474 results about "Water gas" patented technology

The invention discloses preparation of a high-performance carbon matrix embedded iron-based catalyst based on a metal organic framework precursor and application of the high-performance carbon matrix embedded iron-based catalyst in reverse water-gas shift reaction. In the preparation process, commercially available 1, 3, 5-trimesic acid iron (the chemical formula is C9H3FeO6, abbreviated as Fe-BTC) is selected as a raw material, pyrolysis treatment is carried out in an argon atmosphere, then air passivation is carried out, and finally the high-performance carbon matrix embedded iron-based catalyst based on the metal organic framework precursor is successfully prepared. The MOF-600 has excellent performance in many catalysts, the carbon dioxide production rate reaches 24.0 mmol CO.gcat <-1 >. S <-1 > at the temperature of 400 DEG C in a reverse water gas shift reaction, the performance is remarkably superior to that of an existing non-noble metal catalyst, and extremely high catalytic efficiency and application potential are shown.

The invention relates to a method for preparing carbon monoxide by reverse water gas shift, which comprises the following steps: under the catalytic action of a supported catalyst, carrying out reverse water gas shift reaction, carrying out pressure swing adsorption treatment on mixed gas generated in the reaction process, and desorbing to obtain carbon monoxide. By coupling the reverse water gas shift reaction and the pressure swing adsorption process and exerting the synergistic effect of the reverse water gas shift reaction and the pressure swing adsorption process, efficient and rapid separation of carbon monoxide is realized, the reverse water gas shift reaction is promoted to be carried out in the forward direction, the reaction requirement of reverse water gas shift is reduced, the reverse water gas shift reaction is carried out under relatively mild conditions, and the reaction efficiency is improved. The long-period efficient conversion of carbon dioxide is realized, and the conversion rate of carbon dioxide and the selectivity of carbon monoxide are further improved.

The invention provides equipment and a method for testing the emission amount of harmful gas in a tunnel, and relates to the technical field of tunnel construction. Comprising a sleeve, a gas parameter testing unit installed on the sleeve, a water tank communicated with the interior of the sleeve and a gassing module installed on the water tank, and the gassing module is connected with the gas parameter testing unit; one end of the sleeve can be dynamically sealed with the drill rod, and the other end of the sleeve is of an opening structure; the gassing module is used for separating out gas in water and conveying the gas to the gas parameter testing unit; and the gas parameter testing unit is used for detecting the concentration and flow velocity of harmful gas in the sleeve and the concentration of harmful gas separated out from water. A gas parameter testing unit is arranged to monitor the data change of gas gushing out of the drill hole in real time; the gassing module can separate out gas in water in real time and convey the gas to the gas parameter testing unit to measure the concentration of dissolvable gas, so that the calculation of the emission amount is more comprehensive and accurate.

The application provides a reverse water gas shift catalyst, a preparation method and application thereof, and the reverse water gas shift catalyst prepared by the preparation method has excellent catalytic activity and high CO selectivity in a reverse water gas shift reaction. The preparation method comprises the following steps: contacting a precipitating salt solution with a precipitant aqueous solution and performing co-precipitation, and simultaneously controlling the reaction temperature to be 40-80 DEG C and the pH to be 6-8; optionally performing aging after the co-precipitation is completed; filtering the obtained precipitate to obtain a filter cake, washing the filter cake, then drying the filter cake, and calcining the filter cake at 300-500 DEG C to obtain the reverse water gas shift catalyst; wherein the precipitating salt solution is a mixed aqueous solution of a soluble salt of divalent metal ions and a soluble salt of trivalent metal ions, the divalent metal ions are selected from divalent ions of Mg and / or Zn, and the trivalent metal ions are selected from trivalent ions of Al, In and / or Ga.

The invention discloses a numerical simulation method and system for a coal underground gasification process, and belongs to the technical field of energy development. The method comprises the following steps: constructing a gasification cavity, cavity wall and raw coal three-area conceptual model; establishing a kinetic model coupled with five types of chemical reactions (complete oxidation, water vapor conversion, Boudouard reaction, hydrogenization and water-gas shift), and associating porosity change and cavity wall temperature gradient distribution; dynamic evolution prediction of the semi-teardrop-shaped gasification cavity is realized through a numerical flow of cyclically updating the porosity, marking the cavity, calculating the reaction and outputting the synthesis gas; a cavity form and synthesis gas component curve is generated based on a multi-module system (data preparation, numerical calculation, result analysis and visualization). The problem that the gasification cavity evolution simulation precision is insufficient in the prior art is solved, and the method is suitable for UCG engineering design and safety evaluation.

