CN106524666B - Integrated mobile natural gas liquefaction device - Google Patents

Integrated mobile natural gas liquefaction device Download PDF

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Publication number
CN106524666B
CN106524666B CN201610960718.4A CN201610960718A CN106524666B CN 106524666 B CN106524666 B CN 106524666B CN 201610960718 A CN201610960718 A CN 201610960718A CN 106524666 B CN106524666 B CN 106524666B
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tower
heat exchanger
gas
unit
molecular sieve
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CN106524666A (en
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龚晓科
穆云飞
赵阳
王安胜
幸涛
陈宏伟
唐刚
杨敏
王婷
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Ningxia Kai Tian Gas Development Co ltd
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Ningxia Kai Tian Gas Development Co ltd
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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
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
    • F25J1/0215—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • 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
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F25J1/0268—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using a dedicated refrigeration means
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/02—Separating impurities in general from 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration

Abstract

The invention discloses a movable natural gas liquefaction device which is assembled in a movable integrated mode and comprises a heavy hydrocarbon removal unit, a decarburization unit, a dehydration unit, a liquefaction unit, an amine liquid regeneration unit, a cooling unit and public works. The liquefaction device adopts mixed refrigerant and R22 as refrigerant to provide refrigerating capacity for natural gas liquefaction, adopts R134a and air cooling to replace a traditional water cooling system, enables natural gas to be used rapidly and conveniently in regions without water and water shortage, and basically enables natural gas to be liquefied without laying pipelines on the ground. The invention changes the extension set mode into the all-in-one mode, further reduces the occupied area of the equipment, is more flexible, is convenient to move and assemble, is simple and convenient to operate and maintain, and saves manpower and material resources; the novel process is adopted, the energy consumption is saved, the automation degree is greatly improved, the problem of no water source is solved, and the novel process is applicable to various unconventional gases and complex terrains, so that the utilization rate of the unconventional gases is greatly improved.

Description

Integrated mobile natural gas liquefaction device
The technical field is as follows:
the invention belongs to a device for pretreating and liquefying natural gas, and particularly relates to an integrated movable natural gas liquefying device.
Background art:
the traditional LNG liquefaction factory has the disadvantages of complex planning procedure, high investment cost, long construction period, large occupied area, complex process, high overall energy consumption and limited application range, and is not suitable for gas utilization in remote mountain isolated wells, single wells and other places. Based on the great difficulty in developing unconventional natural gas, the complex geographical position of a gas well and the remote unreachable laying of pipelines, most of equipment in the prior art is divided into different modules according to functions at present, mainly modular mobile liquefaction equipment is taken as a main part, and a relatively mature nitrogen expansion process is mainly adopted in a refrigeration process; the absorption tower and the regeneration tower adopt a single high tower, the equipment height is higher, and the transportation has limitations. Therefore, in order to solve the practical problems of large occupied area, long construction period reduction, high cost, low integration, immobility and the like of the traditional liquefaction plant, the applicant develops an integrated mobile natural gas liquefaction device which adopts a low tower and simultaneously adopts a plurality of towers in series to realize decarburization and amine liquid regeneration and balances the energy of the whole circulation system, thereby saving the occupied space of equipment and energy consumption.
The invention content is as follows:
in order to overcome the problems in the prior art, the invention provides an unconventional natural gas pretreatment and liquefaction integrated mobile device which is simple in structure, high in product purity, simple in process, convenient to operate, low in energy consumption, stable in system, small in size and convenient to transport, and realizes a new breakthrough of high integration, integrated package and convenient transportation.
In order to solve the technical problems, the invention adopts the following technical scheme:
the integrated movable natural gas liquefaction device is assembled in a movable integrated mode and comprises a heavy hydrocarbon removal unit, a decarburization unit, a dehydration unit, a liquefaction unit, an amine liquid regeneration unit, a cooling unit and a public project.
