30results about "Hydrogen separation using liquid contact" patented technology

A hydrocarbon stream is combusted within a reactor to produce soot and syngas. Sub-stoichiometric combustion of the hydrocarbon stream within the reactor converts at least 10% of the carbon in the hydrocarbon stream into soot. The syngas is mixed with a steam stream to produce a hydrogenation feed stream. A shift reactor converts at least a portion of the carbon monoxide and steam to carbon dioxide and hydrogen to produce a shifted gas stream. Water is separated from the shifted gas stream to produce a dehydrated gas stream. The dehydrated gas stream is separated to produce a hydrogen product stream and a recycle stream. The recycle stream is recycled to the reactor.

The present application relates to a process for producing synthetic ammonia by using hydrogen-containing tail gas, comprising the following steps: S1: sodium cyanide tail gas is pressurized, then heated and water-cooled. S2: the impurity-removed tail gas is desulfurized. S3: the desulfurized tail gas is mixed with chlor-alkali tail gas, the mixed gas is heated and deoxidized. S4: the deoxidized tail gas is pressurized and enters a PSA (pressure swing adsorption) device for pressure swing adsorption treatment, obtaining high-purity hydrogen. In the PSA device, dehydrating, carbon dioxide, methane, carbon monoxide and nitrogen adsorbents are sequentially arranged. The carbon dioxide adsorbent is activated carbon modified by carbonate and strong alkali, and the nitrogen adsorbent is 13X zeolite molecular sieve modified by Na + and Ba 2+ and Ca 2+ ion exchange. S5: nitrogen reacts with the high-purity hydrogen obtained in step S4 to generate ammonia. The present application can improve the adsorption capacity of the adsorbent for impurity gas, thereby reducing the replacement frequency of the adsorbent, prolonging the service period and service life of the adsorbent, and improving the production efficiency.

The subject of this invention is the system for generation and use of hydrogen in which a subsystem for hydrogen generation (U1) contains a reaction chamber (1) with aluminium (2) and sodium hydroxide (3), to which a water nozzle (4) is attached, connected through a duct (5) to a water pump (6). The upper part of the reaction chamber (1) contains an outlet connection (7) connected to a subsystem for hydrogen purification (U2), which is connected to the subsystem for hydrogen oxidation (U3), to which an inlet (27) through oxygen is supplied, is connected. This system is characterised in that the subsystem for hydrogen purification (U2) contains at least one water tank (9) connected to the subsystem for hydrogen oxidation (U3), which outlet (21) is connected through a non-return valve (22) with the condensing tank (23).

The application discloses a recycling method of condensate of ammonia shift stripping tower, comprising the following steps: S1 condensate cooling: hot condensate with a temperature of 80-100 DEG C is led out from the lower part of the ammonia shift stripping tower; S2 split delivery: the cooled condensate is divided into two routes by a condensate pump: the first route is sent to a synthetic gas washing tower to replace fresh desalted water for cooling and demisting of the synthetic gas, and fresh water consumption is reduced; the second route is sent to a carbonization mother liquor tank; S3 ammonia absorption concentration: the ammonia absorption pump is used to deliver the ammonia absorption mother liquor in the carbonization mother liquor tank to a high ammonia absorber; S4 concentrated ammonia water cooling: the concentrated ammonia water after concentration is sent into an air-cooled heat exchanger; S5 carbonization reaction product: ammonia in the concentrated ammonia water reacts with carbon dioxide to generate ammonium bicarbonate crystals, and ammonium bicarbonate products are obtained after separation and drying. The whole recycling process can be directly connected with the existing ammonia production system, the existing equipment does not need large-scale modification, the investment cost is low, and the industrialization popularization is easy.

