WO2013135037A1 - 采用单一混合工质制冷液化天然气的方法和装置 - Google Patents

采用单一混合工质制冷液化天然气的方法和装置 Download PDF

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Publication number
WO2013135037A1
WO2013135037A1 PCT/CN2012/081340 CN2012081340W WO2013135037A1 WO 2013135037 A1 WO2013135037 A1 WO 2013135037A1 CN 2012081340 W CN2012081340 W CN 2012081340W WO 2013135037 A1 WO2013135037 A1 WO 2013135037A1
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Prior art keywords
gas
heat exchange
liquid
separator
heat exchanger
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PCT/CN2012/081340
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English (en)
French (fr)
Inventor
何振勇
王贵歧
刘丽梅
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新地能源工程技术有限公司
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Application filed by 新地能源工程技术有限公司 filed Critical 新地能源工程技术有限公司
Priority to US14/381,675 priority Critical patent/US20150013378A1/en
Priority to CA2864482A priority patent/CA2864482C/en
Publication of WO2013135037A1 publication Critical patent/WO2013135037A1/zh

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0291—Refrigerant compression by combined gas compression and liquid pumping
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general

Definitions

  • the present invention relates to liquefaction production of hydrocarbon-rich gas, and more particularly to a method and apparatus for refrigerating liquefied natural gas with a single mixed working fluid. Background technique
  • Natural gas has become the best alternative to other fuels due to its environmental friendliness, and its application fields have gradually expanded to include power generation, automotive gas, industrial gas, urban residential gas, and chemical gas.
  • the more mature natural gas liquefaction processes mainly include: a cascade refrigeration process, an expansion refrigeration process, and a mixed refrigerant process.
  • the single mixed refrigerant refrigeration process is favored by medium-sized LNG plants.
  • the refrigerant compression system is secondary compression, and the natural gas liquefaction uses primary heat exchange.
  • the device used includes a motor-driven two-stage hybrid working fluid compressor 1, two coolers 21, 22, two gas-liquid separators 31, 32, two a liquid pump 4, 4', a plate-fin heat exchanger 8 and an LNG storage tank 9; a mixed working medium consisting of C1 ⁇ C5 and N2 is properly proportioned and enters the inlet of the compressor, after a period of compression To 0.6 ⁇ lMPa, enter the first-stage cooler and cool to 30 ⁇ 40°C, then enter the first-stage gas-liquid separation tank for gas-liquid separation. The gas separated at the top of the first-stage gas-liquid separation tank continues to enter the second inlet of the compressor.
  • the liquid separated by the first stage separation bottom is pressurized by the liquid pump and mixed with the gas of the second stage compressor outlet to enter the secondary cooler to be cooled to 30 ⁇ 40 °C, after cooling
  • the mixed working fluid then enters the secondary gas-liquid separation tank for gas-liquid separation.
  • the separated liquid is pressurized by the secondary liquid pump and mixed with the gas obtained at the top of the separator, and then enters the plate-fin heat exchanger, pre-cooled to a certain degree.
  • the throttle is returned to the plate fin change , A heat exchanger to provide cooling for the entire process, the gas enters through the plate-fin heat exchanger LNG storage tank.
  • the present invention provides a method and apparatus for refrigerating liquefied natural gas using a single mixed working fluid.
  • the invention uses a single mixed refrigerant to liquefy natural gas.
  • the invention adopts a method and a device for liquefying natural gas by a single mixed refrigerant, which is divided into a natural gas circulation and a mixed refrigerant refrigeration cycle.
  • the mixed working fluid is accompanied by step-by-step gas-liquid separation in the stepwise compression process, and the liquid phase stream separated by the first-stage compression does not participate in the subsequent compression process, effectively reducing the subsequent gas.
  • Compressed power consumption; the gas phase and liquid phase mixed working fluid streams obtained by compression enter the different channel throttling heat exchange of the heat exchanger group respectively, and the last stage liquid pump is omitted compared with the conventional process, and multi-stage heat transfer is adopted.
  • the heat transfer curves of the heat flux and the cold flow strand are more matched during the whole process; the final gas phase is reheated after throttling and then enters the refrigerant separator, which can effectively avoid cold tank effluent.
  • the invention relates to a device for refrigerating liquefied natural gas using a single mixed working medium, which comprises a mixed refrigerant compression system and a cold box system, wherein the compression system of the mixed refrigerant is compressed by a two-stage mixed working fluid compressor, including a two-stage type Mixed working fluid compressor, two coolers, two gas-liquid separators and one liquid pump.
  • the cold box system consists of a set of plate-fin heat exchangers (secondary heat exchange) and two gas-liquid separators ( It includes a heavy hydrocarbon separator and a refrigerant separator) and two throttling devices; the mixed working fluid and natural gas complete the entire heat exchange process in the cold box system.