The heavy hydrocarbon removal unit comprises an activated carbon purification tower A and an activated carbon purification tower B, namely, the heavy hydrocarbon of the feed gas is removed through the activated carbon purification tower A and the activated carbon purification tower B;
the decarbonization unit includes feed gas liquid separator, decarbonization column group, dust filter I, knockout drum, and the feed gas gets into desorption free water and partial solid impurity at first promptly in the feed gas liquid separator, and the gas of desorption major part water gets into earlier and takes off heavy hydrocarbon unit desorption heavy hydrocarbon, gets into decarbonization column group desorption CO again 2 Then pass through dustRemoving carried solid impurities of the activated carbon by using a filter I, then separating liquid carried in the activated carbon by using a separating tank, and finally removing water by using a dehydration unit;
the decarbonizing tower group is formed by connecting a plurality of decarbonizing towers in series, namely, gas subjected to heavy hydrocarbon decarbonization enters the decarbonizing tower to flow through the series connection of the plurality of towers, namely enters the tower from the middle-lower part of each tower, and is in countercurrent contact with the descending amine liquid at the top of the tower in the ascending process, wherein CO 2 Is absorbed; the gas from the tower top enters the next tower in turn to continuously absorb the CO which is not removed 2 。
The dehydration unit comprises a molecular sieve tower I, a regenerated gas cooler, a fuel gas buffer tank and a dust filter II, namely, raw material gas discharged from the separation tank of the decarburization unit enters the tower from the top of the molecular sieve tower I and passes through the molecular sieve, the moisture in the raw material gas is absorbed by the molecular sieve, and clean raw material gas flows out of the bottom of the molecular sieve tower I and goes to the liquefaction unit; when the adsorbed impurities of the molecular sieve reach saturation, the molecular sieve enters a regeneration state, namely high-temperature gas of the electric heater enters a molecular sieve tower I from the bottom of the tower through a program control valve, takes away the impurities on the molecular sieve in the tower from the top of the tower, and goes to a fuel gas buffer tank after being cooled to normal temperature through a regeneration gas cooler; the feed gas at the bottom of the molecular sieve tower I is subjected to dust removal through a dust filter II to form clean gas;
the liquefaction unit comprises a cold box, an R22 precooling compressor, an air cooling heat exchanger, an R22 storage tank, a mixed refrigerant compressor, a primary oil remover, an R22 precooling heat exchanger, a secondary oil remover, a tertiary oil remover, a molecular sieve tower II and an LNG storage tank, namely, the process of cooling the clean feed gas from the molecular sieve of the dehydration unit in the cold box is to condense the low-temperature refrigerant Freon and the mixed refrigerant into liquid LNG, specifically, the clean feed gas from the molecular sieve of the dehydration unit is cooled in the cold box, the Freon from the R22 precooling compressor is condensed into liquid phase by the R22 precooling heat exchanger, enters the R22 storage tank and is throttled and cooled by a throttle valve to be used as a cold source of the R22 precooling heat exchanger; separating mixed refrigerant and compressor oil from the mixed refrigerant compressor through a primary oil remover, and respectively cooling the mixed refrigerant and the compressor oil in an air-cooled heat exchanger; the method comprises the following steps that compressor oil returns to a mixed refrigerant compressor from an air-cooled heat exchanger, the mixed refrigerant sequentially enters a secondary oil remover, a tertiary oil remover, a molecular sieve tower and a dust filter after passing through the air-cooled heat exchanger, enters a cold box for cooling, and then enters a raw material gas-liquid separator, a gas phase and a liquid phase are divided into two paths to be used as cold sources to be further cooled in the cold box, and then are throttled and cooled by a throttle valve, enter the cold box and then return to the mixed refrigerant compressor;
the cold box comprises a precooling heat exchanger, a main cold heat exchanger I, a main cold heat exchanger II and a supercooling heat exchanger, wherein the four heat exchangers are sealed in a sealed box body and filled with pearlife for cold insulation. The method comprises the following steps that raw gas sequentially passes through a precooling heat exchanger and a main cooling heat exchanger I and then enters a heavy hydrocarbon separation tank, heavy hydrocarbon is separated out, the rest raw gas enters a main cooling heat exchanger II and then enters a gas-liquid separation tank, and the gas phase serving as flash evaporation gas sequentially passes through the main cooling heat exchanger II, the main cooling heat exchanger I and the precooling heat exchanger to recover cold and then serves as counter flow gas to enter a dehydration unit; the feed gas is divided into two paths, a small part of the feed gas is used as overcooling gas, is throttled and cooled by a throttle valve and then enters the overcooling heat exchanger as a cold source, and the rest of the feed gas is used as a cold heat exchanger and a throttle valve to obtain an overcooling LNG product and then enters the LNG storage tank.
