225results about "Hydrogen separation by selective and reversible uptake" patented technology

Helium is recovered from gas streams containing high concentrations of hydrogen gas and low concentrations of helium gas, such as from the recycle stream from the production of ammonia. The inventive process provides for an integrated process for the recovery of both an enriched helium gas stream product and a high purity hydrogen gas stream product.

The invention discloses a method for simultaneously preparing pure hydrogen and pure carbon monoxide by gasification without desorbed gas circulation. The crude synthetic gas prepared by the gasification unit is divided into two parts, one part is used for preparing pure carbon monoxide, and the other part is preparing pure hydrogen. The process of preparing pure carbon monoxide is divided into two parts: one part is used for preparing pure carbon monoxide with the crude synthetic gas prepared by gasification by a heat recovery unit, a low temperature methanol washing I unit, and a cryogenic separation unit; and the other part is used for preparing pure carbon monoxide by the hydrogen rich gas from the outlet of the cold box of the cryogenic separation unit sending into a PSA-CO unit. The feedstock of preparing hydrogen is divided into two parts: one part is the converted gas which is purified by a conversion unit and a low temperature methanol washing II unit with the crude synthetic gas prepared by gasification and contains carbon monoxide -1% (mol), and the other part is the hydrogen rich gas from a resurgent TSA device of the cryogenic separation unit, and the two parts of the gas are mixed and sent into the PSA-H2 unit to prepare pure hydrogen. The method has high recovery rates of carbon monoxide and hydrogen, has no desorbed gas circulation and no resurgent gas introduced by environment, has small investment and low energy consumption, and can adjust product gas scale of hydrogen and carbon monoxide flexibly.

The invention relates to an energy gradient utilization type hydrogen thermal compression system. The system comprises 1-100 stages of hydrogen thermal compressors located in different working temperature intervals and a high-pressure hydrogen total pipe, wherein the hydrogen thermal compressors are provided with low-pressure hydrogen inlets, high-pressure hydrogen outlets and 1-100 metal hydride reaction beds; the low-pressure hydrogen inlets are connected with a low-pressure hydrogen pipeline, and the high-pressure hydrogen outlets are connected with the high-pressure hydrogen total pipe through a high-pressure hydrogen pipeline; an external heat source sequentially passes through multiple stages of the hydrogen thermal compressors through an external heating pipeline from the high working temperature interval to the low working temperature interval; and an interstage heat exchange pipeline is arranged between each two adjacent hydrogen thermal compressors, and an inner-stage heat exchange pipeline is arranged in each stage of the hydrogen thermal compressor. According to the energy gradient utilization type hydrogen thermal compression system, by adequately utilizing reaction heat released during hydrogen absorption of the reaction beds of the hydrogen thermal compressors by virtue of metal hydride as well as sensible heat released during a cooling operation, the thermal efficiency of each hydrogen thermal compressor is improved, and the range and selectivity of waste heat utilization are expanded.

The invention provides a production process and system of high-purity hydrogen and an ammonia synthesis process and system. The production process of high-purity hydrogen comprises the steps of generating water gas by using bituminous coal, generating shifted gas by using the water gas, desulfurizing the shifted gas, and carrying out decarbonization and hydrogen extraction on the shifted gas; the ammonia synthesis process comprises the steps of hydrogen nitrogen-feeding and deoxygenization, nitrogen-hydrogen compression and ammonia synthesis. The production system of high-purity hydrogen comprises a water gas generating part, a shifted gas generating part, a shifted gas desulfurizing part and a shifted gas decarbonization and hydrogen extraction part; and the ammonia synthesis system also comprises a hydrogen nitrogen-feeding and deoxygenization part, a nitrogen-hydrogen compression part and an ammonia synthesis part. The production process of high-purity hydrogen disclosed by the invention is short in flow, small in resistance, low in power consumption and low in operating cost; and the production system of high-purity hydrogen disclosed by the invention is high in degree of automation, less in catalyst consumption, less in species, less in operators, good in operating environment, low in operating cost and remarkable in energy saving and consumption reducing effect.

