Mixed refrigerants in ethylene recovery

The present invention is a process of high efficiency rectification zone separation of cracked or other ethylene-containing gas chilled primarily by two closed mixed refrigerant loops and at least part of the dephlegmated overhead gas. The composition of the mixed refrigerants is optimally chosen to obtain an extremely close approach between the process condensation temperatures in the high efficiency rectification zone and the temperature of the chilling streams. An approach of about 3° F. to 8° F. can be achieved for the full condensation curve in the high efficiency rectification zone operating with either ethane or naphtha derived cracked gas. Highly reliable and stable operation is obtained by closed refrigeration loops in the present invention, in addition to reducing high efficiency rectification zone design cost.

Separation of hydrogen-hydrocarbon gas mixtures using closed-loop gas expander refrigeration

A method for the recovery of hydrogen and one or more hydrocarbons having one or more carbon atoms from a feed gas containing hydrogen and the one or more hydrocarbons, which process comprises cooling and partially condensing the feed gas to provide a partially condensed feed; separating the partially condensed feed to provide a first liquid stream enriched in the one or more hydrocarbons and a first vapor stream enriched in hydrogen; further cooling and partially condensing the first vapor stream to provide an intermediate two-phase stream; and separating the intermediate two-phase stream to yield a further-enriched hydrogen stream and a hydrogen-depleted residual hydrocarbon stream. Some or all of the cooling is provided by indirect heat exchange with cold gas refrigerant generated in a closed-loop gas expander refrigeration cycle.

Purification of carbon dioxide

Impure carbon dioxide (“CO 2 ”) comprising a first contaminant selected from the group consisting of oxygen (“O 2 ”) and carbon monoxide (“CO”) is purified by separating expanded impure carbon dioxide liquid in a mass transfer separation column system. The impure carbon dioxide may be derived from, for example, flue gas from an oxyfuel combustion process or waste gas from a hydrogen (“H 2 ”) PSA system.

Multistoreyed bath condenser

The invention relates to a multistoreyed bath condenser comprising a condenser block (1) provided with evaporation passages (8) for a liquid and condensation passages (2) for a heating medium in addition to possessing at least two vertically superimposed circulation sections (7) . The evaporation passages (8) are respectively provided with at least one inlet (9) for a fluid on the lower end of the circulation section (7) and at least one outlet on the upper end of a circulation section (10). A reservoir for liquid is provided for each circulation section (7). Said reservoir is fluidically connected to the inlet 9) and outlet (10) of the circulation section (7) and is fitted with a gas conduit (18). The inlet to the gas conduit (18) is not located in the region in front of the side (12) of the circulation section (7) where the outlet (10) of the circulation section (7) is arranged.

Multistoreyed bath condenser

The invention relates to a multistoreyed bath condenser comprising a condenser block (1) provided with evaporation passages (8) for a liquid and condensation passages (2) for a heating medium. The condenser block has at least two vertically superimposed circulation sections (7) . The evaporation passages (8) are respectively provided with at least one inlet (9) for a fluid on the lower end of a circulation section (7) and at least one outlet on the upper end of a circulation section (10). The outlets (10) and inlets (9) located on the same side (12) of the condenser block (1) are exclusively provided with means (7,30) for supplying a liquid.

LIQUEFACTION PROCESS

Cryogenic recovery of liquid hydrocarbons from hydrogen-rich

A vapor fraction containing hydrogen and at least one hydrocarbon selected from the group consisting of C 1 to C 4 hydrocarbons is separated from a hydrogen-rich refinery off-gas feed to give a liquid product fraction. The refinery off-gas is fed to and compressed in a compressor/expander having compressor means and expander means mounted and driven on a common shaft, and then cooled and partially condensed to form a two-phase fluid in a heat exchanger followed by separation of the vapor and liquid product phases of the fluid in a separator or a separator/fractionation column stabilizer unit. The separated vapor phase is transmitted to the compressor/expander unit wherein the vapor is depressurized and partially condensed, thereby driving the compressor. The partially condensed depressurized vapor fraction from the expander and, optionally, the liquid phase product fraction from the separator are transmitted in separate streams to the heat exchanger for separate thermal contact with the compressed feed gas wherein the partially condensed depressurized vapor fraction is fully vaporized and the feed gases are cooled. The fully vaporized fraction and the liquid product fraction are recovered in separate streams.

Lower power, freon refrigeration assisted air separation

Liquid oxygen and liquid nitrogen are produced from the separation of air in an installation of reduced size wherein the refrigeration necessary for the operation of the air separation unit is produced from the use of a single compander and a freon refrigeration unit affixed to a split-out stream of the main heat exchanger with appropriate recycling and heat exchange. The process for such an installation is also set forth.

Separation of gas mixtures by partial condensation

In a process for the separation of a gas mixture at superatmospheric pressure by partial condensation at cryogenic temperatures and wherein the separated condensate and uncondensed vapor are passed back as returning streams in indirect countercurrent heat exchange relationship with the incoming feed mixture, the power required for providing the refrigeration and energy requirements for the separation are reduced by supplying said requirements by means of a heat pump alone or together with at least one separate refrigeration cycle and/or some Joule-Thomson expansion of the condensate, and in the heat pump a compressed multi-component gaseous medium is condensed by heat exchange with said returning streams over a first temperature range and then expanded by Joule-Thomson expansion, and the expanded condensate is evaporated by heat exchange with the feed gas mixture over a lower temperature range than said first temperature range, and recycled for recompression.

Apparatus for the liquefaction of natural gas and methods relating to same

A liquefaction plant (102) comprising: a plant inlet (112) configured to be sealingly and fluidly coupled with a source of unpurified natural gas; a turbo expander (156) positioned and configured to receive a first stream of natural gas drawn through the plant inlet and produce and expanded cooling stream therefrom; a compressor (158) mechanically coupled to the turbo expander and positioned and configured to receive a second stream of natural gas drawn through the plant inlet and produce a compresses process stream therefrom; a first heat exchanger (166) positioned and configured to receive the compressed process stream and the expanded cooling stream in a countercurrent flow arrangement to cool the compressed process stream; a first plant outlet (132) positioned and configured to be sealingly and fluidly coupled with the source of unpurified gas and to discharge the expanded cooling stream thereinto subsequent to passage thereof through the heat exchanger; a first expansion valve (174) positioned and configured to receive and expand a first portion of the cooled compressed process stream to form an additional cooling stream, the plant further including conduit structure to combine additional cooling stream with the expanded cooling stream to the expanded cooling stream entering the first heat exchanger; a second expansion valve (176) positioned and configured to receive and expand a second portion of the cooled compressed process stream to form gas-solid-liquid mixture therefrom; a first gas-liquid separator (180) positioned and configured to receive the gas-solid-liquid mixture; and a second plant outlet (114) positioned to be sealingly and fluidly coupled with a storage vessel, the first gas-liquid separator being positioned and configured to deliver a liquid contained therein to the second plant outlet.

Procede de traitement d'un courant de gnl obtenu par refroidissement au moyen d'un premier cycle de refrigeration et installation associee.

Separation of gas mixtures such as methane and nitrogen mixtures

Liquefaction of natural gas with product used as absorber purge

This invention relates to a process for purifying and liquefying a natural gas stream comprising the steps of passing said stream through absorption units to remove impurities, compressing said stream, liquefying said stream by heat exchange with a low temperature nitrogen refrigeration cycle, stripping the nitrogen from said liquefied stream, utilizing said nitrogen in said refrigeration cycle, storing a portion of said liquefied stream, and condensing the boil-off from said storage with low temperature nitrogen from said cycle.

Dephlegmator process with liquid additive

A cryogenic process for the separation of one light gas component from a heavier gas component in a gas feed stream, by injecting a liquid hydrocarbon additive stream into the top or upper portion of a dephlegmator-heat exchanger, to increase the rectification temperature, or to maintain the temperature and reduce the additive flow rate relative to the respective values required with a conventional, single stage condenser.

Separation of hydrogen containing gas mixtures

Enhanced recovery of the methane content of a multicomponent stream containing lower boiling gas components is obtained by effecting condensation of at least the major portion of the methane content in a dephlegmator wherein separated lower boiling components are employed as indirect heat exchange refrigerants.

Acetylene removal in ethylene and hydrogen separation and recovery process

A selected paraffinic or olefinic liquid is used to scrub acetylene from a minor gas fraction of uncondensed gas from a hydrocarbon feed mixture containing ethylene, hydrogen, acetylene and methane. Hydrogen product gas is separated and recovered from said minor gas fraction. The major gas fraction is processed without said acetylene removal operation, but under elevated pressure conditions effectively avoiding acetylene solidification during the separation and recovery of an ethylene-enriched liquid.

Recovery of C3+ hydrocarbons

In the recovery of C 3+ hydrocarbons from a feed stream containing hydrogen and C 1 to at least C 5 hydrocarbons, e.g., a refinery waste gas, comprising cooling and partially condensing the feed stream; separating the partially condensed feed stream into a liquid fraction and a gaseous fraction; expanding the gaseous fraction, and fractionating the liquid fraction in a rectification column to obtain product stream consisting essentially of C 3+ hydrocarbons and a residual gas stream product containing predominantly C 2- hydrocarbons, one improvement comprises passing (a) the gaseous fraction prior to expansion; (b) the liquid fraction prior to rectification; and (c) the gaseous fraction after expansion, in indirect heat exchanger relationship with the feed stream to be cooled. Other improvements comprise separate removal of C 1 and C 2 fractions from the hydrogen gas; the use of a C 5+ fraction as a feed to the rectification column and/or as a scrubbing liquid for separating the partially condensed feed stream.

