WO2023073811A1 - Installation de traitement de gaz naturel - Google Patents

Installation de traitement de gaz naturel Download PDF

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Publication number
WO2023073811A1
WO2023073811A1 PCT/JP2021/039515 JP2021039515W WO2023073811A1 WO 2023073811 A1 WO2023073811 A1 WO 2023073811A1 JP 2021039515 W JP2021039515 W JP 2021039515W WO 2023073811 A1 WO2023073811 A1 WO 2023073811A1
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WO
WIPO (PCT)
Prior art keywords
pressure
pipe
flare
natural gas
low
Prior art date
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PCT/JP2021/039515
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English (en)
Japanese (ja)
Inventor
徹 中山
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日揮グローバル株式会社
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Filing date
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Application filed by 日揮グローバル株式会社 filed Critical 日揮グローバル株式会社
Priority to PCT/JP2021/039515 priority Critical patent/WO2023073811A1/fr
Priority to CN202180101243.2A priority patent/CN117751267A/zh
Publication of WO2023073811A1 publication Critical patent/WO2023073811A1/fr

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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
    • 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
    • F25J1/02—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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas 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
    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0259—Modularity and arrangement of parts of the liquefaction unit and in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
    • F25J1/0277—Offshore use, e.g. during shipping
    • F25J1/0278—Unit being stationary, e.g. on floating barge or fixed platform
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING 
    • B63B35/00—Vessels or similar floating structures specially adapted for specific purposes and not otherwise provided for
    • B63B35/44—Floating buildings, stores, drilling platforms, or workshops, e.g. carrying water-oil separating devices
    • B63B2035/448—Floating hydrocarbon production vessels, e.g. Floating Production Storage and Offloading vessels [FPSO]
    • 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
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • 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
    • 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
    • F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
    • 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
    • F25J2290/60—Details about pipelines, i.e. network, for feed or product distribution

Definitions

  • the present invention relates to a natural gas processing facility that liquefies natural gas or separates and recovers components in natural gas.
  • the natural gas is pretreated to remove various impurities from the natural gas at the natural gas processing facility, and the natural gas after pretreatment is liquefied to produce LNG (Liquidized Natural Gas).
  • LNG Liquidized Natural Gas
  • a liquefaction process to obtain is performed.
  • a natural gas processing facility that separates and recovers heavy components from natural gas and ships it in the form of light hydrocarbon gas.
  • Natural gas processing facilities are equipped with a large number of equipment such as various processing towers and heat exchangers used for pretreatment, liquefaction, and separation of heavy components.
  • excess fluids may be generated in these devices, consisting mainly of combustible gases (such as light hydrocarbons and hydrogen sulfide).
  • the excess fluid is discharged from the flare stack section, which combusts combustible gas and discharges it to the outside in order to prevent the pressure inside the equipment from rising. Excess fluid discharged from the flare stack is also called flare gas.
  • a natural gas processing facility is provided with flare piping through which excess fluid discharged from equipment flows toward a flare stack.
  • a plurality of flare pipes are provided according to the pressure and properties of the device that discharges excess fluid.
  • Flare piping is piping equipment with a large diameter and a long arrangement distance among many piping systems provided in natural gas processing equipment. Therefore, from the viewpoint of suppressing construction costs and maintenance costs, there is a demand for further simplification of the facility configuration related to flare piping.
  • Patent Document 1 describes a technique for reducing the size of flare pipes by distributing fluid discharged from a device provided in a natural gas liquefying apparatus to two types of flare pipes.
  • Patent Literature 1 does not describe a technique for simplifying the system configuration of flare piping provided in a plurality of systems.
  • the present invention was made against this background, and provides a technique for simplifying the system configuration of flare piping provided in natural gas processing facilities.