A vanadium alloy essentially consisting of: vanadium; and aluminium having a content of greater than 0 to 10 at %, and a process of producing thereof.

The invention discloses a hydrogen purification device. The hydrogen purification device comprises a hydrogen storage device filled with hydrogen storage alloy powder, wherein one end of the hydrogenstorage device is connected with an inlet pipeline; the other end of the hydrogen storage device is connected with an outlet pipeline; and the hydrogen storage device is provided with a heat exchangedevice. When a hydrogen raw material mixed with impurity gas enters the hydrogen storage device through the inlet pipeline, hydrogen is absorbed by the hydrogen storage alloy powder in the hydrogen storage device; when the hydrogen raw material is stopped from entering the hydrogen storage device, gas in the hydrogen storage device is slowly discharged through the outlet pipeline, the content of impurity gas in the discharged gas is high, and then the hydrogen with gradually higher purity is slowly discharged. The complexity of the hydrogen purification device is simplified, the occupied spaceof the hydrogen purification device is reduced, the operation condition is mild, the safety is high, and the application range is wide. The invention also discloses a method for detecting hydrogen purification efficiency of the hydrogen purification device, the purification efficiency of pure hydrogen is obtained by calculating the content of impurities, and the detection precision of the hydrogen purification efficiency is improved.

The invention relates to monocrystalline single crystals of metal-organic framework materials comprising at least one aluminium metal ion, processes for preparing the same, methods for employing the same, and the use thereof. The invention also relates to monocrystalline aluminium metal-organic frameworks.

The invention discloses a low-temperature methanol washing device and a method for removing acid gas in synthesis gas. A main low-temperature methanol washing process is reconfigured, semi-lean solution methanol is additionally taken as main washing methanol on the basis of an original full-lean solution absorption process, and the dosage of lean solution methanol is decreased by 15%-30%, so that the dosages of thermal regeneration tower reboiler steam, thermal regeneration tower top condenser circulating water, lean methanol water cooler circulating water and H2S concentration tower gas stripping nitrogen are decreased by 15%-30% to achieve the energy saving and yield increasing targets; meanwhile, a traditional three-stage condensation process on a thermal regeneration tower top is canceled, therefore, methanol losses are reduced, and an ammonia crystallization phenomenon is avoided. Energy saving and yield increasing improvement on a traditional low-temperature methanol washing device is also suitable for the newly-built low-temperature methanol washing device.

The invention belongs to a hydrogen-containing tail gas recycling process of a cyclohexanol production device. The hydrogen-containing tail gas recycling process comprises the following steps: conveying hydrogen-containing tail gas generated by the cyclohexanol production device into a gas-liquid separator, and compressing the gas separated from the gas-liquid separator to be 0.8MPa by a compressor; then cooling the gas to 8 DEG C to 12 DEG C; finally, enabling the gas to enter a filtering separator to obtain waste liquid and crude hydrogen gas, and adsorbing the crude hydrogen gas by an adsorption tower to obtain product hydrogen gas; collecting waste liquid obtained by the filtering separator to a waste oil tank, and standing and separating out water; filtering an organic phase with a fine filter, and heating to 120 DEG C to 140 DEG C; then conveying the organic phase into a desulfurizing tower, and then cooling and conveying the organic phase to the cyclohexanol production device to be used as the raw material. With the adoption of the hydrogen-containing tail gas recycling process of the cyclohexanol production device, moisture and impurities in the tail gas exhausted by a hydrogenation reaction system of the cyclohexanol production device can be effectively separated, and components including benzene, cyclohexene, cyclohexane and the like in the tail gas are recycled very well; with the adoption of the process, the tail gas can be returned back to a dehydration tower of the cyclohexanol production device to be recycled.

