800results about "Cold treatment separation" patented technology

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.

Plant and method for producing hydrogen at cryogenic temperature, comprising: an electrolyzer; a hydrogen circuit to be cooled, comprising an upstream end connected to the hydrogen outlet and a downstream end to be connected to a member for collecting cooled and / or liquefied hydrogen, the plant also comprising a set of heat exchanger(s) in heat exchange with the hydrogen circuit to be cooled, the plant comprising at least one cooling device in heat exchange with at least a portion of the set of heat exchanger(s), the plant further comprising an oxygen circuit comprising an upstream end connected to the oxygen outlet and a downstream end, the oxygen circuit comprising a system for expanding the oxygen stream and at least one heat exchange between the expanded oxygen stream and the hydrogen circuit to be cooled, characterized in that the oxygen circuit comprises at least one oxygen compressor arranged upstream of the oxygen stream expansion system, the oxygen stream expansion system comprising an expansion turbine and in that said expansion turbine and said compressor are coupled to the same rotating shaft to transfer expansion work from the pressurized oxygen stream to the compressor in order to compress the oxygen stream upstream of the turbine.

The invention relates to an installation for liquefying hydrogen, comprising a circuit for hydrogen to be cooled, a set of heat exchanger(s) in heat exchange with the circuit, a cooling system comprising a refrigerator with a cycle of refrigeration of a first cycle gas comprising helium and / or hydrogen, the circuit comprising at least one catalysis section so as to ensure conversion of the ortho-hydrogen into para-hydrogen, the circuit further comprising a first bypass portion bypassing at least one catalysis section, the downstream end of the circuit comprising two parallel branches that are not combined and are supplied respectively with the hydrogen that has passed through the first bypass portion and hydrogen that has passed through the catalysis section so as to provide two distinct hydrogen streams that have different relative proportions of ortho-hydrogen and para-hydrogen.

The invention relates to the technical field of air separation, in particular to a pretreatment module of an air separation system, a high-purity air separation system and a control method.The pretreatment module comprises a precooling unit, and the precooling unit is connected with a cold source; the pre-cooling unit enables cooling water to circularly flow in the supercharging unit through a cooling water pipeline, and the supercharging unit comprises a first air compressor, a second air compressor, a high-temperature expansion machine supercharging end, a first supercharger after-cooler, a low-temperature expansion machine supercharging end and a second supercharger after-cooler which are sequentially connected in series through a main pipeline; supercharged and precooled air is expanded and cooled by the expansion unit and then enters the heat exchange unit; through the arrangement of the pre-cooling unit, the inlet and outlet temperatures of the high-temperature expansion machine and the low-temperature expansion machine are effectively controlled, reheated air returns to the air compressor, the expansion gas amount is increased, reheated gas continuously cools the air participating in rectification in the heat exchange unit, and in conclusion, the production energy consumption of a high-purity liquefied gas product is reduced.

The utility model discloses a recovery system for capturing carbon dioxide. The recovery system comprises a carbon capturing unit, a cooling unit, a drying unit, a liquefying unit and a storage unit which are sequentially connected through pipelines, after the carbon capture unit captures carbon dioxide, the carbon dioxide is cooled by the cooling unit and dried by the drying unit, then enters the liquefaction unit to be compressed and liquefied to form liquid carbon dioxide, and then the liquid carbon dioxide is conveyed to the storage unit to be stored. According to the utility model, CO2 after carbon capture can be stored after being cooled, pressurized and liquefied. The system integrates unloading and reliquefaction functions, liquid CO2 in the storage tank can be lighted to a CO2 receiver, and gaseous CO2 in the storage tank is returned to the storage tank for storage after being cooled, pressurized and liquefied. And the system is provided with a plurality of instruments and meters, so that the whole system is more automatic and safer to operate.

The invention discloses a hydrogen liquefaction control method and system based on AI decision making. The method comprises the steps that real-time operation data and parameters of a hydrogen liquefaction device are obtained; based on the real-time operation data and the parameters, a fuzzy clustering algorithm is utilized to identify the current working condition so as to determine the working condition type to which the current working condition belongs; based on the working condition type, a reinforcement learning algorithm is utilized to generate a target control strategy, and the target control strategy comprises at least one control strategy of the yield, the energy consumption and the equipment service life early warning of the hydrogen liquefaction device; and according to the target control strategy, utilizing a particle swarm optimization algorithm to adjust PID parameters of the hydrogen liquefaction device so as to control at least one of yield, energy consumption and equipment life early warning of the hydrogen liquefaction device. The response speed, stability and anti-disturbance capability of the control loop of the hydrogen liquefaction device can be improved, dependence on experience of operators is reduced, performance degradation of the hydrogen liquefaction device is avoided, and efficient operation of the hydrogen liquefaction device is guaranteed.