The invention relates to the technical field of superfine molybdenum powder preparation, in particular to a preparation device and method for low-oxygen superfine molybdenum powder. The specific preparation device comprises a sublimation bin, a reaction area and a gas-solid separation bin which are sequentially connected, the reaction zone comprises a preheating zone, a reduction zone and a conversion zone; a part of the hydrogen pipeline and a part of the carbon monoxide pipeline are arranged in the preheating area; one end of the hydrogen pipeline extends to the reduction area and is used for providing preheated hydrogen and carrying out gas-phase reduction reaction on the preheated hydrogen and the gas-phase MoO3 subjected to heat preservation; one end of the carbon monoxide pipeline extends to the conversion area and is used for providing preheated carbon monoxide and reacting with water vapor to complete primary water vapor conversion; meanwhile, partial carbon monoxide is subjected to a disproportionation reaction to generate micro carbon powder, and the micro carbon powder and water vapor are subjected to a water gas reaction to complete secondary water vapor conversion. The problem that the oxygen content of existing superfine molybdenum powder prepared through gas-phase molybdenum trioxide reduction is too high is solved.

A process and a plant for the production of hydrogen or for the synthesis of ammonia, said process comprising the following steps: (a) performing a reforming process (101) of a hydrocarbon feedstock (1) to generate a raw syngas (2), said reforming process comprising at least an autothermal reforming step (104) in presence of oxygen-enriched air or pure oxygen (3) produced by an air separation unit (ASU; 103); (b) subjecting said raw syngas (2) to a post-treatment (102) providing hydrogen (H2; 4), a CO2-enriched stream (5), and a residual gas (6); said post-treatment comprising at least a water gas shift conversion step (105) of said raw syngas into a shifted syngas (7), a pressure swing absorption step (106), and a cryogenic separation step (107); wherein said pressure swing absorption step produces said hydrogen and a first tail gas (8) comprising carbon monoxide (CO), carbon dioxide (CO2), residual hydrogen (H2) and unreacted hydrocarbon feedstock from the shifted syngas (7), and said cryogenic separation step separates the CO2-enriched stream and a second tail gas (9) from said first tail gas; said post-treatment (102) comprising a further separation step (120) of a CO2-containing stream (11) and of the residual gas (6) from said second tail gas; (c) recycling said residual gas (6) as feed to said reforming process and / or as fuel to one or more fired heater(s) (10) of said process; (d) optionally feeding a portion (4.8) of said hydrogen (4) obtained in step (b) as fuel to one or more fired heater(s) of said process; (e) optionally an ammonia synthesis step (110) wherein said hydrogen (4) and a nitrogen (N2)-containing stream (12) produced by said ASU (103) are reacted in a given stoichiometric ratio and in ammonia (NH3) synthesis conditions to obtain an ammonia-containing product (13).

A process for the production of hydrogen is described comprising the steps of: (i) reforming a gaseous mixture comprising a hydrocarbon and steam having a steam to carbon ratio in the range of 0.4:1 to 1.8:1, to in a reforming unit comprising an autothermal reformer to produce a reformed gas mixture, (ii) subjecting the reformed gas mixture to an isothermal water-gas shift reaction in an isothermal water-gas shift reactor using water as a heat exchange medium, thereby increasing the hydrogen content of the reformed gas mixture and producing a hydrogen-enriched reformed gas while raising steam, cooling at least some of the hydrogen-enriched reformed gas and separating condensed water therefrom to provide a de-watered hydrogen-enriched reformed gas, (iv) subjecting at least some of the de-watered hydrogen-enriched reformed gas to carbon dioxide separation by performing a reactive amine wash on the hydrogen-enriched reformed gas in a carbon dioxide separation unit to recover carbon dioxide gas and crude hydrogen gas, and (v) subjecting at least some of the crude hydrogen gas to purification in a hydrogen purification unit to produce a purified hydrogen gas and a tail gas, wherein a portion of the tail gas is recycled to the process.