  • a section of the compressor is connected to the primary cooler, and the primary cooler is connected to the primary gas-liquid separator, and the first-stage gas-liquid separator is connected to the second-stage compression, the first-stage gas-liquid separation.
  • the liquid phase end of the bottom of the device is connected to the liquid pump, and the liquid pump outlet is connected with the second-stage compression outlet to be connected to the secondary cooler, and the secondary cooler is connected to the second-stage gas-liquid separator, and the top gas phase separator of the second-stage gas-liquid separator is exchanged.
  • the first heat exchange channel of the heat exchanger group is connected; the bottom liquid phase end of the second gas-liquid separator is connected with the second heat exchange channel of the heat exchanger group;
  • the liquid phase end of the secondary gas-liquid separator from the mixed refrigerant compression system is connected to one end of the first throttle device through a second heat exchange passage in the heat exchanger group, the first throttle device The other end is connected to the third heat exchange channel of the heat exchanger group and connected to a section of compression; the gas phase end obtained at the top of the second-stage gas-liquid separator is pre-cooled through the first heat exchange channel of the heat exchanger group, and then the end of the second throttling device Connecting, the other end of the second throttling device is connected to the fourth heat exchange channel of the heat exchanger group and connected to the refrigerant separator; the natural gas pipeline is connected to the heavy hydrocarbon separator through the fifth heat exchange channel of the heat exchanger group, and the top gas phase of the heavy hydrocarbon separator The ends are sequentially sent to the LNG storage tank through the other heat exchangers of the heat exchanger group, and the bottom liquid phase of the heavy hydrocarbon separator is obtained as liquefied petroleum gas (LPG).
  • LPG
  • the outlet gas of the compressor enters the primary cooler and is cooled by the first-stage gas-liquid separator, and the separated gas phase continues.
  • the separated liquid phase is pressurized by the liquid pump and merges with the hot gas after the second stage compression, and is cooled by the secondary cooler to enter the second stage gas.
  • the liquid separator is separated, and the separated gas phase enters the first heat exchange channel (gas phase channel) of the downstream heat exchanger; the liquid obtained at the bottom of the second gas-liquid separator enters the second liquid phase heat exchange channel of the downstream heat exchanger, respectively.
  • the liquid refrigerant from the bottom of the secondary gas-liquid separator of the refrigerant compression system enters the heat exchanger group and is pre-cooled and then passes through the first throttling device, and the throttled stream enters the refrigerant separator.
  • the middle portion; the gas phase refrigerant from the top of the second-stage gas-liquid separator is pre-cooled by the heat exchanger group and then throttled by the second throttling device, and the throttled stream is reversely entered into the heat exchanger group to be reheated to After a certain temperature, it is taken out to the middle of the refrigerant separator, and after the above-mentioned cooling and throttling (after the first throttling device;), the refrigerant entering the refrigerant separator is merged, and the two are separated into gas and liquid by the refrigerant separator.
  • the two phases, the gas-liquid two phases of the refrigerant separator are combined and returned to the heat exchanger group to provide the cooling capacity.
  • the natural gas is first cooled by the heat exchanger group to a certain temperature and then separated into separators.
  • the bottom part obtains heavy hydrocarbon components, and the gas phase obtained at the top continues to enter the heat exchangers of the other heat exchangers of the heat exchanger group, and is cooled to a supercooled state.
  • the resulting LNG is stored in an LNG storage tank.
  • a device for refrigerating liquefied natural gas using a single mixed working fluid comprising a mixed refrigerant compression system and a cold box system, wherein the compression system comprises a two-stage mixed working fluid compressor, and the two-stage mixed working fluid compressor respectively a first cooler and a second cooler connected to the first and second sections, a first gas-liquid separator and a second unit respectively connected to the first cooler and the second cooler a gas-liquid separator and a liquid pump connected to the first of the two gas-liquid separators,
  • the cold box system includes:
  • a set of plate fin heat exchangers comprising at least six heat exchange passages: first, second, third, fourth, fifth and sixth heat exchange passages, said second heat exchange passage and first
  • the input end of the heat exchange passage is respectively connected to the liquid phase end and the gas phase end of the second gas-liquid separator in the mixed refrigerant compression system via two pipes, and the output end of the third heat exchange channel is connected to the pipeline via a pipe First compression section;
  • a first throttling device connected to an output end of the second heat exchange passage of the plate fin heat exchanger group
  • a second throttling device connected to the output end of the first heat exchange passage of the plate fin heat exchanger group and the input end of the fourth heat exchange passage;
  • a refrigerant separator connected to the input end of the third heat exchange passage of the plate fin heat exchanger group, the output end of the fourth heat exchange passage, and the first throttle device;
  • a natural gas heavy hydrocarbon separator connected to a separate heat exchange passage of the plate fin heat exchanger group, that is, a fifth heat exchange passage
  • the gas phase end of the first gas-liquid separator in the two gas-liquid separators is connected to the second compression section of the two-stage mixed working fluid compressor, and the liquid phase end of the first gas-liquid separator is via a liquid pump
  • the outlet pipe of the second compression section is merged and connected to the office
  • the second cooler of the two coolers, the gas phase end and the liquid phase end of the second gas-liquid separator are respectively replaced with the two heat exchange channels of the set of plate-fin heat exchanger groups
  • the hot channel is connected to the input end of the second heat exchange channel; wherein the first throttling device is connected to the refrigerant separator, and the top gas phase end and the bottom liquid phase end of the refrigerant separator are merged and connected to the third heat exchange channel
  • the input end, the output end of the third heat exchange channel is connected to the first section of the two-stage mixed working fluid compressor, and the second throttling device is connected to the input end of the fourth heat exchange channel and is connected to the refrigerant separat
  • the top gas phase end of the heavy hydrocarbon separator passes through the sixth heat exchange passage of the heat exchanger group in turn and is further connected to the liquefied natural gas storage tank through the other seventh heat exchange passage of the heat exchanger group.