Separation of gaseous mixtures

An incoming stream of gas mixture typically comprising methane and up to 12% by volume of carbon dioxide is subjected to rectification in a first column to form a carbon dioxide depleted fraction that is withdrawn as product from the top of the column and a carbon dioxide-enriched fraction which is withdrawn from the bottom of the column is warmed in a heat exchanger and is introduced into a second rectification column operating at a higher pressure than the first column. A stream in which carbon dioxide predominates is withdrawn from the bottom of the higher pressure column while a stream 34 containing a lower proportion of carbon dioxide than said enriched fraction is withdrawn from the top of the higher pressure column is throttled through a valve and is united with the incoming stream of gas mixture upstream of or in the lower pressure column.

Nitrogen refrigerated process for the recovery of C2+ Hydrocarbons

C 2 and C 3 hydrocarbons, particularly ethylene and propylene, are recovered from refinery or petrochemical plant gas mixtures by cooling and fractionating a feed gas mixture containing these hydrocarbons and lighter components. Refrigeration for the process is provided by a closed-loop gas expander refrigeration process cycle which preferably uses nitrogen as the recirculating refrigerant. Cooling and fractionation may be effected in a dephlegmator.

Dephlegmator system and process

Dephlegmator system without headers, collectors, or distributors at the bottom end of feed circuits in plate and fin exchangers operating in condensing or rectifying service. Each dephlegmator is installed within a pressure vessel, thereby eliminating the need for headers, collectors, or distributors at the bottom end of the feed circuits. In an alternative embodiment of the invention, upper and lower segments of the pressure vessel are isolated by a mid-vessel seal between the vessel and dephlegmator walls, and headers or collectors are not required at the upper and lower ends of the feed circuits.

Olefin plant refrigeration system

The refrigeration system for an ethylene plant comprises a closed loop tertiary refrigerant system containing methane, ethylene and propylene. The tertiary refrigerant from a compressor final discharge is separated into a methane-rich vapor fraction and two levels of propylene-rich liquids so as to provide various temperatures and levels of refrigeration in various heat exchange stages while maintaining a nearly constant refrigerant composition flowing back to the compressor and with the bulk of the total return refrigerant flow going to the first stage compressor section. This tertiary system can also be applied to an ethylene plant with a high pressure demethanizer.

Process for separating hydrogen and methane from an ethylene rich stream

A process for separating hydrogen and methane from a gas mixture containing hydrocarbons heavier than methane in which the gas mixture is passed through a plurality of chilling stages, a bottoms portion from at least one of the chilling stages being passed to a hydrogen stripper before being introduced to a fractionating column, the hydrogen stripper overheads portion being passed back into the chilling train from which a final hydrogen rich stream containing in excess of ninety mole percent hydrogen is separated at a temperature lower than -140° C.

Olefin plant refrigeration system

The refrigeration system for an ethylene plant comprises a closed loop tertiary refrigerant system containing methane, ethylene and propylene. The tertiary refrigerant from a compressor final discharge is separated into a methane-rich vapor fraction and two levels of propylene-rich liquids so as to provide various temperatures and levels of refrigeration in various heat exchange stages while maintaining a nearly constant refrigerant composition flowing back to the compressor and with the bulk of the total return refrigerant flow going to the first stage compressor section. This tertiary system can also be applied to an ethylene plant with a high pressure demethanizer.

Process for the recovery of C2+ hydrocarbons

Distillation of methane and hydrogen from ethylene

An ethylene-containing stream from an ethylene manufacturing plant is sent through a demethanization distillation column which is supplied at an upper plate level, below the top plate, with a condensate stream refrigerated to about - 150*. The condensate so added can be an intermediate reflux stream or a hydrocarbon recycle stream boiling above ethylene, e.g. propane-propylene, as obtained from another separation column in the ethylene recovery system. The added condensate has the effect of reducing both the overhead ethylene loss as well as the amount of overhead reflux required. The overhead reflux can then be generated entirely from the refrigeration gained by expansion of the methane-hydrogen tail gas. Extremely low temperatures are thus generated in the last tail gas separator drum, and because of the very low equilibrium vapor pressure of ethylene at such temperatures, the amount of ethylene lost to the tail gas stream is still further reduced.

Recovery and purification of ethylene

A process for the recovery and purification of ethylene and optionally propylene from a stream containing lighter and heavier components that employs an ethylene distributor column and a partially thermally coupled distributed distillation system.

METHOD FOR SEPARATING C (DOWN ARROW) 5 (DOWN ARROW) (DOWN ARROW) + (DOWN ARROW) HYDROCARBONS FROM A GAS FLOW

Nitrogen refrigerated process for the recovery of C2+ hydrocarbons

C 2 and C 3 hydrocarbons, particularly ethylene and propylene, are recovered from refinery or petrochemical plant gas mixtures by cooling and fractionating a feed gas mixture containing these hydrocarbons and lighter components. Refrigeration for the process is provided by a closed-loop gas expander (147) refrigeration process cycle which preferably uses nitrogen as the recirculating refrigerant. Cooling and fractionation may be effected in a dephlegmator (121).

Fractional condensation of an NG feed with two independent refrigeration cycles

A process for the liquefaction of natural gas which employs a multi-component refrigerant system and a second independent refrigeration system. The process differs from the prior art processes in that the feed gas is cooled only by the independent refrigeration system until it has been freed of those components which could precipitate as solids at the low temperatures of the liquefaction process and thereafter is cooled by the multi-component refrigeration system. The multi-component refrigerant system is a self-contained cycle and does not reject heat to the independent refrigeration system, but directly to the ambient temperature surroundings.

Double mixed refrigerant liquefaction process for natural gas

A process and system are set forth for precooling, liquefying and subcooling a methane-rich feed stream, such as natural gas, with two closed circuit multicomponent refrigerant cycles in which the first refrigerant comprises a binary mixture of propane and butane in a flash refrigeration cycle and the second refrigerant comprises a mixture of nitrogen, methane, ethane, propane and butane in a subcool refrigeration cycle. The first refrigerant preferably cools the feed stream in a plate and fin heat exchanger.

Process for liquefying a gas, notably a natural gas or air, comprising a medium pressure drain and application

Gas separation

By incorporating a gas permeable membrane into a hydrogen purification process at the front end of the cryogenic unit, the low purity hydrogen can be made into a high purity stream and a low purity stream. The critical pressure of the low purity stream is such that the low purity stream can be purified cryogenically without depressurization.

Industrial process for the separation and recovery of chlorine

A gaseous mixture containing chlorine, carbon dioxide and non-condensable gas is compressed and cooled to separate it into a residual gas formed principally of a major portion of the non-condensable gas and a condensate formed primarily of chlorine. The condensate is fed to a stripping column to desorb carbon dioxide and a minor portion of the non-condensable gas dissolved in the condensate. The stripped gas formed primarily of chlorine and carbon dioxide may be treated further. Namely, the stripped gas is mixed with the residual gas. At least a portion of the mixed gas is fed into an absorption column, whereby a major portion of remaining chlorine is absorbed to lower the chlorine content. Removal of chlorine from such a gaseous mixture or an off-gas from the above process can be achieved by washing it with an aqueous solution or suspension containing an alkali metal sulfite and/or an alkaline earth metal sulfite while controlling the pH of the solution or suspension within a range of 1.9-6.3.

Membrane separation process for cracked gases

A process for recovering hydrogen from a cracking effluent wherein a cracking effluent is compressed, and then at least a portion of the hydrogen is separated from the cracking effluent prior to cooling of the cracking effluent to remove lower-boiling components. The separation of hydrogen is preferably accomplished by passing the cracking effluent through at least one semi-permeable membrane.

Membrane-augmented cryogenic methane/nitrogen separation

A membrane separation process combined with a cryogenic separation process for treating a gas stream containing methane, nitrogen and at least one other component. The membrane separation process works by preferentially permeating methane and the other component and rejecting nitrogen. The process is particularly useful in removing components such as water, carbon dioxide or C3+ hydrocarbons that might otherwise freeze and plug the cryogenic equipment.

Gas separation

Olefin plant refrigeration system

The refrigeration system for an ethylene plant comprises a closed loop tertiary refrigerant system containing methane, ethylene and propylene. The tertiary refrigerant from a compressor final discharge is separated into a methane-rich vapor fraction and two levels of propylene-rich liquids so as to provide various temperatures and levels of refrigeration in various heat exchange stages while maintaining a nearly constant refrigerant composition flowing back to the compressor and with the bulk of the total return refrigerant flow going to the first stage compressor section. This tertiary system can also be applied to an ethylene plant with a high pressure demethanizer.

Olefin plant refrigeration system

The refrigeration system for an ethylene plant comprises a closed loop tertiary refrigerant system containing methane, ethylene and propylene. The tertiary refrigerant from a compressor final discharge is separated into a methane-rich vapor fraction and two levels of propylene-rich liquids so as to provide various temperatures and levels of refrigeration in various heat exchange stages while maintaining a nearly constant refrigerant composition flowing back to the compressor and with the bulk of the total return refrigerant flow going to the first stage compressor section. This tertiary system can also be applied to an ethylene plant with a high pressure demethanizer.

