• 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:
    Mercury is removed from natural gas by contacting the gas with a relatively mercury-free liquid state hydrocarbon and recovering a mercury-lean methane-rich gas and a mercury-enriched hydrocarbon liquid. The mercury-free hydrocarbon liquid may be obtained by separation of mercury from the mercury-enriched hydrocarbon liquid or its derivative streams.
    公开号:SU1625321A3
    申请号:SU874203522
    申请日:1987-10-26
    公开日:1991-01-30
    发明作者:Р.Таракад Раманатан；Брукс Кроформ Даффер
    申请人:Дзе М.В.Келлог Компани (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to methods for removing mercury from gases and can be used in natural gas purification processes before using it in catalytic processes and for preventing equipment corrosion.
    The purpose of the invention is the elimination of the replacement of the spent sorbent.
    Example 1. Purification from mercury is subjected to natural gas of the following composition, mol%: methane 85.5; C2 7.5; Sz 2.5; Sl 1.0; Cs 0.5; mercury 1 mg / m. The cleaning circuit is shown in FIG. 1. Natural gas pre
    cooled to 0 ° C with propane chillers (not shown) and injected via line 1 into the cleaning system. In the heat exchanger 2, the stream of purified natural gas is pre-cooled to -23 ° C and introduced into the absorber 3, in which mercury contained in the stream is absorbed in mercury-free liquid absorbent, consisting mainly of liquefied ethane, propane and butane. line 4 to absorber 3 at -37 ° C. Mercury depleted and methane-enriched gas is removed from the absorber via line 5 and combined with
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    a recycle stream 6, consisting essentially of propane and butane, and free from mercury. The term mercury-free absorbent means that there is no mercury in a liquid stream or its content is so small that it is technically difficult to measure, i.e. the mercury content in the absorbent does not exceed 100–10 hours. It is preferable to use liquids containing not more than 5 hours of mercury. The mixed stream is cooled to -37 ° C in heat exchanger 7 and vapor and liquid are introduced into separator 8, in which the condensed hydrocarbons from lines 5 and 6 are separated and pumped to the absorber via line 4. The absorbent flowing through line 4, has the following composition, mol.%: methane 28, 21.0; Sz 20.0; C4 30.0; Sat 1.0; mercury 1,4 10 mol h,
    Methane-enriched stream 9 leaving separator 8 is essentially mercury-free and fed to injection fluidizing means (not shown). A portion of the methane-rich gas may be withdrawn for use as a fuel and / or transferred through the pipeline as a gas.
    From the absorber, the mercury-rich hydrocarbon liquid is fed through conduit 10 to mercury separation device 11. After that, the hydrocarbon liquid through line 12 is introduced into the separation unit 13 of liquefied parts of natural gas, from which light gasoline is returned to line 14 and the separated C1-C4 components are withdrawn as products along lines 15. Part of one or several Sc C3 components are withdrawn from line 15c using line 16 as a recycle stream, which is cooled in heat exchanger 17 to -29 ° C and then fed to the upper part of the absorber via line b.
    Fig. 2 shows a variant of the flowchart shown in Fig. 1, according to which a recirculation stream 16 discharged from the separation unit 13 of liquefied parts of natural gas is fed to the mercury separation device 11. This scheme is used with an acceptable mercury content in lines 14 and 15. Line 18 is intended to reintroduce C3, C4 components into liquefied natural gas if necessary.
    FIG. 3 is a flowchart of the method for the case when the content of the components to be liquefied in the incoming natural gas through line 1 is large enough to condense enough liquid from the methane-rich gas in line 5, which is then processed in the mercury removal device 11 to separate the mercury state, and feed stream 4 of a mercury-free liquid to the gas / liquid contact zone, i.e to absorber 3, the flow from the gas liquefaction device is not used. According to the flow diagrams of the method shown in FIG. 1-3, an additional contact of gas and liquid occurs in the heat exchanger 7 and behind it due to the condensation of Ca and heavy components in streams 5 and 6. This secondary contact further reduces the mercury content in the methane-rich gas obtained in line 9. The heat exchanger 7 can serve as a film absorber cooled by a mixed refrigerant. The heat exchanger 7 and the separator 8 can be combined in one device.
    In an exemplary embodiment of the method of FIG. 1, the separator 8 operates at -37 ° C and the mercury content in methane-rich gas is reduced to 0.1 µg / m. Preferably, the separation zone corresponding to the separator 8 has a cooler temperature of (50-75) ° C to condense a larger volume of liquid and thus reduce the concentration of mercury in methane-rich gas to 0.01-0.001 g / m.
    According to this embodiment of the method in which the hydrocarbon liquid, consisting of a liquefied mixture of ethane, propane and butane or propane and butane, serves as the absorbent, it is preferable to work in the gas-liquid contact zone at temperatures from +10 to -85 ° C. In liquefied gas installations, in which the gas entering the contact zone is usually under a pressure of 17-105 kg / cm2, the upper zone of the primary mercury absorber usually operates at a temperature from 0 to -75 ° C. Preferably, the mercury-poor methane-rich gas leaving the absorber is further cooled to - (30 - 85) ° C to condense additional hydrocarbons heavier than methane from the gas stream. Condensation further reduces the vapor phase mercury content.