The amine liquid regeneration unit comprises a regeneration tower, an amine liquid filter, a lean liquid cooler, a lean liquid pump, an amine liquid storage tank, a reboiler and CO 2 The exhaust gas condenser and the exhaust gas-liquid separator are used for regenerating the amine liquid from the bottom of the decarbonizing tower, wherein the regeneration process is to heat the amine liquid to ensure that CO in the amine liquid 2 Physical process of being desorbed. Desorbing the amine liquid from the bottom of the decarbonizing tower in a regenerating tower, recovering the heat in an amine liquid filter, cooling the amine liquid in a barren solution cooler to normal temperature, pumping the amine liquid back to the decarbonizing tower through a barren solution pump to absorb CO 2 (ii) a The amine liquid from the bottom of the regeneration tower enters an amine liquid storage tank, and the bottom of the amine liquid storage tank is communicated with a reboiler; CO from the regeneration column 2 Carrying a large amount of water vapor, passing through CO 2 Condensing the water in the exhaust gas condenser into liquid, and then feeding the liquid into an exhaust gas-liquid separator to separate water and CO 2 Discharging the water out of the system, and returning the water into the system;
the regeneration tower is formed by connecting a regeneration tower A, a regeneration tower B and a regeneration tower C in series, namely, amine liquid from the bottom of the decarburization tower enters the regeneration tower A from the top of the regeneration tower after being treated by a heat exchanger, the amine liquid is pumped into the regeneration tower B from the bottom of the regeneration tower through a connecting pump, and the amine liquid contacts with steam in a countercurrent manner again to continuously desorb CO in the amine liquid 2 。
The cooling unit comprises an R134a buffer tank, an R134a compressor, a condensing heat exchanger and a liquid storage tank, namely the cooling unit adopts a cooling process combining R134a and air cooling, namely R134a coming from the R134a buffer tank enters the R134a compressor, after being compressed, secondary oil content enters the R134a compressor for primary oil removal, the secondary oil content enters the condensing heat exchanger for condensation, the condensed R134a enters the liquid storage tank and is throttled, then the condensed R134a serves as refrigerant, enters an exhaust gas cooler for cooling medium, and returned gas phase R134a returns to the R134a buffer tank;
the public engineering comprises a heat conduction oil furnace, a regeneration gas heater and an air compressor, namely, the heat conduction oil furnace heats heat conduction oil, and hot heat conduction oil serving as a heat source enters a reboiler, the regeneration gas heater A and the regeneration gas heater B to heat amine liquid and regeneration gas; the air compressor purifies and compresses the air, and then the air is used as an air source of the pneumatic adjusting valve.
The integrated mobile natural gas liquefaction device adopts mixed refrigerant and R22 as refrigerant to provide refrigerating capacity for natural gas liquefaction, adopts the combination of R134a and air cooling to replace a traditional water cooling system, enables the natural gas to be quickly and conveniently used in areas without water and water, and basically enables the natural gas to be liquefied without laying pipelines on the ground.
The integrated mobile natural gas liquefaction device changes the extension set mode into the all-in-one mode, further reduces the occupied area of equipment, is more flexible, and is convenient to move and assemble. The liquefaction process is also improved, namely the original water cooling is reformed into a refrigeration mode combining R134a cooling and air cooling, the air cooling is directly adopted at the low-temperature section, the air cooling is firstly utilized at the high-temperature section, and then the R134a is utilized to cool the refrigerating capacity meeting the process requirement, so that the operation and the maintenance are simple and convenient, and the manpower and the material resources are saved; the new process is adopted to save energy consumption, and the automation degree is greatly improved.
To sum up, this portable natural gas liquefaction device of integration's beneficial effect lies in: (1) the investment cost is reduced, and the water is saved; (2) reduced floor space; (3) The construction period is shortened, and one third of time is saved; (4) The problem of no water source is solved, applicable in various unconventional gas, complicated topography, make unconventional gaseous utilization ratio promote greatly.
Description of the drawings:
FIG. 1 is a floor plan of an integrated mobile natural gas liquefaction plant of the present invention;
in the figure: 1-an active carbon purification tower A, 2-an active carbon purification tower B, 3-a raw gas liquid separator, 4-a decarbonization tower group, 5-a dust filter, 6-a molecular sieve tower IA, 7-a molecular sieve tower IB, 8-a cold box, 9-R22 precooling compressor, 10-a gas cooling heat exchanger, 11-a mixed refrigerant compressor, 12-a first-stage oil remover, 13-R22 precooling heat exchanger, 14-a second-stage oil remover, 15-a third-stage oil remover, 16-a molecular sieve tower II, 17-an amine liquid filter, 18-a lean liquid cooler, 19-an amine liquid storage tank, 20-CO 2 The system comprises a discharge gas condenser, a 21-discharge gas-liquid separator, a 22-regeneration tower A, a 23-regeneration tower B, a 24-regeneration tower C, a 25-R134a compressor and a 26-regeneration gas heater.
