A heat exchanger with a uniquely designed header system which allows tubes carrying independent products to exchange heat with a product in one common shell. Multiple tube sheets provide for tubes carrying different independent products to exchange heat with the product passing through the shell side of the exchanger. The design advantages to this heat exchanger system are threefold, this exchanger design eliminates the need for multiple heat exchangers that perform the same task, it greatly reduces the size and footprint of a traditionally designed multiple heat exchanger systems, which rely on multiple independent heat exchangers to perform the same task, and lastly this new designed heat exchanger reduces the high cost of having to use multiple exchangers to obtain the same results.

Systems and methods for liquefying a gaseous fluid that comprises at least 50% by volume methane into a liquefied fluid that comprises at least 85% by volume methane. Processing can include increasing a pressure of the incoming gaseous fluid to between 10 and 50 bar; pre-treating the gaseous fluid using membrane filtering to a retentate stream having a methane content of at least 85% by volume; liquefying the retentate stream by cryogenic cooling to a temperature between 100 C. and 140 C.; flashing the liquefied fluid into a container; retrieving processed liquid fluid at a first container level at a pressure of between 1 and 10 bar, a temperature of between 120 C. and 160 C., and a methane concentration of at least 85% by volume into a storage device; and retrieving a slurry flow comprising solid CO.sub.2 and water ice at a second container level below the first container level.

Systems and methods for liquefying a gaseous fluid that comprises at least 50% by volume methane into a liquefied fluid that comprises at least 85% by volume methane. Processing can include increasing a pressure of the incoming gaseous fluid to between 10 and 50 bar; pre-treating the gaseous fluid using membrane filtering to a retentate stream having a methane content of at least 85% by volume; liquefying the retentate stream by cryogenic cooling to a temperature between 100 C. and 140 C.; flashing the liquefied fluid into a container; retrieving processed liquid fluid at a first container level at a pressure of between 1 and 10 bar, a temperature of between 120 C. and 160 C., and a methane concentration of at least 85% by volume into a storage device; and retrieving a slurry flow comprising solid CO2 and water ice at a second container level below the first container level.

A liquefaction system is capable of sequentially or simultaneously liquefying multiple feed streams of hydrocarbons having different normal bubble points with minimal flash. The liquefying heat exchanger has separate circuits for handling multiple feed streams. The feed stream with the lowest normal boiling point is sub-cooled sufficiently to suppress most of the flash. Feed streams with relatively high normal boiling points are cooled to substantially the same temperature, then blended with bypass streams to maintain each product near its normal bubble point. The system can also liquefy one stream at a time by using a dedicated circuit or by allocating the same feed to multiple circuits.

A system includes a waste heat recovery heat exchanger configured to heat a heating fluid stream by exchange with a heat source in a crude oil associated gas processing plant; and an Organic Rankine cycle energy conversion system. The Organic Rankine cycle energy conversion system includes a heat exchanger configured to heat a first portion of a working fluid by exchange with the heated heating fluid stream; and a cooling subsystem including one or more cooling elements each configured to cool one or more of a process stream from the crude oil associated gas processing plant and a cooling water stream for ambient air cooling by exchange with a second portion of the working fluid. The Organic Rankine cycle energy conversion system includes an ejector configured to receive the second portion of the working fluid from the cooling subsystem and a third portion of the working fluid; a turbine and a generator configured to generate power by expansion of a fourth portion of the working fluid; and a cooling element configured to cool a stream of working fluid including an output stream of working fluid from the ejector and the expanded fourth portion of the working fluid from the turbine and generator.

Provided are apparatus and systems for performing a swing adsorption process. This swing adsorption process may involve passing streams through adsorbent bed units to remove contaminants, such as water, from the stream. As part of the process, the adsorbent bed unit is purged with a purge stream that is provided from the overhead of the demethanizer. The configuration integrates a RCTSA dehydration system with a cryogenic recovery system.

A system includes a waste heat recovery heat exchanger configured to heat a heating fluid stream by exchange with a heat source in a crude oil associated gas processing plant. The system includes an Organic Rankine cycle energy conversion system including a pump, an energy conversion heat exchanger configured to heat the working fluid by exchange with the heated heating fluid stream, a turbine and a generator configured to generate power by expansion of the heated working fluid, a cooling element configured to cool the expanded working fluid after power generation, and an accumulation tank. The heating fluid flows from the accumulation tank, through the waste heat recovery heat exchanger, through the Organic Rankine cycle energy conversion system, and back to the accumulation tank.

Systems, devices, and methods for recovering mixed refrigerant and/or nitrogen within liquefaction systems are provided. The systems, devices, and methods facilitate recovering mixed refrigerant (MR) and/or nitrogen vapor that can leak from a compressor, separating the MR from the nitrogen, and reusing the MR and/or the nitrogen within the liquefaction system. Recovering and reusing MR and/or nitrogen can minimize loss of MR and nitrogen which can lower the total operating cost of a liquefaction system. Additionally, recovering the MR, rather than burning it, can reduce environmental emissions by reducing the amount of MR that is burned.

An expander and motor-compressor unit is disclosed. The unit includes a casing and an electric motor arranged in the casing. A compressor is arranged in the casing and drivingly coupled to the electric motor through a central shaft. Furthermore, a turbo-expander is arranged for rotation in the casing and is drivingly coupled to the electric motor and to the compressor through the central shaft.

A method for separating a vapor from a carrier gas is disclosed. A hydrocyclone is provided with one or more nozzles on the wall of the hydrocyclone. A cryogenic liquid is provided to the tangential feed inlet at a velocity that induces a tangential flow and a cyclone vortex in the hydrocyclone. The carrier gas is injected into the hydrocyclone through the one or more nozzles. The vapor dissolves, condenses, desublimates, or a combination thereof, forming a vapor-depleted carrier gas and a vapor-enriched cryogenic liquid. The vapor-depleted gas is drawn through the vortex finder while the vapor-enriched cryogenic liquid is drawn through the apex nozzle outlet. In this manner, the vapor is removed from the carrier gas.