2066results about "Cold treatment separation" patented technology

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.

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 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 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 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 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.

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.

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.

Methods and systems for recuperating power from a pressurized fluid stream of a carbon capture system are disclosed. A compressor pressurizes the carbon dioxide containing feed fluid and passes this fluid stream through a carbon capture process. The pressurized stream is expanded across a turbine where power is recovered.

The invention discloses a liquid air energy storage system based on air separation, which is characterized by comprising an air purification unit, an energy storage unit, an air rectification unit and an LNG (Liquefied Natural Gas) cold supply unit, wherein the air purification unit comprises an air filter, an air compressor, a first cooler, an adsorber and a first heater, and the energy storage unit comprises a first liquid separation tank, a liquid air storage tank, a liquid air pump and an air expansion machine. The air rectification unit comprises a rectification tower, a main cold box, a second liquid separation tank, a second subcooler, a first heat exchanger, a liquid nitrogen storage tank, a liquid oxygen storage tank, a second heat exchanger, an argon rectification system and a liquid argon storage tank; and the LNG cold supply unit comprises a first nitrogen supercharger, a second nitrogen supercharger, an LNG cold box and a first subcooler. The system has the functions of air separation and electric energy storage at the same time, and cold energy of the LNG receiving station is fully utilized for air separation and energy storage to participate in construction of a novel power system of a power grid.

Provided are a micro-scale apparatus and method for liquefying natural gas The apparatus comprises a first heat exchanger that cools a natural gas feed stream by heat exchange with a first cooling fluid from a chiller, a compressor configured to compress the cooled natural gas, an air cooler configured to further cool the compressed natural gas, a second heat exchanger configured to further cool the natural gas by heat exchange with a second cooling fluid, a third heat exchanger configured to further cool the cooled natural gas, a joule-thompson (JT) valve configured to cool the flow of cooled natural gas to create LNG, a separator configured to separate a liquified LNG from a vapour phase, and a return flow path connected to the natural gas inlet, wherein the return flow path is optionally configured to pass as cooling medium via the third heat exchanger, wherein optionally the return flow path is configured to transport the vapour phase from the separator via the third heat exchanger for heating by heat exchange a gas flow entering the inlet of the third heat exchanger, and to combine the heated vapour phase with the natural gas feed stream.

The invention relates to a combustion optimization and cryogenic separation-based carbon dioxide enrichment and hydrogen production synergy process for a combined device, which is characterized in that regeneration of a spent catalyst in a catalytic cracking device is changed into pure oxygen incomplete combustion, and circulating carbon dioxide is used for stabilizing fluidization and controlling tail combustion. And after the regenerated flue gas is subjected to deep purification and cryogenic separation, the part rich in carbon monoxide is fed into a medium-temperature change reactor of the steam hydrocarbon reforming device for hydrogen production, so that resource upgrading of catalytic coke is realized. And compressing and cooling the part rich in carbon dioxide to obtain about 98% of liquid phase product for subsequent application. According to the catalytic cracking device, only the regenerator needs to be adjusted, the deep purification and compression cryogenic separation unit is additionally arranged, the hydrogen production device can improve the treatment capacity of the medium-temperature change reactor, implementation is convenient, and the catalytic cracking device is suitable for new and old devices. The invention further relates to a system for carbon dioxide enrichment and hydrogen production synergy of the integrated device based on combustion optimization and cryogenic separation.

A method of controlling the renewable energy absorbed by a hybrid power train for driving a load, and in particular compressors for a liquefied natural gas (LNG) plant is disclosed. The method comprises an analysis of the health status of part and of the whole hybrid power plant that drive the load. A power plant is also disclosed, operated by the controlling method.

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.