  • the natural gas processing facility of the present invention is a natural gas processing facility that liquefies natural gas or separates and recovers components in natural gas, a high-pressure operating device operated at a pressure higher than normal pressure; a low-pressure operating device operated at a pressure lower than that of the high-pressure operating device; a flare stack section provided with a burner for burning combustible gas and releasing it to the atmosphere; a flare pipe connected to the flare stack portion and through which a wet first surplus fluid containing the combustible gas discharged from the high-pressure operating device flows; an external discharge pipe through which the wet second surplus fluid containing the combustible gas discharged from the low-pressure operating device flows and discharges the second surplus fluid to the outside without passing through the flare stack; a discharge pipe having one end connected to the low-pressure operating equipment and provided with a control valve for adjusting the discharge amount of the second excess fluid; a depressurization pipe having one end connected to the low-pressure operating device and provided with a safety valve that opens when the pressure in the
  • the natural gas processing facility may also include the following features.
  • the design pressure of the low-pressure operation equipment is set higher than the design pressure of the external discharge pipe.
  • the design pressure of the low-pressure operation equipment is set to a pressure corresponding to the flare piping.
  • the low-pressure operation device includes a device that discharges an acid gas as the combustible gas, and the device that discharges the acid gas includes the second An incineration pipe must be connected to drain excess fluid from the tank.
  • the external discharge pipe is higher than the installation surface where the natural gas processing equipment is installed, and is directed to the atmosphere, which is the outside.
  • a plurality of devices constituting the natural gas processing facility are installed on a floating facility installed on the water.
  • a discharge pipe provided with a control valve for adjusting the discharge amount of the surplus fluid and a safety valve are provided for the discharge destination of the surplus fluid (second surplus fluid) discharged from the common low-pressure operation equipment. It is connected to a discharge destination different from the provided depressurization pipe.
  • FIG. 10 is a system diagram for discharging surplus fluid from low-pressure operation equipment according to the conventional configuration.
  • FIG. 4 is a system diagram for discharging surplus fluid from the low-pressure operation equipment according to the embodiment;
  • 1 is a schematic diagram of an FLNG with a conventional natural gas processing facility;
  • FIG. 1 is a schematic diagram of an FLNG with a natural gas processing facility according to an embodiment;
  • FIGS. 1 and 2 are schematic configuration diagrams of a conventional configuration and a natural gas processing facility according to an embodiment, respectively. These figures show an example in which natural gas processing equipment is configured by an LNG plant that produces LNG from gaseous natural gas (NG).
  • NG gaseous natural gas
  • the NG supplied to the LNG plant undergoes pretreatment to remove impurities in each of the gas-liquid separation unit 21, the acid gas removal unit 22, the water removal unit 23, and the mercury removal unit 24. Further, the NG passes through the heavy component separation unit 25 that separates the heavy components, and is liquefied and supercooled in each processing unit of the liquefaction unit 26 and the end flash unit 27. Then, the LNG tank 28 for shipping stored in Further, the heavy fraction separated by the heavy fraction separation section 25 is distilled into hydrocarbons in the distillation section 33 .
  • the light components (C1, C2) are sent to the liquefying section 26, the C3, C4 are stored in the LPG tank 34, and the condensate is stored in the condensate tank 32, respectively.
  • the liquid component separated from the natural gas by the gas-liquid separation unit 21 is stored in the condensate tank 32 after the vapor pressure is adjusted to remove light hydrocarbons by the vapor pressure adjustment unit 31 .
  • surplus fluid containing combustible gases may be discharged during operational fluctuations.
  • Such surplus fluid is discharged toward a flare stack section provided with a burner for burning combustible gas and releasing it to the atmosphere.
  • Excess fluid flows toward the flare stack section via the flare piping.
  • the conventionally configured LNG plant shown in FIG. 1 has four flare piping systems (HP-WET flare piping 110, HP-DRY flare piping 120, An LP-WET flare pipe 130 and an LP-DRY flare pipe 140) are provided.
  • the HP-WET flare pipe 110 and the HP-DRY flare pipe 120 are equipped with high-pressure operating equipment that operates at a pressure higher than normal pressure, such as a pressure of about 3.1 to 6.1 MPag (30 to 60 Barg). High-pressure equipment is connected.
  • high-pressure operating equipment connected to the HP-WET flare pipe 110 equipment provided in the gas-liquid separation section 21 and the water removal section 23 can be exemplified.