The disclosure describes processes which include cooling a natural gas product stream to a cryogenic liquid storage temperature by way of refrigeration streams which include a primary refrigeration stream, a secondary refrigeration stream, and a tertiary refrigeration stream in a refrigeration system. After leaving the refrigeration system, the pressure of each refrigeration stream is increased, and upon reaching a sufficient pressure, the refrigeration streams are recycled to flow back into the refrigeration system as a recycle stream. The disclosure further describes systems capable of performing the processes. The processes and systems can include one or more sensors and one or more controls capable of adjusting a flow rate, flow volume, and / or flow ratio among one or more gas streams to maximize cooling efficiency based on monitoring from the one or more sensors. Mobile natural gas liquefaction systems are also described.

Provided are an air separation device and an air separation method that have high argon yield without increasing the heat transfer area of a deoxidized argon condenser that generates reflux liquid in an argon tower generating deoxidized argon to be used as a raw material in a high-purity argon tower. Specifically provided is an air separation device comprising: an argon tower (700) that distills argon-containing oxygen drawn from a low-pressure tower (600) and generates deoxidized argon from which oxygen has been removed; a deoxidized argon condenser (400) that generates reflux liquid in the argon tower (700); a high-purity argon tower (800) that distills deoxidized argon and extracts pure argon from which nitrogen has been removed; a high-purity argon condenser (900) that generates reflux liquid for the top portion of the high-purity argon tower (800); a high-purity argon evaporator (910) that generates ascending gas for the bottom portion of the high-purity argon tower (800); a pipeline (622) that sends liquid nitrogen to the high-purity argon condenser (900) as a cooling medium; and a pipeline (42) that sends liquid derived from a high-pressure tower (500) to the high-purity argon evaporator (910) as a heating medium.

The application discloses a modular hydrogen liquefaction system, comprising: one or more parallelly arranged liquefaction modules, a hydrogen inlet of the liquefaction module being connected with a hydrogen source, and a product outlet of the liquefaction module being connected with one or more parallelly arranged liquid hydrogen storage tanks; each of the liquefaction modules is an integrated structure capable of hydrogen cooling, liquefaction, primary and secondary hydrogen conversion and independent start and stop. The application realizes hydrogen liquefaction by connecting a large number of refrigeration units in series and in parallel to form modules at different levels, can effectively utilize the benefit of large-scale production of standard refrigeration units, and reduces equipment cost. By controlling the number of different level modules and refrigeration units to be started, the application can also realize large-range liquid hydrogen production capacity adjustment. In addition, by using a regenerative refrigerator as a standard refrigeration unit, rapid cooling and instant shutdown can be realized, so that the system has the advantages of rapid start and stop. The above advantages make the application particularly suitable for matching with renewable energy to produce green liquid hydrogen.

The utility model discloses a system for efficiently preparing liquid nitrogen by using a two-stage membrane separation technology, and relates to the technical field of industrial purification and liquefied nitrogen. The membrane separation technology and the gas liquefaction technology are combined, so that nitrogen in air is purified, the residual pressure of medium-pressure gas is fully utilized to provide cold energy for high-concentration nitrogen liquefaction, and the residual potential energy of the high-concentration gas is utilized to improve the nitrogen generation efficiency. A compressor, a gas cooling module, a first-stage separator and a second-stage separator of the system are sequentially arranged in the flowing direction of air. A high-pressure outlet of the second-stage separator is communicated with a first hot end inlet of the first heat exchanger; a first outlet of the first heat exchanger is communicated with a hot end inlet of the second heat exchanger, a second hot end inlet is communicated with a side backpressure outlet of the first-stage separator, a second outlet is communicated with a cold end inlet of the second heat exchanger through an expansion machine, a third outlet is communicated with atmosphere, and the cold end inlet is communicated with a second outlet of the second heat exchanger; and a side backpressure outlet of the second-stage separator is communicated with the compressor.

Pure liquid nitrogen, liquid air or dirty liquid nitrogen generated by a rectifying tower of the air separation device is subjected to secondary pressurization through a hydraulic pump and then enters a main heat exchanger or a recooling device to recover cold energy, and high-pressure gas formed by heat absorption and gasification enters a high-pressure expansion machine to expand and do work; exhaust gas of the high-pressure expansion machine enters the rectifying tower to provide cold energy required by air separation, and pure nitrogen, waste nitrogen and pure oxygen which are discharged from the rectifying tower and are subjected to cold energy recovery through the main heat exchanger are output. The purposes of energy conservation and consumption reduction of the air separation device are achieved through the processes of primary pressurization of the compressor, secondary pressurization of the hydraulic pump, cold returning, gasification and expansion.