Olefin plant refrigeration system

Processing of hydrocarbon gases

Distillation of low-boiling components

Employing bottoms of a second fractionator as a refrigerant medium for first fractionator overhead

Cryogenic recovery of high purity hydrogen

A process for the cryogenic purification of industrial by-product hydrogen streams to recover a high yield of a high purity hydrogen product is disclosed in which two or more of such by-product streams, one containing detrimental amounts of non-readily condensible impurities having boiling points below that of methane, e.g., nitrogen, helium and the like, the other containing by-product hydrogen gas streams which are substantially free of non-readily condensible impurities. These two feed streams are then separately passed through successive cooling and separation stages. At each separation stage, a liquid bottom fraction containing readily condensible hydrocarbons is separated from the overhead of each of the two feed streams. Successive separations are carried out until the overhead from the stream which is substantially free of non-readily condensible impurities (but which contains a significant amount of readily condensible impurities, including methane) attains the desired degree of purity. At this point, the bottom fraction of this stream is predominantly liquid methane, and this bottom fraction is used to scrub a preponderance of nitrogen and like impurities from the overheads of the stream containing significant amounts of these non-readily condensible impurities.

Hydrocarbon gas processing

A process for the recovery of ethane, ethylene, propane, propylene and heavier hydrocarbon components from a hydrocarbon gas stream is disclosed. The stream is divided into first and second streams. The first stream is cooled to condense substantially all of it and is thereafter expanded to the fractionation tower pressure and supplied to the fractionation tower at a first mid-column feed position. The second stream is expanded to the tower pressure and is then supplied to the column at a second mid-column feed position. A recycle stream is withdrawn from the tower overhead after it has been warmed and compressed. The compressed recycle stream is cooled sufficiently to substantially condense it, and is then expanded to the pressure of the distillation column and supplied to the column at a top column feed position. The pressure of the compressed recycle stream and the quantities and temperatures of the feeds to the column are effective to maintain the column overhead temperature at a temperature whereby the major portion of the desired components is recovered.

Adsorption condensation solvent recovery system

A volatile component is recovered from an inert gas blanketed gas source containing the volatile component, an inert carrier gas, water vapor and oxygen as an impurity by a continuous process including the steps of adsorbing the water vapor from the stream, condensing substantially all of the volatile component from the stream, heating the water vapor-free and volatile component-free gas stream, purging the adsorbers with the heated gas stream and venting the purge gas and desorbed moisture. Inert gas depleted from the source is replenished with oxygen-free inert gas, thereby minimizing the concentration of oxygen in the source.

Gas separation process

Hydrogen and carbon monoxide are each separately recovered in high yield from a multicomponent gas stream containing these compounds to­gether with carbon dioxide and a zero to minor amount of one or more gaseous components from the group consisting of nitrogen, methane, water vapor and C₁-C₆ hydrocarbons, by a process wherein the multicomponent gas stream, such as that obtained by steam methane reforming, is initial­ly treated in a pressure swing adsorption unit to remove water and CO₂, and the obtained effluent freed of CO₂ and water is then further sub­jected to (1) cryogenic fractionation to condense CO and to (2) hydrogen purification by selective adsorption (in either order) to recover high purity carbon monoxide and essentially pure hydrogen. The CO₂-laden adsorbent is regenerated by purging with a H₂O and CO₂-free waste gas stream from the hydrogen purification adsorbent bed or from the cryogenic fractionation or from both of these.

Temperature swing adsorption process for purification of oxygen by cryogenic adsorption

Separation of hydrogen-hydrocarbon gas mixtures using closed-loop gas expander refrigeration

A method for the recovery of hydrogen and one or more hydrocarbons having one or more carbon atoms from a feed gas (101) containing hydrogen and the one or more hydrocarbons, which process comprises cooling and partially condensing (103) the feed gas (101) to provide a partially condensed feed (105); separating (107) the partially condensed feed to provide a first liquid stream (109) enriched in the one or more hydrocarbons and a first vapor stream (111) enriched in hydrogen; further cooling and partially condensing (123) the first vapor stream to provide an intermediate two-phase stream (125); and separating (127) the intermediate two-phase stream to yield a further-enriched hydrogen stream (129) and a hydrogen-depleted residual hydrocarbon stream (131). Some or all of the cooling is provided by indirect heat exchange (103,123) with cold gas refrigerant generated in a closed-loop gas expander refrigeration cycle (143,150,153,139,141).

Process and apparatus for the purification of hydrogen by cryogenic treatment of a gas containing the same

Process and apparatus for the purification of hydrogen by cryogenic treatment of a gas containing also nitrogen oxides and unsaturated hydrocarbons as two types of constituents which react together in an undesirable fashion when cooling achieves an intermediate temperature higher than the low temperature of the treatment. The process comprises cooling the gas to a first temperature higher than that intermediate temperature; eliminating from the gas one of the two types of constituents at this first temperature; and continuing the cooling of the gas to the low temperature. The elimination of one type of component is effected by washing the gas with a liquid adapted to dissolve it. This liquid contains at least one saturated hydrocarbon and is obtained by a partial condensation of an auxiliary gas which contains at least one of hydrogen and a heavy constituent whose value can be increased. The gas treated can be a residual gas from catalytic cracking in a fluidized bed (FCC), and the auxiliary gas can be a hydrotreatment purge gas.

Absorption and cold separation process for recovering purified hydrogen from a catalytic dehydrogenation zone effluent

Purified hydrogen is recovered from the effluent of a catalytic dehydrogenation zone using an integrated cold absorption process. The effluent, which contains olefinic hydrocarbons and hydrogen is compressed, cooled and contacted with a liquid absorbent. The purified hydrogen can be recycled to the dehydrogenation zone and the olefinic hydrocarbons are recovered as product. The present invention will recover higher purity hydrogen and liquefiable hydrocarbons more economically than prior art processes.

Liquefaction process

A process for producing a liquefied natural product such as LNG is described where a single phase nitrogen refrigerant is used in such a way that the refrigerant stream (10) is divided into at least two separate portions (12, 14) which are passed through separate turbo-expanders (106, 108) before being admitted to separate heat exchangers (103, 104) so that the warming curve of the refrigerant more closely matches the cooling curve of the product being liquefied so as to minimise thermodynamic inefficiencies and hence power requirements involved in operation of the method.

Liquefaction process

A natural gas liquefaction process comprises passing natural gas through a series of heat exchangers (150, 151, 153) in countercurrent relationship with a gaseous refrigerant circulated through work expansion cycle. The work expansion cycle comprises compressing the refrigerant, dividing and cooling the refrigerant to produce at least first and second cooled refrigerant streams (126, 128), substantially isentropically expanding the first refrigerant stream (126) to a coolest refrigerant temperature, substantially isentropically expanding the second refrigerant stream (128) to an intermediate refrigerant temperature warmer than said coolest refrigerant temperature, and delivering the refrigerant in the first and second refrigerant streams (126, 128) to a respective heat exchanger (153, 151) for cooling the natural gas through corresponding temperature ranges. The refrigerant in the first stream (126) is isentropically expanded to a pressure at least 10 times greater than the total pressure drop of the first refrigerant stream across said series of heat exchangers (150, 151, 153), said pressure being in the range of 1.2 to 2.5 MPa.

Process for cryogenic purification of hydrogen

A process for separating condensable contaminants such as methane from a crude hydrogen stream utilizing a series of multipass heat exchangers through which the gas flows for stepwise cooling, with interstage separation of condensates which are expanded and passed in a reverse flow path for autogenous refrigeration. Supplemental refrigeration is provided for the last cooling stage to maintain the plant in proper heat balance for variations in feed gas composition and to facilitate startup.

METHOD FOR DETERMINING C (DOWN ARROW) 3 (DOWN ARROW) (DOWN ARROW) + (DOWN ARROW) HYDROCARBONS

HYDROGEN LIQUEFACTION PROCESS AND PLANT

Downflow plate and fin heat exchanger for cryogenic rectification

A downflow heat exchanger, particularly applicable as the main condenser/reboiler of a double column cryogenic air separation plant, wherein liquid distribution for uniform flow is carried out above the vapor passages and the well distributed liquid is passed into the liquid passages, preferably angularly onto the bridge fins, and then down through the liquid passages cocurrently with vapor in adjacent vapor passages.

PROCESS AND PLANT FOR THE PRODUCTION OF CARBON MONOXIDE AND HYDROGEN

Separation of hydrogen-hydrocarbon gas mixtures using closed-loop gas expander refrigeration

A method for the recovery of hydrogen and one or more hydrocarbons having one or more carbon atoms from a feed gas containing hydrogen and the one or more hydrocarbons, which process comprises cooling and partially condensing the feed gas to provide a partially condensed feed; separating the partially condensed feed to provide a first liquid stream enriched in the one or more hydrocarbons and a first vapor stream enriched in hydrogen; further cooling and partially condensing the first vapor stream to provide an intermediate two-phase stream; and separating the intermediate two-phase stream to yield a further-enriched hydrogen stream and a hydrogen-depleted residual hydrocarbon stream. Some or all of the cooling is provided by indirect heat exchange with cold gas refrigerant generated in a closed-loop gas expander refrigeration cycle.

Nitrogen rejection from condensed natural gas

Method for the rejection of nitrogen from condensed natural gas which comprises (a) introducing the condensed natural gas into a distillation column at a first location therein, withdrawing a nitrogen-enriched overhead vapor stream from the distillation column, and withdrawing a purified liquefied natural gas stream from the bottom of the column; (b) introducing a cold reflux stream into the distillation column at a second location above the first locatino, wherein the refrigeration to provide the cold reflux stream is obtained by compressing and work expanding a refrigerant stream comprising nitrogen; and (c) either (1) cooling the purified liquefied natural gas stream or cooling the condensed natural gas stream or (2) cooling both the purified liquefied natural gas stream and the condensed natural gas stream, wherein refrigeration for (1) or (2) is obtained by compressing and work expanding the refrigerant stream comprising nitrogen. The refrigerant stream may comprise all or a portion of the nitrogen-rich vapor stream from the distillation column.

