CN110762946A - Skid-mounted natural gas treatment device - Google Patents

Skid-mounted natural gas treatment device Download PDF

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Publication number
CN110762946A
CN110762946A CN201911115103.1A CN201911115103A CN110762946A CN 110762946 A CN110762946 A CN 110762946A CN 201911115103 A CN201911115103 A CN 201911115103A CN 110762946 A CN110762946 A CN 110762946A
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China
Prior art keywords
inlet
outlet
heat exchanger
natural gas
tank
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Pending
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CN201911115103.1A
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Chinese (zh)
Inventor
陈康
王福勃
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Dongying Helishi Gas Co Ltd
Shandong Helishi Petrochemical Technology Development Co Ltd
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Dongying Helishi Gas Co Ltd
Shandong Helishi Petrochemical Technology Development Co Ltd
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Priority to CN201911115103.1A priority Critical patent/CN110762946A/en
Publication of CN110762946A publication Critical patent/CN110762946A/en
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    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0295—Start-up or control of the process; Details of the apparatus used, e.g. sieve plates, packings
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/10—Processes or apparatus using other separation and/or other processing means using combined expansion and separation, e.g. in a vortex tube, "Ranque tube" or a "cyclonic fluid separator", i.e. combination of an isentropic nozzle and a cyclonic separator; Centrifugal separation
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/60—Natural gas or synthetic natural gas [SNG]
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/24—Multiple compressors or compressor stages in parallel
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/42—Modularity, pre-fabrication of modules, assembling and erection, horizontal layout, i.e. plot plan, and vertical arrangement of parts of the cryogenic unit, e.g. of the cold box
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/70—Processing device is mobile or transportable, e.g. by hand, car, ship, rocket engine etc.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention relates to a skid-mounted natural gas treatment device which is integrally skid-mounted and delivered, is convenient and quick to assemble on site, is convenient to transport, adopts a convenient and quick construction mode and a safe and reliable operation mode, adopts two-stage compression and two-stage separation, can efficiently recover oil field associated gas resources aiming at different oil area scales and gathering and transportation conditions, is convenient for subsequent harmless treatment, simultaneously carries out deep processing on downstream products, fully utilizes the resources, and is beneficial to oil field production and safety management.

Description

Skid-mounted natural gas treatment device
Technical Field
The invention relates to the field of natural gas treatment, in particular to a skid-mounted natural gas treatment device.
Background
During the production process of the oil field, part of oil associated gas is generated while oil is extracted. The main component of the petroleum associated gas is C1Containing both a moiety C2、C3、C4And C5 +Heavy hydrocarbons, such as methanol, ethanol; like petroleum, associated gas is also a resource with high economic value, but because of the limitation of the scale of oil areas and gathering and transportation conditions, particularly for some remote oil areas, associated gas is not reasonably utilized(ii) a Because the fuel cannot be stored, one part of the fuel is usually directly used as crude oil heating fuel, and the other part of the fuel is emptied and burned, even is allowed to volatilize and is discharged to the air. The disposal mode brings certain potential safety hazard to oil field well sites and gathering and transportation stations, causes air pollution of oil areas, and is huge resource waste. Skid-mounted natural gas processing apparatus to its convenient and fast's mode of construction and safe and reliable operation mode, to different oil district scales and gathering and transportation condition, can both high-efficiently retrieve oil field associated gas resource, be convenient for follow-up carry out innocent treatment, carry out the deep-processing of low reaches product simultaneously, make the resource can make full use of, be favorable to oil field production and safety control.
Disclosure of Invention
The invention aims to provide a skid-mounted natural gas treatment device which is convenient to move and install and can efficiently recover oil field associated gas resources.
The technical scheme for solving the technical problems is as follows: a skid-mounted natural gas treatment device is installed on a plurality of skid blocks and comprises a natural gas compressor unit, a second water cooler, a first-stage liquid separation tank, a first heat exchange cooling device unit and a second-stage liquid separation tank, wherein the natural gas compressor unit comprises a first compression chamber and a second compression chamber, an inlet of the first compression chamber is used for introducing natural gas, an outlet of the first compression chamber is communicated with an inlet of the first-stage liquid separation tank through the second water cooler, a gas phase outlet of the first-stage liquid separation tank is communicated with an inlet of the second compression chamber, an inlet of the second compression chamber is communicated with an inlet of the second-stage liquid separation tank through the first heat exchange cooling device unit, and a gas phase outlet of the second-stage liquid separation tank is used for discharging the treated natural gas.
The invention has the beneficial effects that: the natural gas treatment device is integrally skid-mounted to leave a factory, is simple and quick to assemble on site, is convenient to transport, can efficiently recover oil field associated gas resources according to different oil area scales and gathering and transportation conditions in a convenient and quick building mode and a safe and reliable operation mode. The natural gas treatment in the prior art usually adopts primary compression and water cooling treatment, the separation is not thorough, and the oilfield associated gas cannot be effectively utilized. The skid-mounted natural gas treatment device disclosed by the invention adopts two-stage compression and two-stage separation, can effectively obtain purified dry gas and oil field mixed hydrocarbon products, is simple in process, compact in equipment and convenient to operate, and facilitates subsequent harmless treatment and deep processing of downstream products.
On the basis of the technical scheme, the invention can be further improved as follows.
Further, still include air exhaust device, desulfurizing tower group and raw materials buffer tank, air exhaust device's import and feed gas admission line are connected, its export with the access connection of desulfurizing tower group, the export of desulfurizing tower group with the access connection of raw materials buffer tank, the gaseous phase export of raw materials buffer tank with the access connection of the first compression chamber of natural gas compressor unit.
The beneficial effect of adopting the further scheme is that: the air extractor sucks the feed gas into the system and carries out desulfurization in the desulfurizing tower set, gas-liquid separation is preliminarily realized in the raw material buffer tank, and the gas phase is discharged from a gas phase outlet of the raw material buffer tank and enters the natural gas compressor set for compression.
Further, air exhaust device includes air exhauster, first water cooler and air exhauster buffer tank, the import and the feed gas admission line of air exhauster are connected, its export with the heat medium access connection of first water cooler, the heat medium export of first water cooler with the access connection of air exhauster buffer tank, the gas phase outlet of air exhauster buffer tank with the access connection of desulfurizing tower group.
The beneficial effect of adopting the further scheme is that: the air extractor pumps the raw material gas, the raw material gas is cooled by the first water cooler, part of gaseous mixed hydrocarbon is cooled and liquefied, then the gaseous mixed hydrocarbon enters the air extractor buffer tank for gas-liquid separation, and the gas phase enters the subsequent desulfurization tower set.