  • high-pressure operating equipment connected to the HP-DRY flare pipe 120 equipment provided in the mercury removal section 24, the heavy component separation section 25, and the like can be exemplified.
  • the HP-WET flare pipe 110 is configured to allow wet surplus fluid containing water to flow, and is provided with a knockout drum 111 at its end.
  • the knockout drum 111 has the function of separating liquids such as water and oil from surplus fluid using gravity. Excess fluid after the liquid is separated by the knockout drum 111 is burned by the burner of the flare stack section 112 .
  • the wet surplus fluid discharged from the high pressure operation equipment to the HP-WET flare pipe 110 corresponds to the "first surplus fluid".
  • the HP-DRY flare pipe 120 is configured so that surplus fluid containing almost no water circulates, and the surplus fluid that circulates through the HP-DRY flare pipe 120 is directly burned by the burner of the flare stack section 121. be done.
  • a low-pressure operating device that operates at a pressure lower than the above-described high-pressure operating device, for example, 0.01 to 0.1 MPag (0.1 to 1.0 barg ) is connected to a low-pressure operating device operated at a pressure of about
  • Examples of the low-pressure operating equipment connected to the LP-WET flare pipe 130 include equipment provided in the acid gas removing section 22 and the vapor pressure adjusting section 31 .
  • the low-pressure operation equipment connected to the LP-DRY flare pipe 140 can be exemplified by the LNG tank 28, the LPG tank 34, and the like.
  • the LP-WET flare pipe 130 is configured to allow a wet surplus fluid containing water to flow, and is similar to the HP-WET flare pipe 110 in that a knockout drum 131 is provided at the end.
  • the wet surplus fluid discharged from the low pressure operation equipment corresponds to the "second surplus fluid”.
  • the LP-DRY flare pipe 140 is configured so that surplus fluid containing almost no water flows through, and the surplus fluid is burned directly by the burner of the flare stack section 141 without going through the knockout drum. , HP-DRY flare line 120 .
  • the flare pipes 110, 120, 130, and 140 are one of the pipes with the largest diameter among the pipes arranged in the LNG plant, and the arrangement distance is long.
  • the HP-WET flare pipe 110 and the HP-DRY flare pipe 120 have a diameter of, for example, about 1.5 m (60 inches), and the arrangement distance ranges from tens of meters to 100 meters or more.
  • the LP-WET flare pipe 130 and the LP-DRY flare pipe 140 have a diameter of, for example, about 0.5 m (20 inches), and the arrangement distance is several tens to hundreds of meters or more. Therefore, the flare piping system configuration is a component that greatly affects the construction cost and maintenance cost of the entire LNG plant.
  • FIG. 3 shows an example of piping connection for discharging surplus fluid from low-pressure operating equipment in a conventional configuration.
  • the acidic gas removal unit 22 of this example absorbs acidic gases (for example, carbon dioxide and hydrogen sulfide) in the absorption tower using an absorbent such as amine, and the absorbent after absorbing the acidic gas is transferred to the regeneration tower 222. and is configured to heat and release acid gases.
  • the vapor pressure adjusting unit 31 also includes a stabilizer 312 that adjusts the vapor pressure by distilling and separating light hydrocarbons contained in the condensate after gas-liquid separation from NG.
  • the acidic gas removing unit 22 will be described first. From the top of the regeneration tower 222, the acidic gas released with the thermal regeneration of the absorbent is discharged. The acid gas is supplied to the incinerator 151 through the incineration pipe 225, and the combustible acid gas such as hydrogen sulfide is burned in the incinerator 151 and then released to the atmosphere.
  • the combustible acid gas such as hydrogen sulfide
  • an extraction pipe 221a having a control valve 223 for adjusting the discharge amount of acid gas is provided.
  • the discharge pipe 221a plays a role of circulating acid gas, which is a surplus fluid, toward the LP-WET flare pipe 130, for example, while the operation of the incinerator 151 is stopped for maintenance or the like.