Cryogenic H2 and carbon monoxide production with an impure carbon monoxide expander

A process for obtaining purified carbon monoxide from a gaseous mixture of hydrogen and carbon monoxide and one or more additional impurities to be removed by one or more vapor-liquid separation devices is provided which includes the steps of providing a feed stream of the gaseous mixture, cooling and partially condensing the feed stream to partially separate the feed stream into at least one hydrogen rich vapor substream and at least one carbon monoxide rich liquid substream, withdrawing a first and a second substream from one of the carbon monoxide rich substreams, passing the first substream through a first expansion valve to let down the pressure to a pressure nominally the same as that of a vapor-liquid separation device downstream, vaporizing the second substream using a heat exchange device to produce a third substream at a pressure substantially above that of the vapor-liquid separation device, passing the third substream through a work extraction device to provide a substantial portion of all refrigeration for cooling for the process, feeding the third substream to the vapor-liquid separation device, and withdrawing substantially purified carbon monoxide from the vapor-liquid separation device. A similar apparatus is also disclosed.

Recovery of olefin hydrocarbons

A distillative method of separating a methane overhead product from a mixture thereof with an acid gas, and the products thus obtained

Improved cryogenic production of ammonia synthesis gas

Process for treating industrial gas stream

Recovery and purification of ethylene

A process for the recovery and purification of ethylene and optionally propylene from a stream containing lighter and heavier components that employs an ethylene distributor column and a partially thermally coupled distributed distillation system.

Process for recovery, purification, and recycle of argon

A method and system for the purification and recycle of impure argon is disclosed. The system and process of the present invention can produce very high purity argon, i.e., about 1 ppb or less of impurities. In one embodiment of the invention, a cryogenic separation apparatus is used to remove the nitrogen, hydrocarbon, and hydrogen impurities from the argon stream. A catalyst bed is then operated at ambient temperature to remove hydrogen, oxygen, and carbon monoxide impurities to provide the purified argon product. Also disclosed is a method to minimize to loss of the purified argon product during regeneration of the catalyst bed.

질소 생성방법 및 장치

본 발명은 단일 칼럼 질소 발생기중에서 공기의 분리로부터 질소를 발생시키기 위한 방법 및 장치에 관한 것이다. 질소가 풍부한 수증기는 칼럼기부로서 생성된 산소가 풍부한 액체 스트림의 증발을 통하여 응축되어 역류를 형성한다. 증발된 산소가 풍부한 스트림은 재순환 압축기중에서 일부가 재압축되고, 냉각되고 칼럼으로 재도입되어 질소 생성물을 증가시킨다. 증발된 산소가 풍부한 스트림은 또한 작동의 수행으로 일부가 팽창된다. 팽창의 작동은 압축에 적용된다. 질소 액화 유니트에 의해 생성된 보충 냉각 스트림은 질소를 액체로서 얻고 압축에 적용될 수 있는 팽창의 작동량을 증가시킨다.

Process for the separation of 1,1,1,2-tetrafluoroethane

본 발명은 HFA 134a와 HF 및/또는 CFC 1122로 이루어진 혼합물을 증류탑에 공급하여 순수 HFA 134a로 이루어진 잔사로부터 HFA 134a와 HF 및/또는 CFC 1122 의 공비물 또는 공비물에 가까운 혼합물을 분리해 내는 것으로 이루어지는, HFA 134a와 HF 및/또는 CFC 1122 로 이루어진 HFA 134a가 많은 혼합물로부터 HFA 134a를 분리하는 방법에 관한 것이다. HFA 134a를 생산하는데 대표적인 스트림과 같은 HFA 134a의 HF가 많은 혼합물을 출발 물질로 하는 본 방법은 초기 혼합물로부터 HF를 분리하여 HFA 134a가 많은 혼합물인 HFA 134a와 HF의 공비물 또는 공비혼합물을 가까운 혼합물을 만들어내는 제1증류단계를 포함한다. The present invention provides a mixture of HFA 134a and HF and / or CFC 1122 to a distillation column to separate a mixture of HFA 134a and HF and / or CFC 1122 or a mixture close to azeotrope from a residue consisting of pure HFA 134a. And HFA 134a consisting of HFA 134a and HF and / or CFC 1122. This method, starting with a HF-rich mixture of HFA 134a, such as a representative stream for producing HFA 134a, is isolated from HF 134a-rich mixtures of HFA 134a and HFA 134a and HF azeotrope or azeotrope. It includes a first distillation step to produce a.

氮的产生方法和设备

一种在单塔氮发生器中通过分离空气而产生氮的方法和装置。通过作为塔底产物的富氧液流的气化而使富氮气体冷凝形成回流。气化的富氧流在循环压缩机中被部分地重新压缩、冷却并再引回至蒸馏塔，以提高氮的产率。气化的富氧流也部分地膨胀并作功。膨胀功被用于进行压缩。用一个氮液化单元产生的补充致冷剂流可使氮以液体形式回收，并增加可用于压缩的膨胀功的数量。

Nitrogen rejection from condensed natural gas

농축 천연가스로부터 질소를 제거하기 위한 방법으로, 상기 방법은 (a) 농축 천연가스를 증류 칼럼 내부의 제1 위치로 주입하고, 질소-농후 오버헤드 증기 스트림을 증류 칼럼으로부터 인출하며, 정제된 액화 천연가스 스트림을 상기 칼럼의 바닥으로부터 인출하는 단계와; (b) 찬 환류 스트림을 증류 칼럼 내부의 상기 제1 위치보다 위에 있는 제2 위치로 주입시키는 단계로, 찬 환류 스트림을 공급하기 위한 냉동은 질소를 함유하는 냉매 스트림을 압축 및 일팽창시킴으로써 얻어지게 하는, 찬 환류 스트림의 주입 단계와; (c) (1) 정제된 액화 천연가스 스트림을 냉각하거나 농축 천연가스 스트림을 냉각하는 단계와, (2) 정제된 액화 천연가스 스트림과 농축 천연가스 스트림 양자를 냉각하는 단계 중 하나 이상의 단계로, (1) 단계 혹은 (2) 단계를 위한 냉동은 질소를 함유하는 냉매 스트림을 압축 및 일팽창시킴으로써 얻어지게 하는, 상기 냉각 단계를 포함한다. 냉매 스트림은 증류 칼럼으로부터 나온 질소-농후 증기 스트림의 전부 혹은 일부를 포함할 수 있다. A method for removing nitrogen from concentrated natural gas, the process comprising (a) injecting concentrated natural gas to a first location within a distillation column, withdrawing a nitrogen-rich overhead vapor stream from the distillation column, and purifying the purified liquefaction. Withdrawing a natural gas stream from the bottom of the column; (b) injecting a cold reflux stream to a second location above said first location within the distillation column, wherein refrigeration for supplying the cold reflux stream is achieved by compressing and expanding the refrigerant stream containing nitrogen. Injecting a cold reflux stream; (c) at least one of (1) cooling the purified liquefied natural gas stream or cooling the concentrated natural gas stream, and (2) cooling both the purified liquefied natural gas stream and the concentrated natural gas stream, The refrigeration for step (1) or step (2) includes the cooling step, such that it is obtained by compressing and monoexpanding the refrigerant stream containing nitrogen. The refrigerant stream may comprise all or part of the nitrogen-rich vapor stream from the distillation column.