Further, the desulfurizing tower group comprises a first desulfurizing tower and a second desulfurizing tower which are connected in parallel or in series, the outlet of the air extracting device is connected with the inlet of the first desulfurizing tower and/or the inlet of the second desulfurizing tower, and the outlet of the first desulfurizing tower and/or the outlet of the second desulfurizing tower are connected with the inlet of the raw material buffer tank.
The beneficial effect of adopting the further scheme is that: the two desulfurizing towers can be connected in series or in parallel, the desulfurizing efficiency is high when the two desulfurizing towers are connected in parallel, the desulfurizing agent in one of the desulfurizing towers can be conveniently replaced, and the desulfurizing is more thorough when the two desulfurizing towers are connected in series. The connection mode of the two desulfurizing towers can be flexibly selected according to the content of sulfur in the product.
Further, first heat transfer heat sink group includes reboiler, third water cooler and first heat exchanger, the export of second compression chamber with the gaseous phase access connection of reboiler, the gaseous phase export of reboiler with the heat medium access connection of third water cooler, the heat medium export of third water cooler with the heat medium access connection of first heat exchanger, the heat medium export of first heat exchanger with the access connection of second branch fluid reservoir.
The beneficial effect of adopting the further scheme is that: the boosted natural gas flows through a reboiler to provide a heat source, is cooled through a third water cooler, is cooled to 15 ℃ through a first heat exchanger, is subjected to gas-liquid separation, and then enters a second-stage liquid separation tank to separate a gas phase and a liquid phase.
Further, the device also comprises an electric heater, a first drying tower, a second drying tower and a second heat exchange cooling device group; the gas phase outlet of the second liquid separation tank is respectively connected with the inlet of the first drying tower or the inlet of the second drying tower, the outlet of the first drying tower or the outlet of the second drying tower is connected with the inlet of the second heat exchange cooling device group, the outlet of the second heat exchange cooling device group is connected with the refrigerant inlet of the first heat exchanger, the refrigerant outlet of the first heat exchanger is connected with the purified dry gas external transmission pipeline, the refrigerant outlet of the first heat exchanger is also respectively connected with the inlet of the electric heater or the outlet of the electric heater through a pipeline, the outlet of the electric heater is respectively connected with the outlet of the first drying tower or the outlet of the second drying tower, and the inlet of the first drying tower or the inlet of the second drying tower are both connected with the purified dry gas external transmission pipeline.
The beneficial effect of adopting the further scheme is that: and the separated gas phase is dried by a drying tower and subjected to cooling separation by a second heat exchange cooling device set, and cooling capacity is provided for the first heat exchanger. And after desorption is finished, the purified dry gas discharged from the refrigerant outlet of the first heat exchanger directly reversely enters the first drying tower or the second drying tower, so that the temperature reduction and cooling of the molecular sieve are realized.
Further, the first heat exchange and cooling device group also comprises a rectifying tower, and the second heat exchange and cooling device group comprises a second heat exchanger, a front-cooling heat exchanger, an evaporation heat exchanger, a rear-cooling heat exchanger, a low-temperature separator and a refrigerant circulating device; the outlet of the first drying tower or the outlet of the second drying tower is connected with the heat medium inlet of the second heat exchanger, the heat medium outlet of the second heat exchanger is connected with the heat medium inlet of the front cooling heat exchanger, the heat medium outlet of the front cooling heat exchanger is connected with the heat medium inlet of the evaporating heat exchanger, the heat medium outlet of the evaporating heat exchanger is connected with the heat medium inlet of the rear cooling heat exchanger, the heat medium outlet of the rear cooling heat exchanger is connected with the inlet of the low-temperature separator, the gaseous cold phase outlet of the low-temperature separator is connected with the refrigerant inlet of the rear cooling heat exchanger, the refrigerant outlet of the rear cooling heat exchanger is connected with the refrigerant inlet of the front cooling heat exchanger, the refrigerant outlet of the front cooling heat exchanger is connected with the refrigerant inlet of the first heat exchanger, and the outlet of the refrigerant circulating device is connected with the refrigerant inlet of the evaporating heat exchanger, the refrigerant outlet of the evaporation heat exchanger is connected with the inlet of the refrigerant circulating device; a liquid phase outlet of the cryogenic separator is connected with an inlet of the rectifying tower, a liquid phase outlet of the rectifying tower is connected with a liquid phase inlet of the reboiler, and a liquid phase outlet of the reboiler is connected with an external mixed hydrocarbon storage tank; and the gas phase outlet of the rectifying tower is connected with the inlet of the first liquid separation tank.
The beneficial effect of adopting the further scheme is that: the material from the drying tower is sequentially cooled to-51 ℃ by a second heat exchanger, a front cooling heat exchanger, an evaporation heat exchanger and a rear cooling heat exchanger, and then is cooledIntroducing into a cryogenic separator to separate a liquid phase C3 +The component is removed with C from the component by a rectifying tower2Then the gas phase enters an external mixed hydrocarbon storage tank to be connected, dry gas components of the low-temperature separator are subjected to expansion thermal separation, the temperature of the gaseous cold phase is-70 ℃, and the gaseous cold phase enters a back-cooling heat exchanger and a front-cooling heat exchanger in turn to recover cold.
Furthermore, the low-temperature separator comprises a low-temperature separator body and a cold and dry gas heat separation device arranged in the low-temperature separator body, wherein the cold and dry gas heat separation device is a speed generator or a vortex tube.
The beneficial effect of adopting the further scheme is that: the vortex tube or the velocity generator is adopted to replace the function of the existing expander, so that the cold and dry gas thermal separation in a cryogenic state is realized, and the cost performance is high; the stability of production operation under the device field work condition has been improved, the operating rate and the operating efficiency of device have been improved.
Further, still include import buffer tank and flowing back water diversion tank, the import of import buffer tank with feed gas inlet line connects, the export of import buffer tank, the liquid phase export of air extractor buffer tank the liquid phase export of raw materials buffer tank with the liquid phase export of a grade fluid reservoir all with the liquid phase access connection of flowing back water diversion tank, the sewage outlet and the external sewage jar of flowing back water diversion tank are connected, the export of first drying tower or the export of second drying tower with the pressurized gas access connection of flowing back water diversion tank.
The beneficial effect of adopting the further scheme is that: the inlet buffer tank plays a role in stabilizing the air pressure and the flow velocity of a raw material gas inlet pipeline, simultaneously can realize the separation of oil, water and mechanical impurities, the separated light oil enters the liquid discharge water separation tank, the liquid discharge water separation tank separates oily sewage from light oil, and the oily sewage enters the external sewage tank.
