| 序号 | 专利名 | 申请号 | 申请日 | 公开（公告）号 | 公开（公告）日 | 发明人 |
|---|---|---|---|---|---|---|
| 1 | 低温分离空气的方法和设备 | CN201110349126.6 | 2011-11-07 | CN102564063A | 2012-07-11 | A·阿列克谢耶夫 |
| 在用于氮-氧分离的蒸馏塔体系中用于低温分离空气(1，5)的方法和设备，该蒸馏塔体系具有高压塔(2)和低压塔(3)，其中将第一流体(16，17；29)以液态从高压塔(2)排出并导入(22，23；30)低压塔(3)中。使用第一液体喷射泵(15；28)以将第一流体从高压塔输送至低压塔中。 | ||||||
| 2 | 液体转移方法和设备 | CN93103344.6 | 1993-03-23 | CN1078946C | 2002-02-06 | B·达列迪奥 |
| 将少量提升气流注入膨胀阀(7、10、13)下游的液体提升管(6、9、11、12)，该办法可应用于空气的填充型双馏塔。 | ||||||
| 3 | 液体转移方法和设备 | CN93103344.6 | 1993-03-23 | CN1076775A | 1993-09-29 | B·达列迪奥 |
| 将少量提升气流注入膨胀阀(7、10、13)下游的液体提升管(6、9、1、12)，该办法可应用于空气的填充型双馏塔。 | ||||||
| 4 | 低温分离空气的方法和设备 | CN201110349126.6 | 2011-11-07 | CN102564063B | 2016-09-07 | A·阿列克谢耶夫 |
| 在用于氮‑氧分离的蒸馏塔体系中用于低温分离空气(1，5)的方法和设备，该蒸馏塔体系具有高压塔(2)和低压塔(3)，其中将第一流体(16，17；29)以液态从高压塔(2)排出并导入(22，23；30)低压塔(3)中。使用第一液体喷射泵(15；28)以将第一流体从高压塔输送至低压塔中。 | ||||||
| 5 | Process and apparatus for the recovery of krypton and/or xenon | US10723226 | 2003-11-26 | US20040112084A1 | 2004-06-17 | Paul Higginbotham; Kelvin Graham Hayes; Declan Patrick O'Connor |
| Krypton and/or xenon is separated crudely from a mixture comprising oxygen and at least one rare gas selected from the group consisting of krypton and xenon in a process comprising feeding said mixture or a mixture derived therefrom to a rare gas recovery system and separating said mixture feed in said rare gas recovery system into rare gas-lean gaseous oxygen (nullGOXnull) and rare gas-enriched product. The process is characterized in that at least about 50 mol % of said mixture is fed to the rare gas recovery system in the gaseous phase provided that, when said mixture feed is separated by selective adsorption, the concentration of xenon in the mixture feed is no greater than 50 times the concentration of xenon in air. One advantage of a preferred embodiment of the present invention is that it can easily be retrofitted to existing pumped LOX cycle ASUs. | ||||||
| 6 | Process and apparatus for the low-temperature fractionation of air | US09570385 | 2000-05-12 | US06308533B1 | 2001-10-30 | Thomas Nohlen |
| The process and the apparatus serve for the low-temperature fractionation of air. Feed air (1) is introduced into a first rectification column (3). A transfer fraction (6, 7) of density &rgr; is withdrawn in the liquid state from a reservoir (24, 16) within the first rectification column (3), expanded (14, 14a, 18) and fed to a further process step (5, 23). The liquid level in the reservoir (24, 16) is in this case at a first level h1 and is at a first pressure p1. The expanded transfer fraction is fed to the further process step (5, 23) at a second, higher level h2 (h2 >h1) and at a second, lower pressure (p2 | ||||||
| 7 | Vaporization-condensation apparatus for air distillation double column, and air distillation equipment including such apparatus | US498444 | 1995-07-05 | USRE36435E | 1999-12-14 | Maurice Grenier; Pierre Petit |
| The air distillation double column (1,2) includes an apparatus for vaporizing oxygen and condensing nitrogen which comprises on one hand a running type main heat exchanger (7) which is partially immersed during stoppage of the equipment and on the other hand an auxiliary heat exchanger (20) which alone is responsible for liquid vaporization when the equipment is restarted. | ||||||
| 8 | Multi-column system and method for producing pressurized liquid product | US902887 | 1997-07-30 | US5799510A | 1998-09-01 | Robert A. Mostello |