  • the purified raw natural gas first enters the plate-fin heat exchanger group for pre-cooling, is cooled to -30 ° C ⁇ - 80 ° C and then enters the heavy hydrocarbon separator for gas-liquid separation, separated by the top of the heavy hydrocarbon separator.
  • the gas phase stream continues to enter the remaining heat exchangers of the heat exchanger group and is cooled therein to -130 ° C to - 166 ° C, and the obtained liquefied natural gas is sent to an LNG storage tank for storage.
  • the liquid separated from the bottom liquid phase of the first gas-liquid separator is pressurized to 1.2 ⁇ 5.4 by the liquid pump. After MPaA merges with the second stage compressed outlet hot gas, it enters the secondary cooler and cools to 30 °C ⁇ 40 °C.
  • the cooled mixed working medium then enters the secondary gas-liquid separator for gas-liquid separation, and the second-stage gas-liquid
  • the gas at the top of the separator then enters the first heat exchange channel of the main heat exchanger group to participate in heat exchange, and the liquid separated at the bottom of the second gas-liquid separator enters the second heat exchange channel of the main heat exchanger group to participate in heat exchange;
  • Liquid extracted from the bottom of the secondary gas-liquid separator of the working fluid compression system First enter the second heat exchange channel of the heat exchanger group, where it is pre-cooled to about -30 ° C ⁇ - 80 ° C, after the first throttle valve throttles to 0.2 ⁇ 0.8MPaA, enter the middle of the refrigerant separator
  • the gas phase stream of the mixed working fluid separated from the top of the secondary gas-liquid separator is cooled to -135 ° C to - 169 ° C through the gas phase passage of the heat exchanger group, and then throttled to 0.2 by the second throttle valve.
  • the heat exchanger After returning to the heat exchanger group at ⁇ 0.8MPaA, the heat exchanger is supplied with cooling capacity. After reheating to -30°C ⁇ -80°C, the heat exchanger group is taken into the middle of the refrigerant separator, and separated from the second-stage gas-liquid. After the liquid phase of the bottom of the device is cooled and throttled, the stream entering the refrigerant separator merges and enters the refrigerant separator. The gas-liquid two phases of the refrigerant separator are combined and returned to the heat exchanger group to provide cooling capacity. . Further, after the gas-liquid two phases of the refrigerant separator are merged and returned to the heat exchanger group to provide a cooling amount, they are returned to the compressor as a mixed refrigerant.
  • the pressure unit MPaA is MPa, absolute pressure.
  • the final stage gas phase enters the refrigerant separator after recirculation and reheating after throttling, which can effectively avoid the cold tank effluent, thus ensuring the low load working condition.
  • the energy consumption of the product is close to the energy consumption under normal working conditions.
  • the two-stage mixed refrigerant compressor is used in the method of the invention, and the mixed refrigerant is compressed step by step and separated step by step, thereby reducing the power consumption of gas compression.
  • the liquid stream at the bottom of the first-stage gas-liquid separator does not participate in the subsequent compression process, which reduces the influence of the fluctuation of the mixed refrigerant ratio on the operating conditions of the compressor unit to a certain extent, making the whole device easier to operate.
  • the secondary heat transfer makes the heat transfer curves of the cold fluid and the hot fluid in the whole heat exchange process more matching, which effectively reduces the flow rate of the mixed refrigerant.
  • Figure 1 is a structural view of the prior art
  • FIG. 2 is a view showing a device configuration of the mixed working fluid refrigeration system of the present invention.
