• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention relates to packaged apparatus for controlling the hydrocarbon dewpoint of a gas stream particularly adapted for use in a cold environment. A weather-tight enclosure is provided which includes a liquid desiccant dehydration unit for dehydrating the gas stream and means for cooling the dehydrated gas stream whereby a residue gas stream having a desired hydrocarbon dewpoint is produced. Portions of the dehydration unit and means for cooling the gas stream extend outside the enclosure so that they are subjected to the cold environment and are cooled thereby and heat generated by the dehydration unit and means for cooling the gas stream is utilized to heat the interior of the enclosure.
    公开号:SU1080729A3
    申请号:SU762353360
    申请日:1976-04-29
    公开日:1984-03-15
    发明作者:Джуниор Петерсон Адриан
    申请人:Блэк,Сиволз Энд Брайсон,Инк (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to installations for adjusting the dew point of water and hydrocarbon gas flow.
    A known device for dehydrating and removing condensable hydrocarbon components from a gas stream, comprising a contact tower, a distillation column, a gas burner, a re-concentrator, a balancing vessel of a reconcentrated liquid desiccant, a cooling and separation device G, G,
    A disadvantage of the known installation is that it cannot support a certain dew point.
    The purpose of the invention is to regulate the dew point.
    The goal is achieved by the fact that the installation for dehydration and removal of condensable hydrocarbon components from the gas stream, including a contact tower, a distillation column, a gas burner, a re-concentrator, a equalizing vessel of a reconcentrated liquid desiccant, a cooling and a separation device, interconnected by pipelines, is equipped with a discharge vessel. influences to the casing, under which the lower parts of the contact tower and the distillation column are located, gas burner, equalizer A reconstituted liquid desiccant vessel, a cooling and separation device, and the upper parts of the contact tower and distillation column are located above the casing.
    FIG. 1 shows an axonometric image of the proposed installation; in fig. 2 shows section A-A in FIG. one; in fig. 3 shows a section BB in FIG. 2; in fig. 4 - installation diagram.
    The installation includes a casing 1 with a door and windows installed on the skid x 2. The casing 1 contains a gas flow liquid desiccant concentrator, including reboiler 3, with a gas burner unit 4 located in the reboiler 3. The reboiler 3 is connected with 5 dl hot gas combustion products. A distillation column 6 is connected to the top of the reboiler 3. Below the reboiler 3 there is a leveling vessel 7 of the re-concentrated liquid dryer. The reboiler 3, the distillation column 6 and the leveling vessel 7 are located in the casing 1, but the upper part of the distillation column is located under it, and the end of the reboiler 3, which includes the burner block 4, is one hundred to 5 above the casing.
    The installation includes a heat exchanger 8, a gas flow cooler 9, a gas-liquid separator 10, a cooling unit 11, a tower 12, a pump 13 I for a liquid dryer, a filter 14. The installation also includes a pipe 15, a gas-liquid separation part 16, pipes 17 and 18, a heat exchanger 19, : 5 pipes 20, 21 and 22, coil 23, pipes 24-35, heat exchanger 36, compressor 37, pipes 38 and 39, cooler 40, pipe 41 and accumulator 42.
    The installation works as follows.,
    The gas stream to be treated is directed through pipe 15 to tower 12, the lower part of which includes a gas-liquid separation part 16,
    5 where the liquid contained therein is separated from the incoming gas stream through pipe 17. The liquid is directed into the casing 1 to the place of further processing and storage. No-i hot stream
    Q steps to the top of the tower 12 where it is absorbed. The flow of reconstituted liquid dehumidifier through the pipe 18 enters the heat exchanger 19. The cooled reconcentrated -
    A 5 nd liquid dryer through pipe 20 enters the upper part of tower 12, from where it flows down. A liquid desiccant saturated in the tower 12 with absorbed water is removed through pipe 21, then goes further to filter 14, after solid particles are removed from it, through pipe 22 enters a coil 23 located in leveling vessel 7 for heating. From coil 23, this flow through pipe 24 na5 leads to the upper part of the distillation column b, where it is in contact with hot water.
    The vapor-liquid contact channels or padding material located inside the distillation column b provide such close contact that the water vapor contained in the liquid desiccant is distilled off and separated from it. Separated water is discharged.