  • a safety valve 224 for depressurization that opens and depressurizes when the internal pressure of the regeneration tower 222 rises to an operating pressure (for example, the design pressure of the regeneration tower 222) or more.
  • a pipe 221b is provided.
  • the surplus fluid discharged from the regeneration tower 222 which is a low-pressure operating device, is in a wet state. From this point of view, the excess fluid discharged from the regeneration tower 222 corresponds to the second excess fluid.
  • the extraction pipe 221a and the depressurization pipe 221b are comprehensively described as the surplus fluid pipe 221. As shown in FIG.
  • the light hydrocarbons separated by distillation from the condensate are discharged as offgas from the stabilizer 312.
  • the off-gas is utilized within the LNG plant as fuel for furnaces and the like.
  • an extraction pipe 311a having a control valve 313 for adjusting the discharge amount of off-gas is provided.
  • the extraction pipe 311a serves to distribute offgas, which is a surplus fluid, toward the LP-WET flare pipe 130 when the demand for offgas in the LNG plant decreases.
  • a depressurization pipe 311b equipped with a safety valve 314 that opens and depressurizes when the internal pressure of the stabilizer 312 rises and becomes equal to or higher than the operating pressure (for example, the design pressure of the stabilizer 312). is provided.
  • the surplus fluid discharged from the stabilizer 312 which is a low-pressure operating device, is in a wet state. From this point of view, the excess fluid discharged from the stabilizer 312 corresponds to the second excess fluid.
  • the extraction pipe 311a and the depressurization pipe 311b are also comprehensively described as the surplus fluid pipe 311. As shown in FIG.
  • one end of the discharge pipe 221a provided with the control valve 223 is connected to the top of the regeneration tower 222, and the other end is connected to the external discharge pipe 160.
  • One end of an extraction pipe 311 a provided with a control valve 313 is connected to the top of the stabilizer 312 , and the other end is connected to the external discharge pipe 160 .
  • an LNG plant is provided with an external discharge pipe 160 for discharging the gas to the outside without going through the flare stack portions 112, 121, and 141 for the purpose of discharging non-flammable gas discharged from operating equipment.
  • the external discharge pipe 160 may be configured to directly discharge the fluid flowing therein to the atmosphere.
  • the external discharge pipe 160 may be configured such that the end portion is connected to a packed tower filled with an adsorbent, and the remaining gas is discharged to the atmosphere after a predetermined component is removed by adsorption with the adsorbent. good.
  • the second surplus fluid When the second surplus fluid is discharged to the atmosphere from the end of the external discharge pipe 160, the second surplus fluid may contain components that affect the human body and the environment.
  • the end of the external discharge pipe 160 is placed at a higher place than the installation surface where the LNG plant is installed, and is exposed to the outside atmosphere. It is preferably configured to discharge the second excess fluid towards.
  • the installation height of equipment is the height dimension from a predetermined reference height (for example, the height of zero meters above sea level) to the position where each equipment is installed.
  • a predetermined reference height for example, the height of zero meters above sea level
  • the height dimension from the reference height to the bottom end of the equipment installed on the mounting table is Corresponds to the installation height. Since a large number of devices are installed in an LNG plant, a case can be exemplified in which the end portion of the external discharge pipe 160 is arranged at a position higher than the device having the maximum installation height among these devices.
  • the second surplus fluid may contain a component subject to management whose allowable concentration in the air is sampled at a position a preset distance away from the discharge position from the external discharge pipe 160 .
  • the end of the external discharge pipe 160 is provided at a height position where the concentration of the controlled component in the sample is less than the allowable concentration. This height position can be grasped in advance by atmospheric diffusion simulation using fluid analysis software.
  • the end of the external discharge pipe 160 is often provided at a high place.
  • the end of the external discharge pipe 160 may be arranged in a common tower with the other flare stack portions 112, 121, 141, as in the example of the FLNG 4 described later with reference to FIG.
  • the height position of the distal end of the external discharge pipe 160 is arranged at the same height position as the proximal end of the flames of the flare stacks 112, 121, 141 or lower than it.