Further, the natural gas compressor unit comprises a first natural gas compressor and a second natural gas compressor, wherein the first natural gas compressor and the second natural gas compressor are arranged in parallel and are provided with the first compression chamber and the second compression chamber.
The beneficial effect of adopting the further scheme is that: two natural compressors are connected in parallel, so that the working efficiency is ensured, and the equipment maintenance is convenient.
The invention has the beneficial effects that: the skid-mounted natural gas treatment device is mainly used for carrying out harmless treatment and comprehensive utilization on petroleum associated gas resources of different scales in remote oil areas, processing and producing various socialized products, realizing market sale on the spot and creating economic benefits. Aiming at different gas qualities and gas amounts in an oil area, a low-temperature separation or cold oil absorption method is adopted to carry out the treatment of dehydration, heavy hydrocarbon removal and acid gas removal, and two products of purified dry gas and oil field hydrocarbon mixture are obtained preliminarily; the process can adopt the following two modes, and the more common mode is as follows: two-stage compression (0.12 → 0.75 → 2.15MPa), two-stage refrigeration (shallow cooling plus a speed generator or a vortex tube), two-stage separation, and is characterized by simple process, compact equipment and convenient operation; the other mode is as follows: adopts two-stage compression (0.12 → 0.75 → 2.15MPa), one-stage refrigeration (shallow cooling) and cold oil absorption, and is characterized by high light hydrocarbon yield (C)3 +The yield is more than or equal to 90 percent). The complete natural gas treatment device is delivered from a factory in a whole skid-mounted mode, and is 1-3 multiplied by 104Nm3The device group prying of/d comprises: four production groups pry (7.2 multiplied by 2.5 multiplied by 2.7m), a main control room, an air compressor room (7 multiplied by 2.5 multiplied by 2.6m) and a raw material gas buffer tank (30 m)3) A product tank (50 m)3) A complete set of automatic control system and a complete set of power distribution system; 4 to 8 x 104Nm3The number of devices per unit is two, 50m3The product can and the skid-mounted structure are increased in the same proportion (8.8 multiplied by 3.2 multiplied by 3 m). The mixed hydrocarbon product is directly loaded on a vehicle for external sale after being stored, or is further processed into liquefied petroleum gas and stable light hydrocarbon products; purifying the dry gas product, returning one part of the dry gas product as fuel gas to an oil field for heating crude oil, and outputting the other part of the dry gas product to a gas transmission pipe network; natural gas power generation devices can be configured according to the specific conditions of various regions, and natural gas resources are converted into electric energy for external supply; or matched with CNG and LNG devices, and processed into market products for sale. The complete equipment is designed according to field operation conditions, and the field assembly is simple, convenient and quick; the investment of project operation is saved and the effect is fast.
The device provided by the invention is safe, efficient and stable in operation, and plays an important role in realizing closed exploitation in the oil-propelling region, eliminating potential safety hazards, saving energy, reducing emission, protecting environment and the like. According to the overall arrangement of resource-saving enterprises established by oil field companies, the skid-mounted natural gas treatment device has a good prospect for the application of oil and gas fields with large mining areas, scattered mining areas and high gathering and transportation difficulty, and can generate greater economic and social benefits.
The natural gas treatment device is suitable for the working conditions of 'gas source dispersion and field operation' in remote oil areas, the production device has the advantages of complete process (low energy consumption), compact equipment (skid-mounted type) and high automation level (PLC whole process control), and the technical characteristics are mainly embodied in the following aspects:
1. the device has compact integral structure, and is integrally skid-mounted and precise in structure on the premise of meeting the design specification of a five-level natural gas station; the space and the occupied area are saved to the maximum extent, and the skid-mounted combined structure and the direction can be adjusted according to the conditions of the site topography and the landform.
2. The whole set of production device is designed for movable vehicle-mounted skid mounting and can be conveniently moved along with the change of an air source concentration area; the plug-in type signal cable, the power cable and the metal process hose are connected in a prying manner, so that the field assembly workload is greatly reduced. No special condition exists, water, electricity and gas conditions exist, and after the device falls to the ground on site, the installation, debugging and commissioning are generally completed in 15 working days.
3. All equipment is designed according to the field operation standard, all-weather outdoor operation is realized, complex logistics support and public engineering configuration are not needed, and the device is matched, refined and simplified.
4. Direct-fired naked flame equipment such as a non-heating furnace, a heating medium furnace and the like and strong and weak electric equipment are all in explosion-proof design, meet the design specification of petroleum and natural gas engineering and have good safety performance.
5. According to different gas quality conditions of a gas source, different process configurations of secondary compression and low-temperature condensation or cold oil absorption can be adopted, and efficient gas-liquid separation and absorption are carried out at a process terminal under the working conditions of 35 ℃ below zero and 2.0MPa, so that the satisfactory yield of light hydrocarbon is obtained; can meet various process requirements of light hydrocarbon production, natural gas purification, commodity natural gas pipeline transportation or CNG, LNG processing and the like. The device has large operation flexibility, and can allocate the equipment load according to the actual working condition to realize the optimal combination of energy consumption and benefit.
6. A physical low-temperature separation process is adopted, and the production process is totally closed; no three wastes discharge and no environmental pollution.
7. According to project conditions, the purified dry gas can be directly output, and can also be used for natural gas power generation or further processed into CNG and LNG products; the mixed hydrocarbon product is used as a crude chemical raw material, is directly loaded and sold, has a certain scale (more than or equal to 15t/d) of yield, can be additionally provided with a rectification facility, and is further processed into liquefied petroleum gas and stable light hydrocarbon products. Realizing greater economic benefit.
8. The vortex tube or the velocity generator is adopted to replace the function of the expander, so that the cold and dry gas thermal separation in a cryogenic state is realized, and the cost performance is high; the stability of production operation under the device field work condition has been improved, the operating rate and the operating efficiency of device have been improved.
9. The water cooler and the heat exchanger both adopt high-efficiency antirust aluminum plate fin type heat exchangers, cold and heat exchange of multiple streams of logistics is reasonably arranged, heat sources and medium cold energy are fully utilized, energy consumption is reduced, and device operation cost is reduced.
10. A plurality of water coolers are installed in a centralized mode to form a centralized water cooler, and the centralized water cooler is designed in a dry and wet mode and is suitable for production operation under the water shortage condition.