  • the purified raw material natural gas is first pre-cooled into the fifth heat exchange passage of the plate-fin type main heat exchanger group 8, and is cooled to -30 ° C to - 80 ° C and then enters the heavy hydrocarbon separator.
  • the gas-liquid separation is carried out in 6 , and the gas phase stream separated from the top of the heavy hydrocarbon separator 6 continues to enter the remaining heat exchangers (the sixth heat exchange passage) of the main heat exchanger group 8 and is cooled therein - After 130 ° C ⁇ - 166 ° C, it is sent to the LNG storage tank 9 for storage.
  • the bottom liquid phase of the heavy hydrocarbon separator is liquefied petroleum gas (LPG).
  • the gas separated at the top of the first-stage gas-liquid separator 31 continues to enter the second inlet of the compressor, and is compressed to 1.2 to 5.4 MPaA by the second stage, and the liquid separated from the bottom liquid phase of the first-stage gas-liquid separator 31 is passed through the liquid pump 4. Pressurize to 1.2 ⁇ After 5.4MPaA merges with the second stage compressed outlet hot gas, it enters the secondary cooler 22 and cools to 30°C ⁇ 40°C. The cooled mixed working medium then enters the secondary gas-liquid separator 32 for gas-liquid separation.
  • the gas at the top of the gas-liquid separator 32 then enters the first heat exchange channel of the main heat exchanger group 8 to participate in the heat exchange, and the liquid separated at the bottom of the second gas-liquid separator 32 enters the second heat exchange of the main heat exchanger group 8.
  • the channel participates in heat exchange
  • the liquid drawn from the bottom of the secondary gas-liquid separator 32 of the mixed working fluid compression system first enters the second heat exchange passage of the heat exchanger group, where it is pre-cooled to about -30 ° C to - 80 ° C, and is throttled.