The application discloses a kind of high flash gas multi-element recycling device and method, belong to synthetic ammonia acid gas processing technical field, including hydrogen extraction system, high flash gas sulfur recovery system and high flash gas recovery ammonia system, high flash gas recovery ammonia system is communicated with high flash gas sulfur recovery system, hydrogen extraction system is connected with high flash gas recovery ammonia system.The application uses the above-mentioned one kind of high flash gas multi-element recycling device and method, by the desorption gas compressor of PSA hydrogen extraction device, gasification high flash gas is recovered to shift system, greatly improve the utilization value of high flash gas;By sending part of high flash gas into sulfur recovery device, the natural gas consumption of incinerator can be reduced, and the sulfuric acid production and byproduct steam production are increased;By setting raw material gas heat exchanger, part of purified gas is led to PSA hydrogen extraction device to prepare high-purity hydrogen.

Gasification processes utilizing carbonaceous feeds and preferably biomass are disclosed, which can implement one or more strategies for valuable integration with process streams generated when converting the syngas product of gasification to more valuable end products, such as biomethanol. For example, these waste stream generally referred to as fusel oil may be recycled to where it can be utilized in the gasification process, such as for the upstream conversion of biomass or other carbonaceous material, providing the syngas that is reacted to form the biomethanol. A particular use of fusel oil is in a tar conversion or tar destruction area that may operate with a partial oxidation (POX) burner as an integral or key part of the overall gasification.

The present disclosure relates to a purification system for purifying a gaseous product produced by electrolysis comprising: a separation vessel (10) configured to contain a separating liquid (12), and where the gaseous product is passed through the separating liquid (12) to at least partially remove a contaminant from the gaseous product in use. A condenser vessel (30) operatively connected downstream of the separation vessel (10), the condensing vessel (30) comprising a condenser (24) configured to condense one or more contaminant out from the gaseous product. The separation vessel (10) and the condensing vessel (30) are provided as separate, fluidly connected vessels.

The present application relates to the field of syngas preparation of olefins, and particularly relates to a syngas recovery method and system in syngas preparation of low-carbon olefin products. The recovery method comprises the following steps: (1) performing first gas-liquid separation on the decarburization product after the syngas preparation of low-carbon olefin products is decarburized to obtain a first gas phase and a first liquid phase; (2) performing second gas-liquid separation on the first gas phase to obtain a second gas phase and a second liquid phase; (3) performing cryogenic absorption separation on the second gas phase by using an absorbent to obtain crude syngas and a rich absorbent liquid phase. In the method, the first gas-liquid separation, the second gas-liquid separation and the cryogenic absorption separation are coupled for syngas recovery, and the method has the characteristics of simple process, low energy consumption, high separation efficiency, high syngas recovery rate and high low-carbon olefin removal rate.

A process and system to integrate a steam cracking unit with a blue ammonia unit such that a methane-rich gas stream and / or a hydrogen-rich gas stream is directed from the steam cracking unit to the blue ammonia unit while a hydrogen gas containing stream is directed from the blue ammonia unit to the steam cracking unit.

The utility model relates to the technical field of hydrogen production from methanol, provide a kind of for methanol steam catalytic reforming integrated device, including shell and the first tube being arranged in several in shell. Shell is at least separated into the first heat exchange cavity for accommodating heat conducting medium and the water washing cavity for accommodating desalted water along the axial arrangement, and first tube extends through the first heat exchange cavity and extends to water washing cavity. Wherein, catalyst is equipped in the pipe section of first tube in the first heat exchange cavity;First tube is in fluid communication with water washing cavity, and the conversion gas generated by catalytic reforming reaction is removed after methanol by desalted water in water washing cavity then flows out integrated device again;And desalted water that dissolves methanol is used as part of raw material of catalytic reforming reaction. The integrated device structure of the present disclosure is compact, by setting the first heat exchange cavity in the upper portion of integrated device, setting water washing cavity in lower portion, so that multiple devices (or units) in the hydrogen production system for methanol steam reforming can be integrated, reduce floor area.