Drawings
FIG. 1 is a schematic diagram of a skid-mounted natural gas processing plant of the present invention;
FIG. 2 is an enlarged view of area A of FIG. 1;
FIG. 3 is an enlarged view of area B of FIG. 1;
FIG. 4 is an enlarged view of area C of FIG. 1;
FIG. 5 is an enlarged view of region D of FIG. 1;
FIG. 6 is a front view of the velocity generator;
FIG. 7 is a cross-sectional view of E-E of FIG. 6;
fig. 8 is a schematic top view of a skid-mounted natural gas processing apparatus according to the present invention.
In the drawings, the components represented by the respective reference numerals are listed below:
1. an air extractor, 2, an air extractor buffer tank, 3, a first desulfurization tower, 4, a second desulfurization tower, 5, a raw material buffer tank, 6, a first natural gas compressor, 7, a second natural gas compressor, 8, a first-stage liquid separation tank, 9, a reboiler, 10, a second-stage liquid separation tank, 11, a first drying tower, 12, a second drying tower, 13, a front cooling heat exchanger, 14, an evaporation heat exchanger, 15, a rear cooling heat exchanger, 16, a low-temperature separator, 17, a rectification tower, 18, an electric heater, 19, an inlet buffer tank, 20, a liquid discharge water separation tank, 21, a jet ejector, 22, an oil separator, 23, a refrigeration compressor, 24, a refrigerant storage tank, 25, an economizer, 26, a velocity generator, 261, a gaseous hot phase outlet, 262, an air inlet, 263, a bolt, 264, an end cover, 265, a main shell, 266, an air outlet pipe, 267, a balance pipe, 27, a concentrator, 301, and a first water cooler, 302. the system comprises a second water cooler, 303, a third water cooler, 304, a fourth water cooler, 305, a fifth water cooler, 306, a sixth water cooler, 204, a second heat exchanger, 205, a first heat exchanger, 102, a junction station, 103 and a condensate cooler.
Detailed Description
The principles and features of this invention are described below in conjunction with examples which are set forth to illustrate, but are not to be construed to limit the scope of the invention.
As shown in fig. 1 to 8, this embodiment provides a skid-mounted natural gas processing apparatus, which is installed on a plurality of skid blocks, and includes a natural gas compressor unit, a second water cooler 302, a primary liquid separating tank 8, a first heat exchange temperature reduction device group, and a secondary liquid separating tank 10, where the natural gas compressor unit includes a first compression chamber and a second compression chamber, an inlet of the first compression chamber is used for introducing natural gas, an outlet of the first compression chamber is communicated to an inlet of the primary liquid separating tank 8 through the second water cooler 302, a gas phase outlet of the primary liquid separating tank 8 is communicated to an inlet of the second compression chamber, an inlet of the second compression chamber is communicated to an inlet of the secondary liquid separating tank 10 through the first heat exchange temperature reduction device group, and a gas phase outlet of the secondary liquid separating tank 10 is used for discharging the treated natural gas.
As a further scheme of this embodiment, still include air exhaust device, desulfurizing tower group and raw materials buffer tank 5, air exhaust device's import and feed gas inlet line are connected, its export with the access connection of desulfurizing tower group, the export of desulfurizing tower group with the access connection of raw materials buffer tank 5, the gaseous phase export of raw materials buffer tank 5 with the access connection of the first compression chamber of natural gas compressor unit.
As a further scheme of this embodiment, the air extraction device includes air extractor 1, first water cooler 301 and air extractor buffer tank 2, the import of air extractor 1 is connected with feed gas inlet line, its export with the heat medium access connection of first water cooler 301, the heat medium export of first water cooler 301 with the access connection of air extractor buffer tank 2, the gaseous phase export of air extractor buffer tank 2 with the access connection of desulfurizing tower group.
As a further scheme of this embodiment, the desulfurization tower group includes a first desulfurization tower 3 and a second desulfurization tower 4 connected in parallel or in series, an outlet of the air extraction device is connected to an inlet of the first desulfurization tower 3 and/or an inlet of the second desulfurization tower 4, and an outlet of the first desulfurization tower 3 and/or an outlet of the second desulfurization tower 4 are both connected to an inlet of the raw material buffer tank 5.
As a further scheme of this embodiment, the first heat exchange and temperature reduction device set comprises a reboiler 9, a third water cooler 303 and a first heat exchanger 205, an outlet of the second compression chamber is connected with a gas phase inlet of the reboiler 9, a gas phase outlet of the reboiler 9 is connected with a heat medium inlet of the third water cooler 303, a heat medium outlet of the third water cooler 303 is connected with a heat medium inlet of the first heat exchanger 205, and a heat medium outlet of the first heat exchanger 205 is connected with an inlet of the second fraction liquid tank 10.
As a further scheme of this embodiment, the system further includes an electric heater 18, a first drying tower 11, a second drying tower 12, and a second heat exchange temperature reduction device group; the gas phase outlet of the second fractional liquid tank 10 is respectively connected with the inlet of the first drying tower 11 or the inlet of the second drying tower 12, the outlet of the first drying tower 11 or the outlet of the second drying tower 12 is connected with the inlet of the second heat exchange temperature reduction device set, the outlet of the second heat exchange temperature reduction device group is connected with the refrigerant inlet of the first heat exchanger 205, the refrigerant outlet of the first heat exchanger 205 is connected to the purified dry gas outgoing pipeline, the refrigerant outlet of the first heat exchanger 205 is further connected to the inlet of the electric heater 18 or the outlet of the electric heater 18 through a pipeline, the outlet of the electric heater 18 is connected to the outlet of the first drying tower 11 or the outlet of the second drying tower 12, and the inlet of the first drying tower 11 or the inlet of the second drying tower 12 is connected with a purified dry gas outward conveying pipeline.
As a further scheme of this embodiment, the first heat exchange and temperature reduction device set further includes a rectification tower 17, and the second heat exchange and temperature reduction device set includes a second heat exchanger 204, a front-cooling heat exchanger 13, an evaporation heat exchanger 14, a rear-cooling heat exchanger 15, a low-temperature separator 16, and a refrigerant circulating device; an outlet of the first drying tower 11 or an outlet of the second drying tower 12 is connected with a heat medium inlet of the second heat exchanger 204, a heat medium outlet of the second heat exchanger 204 is connected with a heat medium inlet of the front cooling heat exchanger 13, a heat medium outlet of the front cooling heat exchanger 13 is connected with a heat medium inlet of the evaporation heat exchanger 14, a heat medium outlet of the evaporation heat exchanger 14 is connected with a heat medium inlet of the rear cooling heat exchanger 15, a heat medium outlet of the rear cooling heat exchanger 15 is connected with an inlet of the low-temperature separator 16, a gaseous cold phase outlet of the low-temperature separator 16 is connected with a refrigerant inlet of the rear cooling heat exchanger 15, a refrigerant outlet of the rear cooling heat exchanger 15 is connected with a refrigerant inlet of the front cooling heat exchanger 13, a refrigerant outlet of the front cooling heat exchanger 13 is connected with a refrigerant inlet of the first heat exchanger 205, an outlet of the refrigerant circulating device is connected with an inlet of the evaporation heat exchanger 14, a refrigerant outlet of the evaporation heat exchanger 14 is connected with an inlet of the refrigerant circulating device; a liquid phase outlet of the low-temperature separator 16 is connected with an inlet of the rectifying tower 17, a liquid phase outlet of the rectifying tower 17 is connected with a liquid phase inlet of the reboiler 9, and a liquid phase outlet of the reboiler 9 is connected with an external mixed hydrocarbon storage tank; the gas phase outlet of the rectifying tower 17 is connected with the inlet of the first liquid separation tank 8.
