146results about "Hydrogen separation at low temperature" patented technology

The invention belongs to the technical field of ocean engineering and water electrolysis hydrogen production. In order to solve the problems that a traditional water cooling system is large in size and low in heat dissipation efficiency, a multi-scale thermal sensing network is deployed to collect data; establishing a multi-phase-change cross-scale heat transfer model; constructing a two-stage gradient composite cooling module; constructing and optimizing a cooling decision algorithm; designing a cooperative control loop; deep reinforcement learning control is implemented; creating a functional surface; and constructing a dynamic optimization system. The characteristics of part of the steps are limited, efficient heat management can be achieved, and stable operation of the floating type offshore hydrogen production platform cooling system is guaranteed.

The invention relates to a method and a system for synthesizing N-methylaniline and co-producing N, N-dimethylaniline by a gas phase method, and belongs to the technical field of chemical engineering. The system comprises a raw material gasification unit, a reaction unit, a separation and rectification unit and a hydrogen recovery unit which are connected through pipelines. The method comprises the following steps of: firstly, mainly synthesizing N-methylaniline from raw materials aniline and part of methanol in a first-methylaniline reactor, then partially or completely feeding first-methylaniline reaction gas into a second-methylaniline reactor, adding methanol steam, and further reacting to generate N, N-dimethylaniline. And after the product gas is subjected to heat exchange energy recovery, a liquid phase and a gas phase respectively enter the separation and rectification unit and the hydrogen recovery unit. The purification of N-methylaniline and N, N-dimethylaniline and the recovery of byproduct hydrogen are realized. The yield of N, N-dimethylaniline (in terms of aniline) can be adjusted in a range of 5-30% by adjusting reaction conditions and a feeding ratio.

In a process in which ammonia is cracked to form a hydrogen gas product and an offgas comprising nitrogen gas, residual hydrogen gas and residual ammonia gas, residual ammonia is recovered from the offgas from the hydrogen recovery process by partial condensation and phase separation, and hydrogen is recovered from the resultant ammonia-lean offgas by partial condensation and phase separation. The recovered ammonia may be recycled the cracking process and the recovered hydrogen may be recycled to the hydrogen recovery process to improve hydrogen recovery from the cracked gas. Overall hydrogen recovery from the ammonia may thereby be increased to over 99%.

The power generation system comprises a fuel cell unit adapted to generate electric power using a hydrocarbon-containing gas. A water-gas shift reactor is adapted to receive flue gas from the fuel cell unit and convert carbon monoxide contained in the flue gas into carbon dioxide and hydrogen. A cryogenic carbon dioxide capture unit is adapted to receive flue gas from the water-gas shift reactor and remove carbon dioxide therefrom. A recycle line recycles carbon dioxide-depleted flue gas to the fuel cell unit.

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 application provides a hydrogen deep removal and moisture removal method. High-concentration raw gas is dynamically mixed with dry low-concentration reflux gas in a mixer to form mixed gas, so as to reduce the hydrogen content and reduce the reaction risk. After pressurized heating, oxygen with a precisely matched hydrogen concentration is injected into a reactor for reaction. The reactor is provided with an alternating fixed and rotatable cylinder, and the inner wall of the flow channel is coated with a catalyst; the corresponding cylinder speed is automatically adjusted based on real-time hydrogen concentration detection downstream, and the speed is accelerated when the concentration exceeds the standard to strengthen turbulent contact and prolong the reaction time, combined with the concentration threshold setting decreasing along the flow direction, so that the hydrogen is deeply removed to an ultralow level. The reaction generates moisture, most of which is separated by two-stage water cooling, and then is deeply adsorbed and dried to be completely removed to an ultralow content. Finally, the gas is divided into two parts, one part is output as product gas, and the other part is completely dried reflux gas which is recycled to the initial mixing step to reduce the reaction risk of high hydrogen content.

