A process for recovering at least one fluid (e.g. argon gas and/or nitrogen gas, etc.) from a feed gas (e.g. air) can include utilization of a compression system, primary heat exchanger unit, plant processing units to separate and recover at least one desired fluid (e.g. nitrogen gas, argon gas, etc.). In some embodiments, the process can be configured so that fluid flows output from a low pressure column and/or high pressure column of the plant can provide a condensation duty or refrigeration duty that is utilized to process certain fluid flows for recovery of argon and/or nitrogen gases. Some embodiments can be configured to provide an improved recovery of argon and/or nitrogen as well as an improvement in operational efficiency by reducing an amount of power (e.g. electrical power) needed to recover the nitrogen and/or argon.

A refrigeration system for use in petrochemical plants, such as an ethylene production plant includes a refrigerant vent rectifier. The rectifier purifies the refrigerant by removing low molecular weight inerts. The refrigeration system is more efficient, consumes less energy and increases plant capacity.

A method and system for liquefying a natural gas feed stream and removing nitrogen therefrom.

A system for preparing subcooled liquid oxygen based on mixing of liquid oxygen and liquid nitrogen and then vacuum-pumping, including atmospheric-pressure saturated liquid nitrogen and oxygen tanks. An inlet of the liquid nitrogen tank communicates with pressurized gas, and an outlet is connected to an inlet a of a secondary subcooler. An inlet of the liquid oxygen tank communicates with the pressurized gas, and a first outlet is connected to an inlet b of the secondary subcooler. An outlet c of the secondary subcooler is connected to an inlet d of a primary subcooler. An outlet e of the primary subcooler is connected to a pumping-out device through a rewarming device. A second outlet of the liquid oxygen tank is connected to an inlet n of the primary subcooler. An outlet o of the primary subcooler is connected to an inlet r of the secondary subcooler.

A variable speed liquid LNG expander (X1) and a variable speed two-phase LNG expander (X2) in line, downstream from X1. The rotational speed of both expanders can be controlled and changed independent from each other. The speed of expander X1 and expander X2 is determined in such way that the amount of liquid LNG downstream from the PHS compared to the feed gas supply is maximized and the amount of vapor and boil-off downstream of X2 is minimized.

A system for liquefying production gas from a gas source containing a fluid having C1-C12 entrained gases includes a first phase separator for separating the C1-C12 gases from the fluid from the gas source. The first phase separator has an inlet in fluid communication with the gas source, a gas outlet and at least one alternative outlet. A first cryogenic liquefaction vessel has an inlet and an outlet. The inlet is in fluid communication with the gas outlet of the first phase separator. The first cryogenic liquefaction vessel cools the C1-C12 gases to liquefy the C3-C12 petroleum gases. A second phase separator is provided for separating the C3-C12 liquefied gases from the C1-C2 gases. The second phase separator has an inlet, a liquid outlet and a gas outlet. The inlet is in fluid communication with the outlet of the first cryogenic liquefaction vessel. At least one storage vessel is provided in fluid communication with the liquid outlet of the second phase separator for collection of the liquefied C3-C12 petroleum gases.

A system, apparatus and method for a superduct representing a unique process for helium distillation/liquefaction by means of a hypersonic stochastic switch is described. A supersonically expanded isentropic continuum is switched into a stochastic vortex flux by means of a thermally reactive slanted shafted nosecone and an extreme high pressure source hypersonic vortex flux. The concept can be further developed to a bridge spanning 1-10 miles of superduct segments, owing to its virtual nature and extreme power packaged kinetic energy of the hypersonic stochastic motive system.

A cryogenic method for capturing carbon dioxide in the gaseous emissions produced from the fossil-energy combustion of solid, liquid, or gaseous fossil fuels in a power generation installation employing an OxyFuel mode of combustion. The method includes: producing essentially pure carbon dioxide under elevated pressure and at near ambient temperatures in a Carbon-Dioxide Capture Component from the carbon-dioxide content of at least a part of the gaseous emissions produced from fossil-energy fueled combustion in the Oxyfuel mode of combustion; separating atmospheric air in an Air Separation Component into a stream of liquid nitrogen and a stream of high-purity oxygen; supplying low temperature, compressed purified air to a cryogenic air separation unit (cold box) within the Air Separation Component; collecting low temperature thermal energy from coolers employed within the Carbon-Dioxide Capture Component and the Air Separation Component; and converting the collected thermal energy to electricity within a Thermal-Energy Conversion Component.

A compressed air stream is cooled in an exchanger to form a compressed cooled air stream. The stream is then cryogenically compressed in a first compressor to form a first pressurized gas stream. The first pressurized gas stream is further cooled in the exchanger, cryogenically compressed in a second compressor, and then it is cooled and partially liquefied. The cooled and partially liquefied product is then fed to a system of distillation columns. A liquid product is removed from the system of distillation columns. This product is then pressurized, vaporized and warmed in the exchanger to yield pressurized gaseous product.

A method and apparatus for the production of air gases by the cryogenic separation of air with front end purification and air compression can include using an available compressed dry gas such as nitrogen, oxygen, stored purified air, or synthetic air to repressurize the adsorber without diverting any of the purified air just exiting the currently on-line adsorber or changing the flow rate of the main air compressor or air sent to the cold box. This enables the main air compressor (MAC) to operate at a relatively constant flow rate while also sending a relatively constant air flow to the cold box during this repressurization step, thereby reducing the risks of process upsets and minimizing capital expenditures related to the MAC and other warm-end equipments.