Less hazardous methods for generating energy for heating water, medical supplies or comestible products using improved flameless chemical heaters/flameless ration heaters by novel chemical or electrochemical means, each capable of suppressing the generation of hydrogen gas. Remote unit self heating meals may be heated by forming a reaction mixture comprising magnesium or a magnesium-containing alloy, a hydrogen scavenger and water, and reacting the reaction mixture to generate sufficient energy for heating the water, or other comestible product while simultaneously suppressing the generation of hydrogen. Alternatively, a battery may be employed using Mg and MnO₂.

Provided is a hydrogen penetration barrier for preventing hydrogen from being diffused and discharged through a barrier and preventing hydrogen embrittlement of a material due to diffusion of hydrogen ions into a material. In detail, the hydrogen penetration barrier prevents penetration of hydrogen ions by using a built-in potential of a semiconductor layer doped with a p-type impurity and a semiconductor layer doped with an n-type impurity and a potential applied by a reverse biased voltage and includes an absorption layer absorbing the hydrogen molecules to primarily prevent the penetration of the hydrogen molecules and uses the absorption layer made of the conductive material as an application electrode of the reverse biased voltage and ionizes the hydrogen absorbed to the absorption layer to secondarily prevent the penetration of the hydrogen molecules and prevent the hydrogen embrittlement.

An external gelation process is described which produces granules of metal hydride particles contained within a sol-gel matrix. The resulting granules are dimensionally stable and are useful for applications such as hydrogen separation and hydrogen purification. An additional coating technique for strengthening the granules is also provided.

A catalyst-containing reaction accelerator used in a steam reforming reaction of hydrocarbon comprises a solid catalyst to accelerate the steam reforming reaction, and a composite absorbent which is mixed with the solid catalyst. The composite absorbent has a main absorbent which contains a lithium-containing oxide for absorbing and desorbing carbon dioxide by-produced by the steam reforming reaction, and a molten carbonate holding material which does not react with the main absorbent at a temperature at which the main absorbent absorbs and desorbs carbon dioxide.

The present invention provides a method for reducing iron oxide to metallic iron using coke oven gas, including: dividing coke oven gas from a coke oven gas source into a plurality of coke oven gas streams; providing a first coke oven gas stream to a hydrogen enrichment unit to form a hydrogen-rich product stream that is delivered to a reduction shaft furnace as part of a reducing gas stream; and providing a tail gas stream from the hydrogen enrichment unit to a reforming reactor to form a reformed gas stream that is delivered to a reduction shaft furnace as part of the reducing gas stream. Optionally, a spent top gas stream from the reduction shaft furnace is cleansed of CO₂ and recycled back to the reducing gas stream.

The invention discloses a separation, purification and recovery process of hydrogen in industrial waste gas. The process comprises the following steps that A, after being pressurized by a waste gas pressurizing device, hydrogen-containing industrial waste gas is led into a hydrogen storage alloy container; B, the hydrogen storage alloy container is heated by a hydrogen storage alloy container heating device to reach the temperature of 200-400 DEG C, the temperature is kept for two hours, and then the hydrogen storage alloy container heating device stops heating; C, after the hydrogen storage alloy container is cooled to 20-200 DEG C, an exhaust device is turned on, and the exhaust device is turned off when residual gas in the hydrogen storage alloy container is discharged until pressure inthe hydrogen storage alloy container is lowered to 0.001 Mpa; and D, the hydrogen storage alloy container is heated by the hydrogen storage alloy container heating device to reach the temperature of300-450 DEG C, an exhaust valve is opened, and hydrogen released by hydrogen storage alloy in the hydrogen storage alloy container is discharged into a recovery device. The purity of the recovered hydrogen is greater than 99.999%, recovery safety efficiency is high, and the recovered gas can be reutilized.