This invention belongs to the field of hydrogen production technology, specifically relating to a method and application of hydrogen production via an oxygen-permeable membrane. The method includes the following steps: (1) introducing water vapor into a second oxygen-permeable membrane reactor R2 to generate a high-temperature reactive gas 1; (2) mixing the remaining hydrogen-containing gas on the water vapor side of the second oxygen-permeable membrane reactor R2 with the high-temperature reactive gas 1 and introducing it into a first oxygen-permeable membrane reactor R1; (3) introducing water vapor into the first oxygen-permeable membrane reactor R1, where oxygen migrates through the oxygen-permeable membrane to the oxygen side and reacts with the mixed gas 1 to generate a high-temperature reactive gas 2; (4) introducing a portion of the high-temperature reactive gas 2 as a circulating gas into the second oxygen-permeable membrane reactor R2 and mixing it with fuel; (5) introducing the remaining hydrogen-rich gas on the water vapor side of the first oxygen-permeable membrane reactor R1 into a first condenser C1 to obtain high-purity hydrogen. This invention further reduces energy consumption while increasing the production rate, providing a convenient, efficient, and economical way to produce hydrogen.

A method comprising partially condensing and separating a feed stream comprising helium and hydrogen to produce a first medium-pressure vapor stream and a first medium-pressure liquid stream; reducing the pressure of the first medium-pressure liquid stream or a stream derived from the first medium-pressure liquid stream to produce a low-pressure vapor stream and a low-pressure liquid stream; cooling the first medium-pressure vapor stream by indirect heat exchange against the low-pressure liquid stream to produce a first partially condensed medium-pressure stream; and separating the first partially condensed medium-pressure stream to produce a second medium-pressure vapor stream and a second medium-pressure liquid stream.

There are provided systems and methods for using fuel rich partial oxidation to produce an end product from waste gases, such as flare gas. Lambda sensor modifications and other control parameters that provide closed-loop mixture control at extremely fuel-rich operating conditions utilizing feed-forward and feedback approaches, physics-based engine models, novel use of a lambda sensor (02-based sensor), sensors with intermittent contact with the gas stream. In an embodiment the system and method use air-breathing engines having control systems, control parameters, sensors and input / output (I / O) for the fuel rich (ER of 1.2 and greater), partial oxidation of the flare gas to form syngas. In embodiments the syngas is further converted into an end product. In an embodiment the end product is methanol.

An apparatus for steam reforming includes a reactor, a condensate separator, a condensate stripper, and a steam boiler. The reactor produces hydrogen and is connected to the condensate separator such that a gas mixture is conducted from the reactor into the condensate separator. The condensate separator and the condensate stripper are connected so that condensate separated out in the condensate separator is conducted into the condensate stripper. The condensate separator and the steam boiler are connected such that cleaned condensate can be conducted into the steam boiler. The steam boiler is connected to the reactor and to the condensate stripper in a steam-conducting manner. The boiler water feed line of the steam boiler is connectable to the condensate stripper in a liquid-conducting manner. A supply from the boiler water feed line is at a same location of the condensate stripper as a supply of the condensate from the condensate separator.

A process for steam reforming a hydrocarbon feedstock containing one or more nitrogen compounds, including passing a mixture of the hydrocarbon feedstock and steam through a catalyst bed of one or more nickel steam reforming catalysts disposed within a plurality of externally heated tubes in a tubular steam reformer, each tube having an inlet to which the mixture of hydrocarbon and steam is fed, an outlet from which a reformed gas containing hydrogen, carbon monoxide, carbon dioxide, steam, ammonia and methane is recovered. The steam reforming catalyst at least at the outlet of the tubes comprises nickel dispersed over a porous metal oxide surface present as a coating on a non-porous metal or ceramic structure The nickel content of the metal oxide coating is in the range of 5 to 50% by weight and the thickness of the coating is in the range of 5 to 150 micrometres.

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.

A hydrogen feed stream comprising one or more impurities selected from the group consisting of nitrogen, argon, methane, carbon monoxide, carbon dioxide, oxygen, and water, is purified using a cryogenic temperature swing adsorption (CTSA) process with high overall recovery of hydrogen. The waste gas from regenerating the CTSA may be used to improve the performance of upstream hydrogen processing steps.

The present invention relates to a method for purifying at least one impurity and compressing hydrogen, comprising at least one thermal compression and cooling of the hydrogen to a temperature strictly below 0°C, either simultaneously or starting with one of the two, to a temperature and pressure combination such that said at least one impurity condenses sufficiently so that the remaining quantity of the impurity in the hydrogen is less than a predetermined value. The present invention also relates to a device specially designed to implement the method according to the invention. Abstract figure: Figure 1

The invention relates to a process for producing hydrogen by reforming hydrocarbons with steam, and separating carbon dioxide. The process comprises an endothermic reforming step and an autothermal reforming step for producing a synthesis gas stream, wherein the heat produced in the autothermal reforming step is used for heating in the endothermic reforming step. The process further comprises a step of converting the obtained synthesis gas stream to enrich hydrogen, a step of separating the thus produced hydrogen by pressure swing adsorption, and a step of separating carbon dioxide from the residual gas obtained from the pressure swing adsorption. The reforming units for the endothermic reforming step and the autothermal reforming step are arranged in parallel to each other or in series.