The specific implementation mode is as follows:
the technical solution of the present invention will be described in detail below with reference to the accompanying drawings and the detailed description.
As shown in figure 1, the integrated mobile natural gas liquefaction device adopts a mobile integrated mode and consists of a heavy hydrocarbon removal unit, a decarburization unit, a dehydration unit, a liquefaction unit, an amine liquid regeneration unit, a cooling unit and a public engineering, wherein:
the heavy hydrocarbon removal unit comprises an active carbon purification tower A1 and an active carbon purification tower B2, and the active carbon purification tower A1 is connected with the active carbon purification tower B2;
the decarburization unit comprises a raw material gas-liquid separator 3, a decarburization tower set 4, a dust filter 5 and a separation tank, wherein the raw material gas-liquid separator 3 is connected with the decarburization tower set 4, the tower bottom of the decarburization tower set 4 is connected with the dust filter 5, and the dust filter 5 is connected with the separation tank; the decarbonization tower group 4 is formed by connecting a plurality of decarbonization towers in series;
the dehydration unit comprises a molecular sieve tower I, a regenerated gas cooler and a fuel gas buffer tank, wherein the molecular sieve tower I is formed by connecting a molecular sieve tower IA 6 and a molecular sieve tower IB 7 in series, the tops of the molecular sieve tower IA 6 and the molecular sieve tower IB 7 are sequentially connected with the regenerated gas cooler, and the regenerated gas cooler is connected with the fuel gas buffer tank; the bottoms of the molecular sieve column IA 6 and the molecular sieve column IB 7 are connected to a dust filter 5 in the decarburization unit;
the liquefaction unit comprises a cold box 8, an R22 precooling compressor 9, an air cooling heat exchanger 10, an R22 storage tank, a mixed refrigerant compressor 11, a primary oil remover 12, an R22 precooling heat exchanger 13, a secondary oil remover 14, a tertiary oil remover 15, a molecular sieve tower II 16 and an LNG storage tank, wherein the cold box 8 is connected with a molecular sieve tower I in the dehydration unit, the R22 precooling compressor 9 is connected with the R22 precooling heat exchanger 13, and the R22 precooling heat exchanger 13 is connected with the R22 storage tank; the mixed refrigerant compressor 11 is sequentially connected to the primary oil remover 12, the air-cooled heat exchanger 10, the secondary oil remover 14, the tertiary oil remover 15, the molecular sieve tower II 16 and the dust filter 5 in the decarburization unit; the LNG storage tank is connected with the cold box 8; the cold box 8 comprises a precooling heat exchanger, a main cold heat exchanger I, a main cold heat exchanger II and a supercooling heat exchanger, the precooling heat exchanger, the main cold heat exchanger I, the main cold heat exchanger II and the supercooling heat exchanger are arranged in the sealed box body, and gaps between the precooling heat exchanger, the main cold heat exchanger I, the main cold heat exchanger II and the supercooling heat exchanger are filled with pearled sand for cold insulation; one ends of the precooling heat exchanger and the main cooling heat exchanger are respectively connected to the heavy hydrocarbon separation tank, one end of the main cooling heat exchanger II is connected to the gas-liquid separation tank, and the other ends of the main cooling heat exchanger II, the main cooling heat exchanger I and the precooling heat exchanger are connected to the dehydration unit; the supercooling heat exchanger is connected to the LNG storage tank;
the amine liquid regeneration unit comprises a regeneration tower, an amine liquid filter 17, a lean liquid cooler 18, a lean liquid pump, an amine liquid storage tank 19, a reboiler and CO 2 The system comprises an exhaust gas condenser 20 and an exhaust gas-liquid separator 21, wherein a regeneration tower is connected to the bottom of a decarburization tower in a decarburization unit, an amine liquid filter 17 is connected with the regeneration tower and a barren liquid cooler 18, and the barren liquid cooler 18 is connected with a barren liquid pump; the amine liquid storage tank 19 is connected to the bottom of the regeneration tower, and the bottom of the amine liquid storage tank 19 is communicated with the reboiler; CO2 2 Exhaust gas condenser 20 and regeneration tower, exhaustThe gas-liquid separator 21 is connected; the regeneration tower is formed by connecting a regeneration tower A22, a regeneration tower B23 and a regeneration tower C24 in series;
the cooling unit comprises an R134a buffer tank, an R134a compressor 25, a condensing heat exchanger, a liquid storage tank and an exhaust gas cooler, wherein the R134a buffer tank is connected with the R134a compressor 25, the R134a compressor 25 is connected with the condensing heat exchanger, and the condensing heat exchanger is connected with the liquid storage tank; the liquid storage tank is connected with the exhaust gas cooler;
the public engineering comprises a heat-conducting oil furnace, a regenerated gas heater 26 and an air compressor, wherein the heat-conducting oil furnace is sequentially connected with a reboiler and the regenerated gas heater 26 in the amine liquid regeneration unit; the air compressor purifies and compresses the air, and then the air is used as an air source of the pneumatic adjusting valve.
