Provided is a hydrogen recovery method such that highly concentrated hydrogen gas can be obtained efficiently by adsorbing and removing hydrocarbon gas such as carbon dioxide, carbon monoxide, and methane, using a relatively low pressure, from pyrolysis gas obtained by heat treating biomass. The present invention is the method for recovering hydrogen from pyrolysis gas obtained by heat treating biomass, characterized by including: a first purifying step of adsorbing and removing gas that mainly includes carbon dioxide under pressure from the pyrolysis gas to purify the pyrolysis gas; and a second purifying step of further adsorbing and removing gas that includes carbon dioxide under pressure from purified gas obtained by the first purifying step at a pressure lower than the pressure in the first purifying step to purify the purified gas in order to recover hydrogen from the purified gas.

A device for drying compressed gas with an inlet for compressed gas to be dried originating from a compressor and an outlet for dried compressed gas, where this device includes a number of vessels that are filled with a regeneratable drying agent and a controllable valve system that connects the aforementioned inlet and outlet to the aforementioned vessels, where the device includes at least three vessels, where the aforementioned valve system is such that at least one vessel is always being regenerated, while the other vessels dry the compressed gas, where due to the control of the valve system the vessels are each successively regenerated in turn.

A pressure swing adsorption gas production device that enables performing a desorption process in adsorption towers is provided. The device includes an off gas discharge route connected to the adsorption towers, a membrane separation unit with a separation membrane allowing miscellaneous gas in the off gas discharge route to pass faster than purification target gas, an off gas tank, and a pressure boosting unit that raises the pressure of and supplies the off gas to the membrane separation unit. The off gas tank and the pressure boosting unit are upstream of the membrane separation unit. The device includes a recycle gas return route via which some recycle gas is returned to the source gas supply route. The operation control unit adjusts the off gas adjustment unit so the off gas discharge flow rate is a flow rate where the amount of off gas discharged from one adsorption tower during the desorption process is equivalent to the amount of off gas discharged from the off gas tank when the one adsorption tower starts the desorption process until another starts the desorption process.

A method for the continuous production of ozone and recovery of oxygen in a purge cycle adsorption process having four adsorbent beds. The method has the steps of feeding a mixture of ozone and oxygen to a first and second adsorbent bed wherein the first and the second adsorbent bed adsorb ozone and allow oxygen to pass through; recovering the oxygen from the first bed; feeding the oxygen from the second bed to a fourth adsorbent bed, wherein ozone is desorbed from the fourth bed; feeding clean dry air through a valve to the third adsorbent bed, and measuring the flow rate of the clean dry air through the valve, comparing this flow rate to a pre-calculated value and adjusting the flow rate of the clean dry air to equal the pre-calculated value; desorbing ozone from the third bed; and recovering ozone from the third bed and the fourth bed.

A portable pressure swing adsorption method and system for fuel gas conditioning. A fuel gas conditioning system includes a pressure swing adsorption (PSA) system fluidly coupled to a rich gas stream, the PSA system including a plurality of adsorbent beds and configured to condition the rich natural gas stream and produce therefrom a high-quality fuel gas and gaseous separated heavier hydrocarbons, a product end of the adsorbent beds fluidly coupled to a fuel gas line, wherein the high-quality fuel gas is discharged from the product end and supplied to the fuel gas line, and a feed end of the adsorbent beds configured to be fluidly coupled to the rich natural gas stream or a raw natural gas stream, wherein the produced gaseous separated heavier hydrocarbons are recirculated into the rich natural gas stream or the raw natural gas stream.

The invention relates to a set for separating two or more gases from each other, including: a first adsorption column set comprising at least two columns in series; an optional number of additional column sets comprising additional columns; connectors connecting each parallel additional column to the column; auxiliary equipment feeding a gas mixture to the columns and additional columns jointly and discharging separated gases according to pressure swing adsorption.

Provided is a pressure swing adsorption type hydrogen manufacturing apparatus that can improve the product recovery rate in a state where the purity of the product is kept from being reduced. A process control unit P controls operation of adsorption towers 1 that generate a product gas by adsorbing, using adsorbents, adsorption target components other than hydrogen components from a source gas, in a state where an adsorption process, a pressure-equalization discharge process, a desorption process, and a pressure-restoration process are successively repeated. The process control unit is configured to control operation of the adsorption towers 1 in such a manner that a prior pressure-equalization process of supplying gas inside an adsorption tower 1 undergoing the pressure-equalization discharge process to an adsorption tower 1 undergoing the pressure-restoration process is performed in an initial stage of a unit processing period, a subsequent pressure-equalization process of supplying gas inside the adsorption tower 1 undergoing the pressure-equalization discharge process to an adsorption tower 1 undergoing the desorption process is performed in a final stage of the unit processing period, a pressurization process of introducing a product gas H to perform pressurization is performed, as the pressure-restoration process, subsequently to the prior pressure-equalization process, and the pressurization process is performed while overlapping with the subsequent pressure-equalization process.

A liquid air energy storage system comprises an air liquefier, a storage facility for storing the liquefied air, and a power recovery unit coupled to the storage facility. The air liquefier comprises an air input, an adsorption air purification unit for purifying the input air, and a cold box for liquefying the purified air. The power recovery unit comprises a pump for pressurising the liquefied air from the liquid air storage facility, an evaporator for transforming the high-pressure liquefied air into high-pressure gaseous air, an expansion turbine capable of being driven by the high-pressure gaseous air, a generator for generating electricity from the expansion turbine, and an exhaust for exhausting low-pressure gaseous air from the expansion turbine. The exhaust is coupled to the adsorption air purification unit such that at least a portion of the exhausted low-pressure gaseous air is usable to regenerate the adsorption air purification unit.

A device for drying compressed gas with an inlet for compressed gas to be dried originating from a compressor and an outlet for dried compressed gas, whereby this device comprises a number of vessels that are filled with a regeneratable drying agent and a controllable valve system that connects the aforementioned inlet and outlet to the aforementioned vessels, wherein the device comprises at least three vessels, whereby the aforementioned valve system is such that at least one vessel is always being regenerated, while the other vessels dry the compressed gas, whereby due to the control of the valve system the vessels are each successively regenerated in turn.

Disclosed herein are rapid cycle pressure swing adsorption (PSA) process for separating O.sub.2 from N.sub.2 and/or Ar. The processes use a carbon molecular sieve (CMS) adsorbent having an O.sub.2/N.sub.2 and/or O.sub.2/Ar kinetic selectivity of at least 5 and an O.sub.2 adsorption rate (1/s) of at least 0.2000 as determined by linear driving force model at 1 atma and 86 F.