| 序号 | 专利名 | 申请号 | 申请日 | 公开（公告）号 | 公开（公告）日 | 发明人 |
|---|---|---|---|---|---|---|
| 121 | METHOD AND SYSTEM OF MAINTAINING A LIQUID LEVEL IN A DISTILLATION TOWER | US14516686 | 2014-10-17 | US20150159939A1 | 2015-06-11 | Jaime A. Valencia |
| The present disclosure provides a distillation tower that may include a stripper section constructed and arranged to separate a feed stream at a temperature and pressure at which the feed stream forms no solid; a controlled freeze zone section constructed and arranged to separate the feed stream at a temperature and pressure at which the feed stream forms a solid; a melt tray assembly in the controlled freeze zone section that includes a liquid; an underflow weir in the controlled freeze zone section that alters a flow of the liquid in the melt tray assembly; an overflow weir in the controlled freeze zone section that works with the underflow weir to alter the flow of the liquid in the melt tray assembly and is adjacent to the underflow weir; and a covering element in the controlled freeze zone section that is connected to and extends from the underflow weir. | ||||||
| 122 | Method of treating a hydrocarbon stream comprising methane, and an apparatus therefor | US13807340 | 2011-06-28 | US08931306B2 | 2015-01-13 | Cornelis Buijs; Francois Chantant |
| A wet hydrocarbon stream having at least methane and water, provided at a temperature equal to a first temperature, is cooled thereby lowering the temperature to a second temperature. In a water removal device a wet disposal stream having water is withdrawn from the wet hydrocarbon stream, at the second temperature. An effluent stream having the wet hydrocarbon stream from which the wet disposal stream has been removed, is discharged from the water removal device and passed to a further heat exchanger. A refrigerant stream is also passed to the further heat exchanger, and both the effluent stream and the refrigerant stream are cooled in the further heat exchanger by indirect heat exchanging against an evaporating refrigerant fraction. The effluent stream is heated by indirectly heat exchanging against the wet hydrocarbon stream. The cooling of the wet hydrocarbon stream includes this indirectly heat exchanging. | ||||||
| 123 | PROCESS FOR LIQUEFYING A HYDROCARBON-RICH FRACTION | US14019998 | 2013-09-06 | US20140060111A1 | 2014-03-06 | Heinz Bauer; Martin Gwinner; Ana-Maria Lamuela Calvo; Claudia Gollwitzer |
| Described herein is a process for liquefying a hydrocarbon-rich fraction, in particular natural gas, is described, in which the hydrocarbon-rich fraction that is to be liquefied is cooled in indirect heat exchange against a multistage precooling circuit, the refrigerant of the precooling circuit is at least 95% by volume carbon dioxide, the cooled hydrocarbon-rich fraction is liquefied and subcooled in indirect heat exchange against a mixed cycle, and the mixed refrigerant of the mixed cycle comprises exclusively the component(s) nitrogen, methane and/or ethane. | ||||||
| 124 | METHOD AND APPARATUS FOR SEPARATING AIR BY CRYOGENIC DISTILLATION | US13695162 | 2011-03-25 | US20130247611A1 | 2013-09-26 | Golo Zick |
| A method and apparatus for the cryogenic distillation of air to produce gaseous oxygen with a purity between 75 and 95 mol % and a pressure lower than 5.5 bar abs using a triple column having a high-pressure column, a low-pressure column, and a medium-pressure column, wherein the medium-pressure column is at least partially thermally coupled with the low-pressure column and the high-pressure column is also at least partially thermally coupled with the low-pressure column. | ||||||
| 125 | PROCESS AND APPARATUS FOR THE SEPARATION OF AIR BY CRYOGENIC DISTILLATION | US13778700 | 2013-02-27 | US20130219959A1 | 2013-08-29 | Bao Ha; Jean-Renaud Brugerolle |
| The present invention relates to a process and apparatus for the separation of air by cryogenic distillation. In particular, it relates to a process for separation of air using three cryogenic distillation columns for the production of gaseous oxygen. Certain embodiments of the invention are particularly efficient for the production of gaseous oxygen at pressures between 30 and 45 bars abs, in which the oxygen is produced by removing liquid oxygen from a distillation column, pressurizing the oxygen and vaporizing the pressurized liquid by heat exchange with air. | ||||||
| 126 | COOLING UNIT, AND APPARATUS FOR SEPARATING AIR BY MEANS OF CRYOGENIC DISTILLATION INCLUDING SUCH COOLING UNIT | US13808946 | 2011-07-12 | US20130111950A1 | 2013-05-09 | Patrice Cavagne |