As a further solution of this embodiment, the low-temperature separator 16 includes a low-temperature separator body and a cold-dry gas thermal separation device disposed inside the low-temperature separator body, where the cold-dry gas thermal separation device is a velocity generator or a vortex tube.
As a further scheme of this embodiment, still include import buffer tank 19 and flowing back distributive tank 20, the import of import buffer tank 19 with feed gas inlet line connects, the export of import buffer tank 19, the liquid phase export of air extractor buffer tank 2, the liquid phase export of raw materials buffer tank 5 and the liquid phase export of first fraction liquid jar 8 all with the liquid phase access connection of flowing back distributive tank 20, the sewage outlet of flowing back distributive tank 20 is connected with external sewage tank, the export of first drying tower 11 or the export of second drying tower 12 with the pressure gas inlet connection of flowing back distributive tank 20.
As a further scheme of this embodiment, the natural gas compressor unit includes a first natural gas compressor 6 and a second natural gas compressor 7, where the first natural gas compressor 6 and the second natural gas compressor 7 are arranged in parallel and both have the first compression chamber and the second compression chamber.
As shown in fig. 1-5, the specific working process of the present invention is as follows:
the feed gas from the combined plant comprises about 70% C110% of C 220% of C3、C4And C5 +Heavy hydrocarbons, and components such as water, carbon dioxide, hydrogen sulfide, nitrogen, mechanical impurities. As shown in fig. 1 and 2, a raw material gas inlet pipeline conveys raw material gas from a combined station to an air extractor 1, the raw material gas is cooled by a first water cooler 301 and then enters an air extractor buffer tank 2, the raw material gas is subjected to gas-liquid separation in the air extractor buffer tank 2, as shown in fig. 1 and 3, the gas phase is discharged and then enters a first desulfurizing tower 3 and a second desulfurizing tower 4 which are connected in series or in parallel, the gas phase is subjected to desulfurization and then enters a raw material buffer tank 5, the gas-liquid separation in the raw material buffer tank 5, the gas phase enters first compression chambers of a first natural gas compressor 6 and a second natural gas compressor 7 for primary compression, the gas is pressurized from 0.12MPa to 0.75MPa, the temperature is reduced from 100 ℃ to 25 ℃ by a second water cooler 302, and flows through a combiner 102 and enters a primary divider 102And a liquid tank 8 for gas-liquid separation in the primary liquid separating tank 8, wherein a gas phase is discharged from a gas phase outlet at the top of the primary liquid separating tank 8, enters a second compression chamber of the first natural gas compressor 6 and the second natural gas compressor 7 for secondary compression, the gas is pressurized from 0.75MPa to 2.15MPa, as shown in fig. 1 and 4, the pressurized natural gas flows through a reboiler 9 to provide a heat source, is cooled through a third water cooler 303, is cooled to 15 ℃ through a first water cooler 205 and then enters a secondary liquid separating tank 10 for gas-liquid separation, the separated gas phase enters a first drying tower 11 or a second drying tower 12 for deep dehydration to below 10PPm, and the drying tower is filled with a 4A type molecular sieve for cyclic heat regeneration. As shown in fig. 1 and 5, the dehydrated natural gas flows through the ejector 21 and then enters the second heat exchanger 204 to recover cold energy and cool down, and then sequentially enters the front-cooling heat exchanger 13, the evaporating heat exchanger 14 and the rear-cooling heat exchanger 15 to cool down to about-51 ℃, the cooled gas-liquid mixed phase enters the low-temperature separator 16 to separate gas and liquid, the low-temperature separator 16 is internally provided with a speed generator 26, the speed generator 26 separates the separated gas phase into a gaseous cold phase (about-70 ℃) and a gaseous hot phase (about-19 ℃), the gaseous cold phase enters the rear-cooling heat exchanger 15 to provide a cold source, the gas phase at the refrigerant outlet of the rear-cooling heat exchanger 15 has a temperature of about-35 ℃, then enters the front-cooling heat exchanger 13 to provide the cold source, the gas phase at the refrigerant outlet of the front-cooling heat exchanger 13 has a temperature of about 15 ℃, and then enters the first heat exchanger 205 from the refrigerant inlet, as shown in fig. 4, a part of the dry gas after heat exchange is used for regeneration of the drying tower, a part of the reverse transportation combination station is used for heating crude oil, and the rest of the gas upwards enters the purified dry gas outward transportation pipeline.
As shown in fig. 5, the refrigerant cycle device includes an oil separator 22, a refrigeration compressor 23, a refrigerant storage tank 24, an economizer 25, a fifth water cooler 305, and a sixth water cooler 306, the refrigerant is propane or freon or liquid ammonia, the refrigerant is stored in the refrigerant storage tank 24, flows through the economizer 25, enters the evaporation heat exchanger 14 to provide a cold source, flows from a refrigerant outlet of the evaporation heat exchanger 14 to the refrigeration compressor 23 to be compressed, then enters the oil separator 22 to separate gas phase and lubricating oil, the gas phase refrigerant is cooled to 35 ℃ by the sixth water cooler 306 to be liquefied, and then enters the refrigerant storage tank 24.
Wherein, the gaseous hot phase (about-19 ℃) separated from the low-temperature separator 16 passes through the second heat exchanger 204 to cool the heating medium flowing through the second heat exchanger, and then a part of the gaseous hot phase passes through the confluence device 102 to enter the first fraction liquid tank 8, and the other part of the gaseous hot phase enters the raw material buffer tank 5.