The present application relates to a kind of natural gas combustion flue gas separation utilization method and its system, comprising the following steps: S1, the flue gas to be treated is catalytically oxidized, so that residual oxygen in flue gas is fully reacted and eliminated;S2, flue gas enters preheater, heat exchange is carried out in preheater, so that the heat of flue gas is reduced;S3, compressor is used to compress flue gas, the temperature of flue gas is increased after being compressed by compressor, high temperature flue gas enters heat exchanger and is cooled by cooling water, wherein the water vapor contained is formed into liquid after cooling and discharged etc..The present application has the advantages that: flue gas generated by natural gas combustion is compressed and two-stage expansion refrigeration is used, liquid carbon dioxide and liquid nitrogen are separated in turn. The separation and utilization of natural gas combustion flue gas are realized, and the carbon dioxide discharged to the atmosphere is significantly reduced.

In a process for separating a gaseous mixture, a first piece of process equipment (B) is heated by a first flow rate (15, ) of a first calorigen and supplies heat to a first fluid (D1), the first flow rate of calorigen being heated upstream of the first piece of equipment by a heat source (H1, H2), a second piece of process equipment (C, D) heats a second fluid (D2) by consuming heat, the heat coming from a second flow rate (7,11) of the first calorigen heated by the heat source which heats the second flow rate of the first calorigen to an intermediate temperature lower than the second temperature and by a heater (H3) downstream of the source which reheats the second flow rate of the first calorigen, having been heated by the heat source, from the intermediate temperature to a second temperature higher than the first temperature and if the heat source is not available,The heater warms a flow (13) from the first heat source to the first temperature, and the flow warmed by the heater is sent at the first temperature to the first piece of equipment.

The cryogenic expansion turbine system (10) includes a turboexpander (12) configured to receive and expand a cryogenic gas supply stream (24). A rotating shaft (16) operatively connects the turboexpander to a compressor (14) or a resistance device, such as a braking device. A bearing housing (18) has a bearing cooling fluid inlet port and a bearing cooling fluid outlet port. Electromagnetic bearings (22) are disposed within the bearing housing and rotatably support the rotating shaft. A bearing cooling circuit (72) directs a flow of bearing cooling fluid (62) through the bearing cooling fluid inlet port and into the bearing housing, thereby cooling the electromagnetic bearings, and the resulting warmed bearing cooling fluid (68) exits the bearing housing through the cooling fluid outlet port.

A turbomachine includes: a rotating shaft; a casing including a liquid chamber and a gas chamber in which the rotating shaft extends; a hydrostatic liquid bearing located in the liquid chamber and supporting the rotating shaft through a lubricating liquid supplied to a bearing clearance between the hydrostatic liquid bearing and the rotating shaft; and a hydrostatic gas bearing located in the gas chamber and supporting the rotating shaft through a lubricating gas supplied to a bearing clearance between the hydrostatic gas bearing and the rotating shaft.

A liquid air energy conversion system is provided that integrates three subsystems or unit operations, namely a deep sub-ambient gas compression subsystem, a power expansion and heat recovery subsystem, and an external heat source.

The invention relates to the technical field of neon isotope separation, and discloses a neon isotope separation system and method.The neon isotope separation system comprises a neon gas tank, a supercharger, a first-stage heat exchanger, a second-stage heat exchanger, a mixing refrigerator and a multi-stage rectifying tower, and cold neon discharged from the top of the rectifying tower except the first-stage rectifying tower is subjected to heat exchange through the second-stage heat exchanger and the first-stage heat exchanger and then flows back to the supercharger, and the cold neon is effectively used as a refrigerant to cool neon. And then part of neon cooled by the first-stage heat exchanger is shunted into the reboiler of the multi-stage rectifying tower, the temperature of the neon in the rectifying tower is adjusted, separation of 20Ne and 22Ne is promoted, neon branches in the reboiler converge with neon branches cooled by the second-stage heat exchanger, heat in neon at different stages can be fully utilized, and energy consumption is reduced. The neon cooled by the first-stage heat exchanger is used for heat exchange and temperature adjustment of the neon in the rectifying tower, the temperature difference between the neon and the neon is not too large, the temperature of the neon in the rectifying tower can be effectively and finely adjusted, and then separation of isotopes 20Ne and 22Ne at the low temperature is promoted.