Способ восстановления и очистки этилена

ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß (19) RU (11) 2005 138 792 (13) A (51) ÌÏÊ C07C 11/00 (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÇÀßÂÊÀ ÍÀ ÈÇÎÁÐÅÒÅÍÈÅ (21), (22) Çà âêà: 2005138792/04, 13.12.2005 (71) Çà âèòåëü(è): ÈÍÍÎÂÈÍ ÞÝñÝé ËËÊ (US) (30) Êîíâåíöèîííûé ïðèîðèòåò: 20.12.2004 US 11/017,159 (43) Äàòà ïóáëèêàöèè çà âêè: 27.06.2007 Áþë. ¹ 18 A 2 0 0 5 1 3 8 7 9 2 R U Ñòðàíèöà: 1 RU A (57) Ôîðìóëà èçîáðåòåíè 1. Ñïîñîá èçâëå÷åíè ýòèëåíà èç ãàçîâîé ñìåñè, ñîäåðæàùåé ýòèëåí, ýòàí, àöåòèëåí, ìåòàí, âîäîðîä, è, âîçìîæíî, êîìïîíåíòû ò æåëåå ýòàíà, êîòîðûé âêëþ÷àåò â ñåá ñëåäóþùèå îïåðàöèè: a) íàïðàâëåíèå ãàçîâîé ñìåñè â ïåðâóþ äèñòèëë öèîííóþ êîëîííó è èçâëå÷åíèå èç íåå ïåðâîãî ïàðîâîãî ïîòîêà âåðõíåãî ïîãîíà, ñîäåðæàùåãî ýòàí, ýòèëåí, àöåòèëåí, âîäîðîä è ìåòàí, è ïåðâîãî êóáîâîãî ïîòîêà, ñîäåðæàùåãî êîìïîíåíòû ò æåëåå ýòàíà; b) óäàëåíèå àöåòèëåíà èç ïåðâîãî ïàðîâîãî ïîòîêà âåðõíåãî ïîãîíà ñ ïîëó÷åíèåì ïåðâîãî ïîòîêà âåðõíåãî ïîãîíà ñ íèçêèì ñîäåðæàíèåì àöåòèëåíà; c) íàïðàâëåíèå ïî ìåíüøåé ìåðå ÷àñòè ïåðâîãî ïîòîêà âåðõíåãî ïîãîíà ñ íèçêèì ñîäåðæàíèåì àöåòèëåíà â äèñòèëë öèîííóþ êîëîííó ðàñïðåäåëåíè ýòèëåíà è èçâëå÷åíèå èç íåå ïàðîâîãî ïîòîêà âåðõíåãî ïîãîíà ðàñïðåäåëèòåë ýòèëåíà, ñîäåðæàùåãî ýòèëåí, ìåòàí è âîäîðîä, è ãëàâíûì îáðàçîì íå ñîäåðæàùåãî ýòàí, è êóáîâîãî ïîòîêà ðàñïðåäåëèòåë ýòèëåíà, ñîäåðæàùåãî ýòèëåí è ýòàí; d) ðàçäåëåíèå ïàðîâîãî ïîòîêà âåðõíåãî ïîãîíà ðàñïðåäåëèòåë ýòèëåíà íà ëåãêèé ïîòîê, îáîãàùåííûé âîäîðîäîì, è íà îäèí èëè íåñêîëüêî ïîòîêîâ, îáåäíåííûõ âîäîðîäîì è ñîäåðæàùèõ ýòèëåí, ïðè÷åì óêàçàííà îïåðàöè ðàçäåëåíè âêëþ÷àåò â ñåá ïî ìåíüøåé ìåðå îäíó îïåðàöèþ îõëàæäåíè ïî ìåíüøåé ìåðå ÷àñòè ïàðîâîãî ïîòîêà âåðõíåãî ïîãîíà ðàñïðåäåëèòåë ýòèëåíà; e) íàïðàâëåíèå ïî ìåíüøåé ìåðå ÷àñòè ïî ìåíüøåé ìåðå îäíîãî èç îäíîãî èëè íåñêîëüêèõ ïîòîêîâ, îáåäíåííûõ âîäîðîäîì, â ìåòàíîîòãîííóþ äèñòèëë öèîííóþ êîëîííó è óäàëåíèå èç íåå ïîòîêà âåðõíåãî ïîãîíà äåìåòàíèçàòîðà, ñîäåðæàùåãî ìåòàí è âîäîðîä, è ãëàâíûì îáðàçîì íå ...

Process and device for liquefaction of natural gas

FIELD: gas liquefaction. SUBSTANCE: process and device are related to liquefaction of natural gas having positive pressure above 56.2 kgf/sq.cm (atm). Natural gas is injected into gas-expansion machine to reduce its pressure and to recover work from expansion of natural gas in process of pressure reduction so that flow going out of gas-expansion machine can be cooled in sequence to lower temperature by its passage through number of cooling stages thanks to indirect heat exchange with at least one cooling agent till gas is completely condensed in substance in last cooling stage. EFFECT: design of more economic and efficient equipment to produce liquefied natural gas. 10 cl, 1 dwg БбУЭУУГС ПЧ ГЭ (19) 13) ВИ "” 2144 649 ' 5 МК’ [ 25 4 4/00 СЛ РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 95107192/06, 28.04.1995 (71) Заявитель: Филлипс Петролеум Компани (Ц$) (24) Дата начала действия патента: 28.04.1995 (72) Изобретатель: Вилльям Р.Лау (ЦЗ) (30) Приоритет: 29.04.1994 Ц$ 08/235,775 (73) Патентообладатель: (46) Дата публикации: 20.01.2000 Филлипс Петролеум Компани (ЦЗ) (56) Ссылки: ЗИ 423990 А, 11.09.74. ЗЦ 1355138 АЗ, 23.11.87. СВ 1515326 А, 21.05.18. 4$ 3828564 А, 13.08.74. ОЕ 2319803 В.2, 07.01.82. (98) Адрес для переписки: 129010, Москва, ул.Б.Спасская, д.25, строение 3, ООО "Городисский и Партнеры", патентному поверенному Томской Е.В. (54) СПОСОБ И УСТРОЙСТВО ДЛЯ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА (57) Реферат: заключается в создании более экономичного Способ и устройство для сжижения и эффективного оборудования для природного газа, имеющего избыточное производства сжиженного природного газа. 2 давление выше чем около 56,2 кгс/см? (атм), с. и 8 з.п.ф-лы, 1 ил. в которых природный газ вводят в детандер, с уе который действует для снижения давления х природного газа и извлечения работы от ‚в ва расширения природного газа в процессе снижения давления таким образом, что полученный вытекающий из ...

Method for liquefaction of hydrocarbon-rich gas stream

FIELD: gas liquefaction. SUBSTANCE: method involves providing of indirect heat-exchanging with coolants into cascade-type cycles using coolant mixtures. Each cascade includes at least three cycles using coolant mixtures of various compositions. First cycle is adapted for precooling, second cycle is used for liquefaction, third cycle is used for sub-cooling of liquefiable gas. EFFECT: reduced power consumption and decreased capital investment. 8 cl, 5 dwg

Nitrogen and methane containing raw materials cryogenic processing method and apparatus

FIELD: cryogenics. SUBSTANCE: apparatus has two separators 2, 11 phases, driving off column 3 and apparatus to remove nitrogen. Separator 2 divides raw material for first vapor and first liquid, then first liquid i divided in driving off column 3 for nitrogen beneficiated and methane beneficiated fractions. Nitrogen beneficiated fraction is fed to be rectified in apparatus to remove nitrogen and methane beneficiated fraction is derived as ready product. After partial condensation firs vapor in separator 11, in which it is divided for second vapor and second liquid. Second vapor is fed for rectification and second liquid - for division in driving off column. EFFECT: method and apparatus are used in cryogenics to separate nitrogen and methane by cryogenic rectification. 8 cl, 1 dwg ОС Ос ПЧ Го РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) (51) МПК ВИ "” 2034 210 ' 13) Сл Е 25 4 3/02 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 4895507/06, 11.06.1991 (30) Приоритет: 12.06.1990 Ш$ 536522 (46) Дата публикации: 30.04.1995 (56) Ссылки: Патент США М 4664686, кл. Е 25. 302, опублик. 1987. (71) Заявитель: Юнион Карбайд Индастриал Гэзиз Текнолоджи Корпорейшн (1$) (72) Изобретатель: Равиндра Фулчандр Пахаде[М], Джеймс Джозеф Мэлони[ЦЗ] (73) Патентообладатель: Юнион Карбайд Индастриал Гэзиз Текнолоджи Корпорейшн (1$) (54) СПОСОБ КРИОГЕННОЙ ОБРАБОТКИ СЫРЬЯ, СОДЕРЖАЩЕГО АЗОТ И МЕТАН, И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ (57) Реферат: Использование: изобретение относится к криогенной технике и используется в основном для разделения азота и метана методом криогенной ректификации. Сущность изобретения: устройство содержит два сепаратора 2 и 11 фаз, отгоночную колонну 3 и устройство для удаления азота. В сепараторе 2 сырье разделяют на первый пар и первую жидкость, разделяют последнюю в отгоночной колонне 3 на обогащенную азотом и обогащенную метаном фракции, причем фракцию обогащенную азотом, подают на ректификацию в устройство для удаления азота ...

Method and device for cooling fluid medium in liquefying natural gas

FIELD: integral cycles with built-in multi-stage cascades. SUBSTANCE: cooling agent in form of mixture escaping from last but one stage of compressor is directed to distillation apparatus; vapor phase from upper portion of distillation apparatus is cooled to temperature considerably lower than ambient temperature, after which it is divided into two phases. Vapor phase thus obtained is fed to suction end of last stage of compressor and liquid phase is used as coolant for hot part of heat exchange loop of plant for cooling fluid medium; it is provided with distillation apparatus, devices for cooling its upper portion, auxiliary heat exchanger and denitration column. EFFECT: simultaneous reduction of specific energy of process and outlays. 17 cl, 6 dwg ДЭГ стс ПЧ ГЭ РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) ВИ” 2121 637‘ 13) СЛ 5 МК | 25 4 4/02, 3/06 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 94046343/06, 05.04.1994 (30) Приоритет: 09.04.1993 ЕК 9304276 (46) Дата публикации: 10.11.1998 (56) Ссылки: ЕР 01177933 А, 1984. 4$ 3747359 А, 1973.ЕР 0500355 А, 1992. 5Ц 1158829 А, 1385. ЗЧ 1160211 А, 1985. (71) Заявитель: Газ Де Франс (ЕК) (72) Изобретатель: Морис Гренье (ЕК) (73) Патентообладатель: Газ Де Франс (ЕК) С1 (54) СПОСОБ И УСТАНОВКА ДЛЯ ОХЛАЖДЕНИЯ ТЕКУЧЕЙ СРЕДЫ, В ЧАСТНОСТИ, ПРИ СЖИЖЕНИИ ПРИРОДНОГО ГАЗА (57) Реферат: Способ и установка относятся к интегральным циклам С встроенным многоступенчатым каскадом. Хладагент в виде смеси, выходящей из предпоследней ступени компрессора цикла, направляют в аппарат дистилляции, парообазную фазу из верхней части которого охлаждают до температуры более низкой, чем температура окружающей среды, а затем разделяют на две фазы. При этом полученную таким образом парообразную фазу подают на всасывающую сторону последней ступени компрессора, а жидкую фазу используют в качестве охлаждающей жидкости для горячей части теплообменного контура установки для охлаждения текучей среды, снабженной ...