A process for steam reforming of a hydrocarbon feedstock containing one or more nitrogen compounds is described, the process comprising: passing a mixture of the hydrocarbon feedstock and steam through a catalyst bed consisting of one or more nickel steam reforming catalysts placed in a plurality of externally heated tubes in a tubular steam reformer, wherein each tube has an inlet to feed the hydrocarbon and steam mixture and an outlet to recover a reformate gas containing hydrogen, carbon monoxide, carbon dioxide, steam, ammonia and methane, and wherein at least at the outlet of the tube, the steam reforming catalyst is a structured steam reforming catalyst comprising nickel dispersed on the surface of a porous metal oxide present as a coating on a non-porous metal or ceramic structure, wherein the nickel content in the metal oxide coating is in the range of 5 to 50 wt.-% and the thickness of the coating is in the range of 5 to 150 micrometers.

The invention discloses a hydrogen recovery device and method for PTA (pure terephthalic acid) production, the hydrogen recovery device comprises a first cooler and a first gas-liquid separation tank, the outlet end of the first cooler is connected with the first gas-liquid separation tank, the first gas-liquid separation tank is connected with a hydrogen recovery washing tower through a pipeline, the bottom of the hydrogen recovery washing tower is connected with an acid recovery device through a pipeline, and the acid recovery device is connected with the acid recovery device through a pipeline. The top of the hydrogen recovery washing tower is connected with a second cooler through a pipeline; the hydrogen recovery washing tower is connected with the oxidation device through a conveying pump so as to convey acid into the hydrogen recovery washing tower, and hydrogen-rich steam is sequentially subjected to acid pickling and desalted water spraying from bottom to top in the hydrogen recovery washing tower; the invention aims to provide the hydrogen recovery device and method for PTA (pure terephthalic acid) production, so that the content of methyl acetate and methanol in the hydrogen recovery process is reduced, the purity of hydrogen is improved, and the production cost is reduced.

The invention discloses a process for efficiently recovering hydrogen from waste gas, which belongs to the technical field of hydrogen recovery, and comprises the following steps: 1, pretreatment of raw material gas, including dust removal and dehydration treatment; 2, primary compression and pressure swing adsorption pretreatment: nitrogen / hydrogen mixed gas subjected to primary compression enters a PSA adsorption barrel A or a PSA adsorption barrel B, the PSA adsorption barrels are filled with an adsorbent for primary purification, and the hydrogen concentration is increased to 99.99% or above; and 3, secondary compression and cryogenic distillation: hydrogen subjected to secondary compression firstly enters a main heat exchanger and then enters a rectifying tower, nitrogen is liquefied preferentially in the rectifying tower, and hydrogen with the purity being greater than or equal to 99.999% is output from the tower top. By optimizing the PSA adsorbent, the hydrogen concentration after preliminary purification can be increased to 99.99% or above, the hydrogen recovery rate can reach 90% or above, the adsorption efficiency is high, the hydrogen recovery rate is high, and the purified hydrogen meets the ultra-high purity requirement by further combining with deep cooling.

The present invention relates to a process and system for separating carbon monoxide from a syngas mixture having a high methane content by a cryogenic plant in which a partial condensation cycle is typically employed, and more particularly, to mixing methane-rich liquid exiting a distillation column with a lower boiling mixture, the boiling point of the mixed flow is lower than that of the methane-rich liquid.

A plant and a process for separating hydrogen from natural gas. The plant includes a hydrogen separation module, a heat exchanger, a decompressor, downstream of the heat exchanger and in fluid connection with the heat exchanger through a first outlet duct of the heat exchanger, and a flash separator, downstream of the decompressor and in fluid communication with the decompressor through an outlet duct of the decompressor. The flash separator separates a flow of natural gas with a hydrogen content higher than a predetermined threshold, entering the hydrogen separation module through an inlet duct of the heat exchanger, into a first flow of natural gas containing the excess hydrogen and a second flow of natural gas with a hydrogen content below the predetermined threshold. The flash separator includes an upper outlet and a lower outlet, from which an outlet or recirculation duct extends.