A process for the production of hydrogen is described comprising the steps of: (i) subjecting a gaseous mixture comprising a hydrocarbon and steam to steam reforming in a reforming unit comprising an autothermal reformer to generate a reformed gas mixture; (ii) increasing the hydrogen content of the reformed gas mixture by subjecting it to one or more water-gas shift stages in a water-gas shift unit to provide a hydrogen-enriched reformed gas; (iii) passing the hydrogen-enriched reformed gas and an oxygen-rich gas to an oxidation unit containing an oxidation catalyst that converts carbon monoxide present in the hydrogen-enriched reformed gas to carbon dioxide, to form a carbon dioxide-enriched gas mixture; and (iv) passing the carbon dioxide-enriched gas mixture to a product separation unit to provide a hydrogen gas stream, a carbon dioxide gas stream and a by-product gas stream, wherein at least a portion of the by-product gas stream is compressed and recycled to one or more of the reforming unit, the water-gas-shift unit, the oxidation unit, and the product separation unit.

The invention discloses an LNG (Liquefied Natural Gas) cold energy gradient utilization system coupled with seawater desalination and liquefied air energy storage. A seawater desalination module of the system carries out seawater desalination by using cold energy of liquefied natural gas, and a liquefied air energy storage module carries out air compression and liquefaction in a power off-peak period and releases energy to generate power in a power peak period; the system can switch a seawater desalination priority mode, an energy storage peak regulation mode and a composite energy supply mode. According to the system, a double-loop structure is adopted, liquefied natural gas cold energy, solar heat energy, electric energy and environmental resources are fully coupled, multi-energy complementation, gradient utilization and combined cooling heating and power are achieved, flexible switching of three cooperative operation modes is achieved, the operation state of the system can be adjusted according to the external load requirement, the resource utilization efficiency and the operation economy are improved, and the energy consumption is reduced. The modular design has good expandability and engineering adaptability, has the characteristics of being green, energy-saving, environment-friendly, high in safety and stable in operation, and is suitable for guaranteeing regional water resources and balancing power generation fluctuation of unstable green energy.

The invention is directed to a carbon capture and liquefication system comprising a liquified natural gas (LNG) exergy recovery section. The invention is more specifically directed to such a system to liquify carbon dioxide (CO2) gas from a CO2 containing gas, more particularly from an exhaust gas from a means of maritime transportation. The invention is further directed to a method for recovery of exergy using the exergy recovery section, a means of maritime transportation comprising the system, and the use of such a system for liquefaction of carbon dioxide gas.

The invention relates to the technical field of intelligent control, and discloses a combined refrigeration liquefaction intelligent control system which comprises a natural gas combined refrigeration liquefaction process unit, a BOG recycling and isolated network power generation unit and a self-adaptive intelligent control system. The core of the system is that a safe, efficient and economical liquefaction recovery mode aiming at scattered gas well mouths which are short in life cycle, fast in gas quantity attenuation, weak in field infrastructure and simple in operation and maintenance personnel is realized through a combined refrigeration liquefaction process, BOG (Boil Off Gas) recovery and utilization, isolated network power supply and full-system self-adaptive intelligent control mode. And the adaptive intelligent control system evaluates the health condition of the equipment in real time and predicts the dynamic change of the process by constructing a digital twinborn model synchronous with the physical system. Based on the global optimization and self-healing control module, rolling optimization solution is carried out by taking a comprehensive operation cost as a target function, and a control instruction considering both production efficiency and equipment protection is generated.

The invention discloses a hydrogen deep hypothermia three-loop refrigeration device and method, and relates to the technical field of hydrogen liquefaction. The device comprises a raw material hydrogen supply system, an ortho-parahydrogen conversion system, a three-loop hydrogen refrigerating system, a liquid hydrogen collecting and supercooling system and a gas recycling system. Wherein the raw material hydrogen is sequentially cooled by the pre-cooling cold box and the multi-stage heat exchanger and then enters the ortho-parahydrogen converter to be converted into parahydrogen, and then the parahydrogen is subjected to flash separation to obtain a liquid hydrogen product. The three-loop refrigerating system adopts three modes of high-pressure hydrogen expansion, medium-pressure liquid hydrogen throttling and low-pressure flash steam recovery to supply cold synergistically, and precise matching of the cold capacity of different temperature zones is achieved. Hydrogen is adopted as a refrigerant, the refrigerant cost is low, the heat exchange temperature difference is reduced through three-loop collaborative refrigeration, the flash evaporation loss is reduced, meanwhile, the system stability and the liquid hydrogen quality are improved through expansion work recovery and full parahydrogen conversion, and the system is suitable for large-scale liquid hydrogen preparation.