  • the valve 51 is throttled to 0.2 to 0.8 MPaA and then enters the refrigerant separator 7; the gas phase stream of the mixed working fluid separated by the top of the secondary gas-liquid separator 32 passes through the gas phase passage of the heat exchanger group 8 (first heat exchange) Channel) Cool to -135 °C ⁇ - 169 ° C, then throttling through the throttle valve 52 to 0.2 ⁇ 0.8MPaA, then enter the fourth heat exchange channel of the heat exchanger group 8 and reheat to -30 ° C ⁇ - After 80 °C, the heat exchanger group is taken into the middle of the refrigerant separator 7, and the liquid phase of the second-stage gas-liquid separator 32 is cooled and throttled to form a stream, and

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Abstract

一种采用单一混合工质制冷来液化天然气的装置及方法，该装置包括二段式压缩机（1），分别与二段式压缩机（1）的每一段连接的冷却器（21，22），分别与每一冷却器（21，22）连接的气液分离器（31，32），两个节流阀（51，52），一组板翅式换热器组（8）和一个LNG储罐（9）。该装置中通过逐级压缩、逐级分离混合冷剂，减少了气体压缩功耗；并且通过多级换热，优化了冷、热流体间的换热匹配，有效减少了冷剂流量。此外该装置能更好的适应变负荷运转，可有效避免冷箱底部积液。

Description

采用单一混合工质制冷液化天然气的方法和装置
技术领域
本发明涉及富含烃类气体的液化生产， 具体涉及一种单一混合工质制冷液化天然气的方 法和装置。 背景技术
天然气由于其环保性而成为取代其他燃料的最佳物质， 其应用领域已逐渐扩大到发电、 汽车用气、 工业用气、 城市居民用气、 化工用气等方面。
随着天然气消费量的增长， 作为天然气最有效的供用形式之一， 液化天然气的贸易量也 已成为能源市场增长最快的领域之一。 液化天然气工业的不断发展， 则对天然气液化方法和 装置在能耗、 投资和效率等方面提出了更高的要求。
目前， 比较成熟的天然气液化工艺主要有： 阶式制冷工艺、 膨胀制冷工艺和混合工质制 冷工艺。 其中的单一混合工质制冷工艺则比较受中型 LNG装置的青睐。
现有的单一混合工质制冷的天然气液化方法中， 冷剂压缩系统为二级压缩， 天然气液化 采用一级换热。
现有工艺技术： 如图 1所示， 其使用的装置包括一台电机驱动的二段式混合工质压缩机 1， 二台冷却器 21、 22， 二台气液分离器 31、 32, 二台液体泵 4、 4'， 一台板翅式换热器 8 和一台 LNG储罐 9; 由 C1〜C5和 N2组成的混合工质经过合理配比后进入压缩机的入口， 经一段压缩至 0.6〜lMPa， 进入一级冷却器冷却至 30〜40°C， 再进入一级气液分离罐进行气 液分离，一级气液分离罐顶部分离出的气体继续进入压缩机的二段入口， 经二段压缩至 1.6〜 2.5MPa, 一级分离底部分离得到的液体通过液体泵加压后与二段压缩机出口的气体混合进入 二级冷却器冷却至 30〜40°C， 冷却后的混合工质随后进入二级气液分离罐进行气液分离， 分 离后的液体通过二级液体泵加压后与该分离器顶部得到的气体混合后进入板翅式换热器， 预 冷至一定温度后节流再返回该板翅式换热器， 为整个换热过程提供冷量， 天然气通过板翅式 换热器后进入 LNG储罐内。
在上述工艺， 为保证液体和气体进入同一个板翅式换热器通道参与换热， 末级气液分离 器底部的液体必须要加压以克服分离器底部液体出口到板翅式换热器顶部冷剂入口的高度差 所带来的液柱压力， 必须通过增加末级液体泵来实现。 冷剂和天然气在板翅式换热器中的换 热过程为一级换热， 流股间换热温差的优化受到一定限制， 装置能耗较高， 并且， 此种流程 容易产生冷箱底部积液， 对装置的变负荷运转没有很好的适应性。 发明内容
本发明提供了一种采用单一混合工质制冷液化天然气的方法和装置。 该发明采用单一混 合工质制冷使天然气液化。
本发明采用单一混合工质制冷来液化天然气的方法和装置， 其分为天然气循环和混合工 质制冷循环。 在混合工质回路中， 混合工质在其逐级压缩过程中同时伴随逐级的气液分离， 一级压缩分离出的液相流股不参与后续的压缩过程， 有效的减少了后序气体压缩功耗； 经压 缩得到的气相和液相混合工质流股分别进入换热器组的不同通道节流换热， 相对传统工艺来 说省去了末级液体泵， 且采用多级换热使整个过程中热流股和冷流股的换热曲线更为匹配； 末级气相经节流后的返流复热后进入冷剂分离器， 可有效避免冷箱积液。