The integrated mobile natural gas liquefaction device is used in the unconventional natural gas pretreatment process, and each unit is specifically operated as follows:
the heavy hydrocarbon removal unit is used for removing impurities such as carbon dioxide, water, heavy hydrocarbon, mercury and the like contained in the feed gas through the module so as to achieve the index of removing the subsequent liquefaction module. Namely, the raw gas is heated by a water jacket furnace firstly, and then is throttled and depressurized to 40bar after being heated, and then enters a raw gas-liquid separator 3 to remove free water and some solid impurities. The gas with most of water removed enters an active carbon purification tower A1 and an active carbon purification tower B2 to remove heavy hydrocarbon, and then the carried active carbon solid impurities are removed through a dust filter 5.
The decarbonization unit is used for removing carbon dioxide from the gas subjected to heavy hydrocarbon removal treatment in a decarbonization tower group 4 with six towers connected in series. Absorption of CO using MDEA amine solutions 2 Raw gas flow rate of 2100Nm 3 H, amine liquid flow rate of 12m 3 H, the raw material gas enters the tower from the middle lower part of each tower, and is in countercurrent contact with the descending amine liquid in the tower top in the ascending process, wherein the CO 2 Is absorbed; the gas from the tower top enters the next tower in turn to continuously absorb the CO which is not removed 2 . The whole process gas flows in series through six towers, but the amine liquid flowing into the top of each tower flows into each tower from a main pipe through six branch pipes respectively, then flows out from the bottom of each tower, is collected to the main pipe, goes to a regeneration unit to remove carbon dioxide therein, and is recycledReturning to continue absorption. And (3) feeding the raw material gas discharged from the top of the last decarbonizing tower into a separation tank, separating liquid carried in the raw material gas, then removing water in a dehydration unit, and removing acid gases such as hydrogen sulfide and the like in the raw material gas in the process of removing carbon dioxide.
The dehydration unit adopts a molecular sieve to adsorb moisture in the feed gas. The main equipment consists of a molecular sieve tower IA 6 and a molecular sieve tower IB 7. And (3) raw material gas at normal temperature enters the tower from the top of the molecular sieve tower I and passes through the molecular sieve, moisture in the raw material gas is absorbed by the molecular sieve, and clean raw material gas flows out of the bottom of the molecular sieve tower and enters the liquefaction unit.
When the adsorption impurity of the molecular sieve reaches saturation, the adsorption can not be continued, and the impurities in the molecular sieve must be removed in a regeneration link so as to be put into use again. The clean raw material gas (which needs to be heated to 260 ℃) returned by the subsequent liquefaction process is used for the regeneration to blow off impurities in the clean raw material gas. The molecular sieve for removing impurities is in a high-temperature state because the molecular sieve is blown by high-temperature gas at 260 ℃ for a period of time, can not be directly taken to absorb moisture again, and needs to be cooled to normal temperature, and the clean raw material gas (normal temperature) returned by a subsequent liquefaction module is introduced into the tower to blow the molecular sieve to be cold. Thus, there are three operating states for a molecular sieve column, which are: working, regenerating and blowing cold.
The normal-temperature feed gas enters the molecular sieve column IA 6 from the bottom of the column and flows out from the top of the column. At the moment, the molecular sieve tower IA 6 is in a working state; when the molecular sieve tower IA 6 is saturated in adsorption, immediately entering a regeneration state; at the moment, high-temperature gas of 260 ℃ and 2bar coming from the electric heater enters the molecular sieve tower IA 6 from the bottom of the tower through the program control valve, impurities such as water on the molecular sieve in the tower are taken away from the top of the tower, and the gas is cooled to normal temperature through the regenerated gas cooler and then goes to a fuel gas buffer tank to serve as fuel of equipment such as a boiler and a gas generator. After the regeneration of the molecular sieve tower IA is finished, the temperature is reduced to normal temperature, 2bar is returned from the liquefaction unit, and normal-temperature clean feed gas enters the tower from the bottom of the tower to blow cold the molecular sieve. The hot clean raw material gas coming out from the tower top enters an electric heater to be heated to 260 ℃ and then enters a molecular sieve tower IB 7 to regenerate the molecular sieve tower IB 7, at the moment, a molecular sieve tower IA 6 is in a working state, and the switching of the tower states is controlled by a program control valve, so that every two towers are combined into a group, and the operation is continuous circulation during the work, regeneration, blowing cooling and working. The clean gas which comes out from the bottom of the molecular sieve tower and goes to the liquefied cold box needs to be removed by the dust filter 5 to remove the molecular sieve dust which may be carried, so that the cold box at the back is prevented from being blocked. At this point, the raw material gas is purified to become clean gas, and the requirement of entering the cold box is met.
