, and the power supply and cooling system includes a control device configured to connect the compression stages in series or in parallel.

According to the equipment and the method, hydrogen is pre-cooled with a mechanical low-temperature pre-cooling cycle and a helium cycle through a first-stage heat exchanger, is subjected to ortho-secondary conversion through a second heat exchanger, a fourth heat exchanger and a fifth heat exchanger, and is subjected to heat exchange with cold helium discharged from a first turbo expander in the helium cycle; and liquid hydrogen generated after the liquid hydrogen enters the liquid hydrogen throttling valve to be throttled enters the liquid storage tank, and the hydrogen liquefaction process is completed. Helium entering and exiting the helium circulation low-temperature compressor unit is subjected to mechanical low-temperature precooling, the compression work is reduced through helium low-temperature compression, the expansion work is recycled through the turbo expander, and the thermodynamic efficiency of the system is improved; the hydrogen liquefying system only depends on the cooling capacity provided by the helium circulating system and the mechanical low-temperature pre-cooling circulating system, hydrogen liquefying can be completed without compression, and the system safety is improved; the helium circulation low-temperature compressor unit and the mechanical low-temperature compressor both adopt oil-free gas suspension centrifugal compressors, so that the problems of oil removal and oil return are avoided, and the reliability is remarkably improved.

Title: Process and apparatus for separating CO2 from at least two streams of different compositions. In an integrated separation process, a first stream (1) containing a first percentage of CO2 is compressed (1C), separated in a pre-concentration unit (P), producing a gas (11) enriched in CO2 and depleted in oxygen relative to the first stream, and the CO2-enriched gas is separated (1F) producing a fluid containing at least 95% mol CO2 (19) and at least a first fluid depleted in CO2 (15, 17). A second stream (2) contains a second percentage of CO2 higher than the first percentage. The second stream is compressed (2C), dried in a second drying unit (2D), and separated by partial condensation and / or distillation in a second separation unit (2F, 2G).the second separation unit producing a CO2-enriched fluid (119) containing at least 90 mol% CO2 and depleted in oxygen, as well as a second CO2-depleted and oxygen-enriched fluid (121), and to recover the CO2 present in the second CO2-depleted fluid, this fluid is sent at least partially upstream of the pre-concentration unit. Abstract figure: Fig. 1,

The utility model relates to a liquid air production device which comprises a raw material air compression system, an air cooling and drying system, a circulating pressurization system, an expansion refrigeration system, a heat exchange cold box and a liquid air storage tank. The raw material air compression system comprises a gas feeding air compressor and an air cooler; the air cooling and drying system comprises a freezing dryer and an adsorption dryer; and the circulating supercharging system comprises a circulating supercharger and a supercharging cooler. According to the production method, efficient production of liquid air is achieved through the steps of multi-stage compression, cooling, drying, pressurization, expansion refrigeration and the like. By optimizing energy utilization, low-temperature air cooling capacity is recycled, compression work and power consumption are saved, and the production cost is remarkably reduced. The device is suitable for the fields of energy storage, metal smelting, precision manufacturing and the like.

Disclosed is a gas separation arrangement for separating and containing various types of gas from a collection chamber based on their different atomic masses. The chamber is connected to an ion diverter via a valve that when open permits the various types of gas to migrate from the collection chamber to an ionizer where the gas is ionized. The ionized gas is accelerated through an ion accelerator and dispensed into an ion deflector. The ion deflector comprises a magnetic field within a channel defined by a pair of split-pole magnets. The trajectory of the ions is based on the mass of the ions, which separates the ions. Multiple collectors are positioned at different locations on an exit side of the ion deflector to receive the different ions traveling along their respective trajectories.

The invention relates to an installation (1) for recovering CO2 from a feed gas stream (FG), comprising: - a unit (2) for treating the feed gas stream (FG) in order to produce a CO2-enriched gas stream (FCO2) and a nitrogen-enriched gas stream (FN) from the feed gas stream; - a compression stage (5) for compressing the feed gas stream (FG); - an expansion stage (8) capable of outputting mechanical energy generated by expansion of the nitrogen-enriched gas stream; - a thermal device (10) arranged to enable heat transfer between the gas stream leaving the compression stage (5) and the nitrogen-enriched gas stream before expansion; and - a device (4) for utilizing the mechanical energy output by the expansion stage.

A method for providing a nitrogen product, an oxygen product and a hydrogen product, wherein an air separation installation is used which is designed for the low-temperature separation of feed air and which has a rectification column system, the rectification column system comprising an air-fed rectification column and a main heat exchanger. The provision of the nitrogen product comprises, in particular, subjecting feed air to low-temperature rectification using the air-fed rectification column such that a tops gas is obtained, and using part of the tops gas as the nitrogen product. The provision of the oxygen product and the hydrogen product comprises subjecting water to water electrolysis in an electrolyzer, such that a water-containing oxygen stream and a hydrogen stream are obtained, the water-containing oxygen stream or part thereof being subjected, at least in one operating phase, to drying and, in an unmixed state, to liquefaction in the air separation installation.

A carbon dioxide recovery device provided with a separation device that separates carbon dioxide from to-be-separated gas (for example, combustion exhaust gas) containing carbon dioxide, wherein: in order from the upstream side where the to-be-separated gas is supplied, the separation device and carbon dioxide sublimators, which sublimate (solidify) carbon dioxide that was separated in the separation device, are connected in series, refrigerant circuits in which a fluid having cold heat serves as the refrigerant, are connected to the carbon dioxide sublimators, and the refrigerant is used to sublimate (solidify) the carbon dioxide; and when the carbon dioxide is sublimated (solidified), the carbon dioxide sublimators are depressurized and set to negative pressure so as to draw in the carbon dioxide separated at the separation device.

Systems herein separate an inlet gas stream containing methane, C2 components, C3 components and optionally heavier hydrocarbons into a volatile gas fraction containing methane and a less volatile hydrocarbon fraction containing C2+ components. The system may include piping, valving, and controls configured to flexibly allow the system to operate in a high ethane recovery mode, a high throughput mode, or in some embodiments, a high propane recovery mode.