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 utility model discloses a liquid air energy storage system coupled with air separation and dry ice preparation, which comprises an air compression liquefaction subsystem, a cold energy gradient utilization subsystem, an air expansion power generation subsystem and a heat storage subsystem, the air compression and liquefaction subsystem, the cold energy gradient utilization subsystem and the expansion power generation subsystem are sequentially connected through a compression and liquefaction pipeline and an expansion power generation pipeline, and the heat storage subsystem is connected with the air compression and liquefaction subsystem and the air expansion power generation subsystem through a heat storage circulation pipeline. The cold energy gradient utilization subsystem is arranged to replace an existing low-temperature cold storage unit, the liquid air energy storage system is coupled with the air separation unit and the dry ice preparation unit, liquid air cold energy gradient utilization is achieved, and meanwhile energy consumption and construction cost of the air separation system are reduced. The power generation stability of the liquid air energy storage system is guaranteed, and the comprehensive efficiency and the environmental protection property of the liquid air energy storage system are improved.

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.

A liquefied natural gas (LNG) production facility includes gravity-based structures (GBSs) with process lines for liquefying natural gas. A GBS contains: tanks for each component of a mixed refrigerant, wherein a GBS process line includes a fractionating apparatus for mixed refrigerant component production from a broad fraction of light hydrocarbons; a stabilized gas condensate (SGC) storage tank; and a berth for offloading LNG and SGC into tankers. Each GBS contains an LNG storage tank. One tank per mixed refrigerant component from each GBS is connected by pipe to systems for preparing and compressing all process line refrigerants, thus forming a common component feed system. The SGC storage tank is connected by pipes to condensate-stabilizing apparatus for all process lines, thus forming a common system for storing and offloading SGC. The LNG storage tanks are interconnected by pipes, forming a common system for storing and offloading LNG.

The invention discloses a compressed carbon dioxide energy storage method and system coupled with a heat supply generator set. The method comprises the steps that S1, an energy storage medium is prepared, and energy is stored; s2, performing energy release; s3, the intelligent control module carries out cooperative regulation and control: collecting each energy flow parameter and each equipment stress parameter, carrying out grid division, and retaining each key solution based on epsilon-dominated solution distribution; constructing an objective function and setting constraint conditions; population updating is carried out on the target function, and a current optimal working condition and adjustment parameters of each device are obtained; and the intelligent control module controls the equipment. According to the invention, CO2 separated and purified from boiler flue gas is used as a cycle working medium, energy conversion core cycle of compression heat storage-expansion energy release is combined with a fused salt heat storage tank and intelligent control, efficient storage, release and poly-generation utilization of energy are realized, the core process comprises three stages of carbon medium preparation, energy storage and energy release, and the energy storage and the energy release are integrated. And poly-generation utilization and intelligent optimization control are realized.

A process and an apparatus are disclosed for separation of a hydrocarbon gas stream containing methane and heavier hydrocarbons and significant quantities of nitrogen and carbon dioxide. The gas stream is cooled and expanded, then fractionated in a first distillation column into a first overhead vapor and a hydrocarbon liquid stream containing the majority of the carbon dioxide. The hydrocarbon liquid stream is fractionated into a hydrocarbon vapor stream and a less volatile fraction comprised of heavier hydrocarbons.The first overhead vapor is cooled, expanded, and separated into vapor and liquid streams. Both streams are cooled and expanded before feeding a second distillation column that produces a second overhead vapor that is predominantly nitrogen and a bottom liquid that is predominantly methane. The bottom liquid is vaporized and combined with the hydrocarbon vapor stream to form a volatile residue gas fraction containing the majority of the methane.