A process for reforming for producing hydrogen and generating electricity, comprises: introducing a feed comprising a hydrocarbon stream to a reformer to produce unshifted synthesis gas (syngas); introducing the unshifted syngas to a water gas shift unit to produce a shifted syngas; removing CO2 from the shifted syngas to produce a CO2 depleted syngas and a CO2 product; introducing the CO2 depleted syngas to a pressure swing adsorption unit to produce a hydrogen product and an off-gas comprising carbon monoxide, carbon dioxide, unreacted methane; splitting a portion of the hydrogen product; and providing the portion of the hydrogen product to an electricity generator for generating electricity for use within the process.

This application provides a high-purity hydrogen preparation device with adsorption purification and palladium membrane purification. All components are integrated into a rigid cabinet, eliminating external cascaded high-pressure pipelines, reducing leakage points, improving system rigidity and safety, and facilitating explosion-proof and pressure vessel certification. The device employs a three-section structure: gas-liquid separator – adsorption purification unit – high-temperature palladium membrane. The adsorption unit uses a molecular sieve + palladium catalyst composite filling, combining deep dehydration and catalytic deoxygenation functions, providing a dry, oxygen-free pre-protection environment for the palladium membrane, significantly extending its service life. The pressure-stabilizing isolation section forms a "pressure-stabilizing isolation zone," effectively absorbing pressure fluctuations during switching and preventing damage to the palladium membrane due to pressure alternation. An integrated protection circuit quickly evacuates the palladium membrane cavity in case of abnormal shutdown or gas supply interruption, physically blocking air contact and completely eliminating the risk of high-temperature oxidation.

This disclosure provides a chemical system and method for producing synthesis gas using pyrolysis gas, which contains pyrolysis carbon products and pyrolysis-derived hydrogen, obtained from a pyrolysis reactor that pyrolyzes hydrocarbon feedstocks. A high-temperature carbon separation mechanism separates the pyrolysis carbon products from the pyrolysis gas while maintaining the pyrolysis gas at a temperature above 800°C. A gas stream mainly containing carbon dioxide gas is supplied from a carbon dioxide source. The high-temperature pyrolysis gas, containing pyrolysis-derived hydrogen and carbon dioxide gas, is supplied to a reverse water-gas shift reactor, where the pyrolysis gas reacts with carbon dioxide to produce synthesis gas. The synthesis gas produced in the reverse water-gas shift reactor can be used in a variety of downstream systems and applications, including the reduction of metal oxides such as iron ore to obtain metal oxide reduction products. Recycling and heat exchange are used to further improve the efficiency of the system.

A method for producing hydrogen from ammonia is described. The method includes the use of a two-stage hydrogen PSA configuration. An effluent stream from an ammonia cracking reaction zone is sent to a first hydrogen PSA unit where it is separated into a high purity high pressure hydrogen stream and a low pressure tail gas stream. The high pressure hydrogen stream may be recovered. The low pressure tail gas stream is compressed and sent to a second hydrogen PSA unit where it is separated into a second high pressure stream and a second low pressure tail gas stream. The second high pressure hydrogen stream may be recycled to the first hydrogen PSA unit for further separation.

A hydrogen production process is described that uses a CO2 fractionation column to recover liquid or supercritical carbon dioxide. The process uses the liquid or supercritical carbon dioxide enrichment product from the carbon dioxide recovery system to cool the compressed tail gas upstream of the dewatering unit. The warm CO2 exiting the cooler is returned to the fractionation column as stripping steam.

The application discloses a system for purifying synthetic gas and regenerating rapeseed oil methyl ester, which regenerates the rapeseed oil methyl ester by removing impurities and tar by means of the steam method of a stripping unit, and adds the regenerated rapeseed oil methyl ester into a washing unit, so that the rapeseed oil methyl ester in the washing unit can better absorb the tar under the condition that a small amount of fresh rapeseed oil methyl ester is added into the washing unit, and the phenomenon of supersaturation is reduced as much as possible; the application also uses the regenerated rapeseed oil methyl ester and the mixed emulsion after cooling to make the moisture in the synthetic gas into condensed liquid through condensation, and capture the water-soluble pollutants of the synthetic gas through the condensed liquid; in conclusion, the application can remove the tar and the water-soluble pollutants at the same time under mild conditions, and can efficiently utilize the rapeseed oil methyl ester.