| The invention relates to a cooling unit consisting of an exchange line capable of heating nitrogen originating from the system of columns by exchanging heat with the air to be cooled for the system of columns, and a cooling tower for the heat- and mass-exchange between the water to be cooled sent to the top of the tower and the nitrogen originating from a system of air distillation columns, the lower portion of the tower including an inlet connected to a nitrogen pipe, and the nitrogen pipe being connected to at least one exchanger body of the exchange line, which is capable of heating the nitrogen originating from the system of columns by exchanging heat with the air to be cooled for the system of columns, wherein the tower is arranged above at least one portion of the exchange line. | ||||||
| 127 | AIR SEPARATION METHOD AND APPARATUS | US12855313 | 2010-08-12 | US20120036891A1 | 2012-02-16 | Neil Mark Prosser; Richard John Jibb; James Richard Salge; Lyda Zambrano; Andrew M. Warta |
| An air separation method and apparatus in which a supercritical oxygen product is produced by heating a pumped liquid oxygen stream having a supercritical pressure, through indirect heat exchange with a boosted pressure air stream. The indirect heat exchange is conducted within a heat exchanger and a liquid nitrogen stream is vaporized in the heat exchanger to depress the pressure that would otherwise be required of the boosted pressure air stream to heat the pumped liquid oxygen stream. The pumped liquid oxygen stream constitutes 90 percent of the oxygen-rich liquid removed from an air separation unit in which the air is rectified, the liquid nitrogen constitutes at least 90 percent of the liquid nitrogen that is not used as reflux and a flow-rate ratio between the liquid nitrogen stream and the oxygen-rich liquid is between about 0.3 and 0.90. | ||||||
| 128 | SEPARATION OF CARBON DIOXIDE AND HYDROGEN | US13138574 | 2010-03-05 | US20120000243A1 | 2012-01-05 | Matthew Bough; Jonathan Alec Forsyth; Michael John Godfrey; Badrul Huda |
| A process is described for removing carbon dioxide from a synthesis gas feed stream in a cryogenic separation plant. In an example described the synthesis gas feed stream (3) comprises 40 to 65 mole % hydrogen and is fed to a single stage or a first stage of a series of separation stages (120, 103, 104) at a pressure in the range of 46 to 90 bar absolute. The single stage or a stage of the series is operated at a temperature in the range of −53 to −48° C. and a pressure in the range of 44 to 90 bar absolute. In some examples, the single stage or the combined stages of the series remove 70 to 80% of the total moles of carbon dioxide in the synthesis gas feed stream. Liquefied C02 product stream(s) discharged from the stage (s) (7,10,13) of the cryogenic separation plant may be sequestrated and/or used in a chemical process (71). | ||||||
| 129 | SEPARATION OF CARBON DIOXIDE AND HYDROGEN | US12737608 | 2009-07-24 | US20110203313A1 | 2011-08-25 | Badrul Huda; Jonathan Alec Forsyth; Masahiro Kobayashi; Yasushi Mori |
| A process for separating a synthesis gas stream into a hydrogen (H2) rich vapour stream and a liquid carbon dioxide (CO2) stream in a CO2 condensation plant comprising the steps of: (A) feeding a synthesis gas stream having a pressure in the range of 10 to 120 barg to a compression system of the CO2 condensation plant thereby increasing its pressure to 150 to 400 barg and cooling the resulting high pressure (HP) synthesis gas against an external coolant to remove at least part of the heat of compression; (B) cooling the HP synthesis gas stream to a temperature in the range of −15 to −55° C. by passing the HP synthesis gas stream through a heat exchanger system in heat exchange relationship with a plurality of refrigerant streams that are produced subsequently in the process; (C) passing the cooled HP synthesis gas stream formed in step (B) either directly or indirectly to a gas-liquid separator vessel that is operated at substantially the same pressure as the heat exchanger system and withdrawing a high pressure (HP) hydrogen rich vapour stream from the top of the separator vessel and a high pressure (HP) liquid CO2 stream from the bottom of the separator vessel; and (D) feeding the HP hydrogen rich vapour stream from step (C) to the turboexpansion system wherein the hydrogen rich vapour stream is subjected to isentropic expansion in each of the turboexpanders of the series such that hydrogen rich vapour streams are withdrawn from the turboexpanders of the series at reduced temperature and at successively reduced pressures and wherein isentropic expansion of the hydrogen rich vapour in each of the turboexpanders of the series generates motive power thereby driving a machine that is a component of the CO2 condensation plant and/or driving an alternator of an electric generator. | ||||||