Wherein, the liquid phase (-51 ℃) separated from the low-temperature separator 16 is discharged and then exchanges heat to-30 ℃ through a refrigerant channel of the condensate cooler 103, and then enters a rectifying tower 17 matched with the reboiler 9 for use, and the gas phase C is separated from the gas phase1And C2The liquid phase enters a first-stage liquid separation tank 8 through a flow combiner 102, the liquid phase and the natural gas flowing through a reboiler 9 exchange heat and are heated to 25 ℃, and the C of the liquid phase3、C4And C5 +And enters a mixed hydrocarbon storage tank along a pipeline.
Specifically, as shown in fig. 3, the first desulfurization tower 3 and the second desulfurization tower 4 connected in series or in parallel may be connected in parallel or in series, and may be reversible when connected in series. The inlet of the first desulfurizing tower 3 and the inlet of the second desulfurizing tower 4 are respectively provided with a first valve F1 and a second valve F2 on a pipeline connected with the gas phase outlet of the air extractor buffer tank 2, the outlet of the first desulfurizing tower 3 and the outlet of the second desulfurizing tower 4 are respectively provided with a fifth valve F5 and a sixth valve F6 on a pipeline connected with the raw material buffer tank 5, the outlet of the first desulfurizing tower 3 and the inlet of the second desulfurizing tower 4 are connected through a pipeline and are provided with a third valve F3 on the pipeline, the inlet of the first desulfurizing tower 3 and the outlet of the second desulfurizing tower 4 are connected through a pipeline and are provided with a fourth valve F4 on the pipeline, the gas phase outlet of the air extractor buffer tank 2 and the inlet of the raw material buffer tank 5 are connected through a pipeline and are provided with a seventh valve F7 on the pipeline.
When the desulfurization treatment is not required, the first valve F1, the second valve F2, the third valve F3, the fourth valve F4, the fifth valve F5 and the sixth valve F6 are closed, the seventh valve F7 is opened, and the gas phase outlet of the aspirator buffer tank 2 is directly communicated with the inlet of the raw material buffer tank 5.
When the first desulfurization tower 3 and the second desulfurization tower 4 are connected in parallel, the third valve F3, the fourth valve F4, and the seventh valve F7 are closed, and the first valve F1, the second valve F2, the fifth valve F5, and the sixth valve F6 are opened. The gas phase discharged from the air extractor surge tank 2 is introduced into the first desulfurizing tower 3 and the second desulfurizing tower 4, respectively, and then introduced into the raw material surge tank 5, respectively. When the desulfurizer in the desulfurizing tower needs to be replaced, any desulfurizing tower can be cut off and replaced on the basis that the two desulfurizing towers are connected in parallel, and particularly, when the desulfurizer in the first desulfurizing tower 3 needs to be replaced, the first valve F1 and the fifth valve F5 are closed; when the desulfurizing agent in the second desulfurizing tower 4 needs to be replaced, the second valve F2 and the sixth valve F6 are closed.
When the first desulfurization tower 3 and the second desulfurization tower 4 are connected in series, two series connection modes can be adopted, wherein the first mode is that natural gas firstly enters the first desulfurization tower 3 and then enters the second desulfurization tower 4, the first valve F1, the third valve F3 and the sixth valve F6 are opened, and the second valve F2, the fourth valve F4, the fifth valve F5 and the seventh valve F7 are closed. The second method is that the natural gas firstly enters the second desulfurizing tower 4 and then enters the first desulfurizing tower 3, the second valve F2, the fourth valve F4 and the fifth valve F5 are opened, and the first valve F1, the third valve F3, the sixth valve F6 and the seventh valve F7 are closed.
Specifically, as shown in fig. 4, the first drying tower 11 or the second drying tower 12 is arranged in parallel, one of the two drying towers is in an adsorption state, the other one is in a desorption regeneration state, and the states of the two towers are switched after the desorption is completed. A ninth valve F9 and an eleventh valve F11 are respectively arranged on pipelines connecting an inlet of the first drying tower 11 and an inlet of the second drying tower 12 with a gas phase outlet of the secondary liquid separation tank 10, a thirteenth valve F13 and a fifteenth valve F15 are respectively arranged on pipelines connecting an outlet of the first drying tower 11 and an outlet of the second drying tower 12 with the second heat exchanger 204, an eighth valve F8 and a tenth valve F10 are respectively arranged on pipelines connecting an inlet of the first drying tower 11 and an inlet of the second drying tower 12 with a heat medium inlet of the fourth water cooler 304, a hot coal outlet of the fourth water cooler 304 is connected with a purified dry gas outward conveying pipeline, a twelfth valve F12 and a fourteenth valve F14 are respectively arranged on pipelines connecting an outlet of the first drying tower 11 and an outlet of the second drying tower 12 with an outlet of the electric heater 18, an eighteenth valve F18 is arranged on a connecting pipeline between a refrigerant outlet of the first heat exchanger 205 and an inlet of the electric heater 18, the refrigerant outlet of the first heat exchanger 205 is connected with the outlet pipeline of the electric heater 18 through a connecting pipeline, the connecting pipeline is provided with a seventeenth valve F17, the connecting pipeline at the outlet end of the seventeenth valve F17 is also connected with the heat medium inlet of the fourth water cooler 304 through a pipeline, and the pipeline is provided with a sixteenth valve F16.
When the first drying tower 11 is in the adsorption state and the second drying tower 12 is in the desorption state, the ninth valve F9, the thirteenth valve F13, the tenth valve F10, the fourteenth valve F14 and the eighteenth valve F18 are opened, the eleventh valve F11, the fifteenth valve F15, the eighth valve F8, the twelfth valve F12 and the sixteenth valve F16 are closed, firstly, the seventeenth valve F17 is closed, gas phase discharged from the second separation tank 10 passes through the first drying tower 11 to enter the second heat exchanger 204, a part of natural gas discharged from the refrigerant outlet of the first heat exchanger 205 passes through the eighteenth valve F18 to enter the electric heater 18 to be heated to 200 ℃, then passes through the fourteenth valve F14 to reversely enter the second drying tower 12 to heat the molecular sieve for desorption, then is discharged from the inlet of the second drying tower 12, passes through the tenth valve F10 and the fourth water cooler 304 to be output, after heating for 4 hours, the eighteenth valve F18 is closed and the seventeenth valve F17 is opened, and the natural gas part discharged from the refrigerant outlet of the first heat exchanger 205 passes through a seventeenth valve F17, reversely enters the second drying tower 12 to cool the molecular sieve for 4 hours, then a tenth valve F10 and a fourteenth valve F14 are closed, a sixteenth valve F16 is opened, and the natural gas directly passes through a pipeline where the sixteenth valve F16 is located and is output. The states of the two drying towers are switched every 24 hours, and after the switching, the valves are in a state where the eleventh valve F11, the fifteenth valve F15, the eighth valve F8, the twelfth valve F12 and the eighteenth valve F18 are opened, and the ninth valve F9, the thirteenth valve F13, the tenth valve F10, the fourteenth valve F14, the sixteenth valve F16 and the seventeenth valve F17 are closed. And a part of the natural gas discharged from the second separation tank 10 enters the second heat exchanger 204 through the second drying tower 12, is discharged from the refrigerant outlet of the first heat exchanger 205, enters the electric heater 18 through an eighteenth valve F18 to be heated to 200 ℃, then reversely enters the first drying tower 11 through a tenth valve F12 to heat the molecular sieve for desorption, then is discharged from the inlet of the first drying tower 11, is cooled and output through an eighth valve F8 and a fourth water cooler 304, after the natural gas is heated and desorbed for 4 hours, the eighteenth valve F18 is closed and a seventeenth valve F17 is opened, the part of the natural gas discharged from the refrigerant outlet of the first heat exchanger 205 passes through a seventeenth valve F17 to reversely enter the first drying tower 11 to cool the molecular sieve for 4 hours, then the eighth valve F8 and the twelfth valve F12 are closed, the sixteenth valve F16 is opened, and the natural gas directly passes through a pipeline in which the sixteenth valve F16 is arranged.
