• 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:
    1487466 Liquefying natural gas LINDE AG 21 July 1975 [9 Aug 1974] 30406/75 Heading F4P Natural gas 1 is liquefied by a first multicomponent refrigerant and then a second multi-component refrigerant, each refrigerant being in a respective closed circuit, the first circuit being such that the refrigerant is compressed at 27, 28, 29, partially liquefied by cooler 30 and then separated at 31, the liquid fraction being sub-cooled at 60 and then undergoing successive stages of expansion and separation at 32, 33, 36, 37, 40, 41, a part of each liquid fraction being passed to lines 34, 38, 42 of respective exchangers 2, 6, 7 to cool the natural gas before being returned to the separator from whence they came, whilst the gaseous fraction from separator 31 is cooled in exchangers 2, 6, 7 and 11 before expansion at 44 and passage to separator 41 via exchanger 11, and the second refrigerant circuit being such that the refrigerant is compressed at 45, cooled at 46, partially liquefied in exchangers 2, 6, 7, 11 and then completely liquefied in exchanger 13 in heat exchange with lowerboiling component of the natural gas and itself, it then being returned to compressor 45 via expansion valve 59 and exchanger 13. The feed gas 1 is cooled at 2 to condense out C 5 and higher hydrocarbons and water which are separated at 3. The remaining gas is dried and passed to exchangers 6, 7 where it is partially condensed before moving to a rectification column 8. The sump product of ethane, propane and higher-boiling hydrocarbons is withdrawn at 10 and the gaseous head product of N 2 , methane and ethane, and small quantities of propane and butane, is passed through exchanger 11 for partial condensation before reaching separator 12. The gaseous fraction is liquefied and subcooled in exchanger 13 before passing via exchanger 25 and ejector 14 to column 15. The overhead N 2 -rich product is passed back through exchangers 11, 7, 6, 2. The second circuit may have a two stage compressor with an extra exchanger from which is fed an intermediate refrigerant portion to the second compressor stage (Fig. 2, not shown). Alternatively, the second refrigerant can be separated before being used in a pair of exchangers replacing 13 (Fig. 3, not shown). The successive liquid fractions in the first circuit may be increased in pressure before performing their cooling function, and they are then returned to the preceding separator (Fig. 4, not shown). Finally, an extra separator may be located between 31 and 33, the gaseous fraction being combined with that from 31 after cooling at 2, 6, 7, 11 and expansion (Fig. 5, not shown).
    公开号:SU1029833A3
    申请号:SU752163057
    申请日:1975-07-30
    公开日:1983-07-15
    发明作者:Ферг Вольфганг
    申请人:Линде Аг (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to the gas industry, and specifically to methods for liquefying natural gas. The closest to the invention is a method of liquefying natural gas, including cooling stages using two refrigeration cycles, cleaning, supplying purified gas to the first distillation column, and discharging the resulting bottom product of separating the resulting product into the liquid phase, which is returned to the top of the first distillation column. , and the gas phase, "otea after liquefaction and undercooling, is fed to the bottom of the second distillation column with after feeding into its upper part, output oluchaemogo overhead product, the bottoms produced Dros 1selirovani prod ucts and removal of the resulting liquid and vapor phases 1. The drawback of the known method is a large energy consumption, object of the invention - reduction enesgo zatgrat. This goal is achieved according to the liquefaction method of natural gas, which includes the stages of cooling using two refrigeration cleaning cycles, supplying the purified gas to the first distillation column, discharging the resulting bottom product, dividing the resulting head product into a second phase, which is returned to the top of the first distillation column , and the gas phase, which, after liquefaction and undercooling, is fed to the bottom of the second distillation column with the subsequent feed to its upper part, the output of the obtained bottom product of throttling of the obtained bottom product and removal of the liquid and vapor phases obtained in this way, the working substance of the Second refrigeration cycle is cooled by heat exchange with the working substance of the first refrigeration cycle consisting of three cooling stages, and the vapor phase of the second distillation column obtained by throttling the bottom product served in its upper part with the help of an ejector. The drawing shows one of the possible options for the liquefaction scheme of natural gas according to the proposed method. Natural gas, consisting mainly of nitrogen, methane, ethane, propane and high-boiling hydrocarbons, is fed under pressure of approximately 44 atmospheres to the installation via pipeline 1. After