    5 from the column through the pipe 25, and liquid
    the dryer goes to reboiler 3 in which it is heated. A hot reconcentrated liquid dryer flows through pipe 26 from reboiler 3 to
    0 a leveling vessel 7, in which it moves slowly, is cooled by heat exchange with a stream of water-enriched liquid desiccant flow through a coil 23. Since the upper end of leveling vessel 7 is located outside the casing 1, the cold environment outside the casing additionally cools it, and the desiccant is then removed from the vessel through pipe 27 through pump 13, pipe 18,
    0 a heat exchanger 19, where it is further cooled in front of the tower 12. The upper part of the distillation column 6, located outside the casing 1, is cooled further by atmospheric air,
    5 that facilitates the separation of water and liquid desiccant vapors from the column. The absorption of water vapor from the gas stream by the liquid desiccant in the tower 12 also increases due to its location above the casing 1. The dehydrated gas stream is discharged from the tower 12 through the pipe 28 to the heat exchanger 8, where it is preliminary. but is cooled by the cooled residual gas stream obtained in the separator 10 passing through the tubular side of the heat exchanger 8. Through the pipe 29, the pre-cooled gas stream is directed to the cooler 9, in which it is cooled to a temperature at which the hydrocarbon components are condensed. The resulting mixture of gas and condensed hydrocarbon liquids is removed from cooler 9 through pipe 30, going further along this pipe to a separator, where gases and liquid are separated, and liquid is removed through pipe 31 connected to pipe 17. Gas flow temperature, passage through the cooler 9, is adjusted so that the residual gas flow obtained in the separator has the desired dew point of the hydrocarbon. The residual gas flow through the pipe 32 connected to the separator is directed to the tubular side of the heat exchanger 8 and further along the pipe 33 is withdrawn from the casing. The cooler 9 from the cooling unit 11 through the pipe 34 flows a stream of compressed refrigerant. Here, a known temperature control is used, and an expansion valve (not shown) is arranged in the BT pipe 34 in such a way that the refrigerant stream evaporates as it passes through the chiller 9 .. The evaporated refrigerant stream flows back through the tube 35 to the cooling unit and through the heat exchanger 8, where it is partially cooled, the pipe 38 enters the compensator 37, which pumps the refrigerant flow through the pipe 39 connected to the air cooler 40, in which the air is heated and the refrigerant is cooled and condensed . From cooler 40, the flow of condensed refrigerant through pipe 41 goes to accumulator 42 and then to heat exchanger 36 from the second through pipe 34 it is sent back to cooler. Automatically adjustable or manually louver (depending on temperature) can be located in the wall of the casing 1, so that part of the treated air produced by the air cooler 40 extends beyond the casing 1, thereby preventing overheating of the internal space. The proposed installation is economical in that the location of a part of its structural elements above the casing facilitates dehydration and cooling of the gas sweat and liquid desiccant, which allows constant dew point adjustment.
    g / 3
    gu
    2
    权利要求:
    Claims (1)
    [1]
    INSTALLATION FOR DEHYDRATION AND REMOVAL OF CONDENSABLE HYDROCARBON COMPONENTS FROM THE GAS FLOW, including pipelines connecting tower, distillation column, gas! a burner, a re-concentrator, an equalizing vessel of a reconcentrated liquid dehumidifier, a cooling and separation device, characterized in that, for the purpose of regulating the dew point, it is provided with a casing closed from atmospheric influences, under which the lower parts of the contact tower and distillation column are placed, a gas burner , equalizing vessel of the reconcentrated liquid dehumidifier, cooling and separation devices, and above the casing the upper parts of the contact tower and the distillation column are located.
