US20130206366A1 - Cooler for Feed Gas Of Low-Temperature Methanol Washing - Google Patents
Cooler for Feed Gas Of Low-Temperature Methanol Washing Download PDFInfo
- Publication number
- US20130206366A1 US20130206366A1 US13/812,673 US201113812673A US2013206366A1 US 20130206366 A1 US20130206366 A1 US 20130206366A1 US 201113812673 A US201113812673 A US 201113812673A US 2013206366 A1 US2013206366 A1 US 2013206366A1
- Authority
- US
- United States
- Prior art keywords
- housing
- transfer medium
- heat transfer
- heat
- heat exchanger
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
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Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F1/00—Tubular elements; Assemblies of tubular elements
- F28F1/10—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
- F28F1/12—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/0066—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
- F28F9/001—Casings in the form of plate-like arrangements; Frames enclosing a heat exchange core
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/202—Alcohols or their derivatives
- B01D2252/2021—Methanol
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
- F28D2021/0022—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for chemical reactors
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- General Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Geometry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The invention relates to a cooler for low-temperature methanol washing gas, which comprises a first heat exchanger and a second heat exchanger. The first heat exchanger includes a first housing, a first board, and a first heat exchange tube. The first housing is provided with a first feed gas inlet, a first feed gas outlet, a first heat transfer medium inlet, and a first heat transfer medium outlet. The second heat exchanger includes a second housing, a second board, and a second heat exchange tube. The second housing is provided with a second feed gas inlet, a second feed gas, a second heat transfer medium inlet, and a second heat transfer medium outlet. The second housing and the second board of the second heat exchanger may be made with a relatively thin plate, thereby enormously reducing the material and manufacturing cost for the invention with meeting the requirements of the production.
Description
- The present application is a PCT application No. PCT/CN2011/001202, filed on Jul. 22, 2011, entering the U.S.A. national stage, which claims the priority to the Chinese patent application No. 201020271669.1 filed on Jul. 23, 2010.
- The present invention relates to cooler, in particular to a cooler for low-temperature methanol washing gas.
- To satisfy the require of the next process, the low-temperature methanol washing gas should be cooled, which is usually achieved by a cooler. The present cooler comprises a heat exchanger, as shown in
FIG. 1 , which includes a housing and a heat exchange tube located inside the housing and supported by a board. During the cooling progress, the feed gas flows through the housing while the heat transfer medium flows through the heat exchange tube. The housing is provided with a feed gas inlet and a feed gas outlet, a heat transfer medium inlet which communicates with one end of the first heat exchange tube, and a heat transfer medium outlet which communicates with the other end of the first heat exchange tube. A plurality of heat transfer medium require correspondingly a plurality of heat transfer medium inlets and heat transfer medium outlets, so as to enable the different heat transfer medium to flow in the corresponding heat exchange tubes. The heat transfer medium currently uses CO2 gas (with a usual operating pressure of 0.19 Mpa), H2S tail gas of concentration tower (with a usual operating pressure of 0.08 Mpa) and synthesis gas (with a usual operating pressure of 5.0 Mpa). The feed gas at 40° C. and 5.5 Mpa will enter the feed gas cooler on the housing side and be cooled to the temperature between −13° C. and −20° C. by the heat exchanger. - Though the heat exchanger can be used for cooling the feed gas in low-temperature methanol washing, the housing and the board of the heat exchanger are required to sustain relatively high pressure as the feed gas is a kind of high pressure medium. That is, it's necessary to shape the housing of the heat exchanger into a high-pressure-resistant container with thick walls and use thick boards as the board of the heat exchanger. Obviously, a cooler in such structure will increase the manufacturing cost of the cooler, and it will lead to high investment cost.
- It is an object of the present invention to provide a cooler for low-temperature methanol washing gas with low cost.