Amine liquid (rich in CO) from the bottom of the decarbonizing tower of the amine liquid regeneration unit 2 Known as pregnant solution) must be regenerated. The regeneration process is to heat the amine liquid to make CO in the amine liquid 2 Physical process of being desorbed. Rich solution is treated with CO 2 The exhaust gas condenser 20 and the lean liquid cooler 18 obtain a part of heat from the hot lean liquid, and then enter the regeneration tower A22 from the top thereof, and are heated by steam from the bottom thereof, wherein CO is obtained 2 And part of the water was distilled off from the top of the column. The amine liquid is pumped into a regeneration tower B23 from the tower bottom through a connecting pump, and is contacted with steam in a countercurrent manner again to continuously desorb CO in the amine liquid 2 . Sequentially passing through three towers for three times to desorb CO 2 After being removed below the required precision, the product contains CO 2 The content is very low and is called lean liquor. The barren solution has a temperature of about 100 ℃, is not suitable for being directly used as an absorbent and needs to remove CO 2 The exhaust gas condenser 20 recovers its heat, leaving the CO 2 The temperature of the discharged gas is reduced to about 60 ℃ by a condenser 20, then the discharged gas is cooled to the normal temperature by a barren solution cooler 18, and finally the discharged gas is pumped back to the decarburization tower group 4 by a barren solution pump to absorb CO 2 . The lean solution from the bottom of the regeneration tower C24 enters the amine solution storage tank 19 through the amine solution pump of the regeneration tower, and all the heat required by the regeneration process is provided by the steam. The steam of 8bar heats the amine liquid to generate a large amount of steam, the steam enters the three regeneration towers from the side parts of the bottoms of the towers through the main pipe and the three branch pipes respectively, and the amine liquid descending in the towers is heated to promote the amine liquid to be desorbed. CO from three regeneration columns 2 Carrying a large amount of water vapor, condensing the water in the lean solution into liquid through a lean solution cooler 18, and then separating the water and CO in a separation tank 2 The water is discharged out of the system and then returned to the system.
Clean raw material gas from the molecular sieve of the liquefaction unit enters a cold box, and is condensed into liquid LNG by low-temperature refrigerant (Freon and mixed refrigerant) in the cold box. After the freon coming from the R22 precooling compressor 9 passes through the air cooling heat exchanger 10, the freon is completely condensed into a liquid phase, enters the R22 storage tank, is throttled and cooled by the throttle valve, and then is used as a cold source of the R22 precooling heat exchanger 13 to cool the mixed refrigerant and the raw material gas. The mixed refrigerant from the mixed refrigerant compressor 11 passes through the first-stage oil remover 12 to separate out mixed refrigerant and compressor oil, and respectively enters the corresponding heat exchangers for cooling, the compressor oil returns to the R22 precooling compressor 9 after coming out of the R22 precooling heat exchanger 13, the mixed refrigerant sequentially enters the second-stage oil remover 14, the third-stage oil remover 15, the molecular sieve tower II 16 and the dust filter 5 and then enters the precooling heat exchanger for precooling, the main cooling heat exchanger is further cooled and then is throttled and cooled by the throttle valve and then enters the gas-liquid separator, the gas phase and the liquid phase are divided into two paths as cold sources to enter the second main cooling heat exchanger, and the gas phase and the liquid phase are returned to the mixed refrigerant compressor 11 after passing through the first main cooling heat exchanger.
The feed gas then passes through the precooling heat exchanger in proper order, and main cold heat exchanger is the back, gets into the heavy hydrocarbon knockout drum, separates out the heavy hydrocarbon, and remaining feed gas gets into main cold heat exchanger two after, gets into the gas-liquid separation jar, and wherein the gaseous phase is through main cold heat exchanger two as flash distillation gas in proper order, and main cold heat exchanger one, after the cold volume is retrieved to the precooling heat exchanger, goes the dehydration unit as the refluence gas. The feed gas is divided into two paths, a small part of the feed gas is used as overcooled gas, is throttled and cooled by a throttle valve and then enters a supercooling heat exchanger as a cold source, and the rest of the feed gas is used as a supercooled LNG product after passing through the supercooling heat exchanger and the throttle valve to enter an LNG storage tank.