  • the end portion of the external discharge pipe 160 and the flare stack portions 112, 121, 141 are installed at different positions within the premises of the LNG plant, the height at which the end portion of the external discharge pipe 160 is arranged Positions are not constrained by burner flame considerations.
  • the external discharge pipe 160 is a pipe with a diameter of about 1.2 m (48 inches), for example, and has lower pressure resistance performance (LP-WET flare The thickness of the pipe is also thinner than that of the pipe 130). In this case, by omitting the installation of the LP-WET flare pipe 130 and the knockout drum 131 and flare stack section 132 which are incidental equipment, construction costs and maintenance costs can be greatly reduced.
  • the second surplus fluid flowing through the extraction pipes 221a and 311a is discharged as exhaust gas during normal operation.
  • the incinerator 151 When the incinerator 151 is installed, the second surplus fluid is incinerated in the incinerator 151, so there is little opportunity for the second surplus fluid to be released to the atmosphere as it is. Further, even if the installation of the incinerator 151 is omitted as a result of connecting the extraction pipe 221a of the acid gas removal unit 22 to the external discharge pipe 160, the content in the crude oil is The amount of hydrogen sulfide contained in NG is very small. Also, as described above, the atmosphere may be released after removing components such as hydrogen sulfide in a packed tower filled with an adsorbent.
  • the extraction pipes 221a, 311a for adjusting the discharge amount using the control valves 223, 313 are connected to the external discharge pipe 160, and direct the second surplus fluid to the external discharge pipe 160. It is configured to be ejectable.
  • the design pressure of the regeneration tower 222 and the stabilizer 312 which are low-pressure operation equipment is set higher than the design pressure of the external discharge pipe 160 . That is, since the design pressure of the external discharge pipe 160 is low, it cannot be connected to the depressurization pipes 221b and 311b provided with the safety valves 224 and 314 .
  • one end of the depressurization pipe 221b provided with the safety valve 224 is connected to the top of the regeneration tower 222, and the other end is connected to the HP-WET flare pipe 110. It is connected to the.
  • One end of a depressurization pipe 311 b provided with a safety valve 314 is connected to the top of the stabilizer 312 , and the other end is connected to the HP-WET flare pipe 110 . That is, in the HP-WET flare pipe 110, the first surplus fluid, which is the wet surplus fluid discharged from the high-pressure operation equipment such as the gas-liquid separation unit 21 and the water removal unit 23, flows.
  • the second surplus fluid discharged from the depressurization pipes 221b and 311b of the equipment (acid gas removing unit 22, vapor pressure adjusting unit 31) flows.
  • the HP-WET flare pipe 110 has a higher design pressure. Therefore, the operating pressure of the safety valves 224 and 314 provided in the depressurization pipes 221b and 311b is about 0.5 MPa (3.5 Barg) when connected to the LP-WET flare pipe 130 (for example, about 0.5 MPa (3.5 Barg)). than when connected to the HP-WET flare pipe 110 (for example, 0.8 to 1.1 MPa (7 to 10 Barg)).
  • the design pressure of the regeneration tower 222 and the stabilizer 312, which are low-pressure operating devices, must have pressure resistance performance corresponding to the safety valves 224 and 314 that can be connected to the HP-WET flare pipe 110.
  • the thickness of the constituent members is set so that the safety valves 224 and 314 are connected to the LP-WET flare pipe 130.
  • the LNG plant according to the embodiment has the following effects.
  • the destination of the surplus fluid (second surplus fluid) discharged from the low-pressure operation equipment (regeneration tower 222, stabilizer 312) extraction pipes 221a, 311a provided with control valves 223, 313 and safety valves 224, 314 are connected to different discharge destinations from the depressurization pipes 221b and 311b.
  • the installation of the LP-WET flare pipe 130 for low-pressure operation equipment which was provided as a common discharge destination for these extraction pipes 221a, 311a and the depressurization pipes 221b, 311b, is omitted, and the flare pipe system Configuration can be simplified.
  • FLNG 4 a and 4 in which a plurality of equipment constituting the LNG plant are provided on the floating facility installed on the water are shown in FIGS. will be described with reference to.
