A photoelectric hydrogen production energy storage and cold energy recovery coupled dry ice production device and a use method are disclosed. The device comprises a photoelectric conversion liquid hydrogen energy storage unit, photoelectricity participates in electrolysis of water in the storage unit to prepare hydrogen, and surplus hydrogen meeting downstream process requirements is liquefied in the unit; liquid hydrogen is output, so that intermittent photoelectric energy is converted into hydrogen energy to be stored. When hydrogen production through electrolysis of water is insufficient but industrial hydrogen is continuously used, high-grade and low-grade cold energy of low-temperature liquid hydrogen serving as cold sources in the unit is recovered from industrial tail gas purified CO.sub.2 and air separation nitrogen, liquid nitrogen and liquid CO.sub.2 are output and used for the storage unit and dry ice production respectively, and the liquid hydrogen is reheated and supplied to a downstream process.

A process for the production of a liquid oxygen stream and a liquid hydrocarbon-rich stream by the cryogenic rectification of an inlet air stream, including dividing the inlet air stream into a first portion, and a second portion. Cooling the first portion, and the second portion against a cooled multicomponent refrigerant circuit, thereby producing a first cooled portion, and a second cooled portion. Condensing the first cooled portion, thereby producing a condensed first portion, then introducing the condensed first portion into one or more distillation columns. Expanding the second cooled portion in a turbo-expander, thereby producing an expanded second portion, then introducing the expanded second portion within the one or more distillation columns. Producing within the one or more distillation columns at least a waste nitrogen stream, a nitrogen enriched stream, and an oxygen enriched stream.

A hybrid process of air separation and gas liquefaction, including dividing a compressed multicomponent refrigerant stream into a first portion and a second portion, introducing the first portion into a gas liquefaction system, thereby producing a first multicomponent refrigerant return stream, and introducing the second portion into an air separation system, thereby producing a second multicomponent refrigerant return stream. Wherein the first multicomponent refrigerant return stream and the second multicomponent refrigerant return are recompressed in a common compression system, thereby producing the compressed multicomponent refrigerant stream.

An integrated industrial unit is provided, which can include: a nitrogen source comprising an air separation unit that is configured to provide pressurized gaseous nitrogen and liquid nitrogen; a hydrogen source; a hydrogen liquefaction unit, wherein the hydrogen liquefaction unit comprises a precooling system, and a liquefaction system; and a liquid hydrogen storage tank, wherein the precooling system is configured to receive the gaseous hydrogen from the hydrogen source and cool the gaseous hydrogen to a temperature between 70K and 100K, wherein the precooling system comprises a primary refrigeration system and a secondary refrigeration system, wherein the liquefaction system is in fluid communication with the precooling system and is configured to liquefy the gaseous hydrogen received from the precooling system to produce liquid hydrogen, wherein the liquid hydrogen storage tank is in fluid communication with the liquefaction system and is configured to store the liquid hydrogen received from the liquefaction system.

A process for producing liquid oxygen, including, a first operating mode, and a second operating mode. During the first operating mode, the distillation column produces a first flowrate of product liquid oxygen, and a first flow rate of liquid nitrogen product. During the second operating mode, the distillation column produces a second flowrate of product liquid oxygen, and a second flow rate of liquid nitrogen product. Wherein, the second flowrate of product liquid oxygen is greater than the first flowrate of product liquid oxygen.

A method for recovering associated gaseous hydrocarbons from a well for producing liquid hydrocarbons, the method comprising (i) providing gaseous hydrocarbons from a hydrocarbon well; (ii) providing a cryogenic liquid from an air separation unit or an associated nitrogen liquefaction facility within proximity of the hydrocarbon well; (iii) liquefying the gaseous hydrocarbons at a hydrocarbon liquefaction facility within proximity to the hydrocarbon well to thereby produce a liquefied hydrocarbon gas, where heat associated with the gaseous hydrocarbons is transferred to the cryogenic liquid; and (iv) transferring the liquefied hydrocarbon gas to an air separation unit or nitrogen liquefaction facility.

A system and method for cooling an oxygen stream by heat exchange with a warming supply nitrogen stream having of a heat exchanger having at least a Zone A and a Zone B, the system having indirect heat exchange between a gaseous oxygen stream, and a high-pressure liquid nitrogen stream split into at least a first portion which passes through a Zone A, and a second portion which passes through a Zone B during a first phase of operation. And a high-pressure liquid nitrogen stream passing through Zone A, thereby producing a high-pressure nitrogen vapor stream, which passes through an expansion turbine, thereby producing an expansion turbine outlet stream which then passes through Zone B, during a second phase of operation, thereby producing a liquid oxygen stream.

A process for co-producing a liquid oxygen and a liquefied hydrocarbon stream, including introducing a gaseous hydrocarbon stream and a gaseous nitrogen stream into a liquefier, thereby producing a liquefied hydrocarbon stream and a liquid nitrogen stream, liquefying a gaseous oxygen stream, wherein at least a portion of the required refrigeration is obtained from the liquid nitrogen stream. Wherein the liquefied hydrocarbon stream and the liquefied gaseous oxygen stream have mass flow rates. The liquid oxygen stream may be produced in an aft separation unit, wherein at least a portion of the required refrigeration is obtained from the liquid nitrogen stream.

A liquefier device which may be a retrofit to an air separation plant or utilized as part of a new design. The flow needed for the liquefier comes from an air separation plant running in a maxim oxygen state, in a stable mode. The three gas flows are low pressure oxygen, low pressure nitrogen, and higher pressure nitrogen. All of the flows are found on the side of the main heat exchanger with a temperature of about 37 degrees Fahrenheit. All of the gasses put into the liquefier come out as a subcooled liquid, for storage or return to the air separation plant. This new liquefier does not include a front end electrical compressor, and will take a self produced liquid nitrogen, pump it up to a runnable 420 psig pressure, and with the use of turbines, condensers, flash pots, and multi pass heat exchangers. The liquefier will make liquid from a planned amount of any pure gas oxygen or nitrogen an air separation plant can produce.

A process for the production of at least liquid oxygen and/or liquid nitrogen in cryogenic rectification. During a first period, during which electrical power prices are low, a process stream utilized by the ASU is liquefied and stored. During a second period, during which electrical prices high, at least a portion of the stored, liquefied process stream is withdrawn and introduced into the ASU. Wherein the MAC has a discharge pressure of greater than 10 bara during the first period, a first molar flowrate (LF) and a first pressure (LP) during the first period, a second molar flowrate (HF) and a second pressure (HP) during the second period. Wherein C=(LF/HF)/(LP/HP). And wherein second molar flowrate (HF) is <90% of first molar flowrate (LF) and C is between 0.9 and 1.05.