The cooling unit adopts a cooling process combining R134a and air cooling, namely, R134a from an R134a buffer tank enters an R134a compressor 25, after compression, secondary oil is subjected to primary oil removal, and then the oil enters a condensing heat exchanger for condensation. The condensed R134a enters a liquid storage tank, is throttled and then enters an exhaust gas cooler as refrigerant to cool the medium, and the returned gas phase R134a returns to the R134 buffer tank.
The heat conduction oil furnace of the public engineering heats the heat conduction oil, the hot heat conduction oil is used as a heat source and enters the reboiler, the regenerated gas heater 26 and the regenerated gas heater 26 to heat the amine liquid and the regenerated gas; the air compressor purifies and compresses the air, and then the air is used as an air source of the pneumatic adjusting valve.
The integrated mobile natural gas liquefaction device has a plurality of complex components, only 87 main devices are provided, wherein the dynamic devices comprise an R22 compressor, an R134a compressor, a mixed refrigerant compressor, a barren liquid pump, an amine liquid connecting pump, an air compressor, a vacuum pump and the like, and the static devices comprise various rectifying towers, storage tanks, reactors, reboilers and the like. Although the equipment is multiple and complex, the integrated mobile liquefaction equipment is highly integrated, integrally packaged and convenient to transport under the condition that the equipment is so many, so that the natural gas liquefaction device can be moved to a new height. The whole set of equipment only has one skid-mounted machine set, the length of the skid-mounted machine set is 30 meters, the width of the skid-mounted machine set is 13 meters, and the height of the skid-mounted machine set is 3.2 meters. The occupied area is smaller, the investment and construction period is shorter, and the energy consumption and the water consumption are both greatly reduced. The equipment adopts mixed refrigerant and R22 as refrigerant to provide refrigerating capacity for natural gas liquefaction, adopts R134a and air cooling to replace a traditional water cooling system, enables natural gas to be used rapidly and conveniently in regions without water and water shortage, and basically enables natural gas to be liquefied without laying pipelines on the ground.
The integrated mobile natural gas liquefaction device has the characteristics that:
(1) Flexibility: the movable air-conditioning unit can be moved at any time and transported by an automobile to different air source places for production;
(2) Stability: the process is mature and reliable, and the equipment is produced in a standardized way;
(3) Convenience: the device completes production debugging in a factory, and the gas source can be put into operation only by simple connection on site;
(4) Space saving: the whole device occupies small area, and only needs 180 square meters;
(5) The economic efficiency is as follows: the investment is greatly lower than that of a fixed factory with the same production capacity, and the investment can be saved by 30 percent;
(6) The construction period is short: the device is delivered for use in 3 months, and the period is shortened by about two thirds compared with the period for building a fixed factory.
The advantages are that:
(1) The device is highly intelligent and integrated;
(2) The innovative purification process has lower energy consumption and more miniaturized equipment;
(3) The utility model is modularized and controlled in container type;
(4) Each module is controlled by a PLC (programmable logic controller), and the PLC is communicated with an upper computer through a TCP/IP (transmission control protocol/Internet protocol) protocol to reduce instrument wiring;
(5) The perfect control scheme is simple and convenient to operate and stable in performance;
(6) The comprehensive recycling of various unconventional gases is realized;
(7) The adoption of the field liquefaction mode avoids a large amount of investment on ground facilities and pipelines,
(8) The novel purification method is adopted to purify the feed gas, the purification process is simple to operate, the energy consumption is low, the application range is wide, and the novel purification method can be used for various common natural gas sources and various unconventional gases and can be applied to complex terrains, so that the utilization rate of the unconventional gases is greatly improved.