Specifically, an inlet buffer tank 19 is connected with the raw material gas inlet pipeline, the inlet buffer tank 19 stabilizes the natural gas in the system, an outlet of the inlet buffer tank 19 and a liquid phase outlet of the air extractor buffer tank 2, the liquid phase outlet of the raw material buffer tank 5 and the liquid phase outlet of the first liquid separating tank 8 are both connected with a liquid phase inlet of a liquid drainage water separating tank 20, water and light oil enter the liquid drainage water separating tank 20, partial charging gas at the outlets of the first drying tower 11 and the second drying tower 12 enters from a gas phase inlet of the liquid drainage water separating tank 20 along a pipeline to provide low temperature and pressure for the liquid drainage water separating tank 20, oil-containing sewage separated in the liquid drainage water separating tank 20 enters a sewage tank, the light oil separated in the liquid drainage water separating tank 20 and a liquid phase separated from the second liquid separating tank 10 are cooled and separated by a condensate cooler 103, the gas phase enters an ejector 21, and the liquid phase enters a mixed hydrocarbon storage tank.
Specifically, as shown in fig. 6 and 7, the velocity generator 26 includes an end cover 264, a main housing 265 and an outlet pipe 266, the end cover 264 and the main housing 265 are paired and ground and fixedly connected through a bolt 263, an inlet 262 is arranged between one end of the end cover 264 and one end of the main housing 265 and arranged along a parabola from the tangential direction, the width d of the inlet 262 is 2.5mm, the diameter of the main housing 265 is 400mm, the main housing 265 has a gaseous heat phase outlet 261 and a balance pipe 267 arranged along the tangential direction, the outlet pipe 266 is fixedly connected with the middle part of the other end of the main housing 265 and communicated with an inner cavity of the main housing 265, and a deflector arranged inside the main housing 265 is further fixedly connected to the end cover. After entering from the gas inlet 262, the gas forms a high-speed vortex in the main housing 265, the gas with lower temperature at the center of the main housing 265 is called a gaseous cold phase and is discharged by the gas outlet pipe 266, and the gas with higher temperature at the periphery of the main housing 265 is called a gaseous hot phase and is discharged by the gaseous hot phase outlet 261. As shown in fig. 6, the gaseous hot phase outlet 261 is communicated with the balance pipe 267, the gaseous hot phase outlet 261 is communicated with the inner cavity of the main casing 265, a valve for controlling flow is arranged on the pipeline of the gaseous hot phase outlet 261, the gaseous hot phase outlet 261 and the balance pipe 267 are also provided with a regulating valve, as shown in fig. 6, the gas rotates anticlockwise at the speed of mach 1 in the main casing 265, part of the gaseous hot phase is discharged from the gaseous hot phase outlet 261, one end of the balance pipe 267 is communicated with the main casing 265 and the gaseous hot phase outlet 261, the other end is closed, and the other part of the gaseous hot phase returns to the main casing 265 through the balance pipe 267.
Specifically, as shown in fig. 8, in the present invention, the heat medium pipelines of the first water cooler 301, the second water cooler 302, the third water cooler 303, the fourth water cooler 304, the fifth water cooler 305 and the sixth water cooler 306 are installed side by side in a centralized manner to form a centralized water cooler 27, which provides a refrigerant in a centralized manner, and has a compact structure and is more energy-saving. The skid-mounted natural gas treatment device is respectively arranged on the first skid block M101, the second skid block M102, the third skid block M103 and the fourth skid block M104, has compact and strict structure, and can flexibly adjust the position and the combined structure of each skid block according to the site topographic and topographic conditions.
In the present invention, the opening or closing of the valve can be realized by using a control method in the prior art, or can be realized by manual adjustment, and for brevity, the description is omitted here. In describing the present invention, the terms 'connected' or 'connected' used in describing the relationship between the devices of fig. 1-5 refer to connection via a conduit unless otherwise specifically stated and limited.
In the description of the present invention, it should be noted that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc., indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.
In the description herein, references to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.

Claims (10)

1. The skid-mounted natural gas treatment device is characterized by being mounted on a plurality of skid blocks and comprising a natural gas compressor unit, a second water cooler (302), a primary liquid separating tank (8), a first heat exchange cooling device group and a second liquid separating tank (10), wherein the natural gas compressor unit comprises a first compression chamber and a second compression chamber, an inlet of the first compression chamber is used for introducing natural gas, an outlet of the first compression chamber is communicated to an inlet of the first liquid separating tank (8) through the second water cooler (302), a gas phase outlet of the first liquid separating tank (8) is communicated with an inlet of the second compression chamber, an inlet of the second compression chamber is communicated to an inlet of the second liquid separating tank (10) through the first heat exchange cooling device group, and a gas phase outlet of the second liquid separating tank (10) is used for discharging the treated natural gas.
2. The skid-mounted natural gas treatment device according to claim 1, further comprising an air extractor, a desulfurization tower set and a raw material buffer tank (5), wherein an inlet of the air extractor is connected with a raw material gas inlet pipeline, an outlet of the air extractor is connected with an inlet of the desulfurization tower set, an outlet of the desulfurization tower set is connected with an inlet of the raw material buffer tank (5), and a gas phase outlet of the raw material buffer tank (5) is connected with an inlet of the first compression chamber of the natural gas compressor set.