The utility model discloses a kind of methanol hydrogen production systems, including methanol hydrogen production unit, the hydrogen production unit includes heater and reforming reactor, the hydrogen production unit also includes multiple flow heat exchanger, the multiple flow heat exchanger includes first inlet, second inlet, third inlet, fourth inlet and first outlet, second outlet, third outlet, fourth outlet;The first inlet is imported methanol water mixed solution;The first outlet is communicated with the material inlet of the reforming reactor;The second inlet is communicated with fourth outlet, the second outlet is communicated with the hot medium inlet of the reforming reactor, the third inlet is communicated with the reforming mixed gas outlet of the reforming reactor;The fourth inlet is communicated with the hot medium outlet of the reforming reactor.In methanol hydrogen production unit, multiple flow heat exchanger is used to carry out heat energy exchange, not only reduce the floor area of methanol hydrogen production unit, also improve heat exchange efficiency.

The application relates to the technical field of hydrogen purification, in particular to a deoxygenation isobaric drying system and process, which comprises a deoxygenation tower, a support plate is arranged in the deoxygenation tower, the support plate is located at the middle position of the deoxygenation tower, a separation assembly is arranged on the two sides of the support plate, the separation assembly and the support plate are used for separating multiple reaction cavities in the deoxygenation tower, air channels are arranged on the support plate, the air channels are used for connecting adjacent reaction cavities on the two sides of the support plate, and deoxygenation catalysts are filled in the air channels. The application has the effect of improving the purity of the purified hydrogen.

A method of separating and reusing unconverted ammonia from cracked ammonia gas provided by an ammonia cracking unit is provided. The method includes introducing a cracked ammonia gas stream into a water wash column, thereby producing a clean gas stream and a water-containing effluent stream and introducing the water-containing effluent stream into a stripping column, thereby producing a cleaned wash water stream and a recovered ammonia stream. Wherein the cracked ammonia gas stream has an ammonia concentration of between 0.003 mol % and 10 mol %. Wherein the clean gas stream has an ammonia concentration of between 1 ppm and 2500 ppm. And wherein at least a portion of the recovered ammonia stream is used as fuel within the ammonia cracking unit.

A process for producing low or no carbon intensity hydrogen. In one embodiment, the process includes the step of pretreating a hydrocarbon gas stream. The pretreated hydrocarbon gas stream is fed into a reformer. The pretreated hydrocarbon gas steam is heated in the reformer to produce a synthesis gas stream and a flue gas stream. The flue gas stream is fed to a waste heat recovery section. Waste heat is recovered to increase the thermal efficiency of the process. The synthesis gas stream is fed to a shift gas reactor. Carbon monoxide from the synthesis gas stream in the shift gas reactor is converted to produce hydrogen and carbon dioxide. The carbon dioxide is separated from the synthesis gas stream and the hydrogen is separated. In another embodiment, the carbon dioxide is captured following the hydrogen separation. In another embodiment, the carbon dioxide is captured from the flue gas.

The application relates to the technical field of chemical purification, in particular to an underground hydrogen separation and purification process. The process comprises the following steps: (1) the mixed gas to be separated and purified is introduced into a -5 to -1 DEG C tetrachloromethane solution to remove residual water, and then introduced into a calcium chloride dryer to remove residual water; (2) the mixed gas after the water is removed is introduced into a reaction bed paved with 50 to 60 DEG C chromium slag to remove residual hydrogen sulfide, and then introduced into a hydrogen sulfide absorption liquid to remove residual hydrogen sulfide; (3) the mixed gas after the hydrogen sulfide is removed is filtered through a composite permeation membrane to obtain hydrogen after separation and purification; the composite permeation membrane comprises a palladium layer, a vanadium layer and a polysulfone base layer, and the vanadium layer is located between the palladium layer and the polysulfone base layer. The purification process can improve the separation purity and speed of hydrogen by adopting the composite permeation membrane composed of the palladium layer, the vanadium layer and the polysulfone base layer, and can protect the palladium layer and improve the separation effect of the palladium layer on hydrogen by two-step water removal and two-step hydrogen sulfide removal.