A technology for synthesizing low carbon alcohol and hydrogen as byproduct from coke oven gas comprises the following steps: compressing the coke oven gas, carrying out desulphurization and decarburization treatment to obtain purified coke oven gas with the H2S content being smaller than 1ppm, allowing the purified coke oven gas to enter a pressure swing adsorption unit in order to remove CH4, allowing removed CH4 and CO2 obtained after purification to enter a coke oven gas reforming unit, reforming, mixing the obtained reformed gas with the coke oven gas obtained after pressure swing adsorption to obtain synthetic gas meeting low carbon alcohol synthesis requirements, carrying out low carbon alcohol synthesis, allowing the obtained low carbon alcohol mixture to enter a low carbon alcohol separation unit, and separating to obtain methanol, ethanol, propanol and butanol products. The technology comprises the advantages of reasonable utilization of the coke oven gas, promotion of energy saving and emission reduction, energy structure adjustment, and obvious improvement of the economic and environmental benefits.

The invention discloses a hydrogen purifier, which comprises a main body purifying device, an automatic controller, a heat exchange device and a waste gas treating device, wherein the main body purifying device comprises a gas inlet pipe, a gas inlet pump, a gas inlet valve, a gas inlet cut-off valve, a reaction tank, a gas discharge cut-off valve, a gas discharge valve, a gas discharge pump, a gas discharge pipe, a bypass valve, a reversing gas pipe, a gas discharge reversing valve and a waste gas discharge pipe, the reaction tank comprises a reaction tank outer wall, a reaction tank interlayer, a reaction tank inner wall, a hydrogen storage alloy reaction bed body, a pressure gauge and a filter, and the heat exchange device comprises a hot water box, a cold water box, a two-way water pump and a heat exchanger. According to the present invention, hydrogen purification is performed by using the characteristics of the hydrogen storage alloy; and the hydrogen purifier has characteristicsof small size, low cost, simple process and direct online/offline use, and has great advantages compared to other hydrogen purification methods.

One exemplary embodiment can be a process for catalytic reforming The process can include catalytically reforming a hydrocarbon feed in a reaction zone, obtaining an effluent stream having hydrogen and hydrocarbons from the reaction zone, obtaining from at least a portion of the effluent stream a waste hydrocarbon stream from an adsorption zone, passing at least a portion of the waste hydrocarbon stream as a feed stream across a feed side of a membrane having the feed side and a permeate side, and being selective for hydrogen over one or more C1-C6 hydrocarbons, and withdrawing from the permeate side a permeate stream enriched in hydrogen compared with a residue stream withdrawn from the feed side.

Article of manufacture fabricated by plastic deformation of an intermetallic compound comprising R and M, such as an RM intermetallic compound and a higher order compound thereof, having a CsCl-type ordered crystal structure wherein R is one or more rare earth elements and M is one or more non-rare earth metals. The article of manufacture has a tensile elongation of at least about 5% prior to fracture when tensile tested at room temperature in ambient air. The article of manufacture also can be fabricated by plastic deformation of an intermetallic compound comprising a M′M compound and a higher order compound thereof having a CsCl-type ordered crystal structure wherein M′ and M are one or more different non-rare earth metals.

The invention relates to a technology for producing hydrogen from coke oven gas. The feed gas contains 45-55% of hydrogen. The technology comprises the following steps: removing most of carbon dioxide, C<2+> and methane through first-stage pressure swing adsorption so that the concentration of hydrogen-rich gas is 93-96% and the hydrogen yield is greater than 97%; compressing the hydrogen-rich gas to 0.8-2.8MPa, wherein the compressed exit gas is not cooled (interstage cooling is needed); at 80-110 DEG C, catalyzing oxygen in a deoxygenation tower and generating carbon dioxide with carbon monoxide or catalyzing oxygen and generating water with hydrogen; removing oxygen to below 1ppm and cooling the deoxygenated gas to below 40 DEG C; removing non-hydrogen gas through second-stage pressure swing adsorption; and purifying the hydrogen to 99-99.99999% as required.