Nozzle, inertial separator and method of supersonic separation of component

FIELD: separation of component from flow. SUBSTANCE: proposed inertial separator includes convergent-divergent nozzle for forming emulsion flow at supersonic velocity whose neck has performance diameter D* and performance diameter of inlet is D1 which is located at distance L1 in flow above nozzle neck ; outlet has performance diameter D2 located at distance L2 in flow below nozzle neck at ratio L 2 (D 2 -D*) more than 50 but lesser than 220; separating part is located below nozzle and is provided with at least one outlet for separated component and at least one outlet for remaining gas flow. EFFECT: enhanced efficiency of separation. 12 cl, 1 tbl, 1 ex ссббессс ПЧ сэ диаметр 0»; вход, характеристический РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) ВИ "” 2 229 922 ' (51) МПК? 13) С2 В 010 49/00, 45/12 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 2001121313/15, 29.12.1999 (24) Дата начала действия патента: 29.12.199911.1-12 (30) Приоритет: 31.12.1998 Ш$ 09/223,885 (43) Дата публикации заявки: 27.06.2003 (46) Дата публикации: 10.06.2004 (56) Ссылки: ЕР 0496128 А1, 29.07.1992. $Ц 1745303 АЛ, 07.07.1992. $4 1768242 АЛ, 15.10.1992. $4 776629 А, 07.11.1980. КУ 2057708 СЛ, 10.04.1996. (85) Дата перевода заявки РСТ на национальную фазу: 31.07.2001 (86) Заявка РСТ: ЕР 99/10496 (29.12.1999) (87) Публикация РСТ: М/О 00/40338 (13.07.2000) (98) Адрес для переписки: 103735, Москва, ул. Ильинка, 5/2, ООО "Союзпатент", пат.пов. Л.С.Кишкиной (72) Изобретатель: ТЪЕНК ВИЛЛИНК Корнелис Антони (МЬ), БЕТТИНГ Марко (М), ВАН ХОЛТЕН Теодор (МЕ), ВАН ВЕН Йоханнес Мигюэл Хенри Мария (МЕ) (73) Патентообладатель: ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (№) (74) Патентный поверенный: Кишкина Людмила Сергеевна (54) СОПЛО, ИНЕРЦИОННЫЙ СЕПАРАТОР И СПОСОБ СВЕРХЗВУКОВОГО ОТДЕЛЕНИЯ КОМПОНЕНТА (57) Изобретение предназначено для отделения компонентов из потока. Инерционный сепаратор включает сопло сужающейся-расширяющейся формы для создания эмульсионного потока С ...

Пакетные контактные элементы с упорядоченной структурой и низким сопротивлением из тканых или тканеподобных материалов для применения в массообменных колоннах и способ ректификации с использованием таких элементов

Характеризующиеся низким сопротивлением пакеты контактных элементов для массообменных колонн, диаметр которых соответствует внутреннему диаметру колонны, а высота составляет от 40 до 300 мм, образованы соприкасающимися друг с другом слоями из сохраняющего свою форму и определенным образом структурированного тканого или тканеподобного материала. Контактные элементы отличаются тем, что касающиеся друг друга деформированные слои, которым придается определенная форма, состоит из тканого или тканеподобного материала, предпочтительно из металлической ткани, и они расположены относительно друг друга так, чтобы образовывалось большое число узких сквозных каналов с поперечным сечением, близким по форме к треугольнику, к прямоугольнику или к равностороннему шестиугольнику. Угол наклона образующих каналы складок на отдельных слоях тканого материала в пакете к оси колонны составлял всего лишь от 3 до 14 o . При необходимости для обеспечения механической стабильности пакетов контактных элементов между слоями ткани была пропущена проволока или тонкие прутья в соответствующем направлении или же слои ткани в некоторых точках касания были прочно скреплены между собой. Также осуществляют способ получения чистых веществ из смесей веществ путем ректификации с использованием новых пакетных контактных элементов. 4 с. и 5 з.п.ф-лы, 3 ил. стусегс пы сэ (19) РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ ВИ “” 2 493 445 ^С2 5 МК’ В 04 4 19/32, В ОО 3/40 (21), (22) Заявка: 98102152/12, 29.06.1996 (24) Дата начала действия патента: 29.06.1996 (30) Приоритет: 08.07.1995 ОЕ 19524928.3 13.02.1996 ОЕ 19605286.6 (43) Дата публикации заявки: 10.01.2000 (46) Дата публикации: 27.11.2002 (56) Ссылки: ЗИ 218122 А, 09.08.1968. ЗИ 4230777 А, 01.04.1969. ЕР 0614695 АЛ, 14.09.1994. $Ц 68866 А, 31.07.1947. \!О 9305812, 01.04.1993. $Ц 1286256 АЛ, 30.01.1987. (85) Дата перевода заявки РСТ на национальную фазу: 09.02.1998 (86) Заявка РСТ: ЕР 96/02851 (29.06.1996) (87) Публикация РСТ: М/О 97/02890 (30.01. ...

Method and device for oxygen heavy isotope concentration

FIELD: chemistry. SUBSTANCE: invention relates to method and device for concentration of oxygen heavy isotopes exploiting ozone photochemical decomposition by laser radiation. Proposed method comprises first stage of distillation whereat oxygen and ozone are fed into distillation column filled with diluting gas, stage of oxygen release from distillation column top section, stage of pressure release in distillation column, stage of photodecomposition whereat gas mix consisting of ozone and diluting gas is fed from distillation column bottom section into photochemical reaction chamber, irradiating gas mix by laser radiation, second distillation stage whereat undecomposed ozone and oxygen are forced back into distillation column, stage of oxygen liquefaction using a condenser, stage of extraction of undecomposed ozone from distillation column, third distillation stage whereat oxygen and diluting gas are separated, and release of separated oxygen. Proposed device comprises ozoniser, distillation column, photochemical reaction chamber and ozone decomposer. EFFECT: higher stability and safety, lower costs. 6 cl, 3 dwg, 1 ex РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 446 862 (13) C2 (51) МПК B01D 59/34 (2006.01) C01B 13/10 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2009113340/05, 20.09.2007 (24) Дата начала отсчета срока действия патента: 20.09.2007 (73) Патентообладатель(и): ТАЙЕ НИППОН САНСО КОРПОРЕЙШН (JP) (43) Дата публикации заявки: 20.10.2010 Бюл. № 29 2 4 4 6 8 6 2 (45) Опубликовано: 10.04.2012 Бюл. № 10 (56) Список документов, цитированных в отчете о поиске: RU 2005129723 А, 20.03.2006. JP 2005040668 А, 17.02.2005. JP 2004-261776 А, 24.09.2004. WO 00/27509 А1, 18.05.2000. 2 4 4 6 8 6 2 R U (86) Заявка PCT: JP 2007/068253 (20.09.2007) C 2 C 2 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 09.04.2009 (87) Публикация заявки РСТ: WO 2008/038561 (03.04.2008) Адрес для переписки: 129090, ...

Cryogenic cooling tower

A cryogenic cooling tower in which a process liquid from which heat is to be removed is supplied to the tower interior that has a plurality of plates vertically stacked one above the other, alternating in opposite directions and tilted downwardly at an angle relative to the tower vertical axis. A cryogenic cooling medium is supplied to the tower interior. The process liquid forms a film on the upper surface of the plate and drops from its front end to the next lower plate. While on a plate the process liquid spread into a film provides a greater surface area to react with the cooling medium to effect the heat transfer. The tilt angle of the plates can be adjusted to control the residence time of the process liquid in the tower.

PROCEDURE AND UNIT OF SUPPLY OF A GAS PRESSURE TO A CONSUMER INSTALLATION OF AN AIR CONSTITUENT.

SEGUN ESTE PROCESO: SE DESTILA AIRE EN UN APARATO DE DESTILACION (13) ASOCIADO A UNA LINEA DE INTERCAMBIO TERMICO (11) EN LA QUE SE HACE CIRCULAR UN FLUIDO CALORIGENO A ALTA PRESION, SE ALIMENTA UN ALMACENAMIENTO (23), AL MENOS DE MANERA INTERMITENTE, CON GAS EN FORMA LIQUIDA; Y SE LLEVA A UNA PRESION DE VAPORIZACION DEL GAS E FORMA LIQUIDA, TRASEGADO DEL ALMACENAMIENTO, Y SE VAPORIZA BAJO ESTA PRESION EN LA LINEA DE INTERCAMBIO TERMICO (11). APLICACION EN LA ALIMENTACION DE OXIGENO, DE NITROGENO Y DE ARGON A PRESION DE INSTALACIONES DE PRODUCCION DE ACERO INOXIDABLE TALES COMO LOS HORNOS DE ARCO ELECTRICOS ASOCIADOS A UN PROCESO AOD. ACCORDING TO THIS PROCESS: AIR IS DISTILLED IN A DISTILLATION DEVICE (13) ASSOCIATED WITH A LINE OF THERMAL EXCHANGE (11) IN WHICH A HIGH PRESSURE CALORIGENOUS FLUID IS CIRCULATED, A STORAGE IS SUPPLIED (23) AT LEAST WAY INTERMITTENT, WITH LIQUID GAS; AND IT LEADS TO A VAPORIZATION PRESSURE OF THE GAS IN LIQUID FORM, TRANSFERRED FROM THE STORAGE, AND IT IS VAPORIZED UNDER THIS PRESSURE IN THE LINE OF THERMAL EXCHANGE (11). APPLICATION IN THE SUPPLY OF OXYGEN, NITROGEN AND ARGON UNDER PRESSURE OF STAINLESS STEEL PRODUCTION FACILITIES SUCH AS ELECTRIC ARC FURNACES ASSOCIATED WITH AN AOD PROCESS.