The application discloses a hydrogen separation and purification equipment in mixed gas, which comprises a box, a partition plate is fixed in the middle of the box horizontally, a first processing space and a second processing space for placing purified liquid are formed by the partition plate in the box, a flow-through port is arranged on the front side of the partition plate, a sealing plate is fixed in the second processing space longitudinally, a gas input port is arranged on the back side of the box and can communicate with the second processing space, a plurality of one-way parts for inputting gas to the second processing space in one direction are arranged on the sealing plate, a slowing part is arranged on the front side of the second processing space, a stirring part is arranged in the second processing space, a filtering part is arranged in the first processing space, a slot is arranged on the right side of the box and can communicate with the first processing space, a sealing door is symmetrically and movably hinged in the middle of the slot, and compared with the prior art, the efficiency of hydrogen separation and purification can be improved, and the filtering part can be replaced.

The application discloses a method and device for synthesizing sustainable aviation fuel by solar-driven biomass gasification, which comprises the following steps: heating a heat storage medium by a solar heat collection system to provide heat energy for a gasification reaction and steam generation; feeding biomass raw materials and steam into a gasification furnace to generate a gasification reaction to obtain crude synthesis gas; recovering high-temperature sensible heat of the crude synthesis gas to generate steam and generate electricity, and using the electricity to electrolyze water to prepare first hydrogen; purifying and separating and purifying the crude synthesis gas after heat exchange and temperature reduction to obtain refined synthesis gas, and separating solid carbonaceous residues and methane to be fed into a combustor to be combusted, and heat generated by the combustion is delivered to the gasification furnace; mixing the refined synthesis gas with the first hydrogen and feeding the mixture into a first-stage Fischer-Tropsch synthesis reactor to generate a hydrocarbon mixture by Fischer-Tropsch synthesis reaction under the action of a catalyst; feeding the hydrocarbon mixture and the first hydrogen into a second-stage Fischer-Tropsch synthesis reactor to generate a second-stage Fischer-Tropsch synthesis reaction, and then obtaining sustainable aviation fuel by rectification separation.

In a process for separating a mixture (3) containing carbon monoxide, hydrogen and carbon dioxide, the mixture cooled in a heat exchanger (9) is contacted by a stream of liquid methanol (13) at a temperature below -50°C to produce carbon dioxide enriched methanol (17) and a carbon dioxide depleted gas (15) relative to the cooled mixture, the carbon dioxide depleted gas is cooled in the heat exchanger and is sent to a separation unit (7) to produce a carbon monoxide enriched stream (18) and a hydrogen enriched stream (19) and the streams enriched in carbon monoxide and hydrogen are heated in the heat exchanger by exchanging heat with the mixture.

A method for washing and purification with a low-temperature methanol at least includes the following steps: condensing a raw shift gas and conducting a gas-liquid separation to obtain CO2-containing liquid and a separated raw material gas; and vaporizing the CO2-containing liquid and reducing a pressure by an expansion to obtain a CO2-containing gas; and washing the separated raw material gas with a methanol to obtain a purified gas. The present application combines CO2 condensation and an expander, so that the load of cooling capacity of the system for washing with a low-temperature methanol is reduced by 60%. At the same time, the external work done by the expander reduces the energy consumption of the system. After the CO2 in the purifying gas of desulfurization in the section A of the scrubber is condensed, the amount of CO2 entering the section B is reduced.