The invention discloses a coal-to-methanol conversion treatment system and a coal-to-methanol conversion treatment simulation method. The coal-to-methanol conversion treatment system comprises a gas separator, a conversion furnace, a first water separation device, a stripping tower and a second water separation device. Water gas of a gasification section enters a gas separator, and a gas phase discharged from a gas outlet of the gas separator is divided into a first gas phase and a second gas phase through a flow divider; the inlet of the conversion furnace is connected with the flow divider so that the first gas phase flows into the conversion furnace; the first water separation device is used for performing multi-stage separation on the mixed gas; steam entering the stripping tower from the steam inlet is in contact with condensate entering the stripping tower from the first water separation device; and the second water separation device is connected with the gas outlet of the stripping tower to separate the vent gas and the wastewater. Water gas can be effectively treated, so that the energy consumption of the system is reduced, the water-saving and environment-friendly effects are achieved, and the purposes of improving quality and efficiency can be achieved.

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 application relates to the technical field of catalyst preparation, in particular to an in-situ formed FeO x / Fe3C catalyst as well as a preparation method and application thereof. The FeO x / Fe3C catalyst provided by the application is a heterogeneous composite structure composed of surface iron oxide (FeO x ) and bulk iron carbide (Fe3C), breaks through the limitation of only focusing on a single phase, systematically reveals the dynamic structure evolution law from the surface to the bulk, and clarifies the internal correlation with the reaction mechanism. Based on the synergistic circulation mechanism from the surface to the bulk, the FeO x / Fe3C catalyst exhibits excellent catalytic performance and stability in the reverse water gas shift reaction, which is superior to most of the catalyst systems reported at present.

A system and method for producing methanol and synthetic fuels from waste acid gas streams using a plasma reactor is described in this disclosure. An acid gas stream comprising primarily of H2S and CO2 is fed into a plasma reactor. H2S is converted into H2 and sulfur. Simultaneously, CO is formed by the reverse water gas shift reaction. H2 and CO form a syngas stream. The unreacted H2S is captured in a tail gas treatment unit and recycled back to the plasma reactor. A partial CO2 capture unit is placed downstream of the tail gas treatment unit which is primarily used to adjust the ratio of H2 and CO in the syngas stream to 2-3 for methanol production and 2 for fuel production.

The invention discloses a cascade energy supply and green hydrogen coupling biomass all-carbon directional conversion synthesis gas system and method, and belongs to the technical field of biomass energy conversion. The system comprises a first-stage gasification furnace, a second-stage gasification furnace, a gas-solid separator, an alkane reforming device, a reverse water-gas shift device and a water electrolysis device. The method comprises the following steps: pyrolyzing a biomass raw material and a catalyst in a primary gasifier (500-700 DEG C) to generate semicoke and tar-containing fuel gas; carrying out catalytic co-gasification on the semicoke and tar-containing fuel gas in a secondary gasifier (800-900 DEG C), and realizing tar cracking and CH4 reforming by using a catalyst to obtain crude synthesis gas; after being subjected to high-temperature dust removal, the crude synthesis gas sequentially passes through a self-heating alkane reforming device (CH4lt; 1%) and a reverse water-gas shift device, and finally synthesis gas with the H2 / CO ratio of 2: 1 is produced, so that the chemical application requirements of methanol, Fischer-Tropsch synthesis and the like are completely met, the high energy consumption bottleneck of a traditional process is broken, and full-life-cycle negative carbon emission is achieved.

An ironmaking method comprising the production of hot metal (2) and of a blast furnace top gas (10), the method comprising the steps of capturing at least a part of the top gas (10), separating CO2 from the captured top gas (10) so as to produce a CO2-rich stream (12) and a CO2-lean stream (11), mixing the CO2-rich stream (12) with a H2 makeup stream (30) and subjecting the obtained CO2 / H2 gas mixture to a reverse water gas shift reaction in a reactor (3) to produce a reducing stream (13) comprising CO and H2, separating H2 from the reducing stream to produce a CO- rich stream (14) and an H2-rich stream (15), mixing the H2-rich stream (15) with the CO2-rich stream (12) or with the CO2 / H2 gas mixture in the reactor (3) and subjecting the obtained gas mixture to the reverse water gas shift reaction and feeding at least a portion of the CO-rich stream 14 (13) to at least one chemical or biochemical plant (4) to produce one or more chemical products (16).