  • the FLNGs 4a and 4 are floating facilities placed on the water, and the above-mentioned LNG plant is provided on the upper surface of the hull 40 in which the LNG tank 28, the LPG tank 34, etc. are formed. ing.
  • a turret 45 as mooring equipment is provided on the bow side of the hull 40 .
  • the turret 45 is connected to a mooring line to moor the hull 40, and is connected to a riser for underwater transportation of mined NG (mooring line and riser are not shown).
  • the direction in which the turret 45 is provided is assumed to be the front of the hull 40 .
  • a flare stack 44 is provided on the frame of the hull 40, for example, at a position closer to the port side on the bow side for burning surplus gas generated in LNG plants and LNG tanks. Further, as shown in FIGS. 5(b) and 6(b), the hull 40 has a planar shape that is longer in the longitudinal direction than in the transverse direction.
  • a pipe rack 41 is provided in the center region of the hull 40 in the width direction so as to extend along the length of the hull 40 .
  • the pipe rack 41 is a frame that holds a plurality of plant pipes through which various fluids handled in the FLNG 4a, 4 flow.
  • the areas adjacent to the left and right sides of the pipe rack 41 are plant placement areas 42 in which the equipment that constitutes the LNG plant is placed.
  • a plurality of LNG plant equipment 421 constituting an LNG plant are arranged side by side in the front-rear direction in each of these plant layout areas 42 .
  • These LNG plant equipment 421 include the low-pressure operation equipment and the high-pressure operation equipment described above.
  • FIG. 5 and 6 show an example of an LNG plant constructed by a so-called stick-built system in which a plant arrangement area 42 is individually arranged on the deck of a hull 40.
  • a large number of LNG plant equipment 421 of the LNG plant are divided into a plurality of frames to form modules, and these modules are installed after the frame of the hull 40 is completed to form the LNG plant. good too.
  • the hull 40 and the modules are built at separate locations.
  • the pipe rack 41 includes HP-WET flare piping 110, HP-DRY flare piping 120, and LP-WET flare piping. 130 and LP-DRY flare piping 140 are retained. Also in the conventional LNG plant, the pipe rack 41 holds a large number of pipes including the external discharge pipe 160, but the illustration of these pipes is omitted for convenience of illustration.
  • the end portions of these flare pipes 110, 120, 130, 140 are connected to flare stacks 44 (flare stack portions 112, 121, 132, 141) provided on a common tower.
  • the pipe rack 41 includes the HP-WET flare piping 110 and the HP-DRY flare piping. Only 120 and LP-DRY flare lines 140 are retained. Terminal ends of these flare pipes 110, 120, 140 are connected to a flare stack 44 (flare stack portions 112, 121, 141) provided on a common tower.
  • the LP-WET flare pipe 130, the knockout drum 131 and the flare stack portion 132 are not provided in the FLNG 4 according to the embodiment.
  • FLNG 4 when an LNG plant is installed in a floating facility, there is a restriction on the area of the installation surface where a large number of equipment constituting the LNG plant can be arranged.
  • a space merit can be obtained in which the area that can be allocated to the installation of other equipment is increased.
  • the merit of weight reduction by omitting the installation of the LP-WET flare pipe 130 can also be obtained.
  • FIG. 6(b) also schematically shows how the pipe rack 41 holds the external discharge pipe 160 through which the second surplus fluid discharged from the low-pressure operating equipment (the regeneration tower 222 and the stabilizer 312) flows. It is described.
  • the external discharge pipe 160 is provided so as to extend to a mid-height position of the scaffold holding the flare stack 44 , and its terminal end is below the burner of the flare stack 44 . It is configured to release the second excess fluid or the like to the atmosphere at the location. This arrangement avoids impingement of the burner flames on the external discharge line 160, as previously described.
  • the direction of release to the atmosphere from the external discharge pipe 160 is the direction opposite to the direction in which the living portion 43 is provided when viewed from the flare stack 44 .
  • the floating facility in which the LNG plant according to the embodiment is installed is not limited to this example.