- For achieving the above stated object. A cooler for low-temperature methanol washing gas, comprising: a heat exchanger, which comprises a first heat exchanger, and a second heat exchanger, wherein the first heat exchanger includes a first housing, a first board, and a first heat exchange tube, with a first end and a second end, located inside the first housing and supported by the first board, the first housing is provided with a first feed gas inlet, a first feed gas outlet, a first heat transfer medium inlet which communicates with the first end of the first heat exchange tube, and a first heat transfer medium outlet which communicates with the second end of the first heat exchange tube, the second heat exchanger includes a second housing, a second board, and a second heat exchange tube, with a first end and a second end, located inside the second housing and supported by the second board, the second housing is provided with a second feed gas inlet which communicates with the first end of the second heat exchange tube, a second feed gas outlet which communicates with the second end of the second heat exchange tube, a second heat transfer medium inlet, and a second heat transfer medium outlet.
- Preferably, as the operating pressure of the H2S tail gas of concentration tower is lower than that of the CO2 gas and synthesis gas, the first housing is provided with a plurality of heat transfer medium inlets and a plurality of heat transfer medium outlets, at least one heat transfer medium inlet acting as a CO2 gas inlet, at least one heat transfer medium inlet acting as a synthesis gas inlet. at least one heat transfer medium outlet acting as a corresponding CO2 gas outlet, and at least one heat transfer medium outlet acting as synthesis gas outlet. Therefore, the H2S tail gas of concentration tower flows through the housing side of the second heat exchanger, which makes it probable to produce the second housing and the second board of the second heat exchanger with a relatively thin plate, thus reducing the manufacturing cost.
- Compared with the prior art, in the present invention, two heat exchangers are used for cooling and the second heat exchanger is designed in such a structure that the feed Gas flows through the tube side and the heat transfer medium flows through the housing side. Such improvement in design enables the H2S tail gas of concentration tower with a lower operating pressure to flow through the housing side of the second heat exchanger when the heat exchanger comes into actual use. In such a way, though it's still necessary to shape the first housing into a high-pressure-resistant container with thick walls and use thick boards as the first board, the volume of the first heat exchanger is far smaller than that of the original single heat exchanger and the second housing and the second board of the second heat exchanger may he made with a relatively thin plate, thereby enormously reducing the material and manufacturing cost for the invention. Apart from satisfying the need of production process, the cooler of the present invention has a reasonable and reliable structure also manages to considerably reduce the material and manufacturing cost of the cooler, thus making the product more competitive in the market.
-
FIG. 1 is a view of a cooler in the prior art. -
FIG. 2 is a view of a cooler in accordance with an embodiment of the present invention. - To enable a further understanding of the innovative and technological content of the invention herein, refer to the detailed description of the invention and the accompanying drawings below:
-