| 130 | NATURAL GAS LIQUEFACTION METHOD WITH HIGH-PRESSURE FRACTIONATION | US12739243 | 2008-10-17 | US20110048067A1 | 2011-03-03 | Béatrice Fischer; Gilles Ferschneider; Anne Claire Lucquin |
| The method provides liquefaction of a natural gas by carrying out the following stages: cooling the natural gas, feeding the cooled natural gas into a fractionating column so as to separate a methane-rich gas phase and a liquid phase rich in compounds heavier than ethane, and liquefying the methane-rich stream so as to obtain the liquid natural gas. According to the invention, the operating conditions in the fractionating column are so selected that said liquid phase comprises a molar proportion of methane ranging between 10% and 150% of the molar proportion of ethane. | ||||||
| 131 | METHOD FOR TREATING A PROCESS GAS FLOW CONTAINING CO2 | US12744098 | 2008-09-05 | US20110000366A1 | 2011-01-06 | Ulrich Koss; Manfred Meyer; Alexander Schriefl |
| From the CO2-containing stream of process gas obtained in a process for the treatment of a CO2-containing stream of process gas, which is obtained in the production of pure synthesis gas from raw gas in the partial oxidation of heavy oils, petroleum coke or wastes, or in the gasification of coal, or when processing natural gas or accompanying natural gas, CO2 is removed physisorptively or chemisorptively, and the solvent loaded with CO2 is expanded to a lower pressure for the desorption of CO2. In order to generate CO2 as pure as possible, the contaminated CO2 is condensed to at least 60 bar[a] or below its critical temperature to at least 70 bar[a], and the impurities contained in the liquid CO2 are removed by stripping with gaseous CO2 guided in counterflow. | ||||||
| 132 | ADSORBENT FOR CARBON MONOXIDE, GAS PURIFICATION METHOD, AND GAS PURIFICATION APPARATUS | US12529764 | 2008-03-04 | US20100115994A1 | 2010-05-13 | Masayoshi Hayashida; Akihiro Nakamura; Tatsuya Hidano; Kazuhiko Fujie; Masato Kawai |
| The adsorbent for carbon monoxide of the present invention is obtained by activating a Cu-ZSM5 type zeolite prepared as a catalyst for removal of NOX through heating at 450 to 600° C. in an inert gas atmosphere containing no moisture. The gas purification method of the present invention includes removing carbon monoxide as a trace amount of impurities contained in a gas by a temperature swing adsorption method, wherein the adsorbent for carbon monoxide according to claim 1 is used, and a regeneration operation of the adsorbent for carbon monoxide is carried out at 200 to 350° C. | ||||||
| 133 | PROCESS FOR REMOVING MERCAPTANS FROM LIQUEFIED NATURAL GAS | US12446583 | 2007-10-23 | US20100115993A1 | 2010-05-13 | Anthonius Maria Demmers; Sander Kaart; Adriaan Johannes Kodde |
| The invention provides a process for producing purified natural gas, the process comprising the steps of: expanding a pressurised natural gas stream comprising at least 4 ppmv of mercaptans and supplying it to a first separation column, in which the natural gas stream is separated into a gaseous overhead stream enriched in methane and a first fraction enriched in mercaptans; withdrawing the gaseous overhead stream enriched in methane from the separation column to obtain the purified natural gas; with drawing the fraction enriched in mercaptans from the separation column; removing mercaptans from the first fraction enriched in mercaptans. | ||||||
| 134 | Separation Method Using A Column With A Corrugated Cross Structure Packing For Separating A Gaseous Mixture | US12523475 | 2008-01-10 | US20100107688A1 | 2010-05-06 | Markus Kohlberger; Francois Leclercq |
| A separation method using a column with cross-corrugated structured packing for separating a gas mixture is presented. | ||||||
| 135 | Cryogenic air separation process with excess turbine refrigeration | US12272193 | 2008-11-17 | US07665329B2 | 2010-02-23 | Peter James Rankin; Neil Mark Prosser |
| A process for carrying out cryogenic air separation wherein liquid oxygen is pressurized and vaporized against condensing feed air to produce oxygen gas product wherein excess plant refrigeration is generated such that the aggregate warm end temperature difference of the process exceeds the minimum internal temperature difference of the primary heat exchanger by at least 2K. | ||||||