The invention discloses a CO2-mediated indirect hydrogen metallurgy blast furnace smelting process, and belongs to the technical field of low-carbon metallurgy and hydrogen metallurgy. According to the process, on the premise that the main body structure of a blast furnace is not changed, CO2 in furnace top gas is captured and mixed with external H2, a reverse water-gas shift reaction is carried out in a high-temperature and high-pressure environment outside the furnace, and high-temperature CO reducing gas is generated; and then directly injecting the high-temperature reducing gas into a soft melting zone area of a blast furnace body by utilizing a special device. According to the method, a central coke adding and distributing mode and a quick response coal injection strategy are matched, and part of pulverized coal and coke can be effectively replaced; by constructing a heat transfer mechanism of heat absorption conversion outside the furnace and heat release reduction inside the furnace, the heat absorption reaction is transferred to the outside of the furnace to be completed, meanwhile, high-temperature gas injected into the furnace body is used for directly supplementing heat in the furnace and strengthening indirect reduction reaction, and cyclic utilization of CO2 is achieved.

A process includes feeding atmospheric air to an air separation unit to produce a flow of nitrogen and a flow of oxygen; combining the oxygen with a hydrocarbon flow and water in an auto-thermal reformer to produce a retentate stream to a membrane water gas shift reactor (M-WGSR); generating, from the retentate stream to the M-WGSR, a permeate stream from the M-WGSR that includes a first flow of carbon dioxide and a first combined flow of hydrogen and nitrogen; feeding a retentate stream to a membrane steam methane reformer (M-SMR) to produce a permeate stream from the M-SMR that includes a second flow of carbon dioxide and a second combined flow of hydrogen and nitrogen; feeding the first and second combined flows to an ammonia synthesis unit to produce ammonia; and feeding the first and second flows of carbon dioxide and the ammonia to a urea synthesis unit to produce a flow of urea by fully utilizing the carbon dioxide.

The utility model relates to the technical field of sewage suction trucks, and discloses a water-gas separator of a sewage suction truck, which comprises a sewage storage tank, an exhaust pipe is fixedly sleeved on the upper part of an inner cavity of the sewage storage tank, a fan is fixedly sleeved on the exhaust pipe, a separation cylinder is fixedly sleeved on the exhaust pipe and is positioned on the right side of the fan, and the separation cylinder is fixedly sleeved on the inner cavity of the sewage storage tank. The bottom of the separation barrel is fixedly connected to the upper portion of an inner cavity of the sewage storage tank in a sleeving mode, a fixing pipe is fixedly installed at the top of the inner cavity of the separation barrel, a first through opening is formed in the right portion of the fixing pipe, a channel is formed in the separation barrel, the left end of the channel is fixedly connected with the first through opening, and the right end of the channel is fixedly connected with an exhaust pipe. A cone is fixedly connected to the outer side of the fixed pipe in a sleeving mode, threads are formed in the cone, gas is introduced into the separation barrel, gas flow spirally descends through the threads on the cone, under the action of centrifugal force and gravity, water in the gas is fully separated, ammonia gas in the gas is kept dry, and the recycling efficiency of the ammonia gas by the device is improved.

The invention provides a manganese-based tandem catalyst as well as a preparation method and application thereof. The manganese-based tandem catalyst comprises a reverse water gas shift catalytic unit (CO2 + H2-CO) and a Fischer-Tropsch synthesis catalytic unit (CO + H2-CxHyOz), which are called MnO-FTS system for short, the active center of the reverse water gas shift catalytic unit is MnO; the Fischer-Tropsch synthesis catalytic unit comprises any one of a Cu / ZnCr-based catalyst, a FeNaAl-based catalyst, a Ni / SiO2 catalyst and a Co / SiOO catalyst. By constructing a novel efficient and synergistic MnO-FTS catalyzing system, directional conversion from COhydrogenation to liquid fuel is achieved, meanwhile, side reactions prone to occurring in direct COhydrogenation are avoided, and the overall reaction efficiency and product selectivity are improved.