Claims (3)

1. Portable natural gas liquefaction device of integration adopts the mode equipment of portable integration to form its characterized in that: portable natural gas liquefaction device of integration comprises heavy hydrocarbon unit, decarbonization unit, dehydration unit, liquefaction unit, amine liquid regeneration unit, cooling unit and public work, wherein:
the heavy hydrocarbon removal unit comprises an active carbon purification tower A (1) and an active carbon purification tower B (2), wherein the active carbon purification tower A (1) is connected with the active carbon purification tower B (2);
the decarburization unit comprises a raw material gas-liquid separator (3), a decarburization tower set (4), a dust filter (5) and a separation tank, wherein the raw material gas-liquid separator (3) is connected with the decarburization tower set (4), the tower bottom of the decarburization tower set (4) is connected to the dust filter (5), and the dust filter (5) is connected with the separation tank; the decarbonization tower group (4) is formed by connecting a plurality of decarbonization towers in series;
the dehydration unit comprises a molecular sieve tower I, a regenerated gas cooler and a fuel gas buffer tank, wherein the molecular sieve tower I is formed by connecting a molecular sieve tower IA (6) and a molecular sieve tower IB (7) in series, the tops of the molecular sieve tower IA (6) and the molecular sieve tower IB (7) are sequentially connected with the regenerated gas cooler, and the regenerated gas cooler is connected with the fuel gas buffer tank; the bottoms of the molecular sieve column IA (6) and the molecular sieve column IB (7) are connected to a dust filter (5) in the decarbonization unit;
the liquefaction unit comprises a cold box (8), an R22 pre-cooling compressor (9), a gas-cooling heat exchanger (10), an R22 storage tank, a mixed refrigerant compressor (11), a primary oil remover (12), an R22 pre-cooling heat exchanger (13), a secondary oil remover (14), a tertiary oil remover (15), a molecular sieve tower II (16) and an LNG storage tank, wherein the cold box (8) is connected with a molecular sieve tower I in the dehydration unit, the R22 pre-cooling compressor (9) is connected with the R22 pre-cooling heat exchanger (13), and the R22 pre-cooling heat exchanger (13) is connected with the R22 storage tank; the mixed refrigerant compressor (11) is sequentially connected to the primary oil remover (12), the air-cooled heat exchanger (10), the secondary oil remover (14), the tertiary oil remover (15), the molecular sieve tower II (16) and the dust filter (5) in the decarburization unit; the LNG storage tank is connected with the cold box (8); the cold box (8) comprises a precooling heat exchanger, a first main cold heat exchanger, a second main cold heat exchanger and a supercooling heat exchanger, the precooling heat exchanger, the first main cold heat exchanger, the second main cold heat exchanger and the supercooling heat exchanger are arranged in the sealed box body, and gaps between the precooling heat exchanger, the first main cold heat exchanger, the second main cold heat exchanger and the supercooling heat exchanger are filled with pearled sand for cold insulation;
the amine liquid regeneration unit comprises a regeneration tower, an amine liquid filter (17), a lean liquid cooler (18), a lean liquid pump, an amine liquid storage tank (19), a reboiler, a CO2 exhaust gas condenser (20) and an exhaust gas-liquid separator (21), the regeneration tower is connected to the bottom of a decarbonization tower in the decarbonization unit, the amine liquid filter (17) is connected with the regeneration tower and the lean liquid cooler (18), and the lean liquid cooler (18) is connected with the lean liquid pump; the amine liquid storage tank (19) is connected to the bottom of the regeneration tower, and the bottom of the amine liquid storage tank (19) is communicated with the reboiler; CO2 2 The exhaust gas condenser (20) is connected with the regeneration tower and the exhaust gas-liquid separator (21);
the cooling unit comprises an R134a buffer tank, an R134a compressor (25), a condensing heat exchanger, a liquid storage tank and a discharged gas cooler, wherein the R134a buffer tank is connected with the R134a compressor (25), the R134a compressor (25) is connected with the condensing heat exchanger, and the condensing heat exchanger is connected to the liquid storage tank; the liquid storage tank is connected with the exhaust gas cooler;
the utility project comprises a heat-conducting oil furnace, a regenerated gas heater (26) and an air compressor, wherein the heat-conducting oil furnace is sequentially connected with a reboiler and the regenerated gas heater (26) in the amine liquid regeneration unit; the air compressor purifies and compresses the air, and then the air is used as an air source of the pneumatic adjusting valve.
2. The integrated mobile natural gas liquefaction plant of claim 1, wherein: one ends of the precooling heat exchanger and the main cooling heat exchanger are respectively connected to the heavy hydrocarbon separation tank, one end of the main cooling heat exchanger is connected to the gas-liquid separation tank, and the other ends of the main cooling heat exchanger, the main cooling heat exchanger I and the precooling heat exchanger are connected to the dehydration unit; the supercooling heat exchanger is connected to the LNG storage tank.
3. The integrated mobile natural gas liquefaction plant of claim 1, wherein: the regeneration tower is formed by connecting a regeneration tower A (22), a regeneration tower B (23) and a regeneration tower C (24) in series.
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