Embodiments provide a method for preventing shutdowns in LNG facilities by removing heavy hydrocarbons from the inlet gas supply. According to an embodiment, there is provided an LNG facility treating pipeline quality natural gas that is contaminated with lubrication oil and low concentrations of heavy hydrocarbons. Due to contamination, the behavior of the pipeline quality natural gas is not properly predicted by thermodynamic modeling. In an embodiment, heavy hydrocarbons are removed by a drain system in a heat exchanger. In an embodiment, heavy hydrocarbons are removed by a treatment bed.

The invention relates to a facility for cooling a flow of cryogenic fluid comprising a first circuit for fluid to be cooled, for example liquid nitrogen and / or liquid oxygen, a cryogenic refrigerator with a cycle circuit, at least one heat exchanger providing heat exchange with the first circuit for fluid to be cooled and the cycle circuit of the refrigerator, the facility comprising a second circuit for fluid to be liquefied, for example nitrogen gas and / or oxygen gas, the second fluid circuit being in heat exchange with the cycle circuit of the refrigerator in at least one heat exchanger of the facility, the facility being configured so as to be switchable into a first cooling operating mode, in which the facility cools the first fluid circuit in order to cool a liquefied fluid, preferably in order to generate a quasi-isothermal transformation of said fluid, and a second liquefaction operating mode, in which the facility cools the second fluid circuit with a view to liquefying a gas flow.

A hazardous fluid isolation system is provided for handling hazardous fluids, and includes a barrier that separates and partitions a hazardous zone from a non-hazardous zone. The system includes a processing unit for receiving and processing the hazardous fluid. The processing unit is located in a non-hazardous zone, and a hazardous fluid source is fluidically connected to the processing unit by a pipe network. The pipe network includes at least a first pipe that extends partly into the non-hazardous zone and partly into the hazardous zone, the first pipe being provided with a coupler for connecting a first section of the pipe extending from the hazardous zone to a second section of the pipe extending from the processing unit. The first pipe has an inner pipe and an outer pipe surrounding the inner pipe, partitioning a vacuum space and forming a vacuum insulation jacket surrounding the inner pipe.

The invention relates to a method for liquefying and purifying carbon dioxide from a gas comprising more than 70% by volume of carbon dioxide, the method comprising the following consecutive steps: a step of filtering the gas, then a step of compressing the gas at a pressure of between 60 bar and 80 bar, then a step of drying the gas, then a step of liquefying the gas, then a step of subcooling the liquefied gas, a step of expanding the liquefied gas, then a step of distilling the fluid so as to isolate the carbon dioxide, then a step of recovering the carbon dioxide in liquid form. The invention also relates to the device implementing the method and to the use thereof.

A system and method for liquefying a hydrogen gas feed stream uses a high-pressure hydrogen stream from a storage source to provide refrigeration to the system. After providing refrigeration to the system, the hydrogen from the high-pressure storage source is at a pressure not lower than the pressure of a cold box feed stream of the system, where the cold box feed stream includes the hydrogen gas feed stream and at least one recycle stream, and is not recycled back through the system but instead exits the system.

Methods and systems providing a process for cooling and liquefying a purified gaseous hydrogen feed stream to a liquid hydrogen stream that may be stored in a liquid hydrogen storage tank, as well as a system wherein ortho-hydrogen (o-H2) contained in the purified gaseous hydrogen feed stream may be converted to para-hydrogen (p-H2) through serial low-temperature catalytic converters along the cooling process from normal ambient temperature (300K) to the liquefied temperature about (20K) of the hydrogen.

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 of generating electrical energy using a fuel cell while decarbonizing an exhaust gas generated by the fuel cell is disclosed. Heat generated by an electrochemical reaction within the fuel cell can be recovered at both an anode side and a cathode side of the fuel cell, and at least some of the recovered heat can be used to preheat each of a natural gas fuel feed and an oxidant supplied to the fuel cell. A carbon capture system may be included and used to capture and liquefy carbon dioxide present in an anodic exhaust gas emitted by the fuel cell. The liquefaction subsystem of the carbon capture system may utilize liquefied natural gas from which the natural gas fuel feed is derived as a cooling media for liquefying captured and compressed carbon dioxide.