FIG. 2 shows a cooler for low-temperature methanol washing gas of a preferred embodiment of the present invention. The cooler comprises afirst heat exchanger 1. asecond heat exchanger 2 and amethanol washing system 3. Both of the heat exchangers are disposed in a general structure. The first heat exchanger1 includes a first housing 11, a first board, and a plurality of firstheat exchange tubes 12, with a first end and a second end, located inside the first housing 11 and supported by the first board. The first housing 11 is provided with a first feed gas inlet g1, a first feed gas outlet g2. In this embodiment, the first housing 11 is also provided with a plurality of first heat transfer medium inlets and a plurality of first heat transfer medium outlets, that is, there are two synthesis gas inlets f1, f2, two synthesis gas outlets e1, e2, two CO2 gas inlets b1, b2 and two CO2 gas outlets a1, a2. The firstheat exchange tubes 12 are divided into two groups, the first ends of the first group of the firstheat exchange tubes 12 are respectively connected to the synthesis gas inlets, and the second ends of the first group of the firstheat exchange tubes 12 are respectively connected to the synthesis gas outlets; while the first ends of the second group of the firstheat exchange tubes 12 are respectively connected to the CO2 gas inlets, and the second ends of the second group of the firstheat exchange tubes 12 are respectively connected to the CO2 gas outlets, to make the CO2 gas flow in the one portion of the heat exchange tubes of thefirst heat exchanger 1. - Similarly, the said
second heat exchanger 2 includes asecond housing 21, a second board, and a plurality of secondheat exchange tubes 22, with a first end and a second end, located inside thesecond housing 21 and supported by the second board. Thesecond housing 21 is provided with second feed gas inlets which communicate with the first ends of the secondheat exchange tube 22, and second feed gas outlets which communicate with the second ends of the secondheat exchange tube 22. In this embodiment, the number of the second feed gas inlets is four, there are d1, d2, d3, d4, as show in theFIG. 2 , correspondingly the number of the second feed gas outlets is also four, there are c1, c2, c3, c4, as show in theFIG. 2 . Thesecond housing 21 is also provided with a second heat transfer medium inlet hi and a second heat transfer medium outlet h2, and the heat transfer medium is EMS tail gas of concentration tower, in other words, the H2S tail gas of concentration tower respectively inputs and outputs from the second heat transfer medium inlet h1 and flow out the second heat transfer medium outlet h2. - The
methanol washing system 3 of the embodiment, which adopts the prior art, has methanol poured into in order to prevent moisture from freezing in the cooling process. - During the cooling process, the feed gas output form the
methanol washing system 3 is divided into two groups, one group comes into thefirst heat exchanger 1, that is, one group of the feed gas flows through the first housing 11 of thefirst exchanger 1, and make heat exchange with the synthesis gas and CO2 gas in the firstheat exchange tubes 12 of thefirst heat exchange 1. While the other group comes into thesecond exchanger 2, the other group of the feed gas flows through thesecond housing 21, and makes heat exchange with the H2S tail gas of concentration tower in the secondheat exchange tubes 22 of thesecond heat exchange 2. After the cooling of thefirst heat exchanger 1 and thesecond heat exchanger 2, the feed gas will be synthesized together, and turn into the next step. Therefore, thesecond housing 21 of thesecond heat exchanger 2 only is required with thin-walled plates whose pressure is designed in 0.3 Mpa, and the second board can only use thin hoard. Comparing with the cooler in prior art, at the same heat-exchange effect, the total cost of the cooler the present invention can be reduced to 30%˜40%, so that the material costs and production costs are significantly reduced.
Claims (2)
1. A cooler for low-temperature methanol washing gas, comprising:
a heat exchanger, which comprises a first heat exchanger, and a second heat exchanger, wherein the first heat exchanger includes a first housing, a first board, and a first heat exchange tube, with a first end and a second end, located inside the first housing and supported by the first board, the first housing is provided with a first feed gas inlet, a first feed gas outlet, a first heat transfer medium inlet which communicates with the first end of the first heat exchange tube, and a first heat transfer medium outlet which communicates with the second end of the first heat exchange tube,