The invention discloses a Fischer-Tropsch catalyst as well as a preparation method and application thereof. The Fischer-Tropsch catalyst comprises a carrier and a metal active component loaded on the carrier; the carrier is a hydrophobic carrier Al2O3-ZrO2 / MgO, a composite oxide Al2O3-ZrO2 / MgO is adopted as the carrier, the carrier is treated in a physical etching mode in the preparation process of the carrier, silicon carbide is embedded into the interior and the exterior of a colloid at the same time, and the surface roughness degree of the carrier can be increased; and the immersion of the hydrophobic solution is carried out while physical etching is carried out, so that pore channels in the hydrophobic carrier can be uniformly hydrophobic to a greater extent, the hydrophobicity is enhanced, and water generated by reaction is timely desorbed and is inhibited from being re-adsorbed, thereby reducing the occurrence of water-gas shift reaction, reducing the CO2 selectivity and improving the low-carbon olefin selectivity.

The utility model discloses movable PEM hydrogen production equipment which comprises a water supply machine tank, an electrolysis reactor is installed in the water supply machine tank, one end of the electrolysis reactor is connected with a three-way pipe fitting in a sealed mode through a water inlet pipeline, and the other end of the electrolysis reactor is connected with a water-gas separator in a sealed mode through a conveying pipeline. One end of the water-gas separator is hermetically connected with a hydrogen production tank through a gas conveying pipeline, and a proton exchange membrane is mounted in the hydrogen production tank. Water in the water supply machine tank is subjected to electrolytic reaction, so that water molecules are subjected to oxidation reaction at the anode to generate oxygen and protons, the protons are conducted to the cathode through the proton exchange membrane, electrons are obtained at the cathode to generate hydrogen, the hydrogen production device has the advantages of convenience and rapidness in hydrogen production, and the whole device is high in maneuverability and low in cost. The PEM hydrogen production equipment can be conveniently and flexibly transferred, the problem that the conventional PEM hydrogen production equipment is in a field type and cannot be moved is effectively avoided, and the PEM hydrogen production equipment has the advantages of high flexibility and small occupied field area.

This invention discloses a method for preparing a supported molybdenum nitride catalyst suitable for high-temperature countercurrent water gas shift reactions. The invention innovatively employs a bottom-up synthesis strategy, first highly dispersing the molybdenum salt precursor on the support surface, and then directly performing amination treatment in an ammonia atmosphere without oxidation. This achieves the controllable synthesis of small-sized molybdenum nitride, yielding highly dispersed molybdenum nitride material. The highly dispersed molybdenum nitride catalyst prepared by this method exhibits high activity, high CO selectivity, and good stability in countercurrent water gas shift reactions, remaining active even after repeated cycling for extended periods, and shows broad application prospects in the field of high-temperature countercurrent water gas.

A process is described for synthesising hydrocarbons comprising the steps of: (a) feeding a gas mixture comprising hydrogen and carbon dioxide to a reverse water-gas shift unit to form a crude synthesis gas comprising hydrogen, carbon monoxide carbon dioxide and steam, (b) cooling the crude synthesis gas to condense water and removing water, and optionally carbon dioxide, from the crude synthesis gas to produce a feed stream comprising hydrogen and carbon monoxide, (c) passing the feed stream though a hydrocarbon synthesis unit comprising a reactor containing a Fischer-Tropsch catalyst to form a product stream comprising a mixture of liquid hydrocarbons, a co-produced water stream, and a tail gas stream containing hydrogen, carbon monoxide and gaseous hydrocarbons, and (d) upgrading the product stream in an upgrading unit to produce an upgraded product stream, wherein a naphtha stream is separated from the product stream or the upgraded product stream, at least a portion of the tail gas stream is fed with steam to a first derichment vessel containing a derichment catalyst to form a first gas mixture containing methane, at least a portion of the naphtha stream is fed with hydrogen and steam to a second derichment vessel containing a derichment catalyst to form a second gas mixture containing methane, and the first and second gas mixtures containing methane are fed to the reverse water gas shift unit. A system for performing the process is also provided.