    Example 2, FIG. Figure 4 shows a scheme for carrying out the method according to which the product enriched in methane in line 9 may not liquefy, but it is nevertheless desirable to have a gas with a low content of mercury. This example also illustrates the use of a hydrocarbon liquid under normal conditions, i.e. gasoline, as the main component of the mercury-free absorbent. The incoming gas is cooled to -34 ° C in heat exchanger 2 to enrich stream 10 with component C4 and lighter components. After removing mercury in unit 11 and separating the liquefied parts of natural gas in unit 13, the absorbent stream is separated and cooled to -37 ° C in heat exchanger 19 for use as mercury-free absorbent. Preferably, the separation of mercury from gasoline is carried out at - (20 - 100) ° C. Excess fluid not needed in the absorber 3 is recycled via line 20 as a product for other industries or for additional processing.
    FIG. 5 shows a variant of the technological scheme of FIG. 4, according to which in the mercury removal device 11 the recirculation part of the stream 14 obtained from the gas liquefaction device 13 is processed.
    In example 2, when using gasoline, the gas-liquid contact zone operates at a temperature of from +40 to -40 ° C. If the treated natural gas is under a pressure of 7-140 kg / cm2 and a temperature of from +40 to -35 ° C, then the absorbent must be in the temperature range from +40 to -45 ° C.
    Example 3. FIG. 6 shows a scheme for carrying out the method according to which hydrocarbons are used under general conditions as the main component of a mercury-free hydrocarbon liquid in line 14 when mercury is to be removed rather for toxicity reasons than for corrosion reasons, for example, when a main gas containing C2- and Sat is needed components, and it is obtained through line 9, and separation of the effluent absorber fluid is not required. In this example, the gas in line 9 does not need to be cooled to low temperatures and the gas-liquid contact zone can operate in the temperature range from +40 to -40 ° C.
    Example 4. FIG. 7 shows a flowchart for removing mercury in the form of a liquid or preferably a solid substance from streams of mercury-contaminated fluids formed according to the examples described. Flow 21 of a mercury-contaminated hydrocarbon is cooled to - (18 - 155) ° C in heat exchangers 22 and 23 and input t to separation zone 24, which serves as a simple sump. A substantially mercury-free liquid is continuously withdrawn from the top of the separator through line 25, while liquid or solid mercury is removed occasionally through line 26.
    The temperature to which the mercury-contaminated fluid flow is cooled depends mainly on the desired degree of mercury removal, the choice of hydrocarbons as an absorbent and the location of the mercury removal unit in the process chain. Hydrocarbon liquid with very low
    5 mercury content can be obtained at the lowest temperature of operation of the mercury removal device. When the mercury separation stage is carried out with a liquefied mixture of ethane, propane and butane (Fig. 2 and 3),
    This separation process is carried out at - (45 - 160) ° C. When mercury is removed from the relatively warm liquid effluent of the absorber (FIGS. 1 and 4), the mercury separation is carried out at - (20-100) ° C.
    5 As follows from the examples, according to the proposed method, it is not necessary to replace the sorbent, which has been spent in the process of extracting mercury from a natural gas stream; after separation of mercury from the sorbent, it is returned to the absorption stage. According to a known method, when using a solid sorbent containing sulfur, after the sorbent has been developed, its replacement is required.
    权利要求:
    Claims (5)
    [1]
    1. A method for removing mercury from a natural gas stream, including the supply of sorbent to the zone of its contact with natural gas, contacting the sorbent with natural gas
    0 at elevated pressure and removal of mercury-depleted natural gas from the contact zone, characterized in that, in order to eliminate the replacement of the spent sorbent, as the sorbent is used
    5 mercury-free mixtures of ethane, propane and butane, or propane and butane, liquefied upon cooling, or gasoline; after contact with natural gas, the enriched sorbent is removed from the zone
    0 contact, mercury is separated from it by cooling in liquid or solid form and recycled to the contact zone with natural gas.
    [2]
    2. A pop method, 1, characterized in that when using liquefied
    5 mixtures of ethane, propane and butane or propane and butane, its temperature in the zone of contact with gas is maintained at +10 to -85 ° C, and the gas pressure is maintained at 17-105 kg / cm2.
    0
    [3]
    3. The way pop. 1, characterized in that when using gasoline, its temperature is maintained at +40 to -45 ° C, the gas pressure is maintained at 7-140 kg / cm, and the gas temperature is between +40 and -35 ° C.
    [4]
    4. The method according to paragraphs. 1 and 2, which differs from the fact that the release of mercury from its enriched liquefied mixtures of ethane, propane and butane is carried out at a temperature from -45 to -160 ° C.
    [5]
    5. The method according to paragraphs. 1 and 3, mercury-rich gasoline is carried out at a temperature and with the release of mercury from -20 to -100 ° C.
    T /.
    Fig.Z
    FIG. five
    Z4
    FIG. 7
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    同族专利:
    公开号 | 公开日
    JPS63112692A|1988-05-17|
    DE3763404D1|1990-08-02|
    MX166185B|1992-12-23|
    AU582089B2|1989-03-09|
    CN1009056B|1990-08-08|
    NO874442D0|1987-10-26|
    NO167550B|1991-08-12|
    AU7679487A|1988-04-28|
    IN171012B|1992-07-04|
    JPH037717B2|1991-02-04|
    EP0266493A1|1988-05-11|
    CA1302051C|1992-06-02|
    US4693731A|1987-09-15|
    NO167550C|1991-11-20|
    EP0266493B1|1990-06-27|
    CN87107491A|1988-05-18|
    NO874442L|1988-04-28|
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    引用文献:
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/923,462|US4693731A|1986-10-27|1986-10-27|Removal of mercury from gases|
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