本发明涉及采用单一混合工质制冷液化天然气的装置， 其包括混合冷剂压缩系统和冷箱 系统， 其中混合制冷剂的压缩系统采用二段式混合工质压缩机压缩， 包括一台二段式混合工 质压缩机、 两台冷却器、 两台气液分离器和一台液体泵， 冷箱系统包括一组板翅式换热器组 (二级换热）、 两台气液分离器 （包括一台重烃分离器和一台冷剂分离器） 和两台节流装置； 混合工质和天然气在冷箱系统中完成整个换热过程。
在混合冷剂压缩系统中， 压缩机一段出口连接一级冷却器， 一级冷却器再与一级气液分 离器连接， 一级气液分离器气相端连接二段压缩， 一级气液分离器底部液相端连接液体泵， 液体泵出口与二段压缩出口汇合后连接二级冷却器， 二级冷却器再与二级气液分离器连接， 二级气液分离器顶部气相端与换热器组第一换热通道连接； 二级气液分离器底部液相端与换 热器组第二换热通道连接；
在冷箱系统中， 由混合冷剂压缩系统来的二级气液分离器液相端通过换热器组中的第二 换热通道连接第一节流装置的一端， 第一节流装置的另一端连接换热器组的第三换热通道后 连接一段压缩； 二级气液分离器顶部得到的气相端通过换热器组第一换热通道预冷， 再与第 二节流装置一端连接， 第二节流装置另一端连接换热器组第四换热通道后连接冷剂分离器； 天然气管道通过换热器组第五换热通道连接重烃分离器， 重烃分离器顶部气相端依次通过换 热器组其余各级换热器后送入 LNG储罐，重烃分离器底部液相作为液化石油气（LPG)获得。
本发明所述二段式混合工质压缩系统的装置， 在其混合冷剂压缩系统中， 压缩机一段出 口气体进入一级冷却器冷却后通过一级气液分离器分离， 分离后的气相继续进入二段压缩， 分离后的液相经液体泵加压后与二段压缩后的热气体汇合， 经二级冷却器冷却后进入二级气 液分离器分离， 分离后的气相进入下游换热器的第一换热通道（气相通道）； 二级气液分离器 底部得到的液体分别进入下游换热器的第二液相换热通道。 在冷箱系统中， 由冷剂压缩系统 二级气液分离器底部来的液体冷剂进入换热器组预冷后通过第一节流装置， 节流后的该流股 进入冷剂分离器中部； 由二级气液分离器顶部来的气相冷剂经换热器组预冷后经第二节流装 置节流， 节流后的该流股反向进入换热器组中复热至一定温度后引出至冷剂分离器中部， 与 上述冷却节流后 (出第一节流装置后;)的同样进入冷剂分离器的冷剂汇合， 二者经冷剂分离器 分为气液两相， 出冷剂分离器的气液两相汇合后返回至换热器组中提供冷量。 天然气首先经 过换热器组冷却至一定温度后进入分离器分离， 底部得到重烃组分， 顶部得到的气相部分继 续进入换热器组的其余各级换热器换热， 冷却至过冷状态后得到的 LNG进入 LNG储罐中储 存。
为了便于更清楚地理解本发明， 本发明的装置的技术方案概括如下：
采用单一混合工质制冷液化天然气的装置， 该装置包括混合冷剂压缩系统和冷箱系统， 其中该压缩系统包括二段式混合工质压缩机、 分别与所述二段式混合工质压缩机的第一 段和第二段连接的第一台冷却器和第二台冷却器、 分别与所述第一台冷却器和第二台冷却器 连接的第一台气液分离器和第二台气液分离器和与所述两台气液分离器当中的第一台连接的 一台液体泵，
其中冷箱系统包括：
一组板翅式换热器组， 它包含至少六个换热通道： 第一、 第二、 第三、 第四、 第五和第 六换热通道， 所述第二换热通道和第一换热通道的输入端经由两根管道分别与所述混合冷剂 压缩系统中的第二台气液分离器的液相端和气相端连接， 和第三换热通道的输出端经由管道 连接到第一压缩段；
与所述板翅式换热器组的第二换热通道的输出端连接的第一台节流装置；
与所述板翅式换热器组的第一换热通道的输出端和第四换热通道的输入端连接的第二台 节流装置；
禾口
与所述板翅式换热器组的第三换热通道的输入端、 第四换热通道的输出端和第一台节流 装置连接的冷剂分离器；
与所述板翅式换热器组的一个独立换热通道即第五换热通道连接的一台天然气重烃分离 器，
其中两台气液分离器中的第一台气液分离器的气相端与二段式混合工质压缩机的第二压 缩段连接， 第一台气液分离器的液相端经由液体泵与第二压缩段的出口管道汇合后连接到所 述两台冷却器中的第二台冷却器， 第二台气液分离器的气相端和液相端分别与所述一组板翅 式换热器组的两个换热通道即第一换热通道和第二换热通道的输入端连接； 其中上述第一台 节流装置后连接冷剂分离器， 冷剂分离器的顶部气相端和底部液相端汇合后连接第三换热通 道的输入端， 第三换热通道的输出端与二段式混合工质压缩机的第一段连接， 上述第二节流 装置连接第四换热通道输入端后连接到冷剂分离器， 用于输送净化天然气的管道通过换热器 组的上述独立换热通道即第五换热通道连接到重烃分离器， 重烃分离器的顶部气相端依次通 过换热器组的一个换热通道即第六换热通道后连接到液化天然气储罐。
任选地， 重烃分离器的顶部气相端依次通过换热器组的第六换热通道后进一步通过换热 器组的另外第七换热通道连接到液化天然气储罐。
采用单一混合工质制冷来液化天然气的方法的工艺流程如下：
天然气循环：