CRIOGENIC SYSTEM TO PRODUCE NITROGEN.

SE PRESENTA UN SISTEMA DE PROCESAMIENTO DE UN EFLUENTE QUE CONTIENE NITROGENO, A PARTIR DE UN PROCEDIMIENTO INDUSTRIAL EN EL QUE EL EFLUENTE ES ENFRIADO Y EL NITROGENO LIQUIDO SE AÑADE DIRECTAMENTE AL EFLUENTE ENFRIADO. EL CONTACTO DIRECTO Y EL INTERCAMBIO DE CALOR PRODUCE NITROGENO GASEOSO Y PRODUCTOS ORGANICOS LIQUIDOS, QUE SE UTILIZAN AMBOS PARA ENFRIAR EL EFLUENTE Y SON, POSTERIORMENTE, RECUPERADOS. A PROCESSING SYSTEM OF AN EFFLUENT CONTAINING NITROGEN IS PRESENTED, FROM AN INDUSTRIAL PROCEDURE IN WHICH THE EFFLUENT IS COOLED AND THE LIQUID NITROGEN IS ADDED DIRECTLY TO THE COOLED EFFLUENT. DIRECT CONTACT AND HEAT EXCHANGE PRODUCES GASEOUS NITROGEN AND LIQUID ORGANIC PRODUCTS, WHICH ARE BOTH USED TO COOL THE EFFLUENT AND ARE, AFTER, RECOVERED.

저온 액화가스의 저장탱크

산소나 질소등 복수액화가스를 저장해서, 그 가스를 의료기관이나 각종 공장등에 공급하기 위한 저온액화가스 저장탱크에 대해, 그 건설용지의 스페이스 절약화를 도모할 수 있고, 각 액화가스의 등온화를 도모하여, 그 수요선으로 확실한 가스공급을 보전한다. 외측탱크(2)내에 상하 복수의 단으로 내측탱크(4)를 단열창(3)을 개재하여 배설하여 용지를 유효하게 이용한다. 또한 상부의 내측 탱크(4a)고비들점인 액화가스(LG 1 )를 열교환부(11)에 의하여 하부의 내측탱크(4b)의 저비등점인 액화가스(LG 2 )의 공급에 의하여 정온화시키는 것과 그 내부압력을 안정시켜, 상부의 내측탱크(4a)에서의 수요선에 대해 가스(G 1 )의 소비량 변동이 따르는 내부압력의 변동을 억제해서, 그 안정공급을 보전가능하게 한다.

联合生产氨合成混合物和一氧化碳的方法和设备

本发明涉及一种生产氨合成混合物和一氧化碳的方法。在氮清洗塔(61)中提纯氢。在中压汽提塔(62)中，然后在低压蒸馏塔(63)中，从在所述氮清洗塔(61)底部收集的第一种液体馏分(51)中低温回收一氧化碳。从洗涤塔(61)的顶部和底部之间的中间位置排出第二种液体馏分(52)。

고순도산소및저순도산소제조방법및장치

본 발명은 저순도 및 고순도 산소를 제조하기 위한 이중 칼럼의 저압 칼럼 또는 측면 칼럼 내에 평행하게 배열되는 두 개의 정류부를 사용하는 저온 정류 시스템에 관한 것이다.

通过第一制冷循环冷却得到的液化天然气流的处理方法和相关装置

本方法中，在所述第一热交换器(19)内，通过与制冷流体(83)热交换来冷却液化天然气流(11)。使制冷流体(83)经受半开式的第二制冷循环(21)，该第二制冷循环独立于所述第一制冷循环(17)。所述方法包括将过冷液化天然气流(59)引入蒸馏塔(49)内的步骤，以及回收所述蒸馏塔(49)顶部的气体流(69)的步骤。所述第二制冷循环(21)包括：由顶部的气体流(69)的一部分形成制冷流体流(73)的步骤；压缩所述制冷流体流(73)到一高压的步骤；然后将被压缩的制冷流体流(75)的一部分(81)膨胀以形成基本液态的过冷流(83)的步骤。所述基本液态的过冷流(83)在所述第一热交换器(19)内被汽化。

Production of ultra-high purity oxygen from cryogenic air separation plants

본 발명은 초고순도 산소 생성물 및 질소 및/또는 시판용 순도의 산소 생성물을 생성하는 저온 공기 분리 방법에 관한 것이다. 특히, 본 발명은 산소-함유 사이드-드 로우 스트림을 배출하기 위한 위치에 인접한 증류 구간으로부터 증류 컬럼 시스템을 하강하는 액체의 일부를 제거하는 것을 특징으로 한다. The present invention relates to a method for separating cryogenic air products and nitrogen-containing and oxygen-product products of commercial purity. In particular, the present invention is characterized by removing a portion of the liquid descending the distillation column system from the distillation section adjacent to the location for discharging the oxygen-containing side-stream.

Способ очистки и разделения криптоно-ксеноновой смеси ректификацией и устройство для его осуществления

Изобретение относится к криогенной технике, в частности к очистке и разделению криптоно-ксеноновой смеси, получаемой на воздухоразделительных установках. Способ предусматривает очистку и разделение смеси ректификацией с охлаждением в кубах ректификационных колонн сжатого хладагента, отбираемого и возвращаемого в холодильный цикл, причем поток смеси, потоки криптоновой и ксеноновой фракций, а также потоки продукционного криптона и ксенона дополнительно очищают от радионуклидов фильтрационным, и/или адсорбционным, и/или ректификационным, и/или абсорбционным, и/или химическим, и/или физико-химическим методами в дополнительных устройствах очистки от радионуклидов с дополнительной сертификацией потоков и баллонов перед и после их заполнения продуктами разделения на содержание и/или активность по радионуклидам. Предложено устройство для реализации описанного способа. Изобретение позволяет дополнительно очистить продукты разделения от радионуклидов для их применения, например, в медицинских целях, а также увеличивает экономичность процессов очистки и разделения. 2 н. и 4 з.п. ф-лы, 2 ил. ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß (19) RU (11) 2 300 717 (13) C1 (51) ÌÏÊ F25J 3/00 (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÎÏÈÑÀÍÈÅ ÈÇÎÁÐÅÒÅÍÈß Ê ÏÀÒÅÍÒÓ (21), (22) Çà âêà: 2005141204/06, 29.12.2005 (72) Àâòîð(û): Ñàâèíîâ Ìèõàèë Þðüåâè÷ (RU) (24) Äàòà íà÷àëà îòñ÷åòà ñðîêà äåéñòâè ïàòåíòà: 29.12.2005 (73) Ïàòåíòîîáëàäàòåëü(è): Ñàâèíîâ Ìèõàèë Þðüåâè÷ (RU) (45) Îïóáëèêîâàíî: 10.06.2007 Áþë. ¹ 16 R U Àäðåñ äë ïåðåïèñêè: 121433, Ìîñêâà, óë. Çâåíèãîðîäñêà , 8, êîðï.2, êâ.45, Ì.Þ.Ñàâèíîâó (54) ÑÏÎÑÎÁ Î×ÈÑÒÊÈ È ÐÀÇÄÅËÅÍÈß ÊÐÈÏÒÎÍÎ-ÊÑÅÍÎÍÎÂÎÉ ÑÌÅÑÈ ÐÅÊÒÈÔÈÊÀÖÈÅÉ 2 3 0 0 7 1 7 R U (57) Ðåôåðàò: Èçîáðåòåíèå îòíîñèòñ ê êðèîãåííîé òåõíèêå, â ÷àñòíîñòè ê î÷èñòêå è ðàçäåëåíèþ êðèïòîíîêñåíîíîâîé ñìåñè, ïîëó÷àåìîé íà âîçäóõîðàçäåëèòåëüíûõ óñòàíîâêàõ. Ñïîñîá ïðåäóñìàòðèâàåò î÷èñòêó è ðàçäåëåíèå ñìåñè ðåêòèôèêàöèåé ñ îõëàæäåíèåì â êóáàõ ðåêòèôèêàöèîííûõ êîëîíí ...

Separation and recapturing method of chlorine

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Method and apparatus for producing a purified liquid

본 발명은 일반적으로 액체를 정제하기 위한 방법 및 장치를 제공한다. 보다 구체적으로, 벌크 액체의 정제는 정제된 증기를 형성하기 위한 증류 챔버 및 정제된 증기로부터 응축된 정제된 액체를 수집하기 위한 고리형 챔버 둘다를 포함하는 정제 용기에 액체 스트림을 도입함으로써 수행된다. 냉매 시스템은 냉매 시스템의 일부에서 발생한 폐기 열을 냉매 시스템의 다른 부분의 가열을 위해 사용함으로써 상기 정제 방법의 열역학적 효율을 제공한다. 본 발명의 방법 및 장치는 정제된 이산화탄소, 질소산화물, 암모니아 및 불소화탄소를 제조하는데 적용될 수 있다. The present invention generally provides methods and apparatus for purifying liquids. More specifically, purification of the bulk liquid is performed by introducing a liquid stream into a purification vessel that includes both a distillation chamber to form purified vapor and a cyclic chamber for collecting condensed purified liquid from the purified vapor. The refrigerant system provides the thermodynamic efficiency of the purification method by using the waste heat generated in part of the refrigerant system for heating other parts of the refrigerant system. The method and apparatus of the present invention can be applied to produce purified carbon dioxide, nitrogen oxides, ammonia and fluorocarbons.