the second heat exchanger includes a second housing, a second board, and a second heat exchange tube, with a first end and a second end, located inside the second housing and supported by the second board, the second housing is provided with a second feed gas inlet which communicates with the first end of the second heat exchange tube, a second feed gas outlet which communicates with the second end of the second heat exchange tube, a second heat transfer medium inlet, and a second heat transfer medium outlet.
2. The cooler claim 1 , wherein the first housing is provided with a plurality of heat transfer medium inlets and a plurality of heat transfer medium outlets, at least one heat transfer medium inlet acting as a CO2 gas inlet, at least one heat transfer medium inlet acting as a synthesis gas inlet, at least one heat transfer medium outlet acting as a corresponding CO2 gas outlet, and at least one heat transfer medium outlet acting as synthesis gas outlet.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN2010202716691U CN201768471U (en) | 2010-07-23 | 2010-07-23 | Low temperature methanol washing raw gas cooler |
CN201020271669.1 | 2010-07-23 | ||
PCT/CN2011/001202 WO2012009965A1 (en) | 2010-07-23 | 2011-07-22 | Cooler for feed gas of low-temperature methanol washing |
Publications (1)
Publication Number | Publication Date |
---|---|
US20130206366A1 true US20130206366A1 (en) | 2013-08-15 |
Family
ID=43748300
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US13/812,673 Abandoned US20130206366A1 (en) | 2010-07-23 | 2011-07-22 | Cooler for Feed Gas Of Low-Temperature Methanol Washing |
Country Status (6)
Country | Link |
---|---|
US (1) | US20130206366A1 (en) |
EP (1) | EP2597411A4 (en) |
JP (1) | JP5480450B2 (en) |
KR (1) | KR20130105311A (en) |
CN (2) | CN201768471U (en) |
WO (1) | WO2012009965A1 (en) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN201768471U (en) * | 2010-07-23 | 2011-03-23 | 镇海石化建安工程有限公司 | Low temperature methanol washing raw gas cooler |
US8882890B2 (en) | 2012-12-27 | 2014-11-11 | Uop Llc | Apparatuses and methods for separating liquefiable hydrocarbons from hydrogen-, hydrocarbon-containing gas streams |
CN106281476B (en) * | 2016-08-31 | 2019-05-24 | 上海倍能化工技术有限公司 | A kind of method of sour gas in low temperature washing device for methanol and a kind of removing synthesis gas |
Citations (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2360408A (en) * | 1941-04-16 | 1944-10-17 | Dunn Ned | Method of and means for preheating fuel oil |
US3607048A (en) * | 1967-01-30 | 1971-09-21 | Linde Ag | Regeneration of liquids used to absorb carbon dioxide from gases intended for the production of ammonia synthesis gas |
US4246872A (en) * | 1979-04-30 | 1981-01-27 | General Electric Company | Heat exchanger tube support |
US4256783A (en) * | 1977-07-13 | 1981-03-17 | Nippon Skokubei Kagaku Kogyo Co., Ltd. | Catalytic vapor phase oxidation reactor apparatus |
US4320100A (en) * | 1979-03-06 | 1982-03-16 | Aeci Limited | Purification of gas mixtures |
US4338107A (en) * | 1980-10-30 | 1982-07-06 | Union Carbide Corporation | Wash system gas separation |
US4623370A (en) * | 1984-09-11 | 1986-11-18 | Aeci Limited | Gas treatment process |
US4810417A (en) * | 1982-01-21 | 1989-03-07 | Krupp-Koppers Gmbh | Process for the simultaneous production of methanol synthesis gas and ammonia synthesis gas |
US4904455A (en) * | 1985-06-27 | 1990-02-27 | Stone & Webster Engineering Corporation | Production of synthesis gas using convective reforming |
USRE33528E (en) * | 1985-02-11 | 1991-01-29 | Microtube-strip heat exchanger | |
US5103899A (en) * | 1990-08-31 | 1992-04-14 | Kalina Alexander Ifaevich | Multi-flow tubular heat exchanger |
US5324452A (en) * | 1992-07-08 | 1994-06-28 | Air Products And Chemicals, Inc. | Integrated plate-fin heat exchange reformation |
US6488742B1 (en) * | 1997-04-18 | 2002-12-03 | Metallgesellschaft Ag | Method for regenerating a loaded wash liquid from a gas desulfurization facility |
US20080039652A1 (en) * | 2004-01-22 | 2008-02-14 | Acetex (Cyprus) Limited | Integrated Process for Acetic Acid and Methanol |
US20100251765A1 (en) * | 2009-04-01 | 2010-10-07 | Air Products And Chemicals, Inc. | Cryogenic Separation of Synthesis Gas |
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US1853684A (en) * | 1927-09-10 | 1932-04-12 | Babcock & Wilcox Co | Air heater |