  • the LNG plant according to the embodiments may be provided on a bottom-bottomed structure (GBS) or on a platform fixed to the bottom of the water.
  • GGS bottom-bottomed structure
  • “on the water” is not limited to the sea, and may be on the water such as a lake.
  • the LNG plant may be provided above ground.
  • the natural gas processing equipment to which the present invention is applied is not limited to LNG plants.
  • the present invention can be applied to an NGL (Natural Gas Liquids) plant, which is a natural gas processing facility that separates and recovers heavy components in NG and ships light hydrocarbons in the form of gas. .
  • NGL Natural Gas Liquids

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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)
  • Combustion & Propulsion (AREA)
  • Ocean & Marine Engineering (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

Le problème à résoudre par la présente invention est de fournir une installation de traitement de gaz naturel, la configuration de système d'un tuyau de torche étant simplifiée. La solution selon l'invention porte sur une installation de traitement de gaz naturel comprenant : un dispositif de fonctionnement à haute pression ; un dispositif de fonctionnement à basse pression 222, 312 ; un tuyau de torche 110 qui est connecté à une partie de la torche 112 et fait circuler le premier fluide excédentaire déchargé du dispositif de fonctionnement à haute pression ; et un tuyau de décharge externe 160 qui contourne la partie de la torche 112 et décharge le second fluide excédentaire contenant du gaz inflammable vers l'extérieur. Les tuyaux d'extraction 221a, 311a sont pourvus de soupapes de réglage 223, 313 pour ajuster la quantité de décharge du second fluide en excès, et présentent chacun une extrémité connectée au dispositif de fonctionnement à basse pression 222, 312 et l'autre extrémité connectée au tuyau de décharge externe 160. En outre, les tuyaux de dépressurisation 221b, 311b sont équipés de soupapes de sécurité 224, 314, et présentent chacun une extrémité reliée au dispositif de fonctionnement à basse pression 222, 312 et l'autre extrémité reliée au tuyau de torche 110.
PCT/JP2021/039515 2021-10-26 2021-10-26 Installation de traitement de gaz naturel WO2023073811A1 (fr)

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PCT/JP2021/039515 WO2023073811A1 (fr) 2021-10-26 2021-10-26 Installation de traitement de gaz naturel
CN202180101243.2A CN117751267A (zh) 2021-10-26 2021-10-26 天然气处理设备

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6045659A (en) * 1993-05-03 2000-04-04 Den Norske Stats Oijeselkap A.S. Device for recovery of excess gas in an oil/gas treatment plant
JP2012233534A (ja) * 2011-05-02 2012-11-29 Ihi Marine United Inc ボイルオフガス処理装置及び液化ガスタンク
WO2016088159A1 (fr) * 2014-12-01 2016-06-09 千代田化工建設株式会社 Dispositif et procédé de gestion de sécurité d'équipement et dispositif de liquéfaction de gaz naturel
US20170292784A1 (en) * 2016-04-11 2017-10-12 Geoff ROWE System and method for liquefying production gas from a gas source
US20200317305A1 (en) * 2016-06-01 2020-10-08 Samsung Heavy Ind. Co., Ltd Offshore facility, floating crude oil production facility and method for generating liquefied natural gas

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6045659A (en) * 1993-05-03 2000-04-04 Den Norske Stats Oijeselkap A.S. Device for recovery of excess gas in an oil/gas treatment plant
JP2012233534A (ja) * 2011-05-02 2012-11-29 Ihi Marine United Inc ボイルオフガス処理装置及び液化ガスタンク
WO2016088159A1 (fr) * 2014-12-01 2016-06-09 千代田化工建設株式会社 Dispositif et procédé de gestion de sécurité d'équipement et dispositif de liquéfaction de gaz naturel
US20170292784A1 (en) * 2016-04-11 2017-10-12 Geoff ROWE System and method for liquefying production gas from a gas source
US20200317305A1 (en) * 2016-06-01 2020-10-08 Samsung Heavy Ind. Co., Ltd Offshore facility, floating crude oil production facility and method for generating liquefied natural gas

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