The present application relates to the technical field of reverse water gas shift reaction, and discloses a preparation method of a catalyst for reverse water gas shift reaction, comprising the following steps: weighing magnesium nitrate and zinc acetate, so that the molar ratio of Mg atoms to Zn atoms is 1:1 to 1:10 or 3:1 to 10:1; dissolving the weighed magnesium nitrate and zinc acetate in water, adding urea, stirring and uniformly mixing at room temperature, and then increasing the temperature and stirring to promote the co-precipitation of metal ions; and obtaining the MgO-ZnO composite oxide catalyst by centrifugation, washing, drying and calcination of the obtained precipitate. The MgO-ZnO composite oxide catalyst is prepared by adopting the urea uniform precipitation method, using magnesium nitrate and zinc acetate as raw materials, and precisely controlling the molar ratio of Mg to Zn.

Gasification processes are disclosed, which can implement one or more strategies for heating and humidifying the gasifier effluent, as needed for effective hydrogen enrichment through the water-gas shift (WGS) reaction that converts H2O. Particular aspects, in carrying out these strategies, relate to the use of an evaporator upstream of a WGS reactor and operating at a comparable pressure (e.g., at least about 10 bar, at least about 20 bar, or at least about 30 bar, such as in a range from about 30 bar to about 100 bar). Such high-pressure evaporator may provide sufficient water vapor content, for effective generation of H2 via the WGS reaction, as needed for downstream uses. Advantageously, heat and / or material (e.g., condensate) sources may be available within the process itself, and integrated to meet at least some of the operational demands of the evaporator.

The utility model discloses a horizontal process tank air draft structure which comprises a working cavity defined by a bottom plate, side plates, a cover plate and a partition plate, the cover plate is obliquely arranged, and an acute included angle alpha is formed between the cover plate and the horizontal line; air inlet holes are formed in the side plates in an array manner; an air draft cavity defined by air draft plates is formed in the connecting position of the partition plate and the cover plate, and air draft holes are formed in the air draft plates. The cover plate is arranged at the acute included angle alpha obtained through calculation and simulation, so that accumulated liquid generated at the cover plate in the reaction process of a product can flow to the side plates on the front side and the rear side along the cover plate, and the accumulated liquid is prevented from dripping to pollute the product; the air inlet holes and the air draft holes are evenly distributed so that air in the groove can be evenly replaced, the height difference exists between the front side plate and the rear side plate of the groove body and the air draft cavity so that liquid medicine gas generated by products can be rapidly pumped away by the air draft cavity in the lateral direction in the cover plate direction for air flow replacement, and the fluidity of the air in the groove is integrally optimized. Liquid medicine gas is prevented from being accumulated in the groove to affect the surface appearance of a product, and the product yield and the qualified rate are greatly improved.

The utility model discloses a blast furnace top coal gas sampling and intelligent temperature control device, characterized by cross temperature measuring device cantilever insertion type detector as the basis, through the addition of coal gas sampling channel, the addition of blast furnace top water spraying supply channel, the addition of multi-point blast furnace top water spraying (spraying) nozzle and coal gas sampling port, the cross temperature measuring, blast furnace top water spraying, coal gas sampling and other multiple devices with different functions on the blast furnace top coal gas sealing cover are integrated into a set of device, and intelligent temperature control system and blast furnace condition intelligent auxiliary analysis system realize intelligent and automatic operation. Its advantages are that it can reduce equipment investment and later operation and maintenance cost, reduce too many equipment openings on the coal gas sealing cover, reduce construction engineering quantity, obtain blast furnace internal coal gas distribution curve and improve blast furnace operation. It is suitable for popularization in new construction and transformation projects of various steel enterprises.

The utility model discloses an integrated heat exchanger suitable for frozen drying machine, including the casing, the casing is equipped with the outlet of drying gas, the inlet of water gas, the coolant outlet and the coolant inlet from top to bottom, the upper portion is equipped with the heat exchanger in the casing, still be equipped with the evaporimeter in the casing, still be equipped with the gas liquid separation chamber of gas in the bottom of casing, the evaporimeter is located heat exchanger below and communicates with the heat medium outlet of heat exchanger, the backflow channel of gas is established between evaporimeter and heat exchanger and the inside of casing, and the gas outlet of evaporimeter and the cold medium inlet of heat exchanger communicate with backflow channel. The utility model divides and sets up the upper and lower end in the casing with heat exchange and evaporation function, can simplify the structure setting in the casing, and the production cost is simplified, after setting evaporimeter below heat exchanger, can realize the step -by -step cooling of airflow from top to bottom, is favorable to the gathering of condensate in the bottom of casing and gas -water separation in the cooling process, thereby guaranteeing the drying effect of gas.