| An apparatus and method involving the use of a multi-column system in which higher and lower pressure columns are operatively associated with one another by a condenser-reboiler. A pump is provided for pumping a stream of sump liquid of the lower pressure column to produce a pressurized product. The condenser-reboiler is a falling film type of heat exchanger in which liquid is vaporized to produce boilup in the lower pressure column against vaporizing tower overhead in the higher pressure column to reflux both of the columns. Liquid is recirculated back to the condenser-reboiler by an ejector that uses part of a pumped stream as the motive fluid to draw liquid for recirculation. In such manner, less energy is consumed in the recirculation than had all of the recirculated liquid been pumped. Furthermore, an ejector, unlike a second pump used for recirculation purposes, is a solid state device with no moving parts. | ||||||
| 9 | Double-walled pipe for liquified gas | US59590056 | 1956-07-05 | US2999363A | 1961-09-12 | DER STER JOHANNES VAN |
| 10 | Process for the operation of the vaporizers of air resolution plants | US56871331 | 1931-10-14 | US1970300A | 1934-08-14 | MATHIAS FRANKL |
| 11 | Use of Eductor for Liquid Disposal from Vessel | US15363675 | 2016-11-29 | US20170160010A1 | 2017-06-08 | Daryl A. Kenefake; James T. Wilkins |
| A system for the processing of a hydrocarbon flare gas. An input gas stream contains a gas component and a liquid component. A knock-out drum separates the gas component from the liquid component. An eductor has a motive inlet, a suction inlet, and a discharge outlet. The separated liquid component is introduced into the suction inlet of the eductor. A high-pressure gas stream is introduced into the motive inlet of the eductor. The high-pressure gas stream has a pressure sufficient to draw the separated liquid component from the knock-out drum and through the discharge outlet. | ||||||
| 12 | Process and apparatus for the recovery of krypton and/or xenon | US10723951 | 2003-11-26 | US06829907B2 | 2004-12-14 | Paul Higginbotham; Kelvin Graham Hayes; Declan Patrick O'Connor |
| Krypton and/or xenon is separated crudely from a mixture comprising oxygen and at least one rare gas selected from the group consisting of krypton and xenon in a process comprising feeding said mixture or a mixture derived therefrom to a rare gas recovery system and separating said mixture feed in said rare gas recovery system into rare gas-lean gaseous oxygen (“GOX”) and rare gas-enriched product. The process is characterized in that at least about 50 mol % of said mixture is fed to the rare gas recovery system in the gaseous phase provided that, when said mixture feed is separated by selective adsorption, the concentration of xenon in the mixture feed is no greater than 50 times the concentration of xenon in air. One advantage of a preferred embodiment of the present invention is that it can easily be retrofitted to existing pumped LOX cycle ASUs. | ||||||
| 13 | Heat exchange method and apparatus | US40235 | 1998-03-16 | US5924308A | 1999-07-20 | Thomas Rathbone |
| A heat exchange apparatus, typically for use in association with a double rectification column for the separation of air, has a downflow reboiler with boiling passages. In addition, there is a condenser in a position at a higher elevation than the reboiler. The condenser is fed with liquefied gas to be reboiled from the sump of a lower pressure column forming part of the double rectification column. A first conduit feeds the liquefied gas under gravity to the reboiler. The feeding of the condenser is effected by a vapor lift pump comprising a second conduit and an expansion valve disposed therein. Some of the liquefied gas is vaporized by passage through the expansion valve, and this vapor provides the vapor lifting pumping effect. The vapor is recondensed in the condenser. | ||||||
| 14 | Process and installation for the transfer of liquid | US31490 | 1993-03-15 | US5337569A | 1994-08-16 | Bernard Darredeau |