3. The skid-mounted natural gas treatment device according to claim 2, wherein the air extractor comprises an air extractor (1), a first water cooler (301) and an air extractor buffer tank (2), an inlet of the air extractor (1) is connected with a feed gas inlet pipeline, an outlet of the air extractor is connected with a heat medium inlet of the first water cooler (301), a heat medium outlet of the first water cooler (301) is connected with an inlet of the air extractor buffer tank (2), and a gas phase outlet of the air extractor buffer tank (2) is connected with an inlet of the desulfurization tower set.
4. The skid-mounted natural gas treatment device according to claim 2, wherein the desulfurization tower set comprises a first desulfurization tower (3) and a second desulfurization tower (4) which are connected in parallel or in series, the outlet of the air extraction device is connected with the inlet of the first desulfurization tower (3) and/or the inlet of the second desulfurization tower (4), and the outlet of the first desulfurization tower (3) and/or the outlet of the second desulfurization tower (4) are connected with the inlet of the raw material buffer tank (5).
5. The skid-mounted natural gas treatment device according to any one of claims 1 to 4, wherein the first heat exchange and temperature reduction device set comprises a reboiler (9), a third water cooler (303) and a first heat exchanger (205), the outlet of the second compression chamber is connected with the gas phase inlet of the reboiler (9), the gas phase outlet of the reboiler (9) is connected with the heat medium inlet of the third water cooler (303), the heat medium outlet of the third water cooler (303) is connected with the heat medium inlet of the first heat exchanger (205), and the heat medium outlet of the first heat exchanger (205) is connected with the inlet of the second fraction liquid tank (10).
6. The skid-mounted natural gas treatment device according to claim 5, further comprising an electric heater (18), a first drying tower (11), a second drying tower (12) and a second heat exchange and temperature reduction device set; the gas phase outlet of the secondary liquid separation tank (10) is respectively connected with the inlet of the first drying tower (11) or the inlet of the second drying tower (12), the outlet of the first drying tower (11) or the outlet of the second drying tower (12) is connected with the inlet of the second heat exchange temperature reduction device set, the outlet of the second heat exchange temperature reduction device group is connected with the refrigerant inlet of the first heat exchanger (205), the refrigerant outlet of the first heat exchanger (205) is connected with a purified dry gas outward transmission pipeline, the refrigerant outlet of the first heat exchanger (205) is also respectively connected with the inlet of the electric heater (18) or the outlet of the electric heater (18) through a pipeline, the outlet of the electric heater (18) is respectively connected with the outlet of the first drying tower (11) or the outlet of the second drying tower (12), and the inlet of the first drying tower (11) or the inlet of the second drying tower (12) is connected with a purified dry gas outward conveying pipeline.
7. The skid-mounted natural gas treatment device according to claim 6, wherein the first heat exchange and temperature reduction device set further comprises a rectifying tower (17), and the second heat exchange and temperature reduction device set comprises a second heat exchanger (204), a front cooling heat exchanger (13), an evaporation heat exchanger (14), a rear cooling heat exchanger (15), a low-temperature separator (16) and a refrigerant circulating device; an outlet of the first drying tower (11) or an outlet of the second drying tower (12) is connected with a heat medium inlet of the second heat exchanger (204), a heat medium outlet of the second heat exchanger (204) is connected with a heat medium inlet of the front cooling heat exchanger (13), a heat medium outlet of the front cooling heat exchanger (13) is connected with a heat medium inlet of the evaporation heat exchanger (14), a heat medium outlet of the evaporation heat exchanger (14) is connected with a heat medium inlet of the rear cooling heat exchanger (15), a heat medium outlet of the rear cooling heat exchanger (15) is connected with an inlet of the low-temperature separator (16), a gaseous cold phase outlet of the low-temperature separator (16) is connected with a refrigerant inlet of the rear cooling heat exchanger (15), a refrigerant outlet of the rear cooling heat exchanger (15) is connected with a refrigerant inlet of the front cooling heat exchanger (13), and a refrigerant outlet of the front cooling heat exchanger (13) is connected with a refrigerant inlet of the first heat exchanger (205), an outlet of the refrigerant circulating device is connected with a refrigerant inlet of the evaporation heat exchanger (14), and a refrigerant outlet of the evaporation heat exchanger (14) is connected with an inlet of the refrigerant circulating device; a liquid phase outlet of the low-temperature separator (16) is connected with an inlet of the rectifying tower (17), a liquid phase outlet of the rectifying tower (17) is connected with a liquid phase inlet of the reboiler (9), and a liquid phase outlet of the reboiler (9) is connected with an external mixed hydrocarbon storage tank; the gas phase outlet of the rectifying tower (17) is connected with the inlet of the first liquid separation tank (8).
8. The skid-mounted natural gas processing plant according to claim 7, wherein the cryogenic separator (16) comprises a cryogenic separator body and a cold dry gas thermal separation device disposed therein, the cold dry gas thermal separation device being a velocity generator or a vortex tube.
9. The skid-mounted natural gas treatment device according to claim 6, further comprising an inlet buffer tank (19) and a liquid discharge water separation tank (20), wherein an inlet of the inlet buffer tank (19) is connected with a raw gas inlet pipeline, an outlet of the inlet buffer tank (19) and a liquid phase outlet of the first liquid separation tank (8) are both connected with a liquid phase inlet of the liquid discharge water separation tank (20), a sewage outlet of the liquid discharge water separation tank (20) is connected with an external sewage tank, and an outlet of the first drying tower (11) or an outlet of the second drying tower (12) is connected with a pressurized gas inlet of the liquid discharge water separation tank (20).
10. The skid-mounted natural gas processing apparatus according to any one of claims 1 to 4 and 6 to 9, wherein the natural gas compressor unit comprises a first natural gas compressor (6) and a second natural gas compressor (7), the first natural gas compressor (6) and the second natural gas compressor (7) are arranged in parallel and are provided with the first compression chamber and the second compression chamber.
CN201911115103.1A 2019-11-14 2019-11-14 Skid-mounted natural gas treatment device Pending CN110762946A (en)

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Application Number Priority Date Filing Date Title
CN201911115103.1A CN110762946A (en) 2019-11-14 2019-11-14 Skid-mounted natural gas treatment device

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CN110762946A true CN110762946A (en) 2020-02-07

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113531386A (en) * 2021-08-25 2021-10-22 西南石油大学 Vehicle-mounted collection system and method for vented natural gas

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113531386A (en) * 2021-08-25 2021-10-22 西南石油大学 Vehicle-mounted collection system and method for vented natural gas
CN113531386B (en) * 2021-08-25 2022-10-11 西南石油大学 Vehicle-mounted collection system and method for vented natural gas

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