cooling in heat exchanger 2, the separated high-boiling hydrocarbons and water are separated in separator 3 and removed through pipeline .4, and separating the hevant natural gas, the wasp is drawn off AND DISCHARGED through pipeline 5 Rirx to further cool down in heat exchangers b and 7, and then to the first distillation column where it is separated. propane-ethanol fraction with high-boiling hydrocarbons for further purification and separation by pipeline 8. The top product of the column 9 is cooled in the α-bore-10 and the separated liquid fraction is separated in the GT separator and returned to the column 8, and the gaseous fraction from the separator 11 is partially flowed 12 is cooled in the heat exchanger 13 and fed through the ejector 14 to the upper part of the second low-pressure distillation column 15, the cube 15 is heated with a stream 16 and is throttled into the middle part of the column with stream 17 through the recuperative heat the heat exchanger 18 is throttled into the top of the column 15, the product of the head enriched with nitrogen,; Olnns 15 are removed from the installation for disposal through pipeline 19, recovering cold in heat exchangers 18, 10, 7, b and 2. The bottom product of the column 15, consisting mainly of methane, is throttled to atmospheric pressure in a separator 20, from which the liquid phase pipe 21 is removed from the plant, and the vapor phase is pressed in ejector 14 by stream 12 and their mixture is introduced into the upper part of column 1 5. The main amount of cold consumed during liquefaction is formed in e) zuh to ac to ad-located refrigerated cycles. The first cycle is three-stage, the refrigerant in it is a mixture of propane and ethane. The cold produced in the cycle is released in heat exchangers 10 and 7 at a low boiling pressure of the refrigerant, in heat exchanger 6 - at an average intermediate pressure, in heat exchanger 2 at a high intermediate pressure. The second refrigeration cycle is single-stage, the refrigerant is a mixture of nitrogen, methane, ethane and propane, cooled in heat exchangers 2, 6 and 7 and condensed in heat exchangers 10 and 13, and evaporation of the refrigerant takes place in heat exchanger 13. The advantage of the proposed combination of refrigeration refrigeration cycles is the possibility of reducing the temperature head in the heat exchangers when the natural gas is cooled, the possibility of significant demethanization of the heated bottom product of the first column due to high reflux ratio, provided by significant condensation of the column head in the heat exchanger 10 and significant condensation in the second cycle of the soldering unit cooling,
    31029833
    Compression of the vapor phase, formed by the expansion of the natural gas to be separated after throttling of the bottom gas.
    duct low pressure column, the total energy consumption in the proposed
    the ejector allows to reduce losses. the method is significantly reduced
    the product and it is useful to use the pr-0.26 kWh / s.
    权利要求:
    Claims (1)
    [1]
    A METHOD FOR LIQUIDING NATURAL GAS, including the stages of cooling using two refrigeration cycles, purification, supplying purified gas to the first distillation column, withdrawing the resulting bottoms product, separating the resulting overhead product into a liquid phase, which is returned to the top of the first distillation column, and the gas phase, which, after liquefaction and supercooling, is fed into the lower part of the second distillation column with subsequent supply to its upper part, the output of the resulting overhead product, chokes of the obtained bottoms product and the removal of the resulting liquid and vapor phases # characterized in that, in order to reduce energy consumption, the working substance of the second refrigeration cycle is cooled by heat exchange with the working substance of the first refrigeration cycle, which consists of three cooling stages, and the vapor phase of the obtained when throttling the bottoms product, the second distillation column is fed into its upper part using an ejector.
    sew and discharge through the pipe 5 dattg of further cooling in heat exchangers 6 and 7, and then into the first distillation column; where they isolate, the propane-ethane fraction with high-boiling hydrocarbons and withdrawn for further purification and separation by pipeline 8. The upper product of the column 9 is cooled in a β-exchanger 10
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    同族专利:
    公开号 | 公开日
    US4112700A|1978-09-12|
    NO752394L|1976-02-10|
    GB1487466A|1977-09-28|
    JPS5632540B2|1981-07-28|
    JPS5128101A|1976-03-09|
    NO141385B|1979-11-19|
    NO141385C|1980-02-27|
    DE2438443C2|1984-01-26|
    DE2438443A1|1976-02-19|
    FR2281550A1|1976-03-05|
    FR2281550B1|1979-05-11|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE2438443A|DE2438443C2|1974-08-09|1974-08-09|Process for liquefying natural gas|
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