| Process and installation for transferring a liquid, via a rising conduit (6, 9, 11, 12) provided with an expansion valve (7, 10, 13), from a first distillation column (2), operating at a first pressure, to equipment (3), particularly a second distillation column, operating at a pressure lower than the first pressure. There is injected into the rising conduit, downstream of the expansion valve, a lift gas available at a pressure greater than the pressure created by a column of liquid between the point of injection of the gas and the point of introduction of the liquid into the equipment (3). The lift gas is available at the pressure of the first distillation column (2) and is injected into the liquid in the rising column above the point of withdrawal of this liquid. There is used as lift gas a gas withdrawn from a point in the first column (2) and so chosen as not to modify substantially the composition of the transferred liquid, or a portion of the air feed to the installation can be used for this purpose. | ||||||
| 15 | Vaporization-condensation apparatus for air distillation double column, and air distillation equipment including such apparatus | US558091 | 1990-07-25 | US5071458A | 1991-12-10 | Maurice Grenier; Pierre Petit |
| The air distillation double column (1,2) includes an apparatus for vaporizing oxygen and condensing nitrogen which comprises on one hand a running type main heat exchanger (7) which is partially immersed during stoppage of the equipment and on the other hand an auxiliary heat exchanger (20) which alone is responsible for liquid vaporization when the equipment is restarted. | ||||||
| 16 | Heat control for gas-fractionating column | US80818359 | 1959-04-22 | US3078684A | 1963-02-26 | DER STER JOHANNES VAN; LAURENS KOHLER JACOB WILLEM |
| 17 | Method and apparatus for fraction-ating gaseous mixtures | US42807954 | 1954-05-06 | US2913882A | 1959-11-24 | SCHILLING CLARENCE J |
| 18 | Process and apparatus for the recovery of krypton and/or xenon | EP10174217.9 | 2003-12-10 | EP2253912A2 | 2010-11-24 | Higginbotham, Paul; Hayes, Kelvin Graham; O'Connor, Declan Patrick |
Krypton and/or xenon is separated crudely from an oxygen product 800 comprising oxygen and at least one rare gas selected from the group consisting of krypton and xenon in a dephlegmation process in a rare gas recovery system comprising at least one heat exchanger 80. The process is characterised in that the pressure of the oxygen product 800 is increased before being fed to the rare gas recovery system, and in that at least about 50 mol % of said oxygen product 800 is fed to the rare gas recovery system in the gaseous phase. One advantage of a preferred embodiment of the present invention is that it can easily be retrofitted to existing pumped LOX cycle ASUs.
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| 19 | Process and apparatus for the separation of air by cryogenic distillation | EP03075304.0 | 2003-01-31 | EP1338856A2 | 2003-08-27 | Briglia, Alain; Turney, Michael |
Nitrogen and/or oxygen are produced by cryogenic distillation of air in an air separation unit comprising at least a medium pressure column (24) and a low pressure column (23) in which air (7,9) is sent to at least the medium pressure column, an oxygen enriched liquid (11) and a nitrogen enriched liquid (12) are removed from the medium pressure column, at least part of the nitrogen enriched liquid (12) is expanded to produce a two phase nitrogen enriched fluid (15), at least part of the expanded nitrogen enriched fluid containing at least 3,5 % gas, preferably at least 4 % gas is sent into the low pressure column and oxygen rich fluid (16) and nitrogen rich fluid (20) are removed from the low pressure column. |
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| 20 | Appareil de vaporisation-condensation pour double colonne de distillation d'air | EP90401934.6 | 1990-07-04 | EP0410832B1 | 1992-12-16 | Grenier, Maurice; Petit, Pierre |
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