净化后的原料天然气首先进入板翅式换热器组进行预冷， 被冷却至 -30°C〜- 80°C后进入 重烃分离器进行气液分离， 由重烃分离器顶部分离出的气相流股继续进入换热器组的其余各 级换热器， 并在其中被冷却至 -130°C〜- 166°C， 得到的液化天然气送入 LNG储罐中储存。
混合冷剂循环：
由 C1〜C5和 N2组成的混合工质， 即选自 Cl、 C2、 C3、 C4和 C5链烷烃和 N2中的四种、 五种或六种， 它们按照任意体积比例或按照大约等同的体积比例， 进入压缩机的入口， 经一 段压缩至 0.6〜1.8MPaA，进入一级冷却器冷却至 30°C〜40°C，再进入一级气液分离器进行气 液分离，一级气液分离器顶部分离出的气体继续进入压缩机的二段入口， 经二段压缩至 1.2〜 5.4MPaA,一级气液分离器底部液相端分离出的液体经液体泵加压至 1.2〜5.4MPaA与二段压 缩出口热气体汇合后， 再进入二级冷却器冷却至 30°C〜40°C， 冷却后的混合工质随后进入二 级气液分离器进行气液分离， 二级气液分离器顶部气体随后进入主换热器组的第一换热通道 参与换热， 二级气液分离器底部分离出的液体进入主换热器组的第二换热通道参与换热； 从混合工质压缩系统二级气液分离器底部引出的液体首先进入换热器组的第二换热通 道， 在其中被预冷至约 -30°C〜- 80°C， 经第一节流阀节流至 0.2〜0.8MPaA后进入冷剂分离器 中部， 由二级气液分离器顶部分离出的混合工质的气相流股通过换热器组的气相通道冷却至 -135 °C〜- 169°C， 再经第二节流阀节流至 0.2〜0.8MPaA后反向进入换热器组为换热器提供冷 量， 复热至 -30°C〜- 80°C后引出换热器组进入冷剂分离器中部， 与二级气液分离器的底部液 相经冷却、 节流后同样进入冷剂分离器的流股汇合， 进入冷剂分离器， 出冷剂分离器的气液 两相汇合后返回至换热器组中提供冷量。 进一步， 出冷剂分离器的气液两相汇合后返回至换 热器组中提供冷量之后， 作为混合冷剂返回到压缩机的一段。 这里， 压力单位 MPaA为兆帕， 绝对压力。
这里已经充分描述了本发明的方法和该方法所使用的装置。
本发明的优点：
1. 对装置的变负荷运转有很好的适应性，末级气相经节流后的返流复热后进入冷剂分离 器， 可有效避免冷箱积液， 从而保证在低负荷工况时， 产品能耗与正常工况能耗接近。
2. 本发明方法中采用了二段式混合冷剂压缩机， 将混合冷剂逐级压缩并逐级分离， 减少 了气体压缩的功耗。
3. 一级气液分离器底部液体流股不参与后续的压缩过程，在一定程度上减少了混合冷剂 配比的波动对压缩机组运行工况的影响程度， 使得整个装置更易于操作。
4. 采用二级换热使得整个换热过程的冷流体和热流体的换热曲线更为匹配，有效减少了 混合冷剂的流量。 附图说明
图 1是现有技术的一种结构图；
图 2是本发明所述混合工质制冷系统的装置配置图。
其中： 1 二段式混合工质压缩机， 6 重烃分离器， 7 冷剂分离器， 21、 22 冷却器， 31、 32 气液分离器， 4、 4' 液体泵， 8 板翅式换热器， 9 LNG储罐， 51、 52 节流阀。 具体实施方式
下面结合附图进一步说明：
天然气循环：
如图 2中所示，净化后的原料天然气首先进入板翅式主换热器组 8第五换热通道中预冷， 被冷却至 -30°C〜- 80°C后进入重烃分离器 6中进行气液分离， 由重烃分离器 6顶部分离出的 气相流股继续进入主换热器组 8 的其余各级换热器 （第六换热通道）， 并在其中被冷却至 -130°C〜- 166°C后， 送入 LNG储罐 9中储存， 重烃分离器底部液相为液化石油气 （LPG)。
混合冷剂循环：
由 C1〜C5和 N2组成的混合工质， 即选自 Cl、 C2、 C3、 C4和 C5链烷烃和 N2中的四种、 五种或六种， 它们按照任意体积比例或按照大约等同的体积比例， 进入压缩机 1的入口， 经 一段压缩至 0.6〜1.8MPaA， 进入一级冷却器 21冷却至 30°C〜40°C， 再进入一级气液分离器 31进行气液分离， 一级气液分离器 31顶部分离出的气体继续进入压缩机的二段入口， 经二 段压缩至 1.2〜5.4MPaA，一级气液分离器 31底部液相端分离出的液体经液体泵 4加压至 1.2〜 5.4MPaA与二段压缩出口热气体汇合后， 再进入二级冷却器 22冷却至 30°C〜40°C， 冷却后 的混合工质随后进入二级气液分离器 32进行气液分离， 二级气液分离器 32顶部气体随后进 入主换热器组 8的第一换热通道参与换热，二级气液分离器 32底部分离出的液体进入主换热 器组 8的第二换热通道参与换热；
从混合工质压缩系统二级气液分离器 32 底部引出的液体首先进入换热器组的第二换热 通道， 在其中被预冷至约 -30°C〜- 80°C， 经节流阀 51节流至 0.2〜0.8MPaA后进入冷剂分离 器 7;由二级气液分离器 32顶部分离出的混合工质的气相流股通过换热器组 8的气相通道 (第 一换热通道） 冷却至 -135 °C〜- 169°C， 再经节流阀 52节流至 0.2〜0.8MPaA后反向进入换热 器组 8第四换热通道， 复热至 -30°C〜- 80°C后引出换热器组进入冷剂分离器 7中部， 与二级 气液分离器 32的液相经冷却、节流后产生的流股汇合， 出冷剂分离器的顶部气相与底部液相 两相汇合后返回至换热器组第三换热通道中提供冷量之后， 作为混合冷剂返回到压缩机的一 段。