    Figure 1
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1080729A3|1984-03-15|Apparatus for dehydrating and removing condensing hydrocarbon components from gas flow
    US3490201A|1970-01-20|Method and apparatus for drying gases
    US7531030B2|2009-05-12|Natural gas dehydrator and system
    US4242110A|1980-12-30|Compressed gas drying apparatus
    US6487872B1|2002-12-03|Dehumidifier system
    US4078390A|1978-03-14|Removal and recovery of sulfur dioxide from stack gases
    US20060130654A1|2006-06-22|Method and apparatus for recovering water from atmospheric air
    US20040031389A1|2004-02-19|Natural gas dehydrator and system
    GB649898A|1951-02-07|Improvements in or relating to method and apparatus for separating mixed gases
    US1959389A|1934-05-22|Adsorption system
    US4148617A|1979-04-10|Water recovery device
    US2203685A|1940-06-11|Cooling and dehumidifying device
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    US3100147A|1963-08-06|Apparatus and methods for treatment of natural gas
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    AU2005202670A1|2005-07-07|Dehumidifier system
    GB1569073A|1980-06-11|Removal and recovery of sulphur dioxide from stack gases
    SU955990A1|1982-09-07|Apparatus for separating gas mixtures
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    CN206420049U|2017-08-18|Direct-expansion type all-fresh air dehumidification air conditioner unit
    同族专利:
    公开号 | 公开日
    NO761490L|1977-04-13|
    NO148058C|1983-08-03|
    IE42559B1|1980-08-27|
    RO69119A|1981-11-24|
    FR2326967B1|1980-02-22|
    IE42559L|1977-04-09|
    NL7604622A|1977-04-13|
    US3989487A|1976-11-02|
    CA1062607A|1979-09-18|
    DE2618045A1|1977-04-21|
    NO148058B|1983-04-25|
    GB1539986A|1979-02-07|
    YU108976A|1982-06-30|
    FR2326967A1|1977-05-06|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2428643A|1947-10-07|Method |
    US1957624A|1930-02-06|1934-05-08|Douglas K Warner|Air conditioning with ground cooling and solar heat|
    US2812827A|1956-06-28|1957-11-12|Black Sivalls & Bryson Inc|Gas dehydration process and apparatus|
    DE1140959B|1960-03-31|1962-12-13|Linde Eismasch Ag|Insulation of a cryogenic system|
    US3182434A|1961-10-23|1965-05-11|Phillips Petroleum Co|Glycol-gas separator system and method|
    US3224212A|1964-01-08|1965-12-21|Chicago Bridge & Iron Co|Process and apparatus for continuously dehydrating gas|
    US3451897A|1967-02-02|1969-06-24|American Tank & Steel Corp|Apparatus for reconcentrating glycol and the like|
    US3886757A|1970-12-24|1975-06-03|Phillips Petroleum Co|Reduction of hydrate formation in a natural gas stream by contacting with anit-freeze agent|DE2728745B1|1977-06-25|1978-10-26|Davy Powergas Gmbh|Process for the re-concentration of wet glycol|
    US5766313A|1994-12-13|1998-06-16|Heath; Rodney T.|Hydrocarbon recovery system|
    US7531030B2|1999-06-15|2009-05-12|Heath Rodney T|Natural gas dehydrator and system|
    US7905722B1|2002-02-08|2011-03-15|Heath Rodney T|Control of an adjustable secondary air controller for a burner|
    US6238461B1|1999-06-15|2001-05-29|Rodney T. Heath|Natural gas dehydrator|
    NO321304B1|2003-09-12|2006-04-24|Kvaerner Oilfield Prod As|Underwater compressor station|
    US20070186770A1|2004-09-22|2007-08-16|Heath Rodney T|Natural Gas Vapor Recovery Process System|
    US20070151292A1|2004-09-22|2007-07-05|Heath Rodney T|Vapor Recovery Process System|
    US9353315B2|2004-09-22|2016-05-31|Rodney T. Heath|Vapor process system|
    DE602005021384D1|2005-12-27|2010-07-01|Fiat Ricerche|FUEL HIGH PRESSURE PUMP, WITH FUEL FEED IN CONNECTION WITH PUMP SUCTION|
    US8529215B2|2008-03-06|2013-09-10|Rodney T. Heath|Liquid hydrocarbon slug containing vapor recovery system|
    US8864887B2|2010-09-30|2014-10-21|Rodney T. Heath|High efficiency slug containing vapor recovery|
    US10052565B2|2012-05-10|2018-08-21|Rodney T. Heath|Treater combination unit|
    US9527786B1|2013-03-15|2016-12-27|Rodney T. Heath|Compressor equipped emissions free dehydrator|
    US9291409B1|2013-03-15|2016-03-22|Rodney T. Heath|Compressor inter-stage temperature control|
    US9932989B1|2013-10-24|2018-04-03|Rodney T. Heath|Produced liquids compressor cooler|
    US10274133B2|2016-06-29|2019-04-30|Thomas Kunkel|All-in-one skid assembly|
    CA2938252A1|2016-08-04|2018-02-04|Wayne Wk Lau|Maunufactured gas wellpad expansion module|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    CA237,318A|CA1062607A|1975-10-09|1975-10-09|Packaged gas stream hydrocarbon dewpoint control apparatus|
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