| 136 | METHOD AND APPARATUS FOR LIQUEFYING A HYDROCARBON STREAM | US12373107 | 2007-07-09 | US20100000251A1 | 2010-01-07 | Michiel Gijsbert Van Aken; Marcus Johannes Antonius Van Dongen; Peter Marie Paulus; Johan Jan Barend Pek; David Bertil Runbalk |
| The present invention provides a method of liquefying a hydrocarbon stream such as natural gas, the method at least comprising the steps of: (a) providing a hydrocarbon stream (10) at a first location (2), wherein the first location is situated onshore; (b) treating the hydrocarbon stream (10) in the first location (2) thereby obtaining a treated hydrocarbon stream (20); (c) transporting the treated hydrocarbon stream (20) via a pipeline (4) over a distance of at least 2 km to a second location (3), wherein the second location is situated off-shore; (d), liquefying the treated, hydrocarbon stream (20) at the second location (3) thereby obtaining liquefied hydrocarbon product (50) at atmospheric pressure. | ||||||
| 137 | CRYOGENIC AIR SEPARATION PROCESS WITH EXCESS TURBINE REFRIGERATION | US12272193 | 2008-11-17 | US20090071191A1 | 2009-03-19 | Peter James Rankin; Neil Mark Prosser |
| A process for carrying out cryogenic air separation wherein liquid oxygen is pressurized and vaporized against condensing feed air to produce oxygen gas product wherein excess plant refrigeration is generated such that the aggregate warm end temperature difference of the process exceeds the minimum internal temperature difference of the primary heat exchanger by at least 2 K. | ||||||
| 138 | Air separation method and apparatus | US11818636 | 2007-06-15 | US20080307828A1 | 2008-12-18 | Neil Mark Prosser; Richard John Jibb |
| A compressed air stream is cooled to a temperature suitable for its rectification within a lower pressure heat exchanger and a boosted pressure air stream is liquefied or converted to a dense phase fluid within a higher pressure heat exchanger in order to vaporize pumped liquid products. Thermal balancing within the plant is effectuated with the use of waste nitrogen streams that are introduced into the higher and lower pressure heat exchangers. The heat exchangers are configured such that the flow area for the subsidiary waste nitrogen stream within the higher pressure heat exchanger is less than that would otherwise be required so that the subsidiary waste nitrogen streams were subjected to equal pressure drops in the higher and lower pressure heat exchangers. This allows the higher pressure heat exchanger be fabricated with a reduced height and therefore a decrease in fabrication costs. | ||||||
| 139 | Integrated process and air separation process | US10778572 | 2004-02-13 | US07197894B2 | 2007-04-03 | Alain Guillard; Patrick Le Bot; Bernard Saulnier |
| An integrated process and air separation process including the steps of: Work expanding at least one first pressurized gas 39 derived from a first process at a first site 1, using work generated by the expansion of the at least one pressurized gas to drive a first air compressor 5 at the first site and removing compressed air from the first air compressor, sending at least part of the compressed air 19 from the first air compressor to an air separation unit 21, located at a second site 2 remote by at least 1 km from the first site, separating at least part of the compressed air sent from the first site to the second site in the air separation unit and removing at least one fluid 37 enriched in a component of air from the air separation unit and sending at least part of the fluid enriched in a component of air to the first site. | ||||||
| 140 | Strip for packing module, corresponding module and column | US10498614 | 2002-12-06 | US07147215B2 | 2006-12-12 | Jean-Yves Lehman; Etienne Werlen; Gilles Lebain |
| A corrugated strip made of sheet material, which may be used in a packing module. The peaks and the troughs of the strip, when viewed in a side view, define lines which have a general sloping direction relative to the direction the fluid flow. Each strip includes a spanning zone and a transition zone. In the transition zone, each peak/trough line extends inside a specific area centered on a curve which extends tangentially from the peak/trough line of the spanning zone. The structured interface region between the spanning and transition zones helps to reduce head loss across the strip. | ||||||
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