ES339041A1 (en) * | 1966-05-03 | 1968-04-16 | Schmidt Sche Heiisdampf G M B | Heat exchanger especially for the cooling of hot gases |
JPS57129391A (en) * | 1981-02-04 | 1982-08-11 | Hitachi Ltd | Heat exchanger |
DE19636018A1 (en) * | 1996-09-05 | 1998-03-12 | Markus Dipl Ing Fohr | Multi-chamber heat-exchanger |
FR2822838B1 (en) * | 2001-03-29 | 2005-02-04 | Inst Francais Du Petrole | PROCESS FOR DEHYDRATION AND FRACTIONATION OF LOW PRESSURE NATURAL GAS |
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KR100720714B1 (en) * | 2006-06-23 | 2007-05-21 | (주)경진티알엠 | Apparatus for large-scale heat pump with two-step shell-tube heat exchanger |
CN201066246Y (en) * | 2007-07-20 | 2008-05-28 | 上海化工装备有限公司 | Transverse-cool type fin heat-exchanging tube heat exchanger |
CN201364052Y (en) * | 2009-01-12 | 2009-12-16 | 张家港市华菱化工机械有限公司 | Shell-and-tube heat exchanger |
CN201419074Y (en) * | 2009-06-03 | 2010-03-10 | 上海国际化建工程咨询公司 | Shunting type energy-saving scrubbing unit using low temperature methanol |
CN201768471U (en) * | 2010-07-23 | 2011-03-23 | 镇海石化建安工程有限公司 | Low temperature methanol washing raw gas cooler |
-
2010
- 2010-07-23 CN CN2010202716691U patent/CN201768471U/en not_active Expired - Lifetime
-
2011
- 2011-07-22 US US13/812,673 patent/US20130206366A1/en not_active Abandoned
- 2011-07-22 JP JP2013519939A patent/JP5480450B2/en active Active
- 2011-07-22 KR KR1020127033779A patent/KR20130105311A/en not_active Application Discontinuation
- 2011-07-22 WO PCT/CN2011/001202 patent/WO2012009965A1/en active Application Filing
- 2011-07-22 CN CN2011800090731A patent/CN103025406A/en active Pending
- 2011-07-22 EP EP11809154.5A patent/EP2597411A4/en not_active Withdrawn
Patent Citations (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2360408A (en) * | 1941-04-16 | 1944-10-17 | Dunn Ned | Method of and means for preheating fuel oil |
US3607048A (en) * | 1967-01-30 | 1971-09-21 | Linde Ag | Regeneration of liquids used to absorb carbon dioxide from gases intended for the production of ammonia synthesis gas |
US4256783A (en) * | 1977-07-13 | 1981-03-17 | Nippon Skokubei Kagaku Kogyo Co., Ltd. | Catalytic vapor phase oxidation reactor apparatus |
US4320100A (en) * | 1979-03-06 | 1982-03-16 | Aeci Limited | Purification of gas mixtures |
US4246872A (en) * | 1979-04-30 | 1981-01-27 | General Electric Company | Heat exchanger tube support |
US4338107A (en) * | 1980-10-30 | 1982-07-06 | Union Carbide Corporation | Wash system gas separation |
US4810417A (en) * | 1982-01-21 | 1989-03-07 | Krupp-Koppers Gmbh | Process for the simultaneous production of methanol synthesis gas and ammonia synthesis gas |
US4623370A (en) * | 1984-09-11 | 1986-11-18 | Aeci Limited | Gas treatment process |
USRE33528E (en) * | 1985-02-11 | 1991-01-29 | Microtube-strip heat exchanger | |
US4904455A (en) * | 1985-06-27 | 1990-02-27 | Stone & Webster Engineering Corporation | Production of synthesis gas using convective reforming |
US5103899A (en) * | 1990-08-31 | 1992-04-14 | Kalina Alexander Ifaevich | Multi-flow tubular heat exchanger |
US5324452A (en) * | 1992-07-08 | 1994-06-28 | Air Products And Chemicals, Inc. | Integrated plate-fin heat exchange reformation |
US6488742B1 (en) * | 1997-04-18 | 2002-12-03 | Metallgesellschaft Ag | Method for regenerating a loaded wash liquid from a gas desulfurization facility |
US20080039652A1 (en) * | 2004-01-22 | 2008-02-14 | Acetex (Cyprus) Limited | Integrated Process for Acetic Acid and Methanol |
US20100251765A1 (en) * | 2009-04-01 | 2010-10-07 | Air Products And Chemicals, Inc. | Cryogenic Separation of Synthesis Gas |
Also Published As
Publication number | Publication date |
---|---|
CN103025406A (en) | 2013-04-03 |
WO2012009965A1 (en) | 2012-01-26 |
JP5480450B2 (en) | 2014-04-23 |
EP2597411A1 (en) | 2013-05-29 |
EP2597411A4 (en) | 2014-10-08 |
KR20130105311A (en) | 2013-09-25 |
CN201768471U (en) | 2011-03-23 |
JP2013535642A (en) | 2013-09-12 |
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Owner name: ZHENHAI PETROCHEMICAL JIANAN ENGINEERING CO.,LTD, Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ZHANG, XIAN'AN;WANG, JIANLIANG;CHEN, YONGDONG;AND OTHERS;REEL/FRAME:029704/0584 Effective date: 20121204 |
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