Claims

权利 要 求
1、采用单一混合工质制冷液化天然气的装置，该装置包括混合冷剂压缩系统和冷箱系统， 其中该压缩系统包括二段式混合工质压缩机、 分别与所述二段式混合工质压缩机的第一 段和第二段连接的第一台冷却器和第二台冷却器、 分别与所述第一台冷却器和第二台冷却器 连接的第一台气液分离器和第二台气液分离器和与所述两台气液分离器当中的第一台连接的 一台液体泵，
其中冷箱系统包括：
一组板翅式换热器组， 它包含至少六个换热通道： 第一、 第二、 第三、 第四、 第五和第 六换热通道， 所述第二换热通道和第一换热通道的输入端经由两根管道分别与所述混合冷剂 压缩系统中的第二台气液分离器的液相端和气相端连接， 和第三换热通道的输出端经由管道 连接到第一压缩段；
与所述板翅式换热器组的第二换热通道的输出端连接的第一台节流装置；
与所述板翅式换热器组的第一换热通道的输出端和第四换热通道的输入端连接的第二台 节流装置；
禾口
与所述板翅式换热器组的第三换热通道的输入端、 第四换热通道的输出端和第一台节流 装置连接的冷剂分离器；
与所述板翅式换热器组的一个独立换热通道即第五换热通道连接的一台天然气重烃分离 器，
其中两台气液分离器中的第一台气液分离器的气相端与二段式混合工质压缩机的第二压 缩段连接， 第一台气液分离器的液相端经由液体泵与第二压缩段的出口管道汇合后连接到所 述两台冷却器中的第二台冷却器， 第二台气液分离器的气相端和液相端分别与所述一组板翅 式换热器组的两个换热通道即第一换热通道和第二换热通道的输入端连接； 其中上述第一台 节流装置后连接冷剂分离器， 冷剂分离器的顶部气相端和底部液相端汇合后连接第三换热通 道的输入端， 第三换热通道的输出端与二段式混合工质压缩机的第一段连接， 上述第二节流 装置连接第四换热通道输入端后连接到冷剂分离器， 用于输送净化天然气的管道通过换热器 组的上述独立换热通道即第五换热通道连接到重烃分离器， 重烃分离器的顶部气相端依次通 过换热器组的一个换热通道即第六换热通道后连接到液化天然气储罐。
2、 根据权利要求 1所述的采用单一混合工质制冷液化天然气的装置， 特征在于： 重烃分离器的顶部气相端依次通过换热器组的第六换热通道后进一步通过换热器组的另 外第七换热通道连接到液化天然气储罐。
3、采用单一混合工质制冷来液化天然气的方法， 其特征在于： 该方法包括天然气循环和 混合冷剂循环：
天然气循环：
净化后的原料天然气首先进入板翅式换热器组进行预冷， 被冷却至 -30°C〜- 80°C后进入 重烃分离器进行气液分离， 由重烃分离器顶部分离出的气相流股继续进入换热器组的其余各 级换热器， 并在其中被冷却至 -130°C〜- 166°C， 得到的液化天然气送入 LNG储罐中储存； 混合冷剂循环：
由 C1〜C5和 N2组成的混合工质进入压缩机的入口， 经一段压缩至 0.6〜1.8MPaA， 进 入一级冷却器冷却至 30°C〜40°C， 再进入一级气液分离器进行气液分离， 一级气液分离器顶 部分离出的气体继续进入压缩机的二段入口， 经二段压缩至 1.2〜5.4MPaA， 一级气液分离器 底部液相端分离出的液体经液体泵加压至 1.2〜5.4MPaA与二段压缩出口热气体汇合后，再进 入二级冷却器冷却至 30°C〜40°C，冷却后的混合工质随后进入二级气液分离器进行气液分离， 二级气液分离器顶部气体随后进入主换热器组的第一换热通道参与换热， 二级气液分离器底 部分离出的液体进入主换热器组的第二换热通道参与换热；
从混合工质压缩系统二级气液分离器底部引出的液体首先进入换热器组的第二换热通 道， 在其中被预冷至约 -30°C〜- 80°C， 经第一节流阀节流至 0.2〜0.8MPaA后进入冷剂分离器 中部， 由二级气液分离器顶部分离出的混合工质的气相流股通过换热器组的气相通道即第一 换热通道冷却至 -135 °C〜- 169°C， 再经第二节流阀节流至 0.2〜0.8MPaA后反向进入换热器组 第四换热通道为换热器提供冷量， 复热至 -30°C〜- 80°C后引出换热器组也进入冷剂分离器中 部， 与出第一节流阀后的同样进入冷剂分离器的流股汇合， 出冷剂分离器的气液两相汇合后 返回至换热器组第三换热通道中为换热器组提供冷量， 然后作为混合冷剂返回到压缩机的一 段。
4. 根据权利要求 3所述的采用单一混合工质制冷来液化天然气的方法， 其特征在于， 由 C1〜C5和 N2组成的混合工质为选自 Cl、 C2、 C3、 C4和 C5链烷烃和 N2中的四种、 五种或 六种， 每一种按照任意体积比例或按照大约等同的体积比例。
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