The utility model discloses a device for preparing high-purity nitrogen and ultra-pure nitrogen. The device comprises a lower tower, an upper tower, a main condensation evaporator, a subcooler, a main heat exchanger, a turbine expansion unit and an ultra-pure nitrogen tower, a raw material air outlet and an expanded air outlet are formed in the main heat exchanger, gas flowing out of the raw material air outlet is communicated with the bottom of the lower tower through a pipeline, and gas flowing out of the expanded air outlet is sequentially connected with the turbine expansion unit and the upper tower through pipelines; a second lower tower liquid nitrogen outlet in the middle of the lower tower is communicated with the ultra-pure nitrogen tower through a pipeline; an ultra-pure nitrogen product pipeline is arranged at the upper part of the ultra-pure nitrogen tower; and ultra-pure nitrogen or ultra-pure liquid nitrogen is discharged from the ultra-pure nitrogen product pipeline. The nitrogen and the liquid nitrogen in the lower tower are used as heat exchange media for rectifying the nitrogen by the ultra-pure nitrogen tower, so that the rectifying effect of the ultra-pure nitrogen tower is improved, the operation pressure of the ultra-pure nitrogen tower is reduced, more purified air enters the lower tower to participate in rectification, and the extraction rate of ultra-pure nitrogen and high-purity nitrogen is improved.

The invention discloses a natural gas and hydrogen liquefaction method and system with ultralow energy consumption and carbon emission. An ammonia water absorption type refrigeration cycle and an automatic cascade absorption type refrigeration cycle are adopted to replace an electric drive compression type / expansion type pre-cooling cycle, and wide-temperature-zone and deep pre-cooling cold supply is provided for the liquefaction process in a cascade cooling mode. The ammonia water absorption refrigeration cycle provides pre-cooling cold energy for a high-temperature area, and the ACAR cycle provides pre-cooling cold energy for a low-temperature area; and the two can be driven by low-grade waste heat discharged by a liquefaction factory, so that the dependence of the liquefaction system on high-grade electric energy is obviously reduced. Based on the condensation heat temperature slippage effect of the non-azeotropic mixed working medium and the heat pump principle, the configuration of ACAR circulation and ammonia water circulation can be improved, so that the utilization efficiency of low-grade heat energy is improved, and the pump power consumption in the solution boosting process is reduced. As the number of high-speed moving parts in the system is reduced, the operation stability is improved, the service life is prolonged, and the maintenance cost is correspondingly reduced.

Disclosed herein is a temperature-control device for controlling the temperature a fluid and method thereof. The temperature-control device includes a coil with first and second coils aligned along a coaxial direction and spaced apart from each other so that a magnetic field can be generated within a region between them. The temperature-control device includes a magnetocaloric member attached movably relative to the coil such that the magnetocaloric member and the coil can be moved relative to each other along a direction at an angle to the coaxial direction in the region to generate a magnetocaloric temperature control of the magnetocaloric member based on a magnetic field change during the movement of the coil arrangement and the magnetocaloric member relative to each other. The temperature-control device includes a heat transfer system thermally contacting the magnetocaloric component for providing heat transfer toward and / or away from the magnetocaloric component.

A gas separation device for separating and containing various types of gases from a collection chamber based on different atomic masses is disclosed. The chamber is connected to an ion diverter by a valve that, when opened, allows various types of gases to migrate from the collection chamber to an ionizer in which the gases are ionized. The ionized gas is accelerated by the ion accelerator and distributed into the ion deflector. The ion deflector includes a magnetic field within a channel defined by a pair of split-pole magnets. The trajectory of the ions is based on the ion mass of the separated ions. A plurality of collectors are located at different locations on the exit side of the ion deflector for receiving different ions moving along respective trajectories.

The invention discloses a liquid hydrogen production device and a working method thereof.The liquid hydrogen production device comprises a first heat exchanger, a pipe mechanism, a conversion mechanism, a cooling mechanism and a valve bank, a second cooling medium inlet, a first inlet and a first outlet are formed in the first heat exchanger, and the pipe mechanism comprises a first cooling pipe; and the first cooling pipes are connected with the first heat exchanger. The valve set comprises a second throttling valve, the second throttling valve is installed on a first cooling pipe, the first cooling pipe is communicated with a first outlet and a second cooling medium inlet, and circulating hydrogen entering the first heat exchanger from the first inlet exchanges heat with circulating hydrogen cooled and depressurized through the cooling mechanism. And the first cooling medium flows into the first cooling pipe from the first outlet, is throttled by the second throttling valve and enters the first heat exchanger from the second cooling medium inlet. The raw material hydrogen is cooled through the mode that expansion continuous refrigeration of the cooling mechanism cooperates with high-pressure throttling refrigeration, energy is saved, and meanwhile the product hydrogen with the parahydrogen content reaching 97% is produced.