Process for separating isotopes

A process for producing an isotopically enriched compound of a desired isotope includes (a) providing a cryogenic reaction zone containing a catalyst adapted to catalyze an isotope exchange reaction at a cryogenic reaction temperature, (b) feeding to the cryogenic reaction zone an enriched mixture comprising at least a compound containing the desired isotope, wherein the enriched mixture is enriched in the desired isotope above a natural abundance of the desired isotope, (c) reacting the enriched mixture in the cryogenic reaction zone thereby forming a resulting mixture containing the isotopically enriched compound, and (d) separating the resulting mixture into an enriched product which is enriched in the isotopically enriched compound and a depleted product which is depleted in the isotopically enriched compound.

저온 정류를 위한 하류 플레이트 및 핀 열 교환기

본 발명은 하류 열 교환기, 구체적으로는 이중 컬럼 저온성 공기 분리 플랜트의 주 컨덴서/리보일러로서 적용될 수 있는 하류 열 교환기에 관한 것이다. 균등한 흐름을 위한 액체 분배는 증기 통로들 위에서 수행되고 잘 분배된 액체는, 바람직하게 브리지 핀상에서 기울여져서 액체 통로들 안으로 이송된 후, 증기 통로들에 근접된 증기를 이용하여 병류적으로 액체 통로들을 통해 아래로 이송된다.

Liquefaction method

FIELD: gas production method. SUBSTANCE: according to method, liquefaction of natural gas is performed by passing natural gas through series of successively installed heat exchangers in counterflow with respect to gaseous cooling agent circulating in cycle of working expansion. Working expansion cycle includes compression of cooling agent, separation and cooling of agent for creation of at least first and second flows of cooled agent. Then follows is isoentropic expansion of first flow of cooling agent to maximal low temperature, and isoentropic expansion of second flow of cooling agent to intermediate temperature of cooling agent. Performed is delivery of cooling agent in first and second flow into corresponding heat exchanger for cooling of natural gas down to respective ranges of temperature. Cooling agent of first flow is expanded isoentropically to pressure which is at least 10 times higher than total pressure drop of cooling agent in first flow of cooling agent in succession of heat exchangers, and this pressure stays within range of 1.2-2.5 MPa. Application of aforesaid method allows for performing liquefaction of natural gas directly at recovering gas at sea. EFFECT: higher efficiency. 17 cl, 13 dwg рэ гс ПЫ ГЭ (19) РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ ВИ” 2144 611‘ (51) МПК 13) Сл Е 25 4 1/02 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 98108463/06, 04.10.1996 (24) Дата начала действия патента: 04.10.1996 (30) Приоритет: 05.10.1995 СВ 9520356.8 05.10.1995 СВ 9520303.0 05.10.1995 СВ 9520348.5 05.10.1995 СВ 9520349.3 (46) Дата публикации: 20.11.1999 (56) Ссылки: МО 95/27179 АЛ, 02.10.95. ЕР 0293882 А2, 12.07.88. 5Ц 1775582 А, 15.11.92. $9 476766 А, 10.12.75. СВ 1515326 А, 21.05.78. СВ 2145508 А, 27.03.85. ОЕ 2319803 В2, 07.01.82. 4$ 38285564 А, 13.08.14. (85) Дата перевода заявки РСТ на национальную фазу: 05.05.98 (86) Заявка РСТ: СВ 96/02443 (04.10.96) (87) Публикация РСТ: М/О 97/13109 (10.04.97) (98) Адрес для ...

Method and apparatus for removing nitrogen from condensed natural gas

低温生产氦的方法和设备

一种氦低温生产系统，其中内含二氧化碳的原料在包括上游较高温度和较高压力的塔或分馏柱的双温系统中处理，因此，无需一个单独的非低温二氧化碳除去步骤。

고순도 산소 및 저순도 산소 제조 방법 및 장치

본 발명은 저순도 및 고순도 산소를 제조하기 위한 이중 칼럼의 저압 칼럼 또는 측면 칼럼 내에 평행하게 배열되는 두 개의 정류부를 사용하는 저온 정류 시스템에 관한 것이다.

プレートフィン熱交換器内蔵型の多段サーモサイホン

저온 공기분리 플랜트로부터 초고순도 산소를 분리하는 방법

본 발명은 초고순도 산소 생성물 및 질소 및/또는 시판용 순도의 산소 생성물을 생성물을 생성하는 저온 공기 분리 방법에 관한 것이다. 특히, 본 발명은 산소-함유 사이드-드로우 스트림을 배출하기 위한 위치에 인접한 증류구간으로부터 증류 컬럼 시스템을 하강하는 액체의 일부를 제거하는 것을 특징으로 한다.

Structured packing with asymmetric crimp pattern

본 발명은 정류 컬럼에 사용하기 위해 모듈을 성형하기 위한 주름진 구조용 패킹에 관한 것으로서, 주름진 구조용 패킹은 구조용 패킹 시트의 중심선에 대해 수직으로 그어진 라인에 대해 비대칭인 크림프 패턴에서, 주름의 골로부터 이에 인접한 주름의 산로의 중심선을 따르는 축선 거리가 중심선의 양측 면을 균등하게 분할하지 않는 패턴을 가지며, 이로 인해 질량 전달을 촉진하여 비효율적인 압력손실이 감소되며, 이에 따라 필요한 컬럼의 높이가 감소된다. The present invention relates to a corrugated structural packing for molding a module for use in a rectifying column, wherein the corrugated structural packing is adjacent to the valley of the corrugation in a crimp pattern that is asymmetrical with respect to the line drawn perpendicular to the centerline of the structural packing sheet. The axial distance along the centerline of the corrugated ramp has a pattern that does not evenly divide both sides of the centerline, thereby facilitating mass transfer and reducing inefficient pressure loss, thereby reducing the required column height.

Method of liquefaction of natural gas and device for realization of this method

FIELD: method of liquefaction of natural gas. SUBSTANCE: flow of cooling agent is divided into at least two parts which are passed through separate turbo-expanders before they enter separate heat exchangers. Cooling agent heating curve crowds with curve of cooling the product to be liquified. EFFECT: reduced power requirements. 19 cl, 6 dwg 90 гс ПЧ Го (19) РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (51) МПК 13) ВИ "” 2 137 066. Е 25 34102 СЛ 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 96121562/06, 05.04.1995 (24) Дата начала действия патента: 05.04.1995 (30) Приоритет: 05.04.1994 АЦ РМ 4856 (46) Дата публикации: 10.09.1999 (56) Ссылки: СВ 2145508 А, 27.03.85. Ц$ 3874185 А, 01.04.75. 5 476766 А, 10.12.15. $Ч 690255 А, 08.10.79. 54 1576813 АЛ, 07.07.90. ОЕ 2636933 АЛ, 23.02.78. ЕК 1523126 А, 18.05.68. (85) Дата перевода заявки РСТ на национальную фазу: 05.11.96 (86) Заявка РСТ: АЦ 95/00191 (05.04.95) (87) Публикация РСТ: М/О 95/27179 (12.10.95) (98) Адрес для переписки: 105023, Москва, ул.Большая Семеновская, д.49, оф.404, Центр "ИННОТЭК", Патентному поверенному Вахниной Т.А. (71) Заявитель: Би-Эйч-Пи Петролиум ПТИ, Лтд. (АЦ) (72) Изобретатель: Дьюбар Кристофер Альфред (СВ) (73) Патентообладатель: Би-Эйч-Пи-Петролиум ПТИ, Лтд. (АЦ) (54) СПОСОБ СЖИЖЕНИЯ ПРИРОДНОГО ГАЗА И УСТРОЙСТВО ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ (57) Реферат: Поток хладагента разделяют по меньшей мере на две части, которые пропускаются через отдельные турбодетандеры до того, как они поступят в отдельные теплообменники. При этом кривая нагревания хладагента сближается с кривой охлаждения продукта, подвергаемого сжижению. Использование изобретения позволяет снизить энергетические затраты. 2 с. и 16 з.п. ф-лы, 1 табл., б ил. +0.0 Г 200- 66 т -200. Юуиная охлаждения ' СПГ/ззота -400 т Кривая нагревания азотныго хладагента - 80 1 Температура, С - 8.0 100,01 =120.5- ео -160.0 * тт 1 + + -=- 1 ПР ЗО И НИ" 0 250 68.0 7:5 964 1200 1449 1680 15.0 2160 — 140.0 Энтальпийноа иаменение ...

Process and installation for feeding an air separation apparatus

본 발명은 공기 분리 장치(A)에 관한 것으로, 이 장치에 선택적으로 전용인 단열 압축기(1)에서 압축된 유동에 의해 공급된다. 발생한 부가적인 열은 여러 방법으로 이용한다. The present invention relates to an air separation device (A), which is supplied by compressed flow in an adiabatic compressor (1) which is optionally dedicated to this device. The additional heat generated is used in several ways.