In a method for separating CO2 by partial condensation and / or distillation - a first gas (1) containing hydrogen, water and carbon dioxide is compressed in a compressor (17), dried in an adsorption drying unit (19) and then separated by partial condensation and / or distillation to produce a CO2-enriched fluid (25) and - a second gas (3), containing carbon dioxide, hydrogen and water, originating from an absorption separation process (A), is cooled in order to condense at least a portion (7) of the water that it contains, the water is separated from the gas forming a dried gas (9) and the dried gas is mixed with the first gas upstream of the adsorption drying unit and optionally upstream of the compressor.

The invention discloses a methanol reforming hydrogen production system and method, and relates to the technical field of on-site hydrogen production process, and the methanol reforming hydrogen production system comprises a methanol storage tank, a methanol steam reforming reactor, a second condenser and a hydrogen outlet which are communicated in sequence, an external heat exchange shell layer of the methanol steam reforming reactor is respectively communicated with an air fan and a methanol storage tank through a methanol catalytic oxidation reactor, and a connecting pipeline between the methanol catalytic oxidation reactor and the methanol steam reforming reactor is also communicated with a hydrogen combustion reactor; an inlet of the hydrogen combustion reactor is communicated with a gas outlet of the second condenser, the inlet of the hydrogen combustion reactor is further communicated with an air fan, and an outlet of the external heat exchange shell layer is communicated with the first condenser. The cooling water outlet of the first condenser and the cooling water outlet of the second condenser are communicated with the connecting pipeline of the methanol storage tank and the methanol steam reforming reactor through the liquid storage tank, and the required raw materials are single and only methanol and air or oxygen are needed.

The invention discloses a wide-load high-recovery-rate hydrogen deep purification method which comprises the following steps: introducing crude hydrogen containing oxygen, water and carbon dioxide into a deoxidation reactor filled with a catalyst for catalytic deoxidation reaction, and enabling the oxygen and the hydrogen to react to generate water so as to obtain high-temperature wet hydrogen; wherein the deoxidation reactor is at least filled with a low-temperature activation catalyst and a medium-high-temperature main catalyst; cooling the high-temperature wet hydrogen, and separating liquid water generated by condensation to obtain saturated micro-wet hydrogen rich in carbon dioxide; and introducing the saturated micro-wet hydrogen into an adsorption system, and carrying out deep dehydration and decarbonization on the saturated micro-wet hydrogen to obtain a high-purity hydrogen product. According to the embodiment of the invention, a stable high purification effect can be kept in a wide load range, and application requirements are met.

A hydrogen supply system is used to supply hydrogen. The hydrogen supply system includes: a dehydrogenation reaction unit that obtains hydrogen-containing gas by causing a hydride-containing feedstock to undergo a dehydrogenation reaction; and a control unit that controls the hydrogen supply system. When the generation of hydrogen-containing gas in the dehydrogenation reaction unit is stopped, the control unit causes the hydrogen supply unit to supply hydrogen to the dehydrogenation reaction unit. The hydrogen supply unit supplies at least one of the hydrogen-containing gas between the dehydrogenation reaction unit and a gas-liquid separation unit for separating dehydrogenation products from the hydrogen-containing gas, and the hydrogen-containing gas separated by the gas-liquid separation unit for separating dehydrogenation products from the hydrogen-containing gas.

The invention discloses a refrigeration cycle-based PEM water electrolysis hydrogen production and waste heat utilization system, which comprises a water electrolysis hydrogen production system, a refrigeration cycle system, a gas purification system and a waste heat utilization system, and is characterized in that the water electrolysis hydrogen production system is used for electrolyzing water to produce hydrogen and oxygen, carrying out steam-water separation, cooling gas and removing water; refrigerant of the refrigeration cycle system absorbs heat in the evaporator to cool water or gas, and releases heat in the condenser to heat water or gas. The gas purification system is used for drying the hydrogen to finally obtain high-purity hydrogen; the waste heat utilization system is used for heating alkali liquor at an inlet of the electrolytic bath in the circulation loop by using waste heat generated by electrolyzing water; the waste heat utilization in the PEM water electrolysis hydrogen production process is realized, the adaptability of the PEM electrolytic bath to the new energy power generation power fluctuation is further improved, the loss of water, heat and electric energy in the PEM water electrolysis process is reduced, the energy utilization rate of a PEM hydrogen production system is improved, the PEM water electrolysis hydrogen production cost is reduced, and the economic benefit is improved.