The utility model relates to humidifying jar technical field discloses a kind of anti-water multi-stage protection device of humidifying jar, including anti-water gas storage tank body, the upper portion of anti-water gas storage tank body is fixedly provided with air inlet component, the inboard of anti-water gas storage tank body is fixedly provided with pressure gauge, liquid level sensor is fixedly provided on anti-water gas storage tank body, the lower portion of anti-water gas storage tank body is fixedly provided with drainage component, the right side of anti-water gas storage tank body is fixedly provided with air guide component, the other side of air guide component is fixedly provided with humidifying jar body. The anti-water multi-stage protection device of humidifying jar can effectively prevent the liquid in the humidifying jar from flowing back to the upstream gas pipeline during abnormal conditions, damaging the instruments in the upstream equipment, causing other equipment failures, and automatically discharging the backflow water during abnormal conditions. The backflow water in the pipelines and equipment does not need to be manually removed, improving the safety and reliability of the humidification process production line and the degree of automation.

Hydrogen reforming system, comprehensive: a reformer (100) which produces a first mixed gas by means of a reforming reaction between fuel gas and water; a transformer (200) which is fed with the first mixed gas and produces a second mixed gas from which carbon monoxide is removed by means of a water-gas shift reaction; a unit (300) for pressure swing adsorption (PSA) that cleans and separates hydrogen from the second mixed gas generated in the transformer and discharges hydrogen-free exhaust gas; a heat exchanger (400) provided between the reformer and the transformer and between the transformer and the pressure swing adsorption (PSA) unit to control the temperatures of the first mixed gas and the second mixed gas by means of heat exchange with water; a water feeder (500) that communicates with the heat exchanger and supplies water to the heat exchanger and supplies the water exiting the heat exchanger to the reformer; and a control valve (600) which is provided on a line through which water is discharged from the water supply and which adjusts a flow rate of water supplied to the heat exchanger in order to control the first mixed gas and the second mixed gas separately, wherein the heat exchanger (400) comprises a first heat exchanger (410) provided between the reformer (100) and the transformer (200) in which heat exchange takes place between the first mixed gas and water; and a second heat exchanger (420) and a third heat exchanger (430) provided between the transformer (200) and the PSA unit in which heat exchange takes place between the second mixed gas and water, and wherein the water supply (500) comprises a first supply line (510) connected to and supplying water to the first heat exchanger (410), a second supply line (520) connected to and supplying water to the second heat exchanger (420), and a third supply line (530) connected to and supplying water to the third heat exchanger (430), thereby allowing the temperatures of the first mixed gas and the second mixed gas to be controlled separately, wherein the control valve (600) comprises a first control valve (610) provided on the first supply line (510) to control a flow rate of water flowing through the first supply line, and a second control valve (620) provided on the third supply line (530) to control a flow rate of water flowing through the third supply line (530), thereby separately controlling the flow rates of water flowing through the first supply line (510) and the third supply line (530).

A process for producing ammonia comprises a first operation mode and a second operation mode; the first operation mode comprises the steps of: producing a gaseous CO stream by electrolysis in electrolytic cells supplied with energy and a CO2 stream; liquefying the gaseous CO stream obtaining a liquid CO stream that is stored in a CO storage unit (5); sending a high pressure CO stream, taken from the CO storage unit (5), to a CO conversion unit (13) together with a liquid water stream to conduct a water-gas shift reaction and produce H2 to use in the ammonia synthesis reaction; the second operation mode comprises the steps of: operating at least a part of the electrolytic cells in reverse mode, i.e., as fuel cells, where CO and O2 are fed and CO2 is produced with generation of electricity; the cells operating as fuel cells being supplied with CO taken and pumped from the CO storage unit (5) and stored in the first operation mode, and with O2 produced in an air distillation step.