A system for hydrogen production including a first separation system (10), a first purification unit (17), a second purification unit (19), an oxygen scavenger (25), a catalytic reactor (29), a second separation system (33), and a liquefier (39). A method for hydrogen production including separating oxygen-containing components from a feed (5) also containing hydrogen sulfide and methane. The method further includes separating the hydrogen sulfide from the methane and feeding the hydrogen sulfide (13) to a first purification unit (17). The method includes feeding the methane (15) to a second purification unit (19). The method further includes feeding the purified hydrogen sulfide and methane to an oxygen scavenger unit (25) to remove residual oxygen before reacting the two streams in a catalytic reactor (29). The method includes separating the gaseous hydrogen and liquid carbon disulfide (31) exiting the catalytic reactor (29) and then purifying and liquefying the gaseous hydrogen stream (34) to produce a purified liquid hydrogen stream (41).

The present invention discloses a process for efficiently recovering hydrogen from waste gas, which belongs to the field of hydrogen recovery technology and includes the following steps: 1. Raw gas pretreatment: including dust removal and dehydration treatment; 2. Primary compression and pressure swing adsorption pretreatment: The primary compressed nitrogen / hydrogen mixed gas enters PSA adsorption cylinder A or PSA adsorption cylinder B, and the PSA adsorption cylinder is filled with adsorbent for preliminary purification, and the hydrogen concentration is increased to more than 99.99%; 3. Secondary compression and cryogenic distillation: The secondary compressed hydrogen first enters the main heat exchanger and then enters the distillation tower, where the nitrogen is preferentially liquefied, and hydrogen with a purity of ≥99.999% is output from the top of the tower. The present invention optimizes the PSA adsorbent so that the hydrogen concentration can be increased to more than 99.99% after preliminary purification, and the hydrogen recovery rate can reach more than 90%, with high adsorption efficiency and high hydrogen recovery rate. Further combined with cryogenic distillation, the purified hydrogen meets the ultra-high purity requirements.

The application provides an energy consumption optimization system and method based on a hydrogen purification process, and relates to the technical field of hydrogen production by water electrolysis.The energy consumption optimization system based on the hydrogen purification process comprises a crude hydrogen input pipeline, a first waste heat recovery pipeline, a second waste heat recovery pipeline, a deoxidization cooling unit, a first hydrogen cooling and drying unit, a second hydrogen cooling and drying unit, a third hydrogen cooling and drying unit, a hydrogen conveying pipeline before cooling, and a pure hydrogen output pipeline.The crude hydrogen input pipeline is in communication with the deoxidization cooling unit.The first waste heat recovery pipeline and the second waste heat recovery pipeline are both in communication between the deoxidization cooling unit, the first hydrogen cooling and drying unit, the second hydrogen cooling and drying unit, and the third hydrogen cooling and drying unit.The application has the beneficial effect of reducing the energy loss of the hydrogen purification process and improving the energy utilization efficiency.

A process (100, 200) for producing ammonia, in particular blue ammonia, is proposed, in which hydrogen (2) is provided, mixed with nitrogen, and subjected to ammonia synthesis (30) to obtain an ammonia-containing product gas (4). The ammonia-containing product gas (4) is subsequently subjected to cooling (40) to obtain liquefied ammonia (5). To provide the hydrogen (2), a gas mixture (1) containing hydrogen and carbon dioxide is provided and, to obtain hydrogen (2) and carbon dioxide (6, 8), is subjected to processing steps comprising hydrogen processing (60) and carbon dioxide separation (20). The carbon dioxide (6, 8) or a portion thereof is used as the cooling medium for the cooling (40). A corresponding system (100, 200) is also proposed.

A method of producing hydrogen from a hydrocarbon feedstock is provided. Wherein, at least a portion of a fuel stream comprises a superheated ammonia stream. And, at least: a first portion of a hydrogen-rich stream is combined with a shifted syngas stream prior to introduction into a pressure swing adsorber, a second portion of the hydrogen-rich stream is combined with the fuel stream prior to introduction into a steam methane reformer, and / or a third portion of the hydrogen-rich stream is combined with a hydrocarbon containing feedstock stream and a steam stream prior to introduction into a feed pre-heater. Heat integration between the ammonia vaporization and superheating steps is employed to cool process streams to minimize and even eliminate a dedicated cryogenic refrigeration system.