CN205002518U - Take flash vessel and methane gas recovery system of heat transfer - Google Patents

Take flash vessel and methane gas recovery system of heat transfer Download PDF

Info

Publication number
CN205002518U
CN205002518U CN201520244116.XU CN201520244116U CN205002518U CN 205002518 U CN205002518 U CN 205002518U CN 201520244116 U CN201520244116 U CN 201520244116U CN 205002518 U CN205002518 U CN 205002518U
Authority
CN
China
Prior art keywords
tank body
gas
methane
methane gas
flash vessel
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201520244116.XU
Other languages
Chinese (zh)
Inventor
陈�峰
邢浩
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
New Austrian Energy Engineering Technology Co Ltd
Original Assignee
ENN Coal Gasification Mining Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by ENN Coal Gasification Mining Co Ltd filed Critical ENN Coal Gasification Mining Co Ltd
Priority to CN201520244116.XU priority Critical patent/CN205002518U/en
Application granted granted Critical
Publication of CN205002518U publication Critical patent/CN205002518U/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
    • 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
    • F25J1/0032—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • 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
    • F25J1/0201—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 only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—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 only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • 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
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/24—Multiple compressors or compressor stages in parallel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream

Landscapes

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

Abstract

The utility model relates to a take the flash vessel of heat transfer, the flash vessel is including a jar body, internal being equipped with of jar is located jar gas -liquid separation of body lower part and is located jar heat transfer device on body upper portion, heat transfer device includes two at least passageways, wherein first passageway with jar be used for the first air inlet intercommunication of receiver gases on the body, the second channel with second air inlet on the jar body is linked together, wherein the second air inlet passes through the first gas outlet on jar body top is connected with compressor arrangement, the bottom of the jar body is equipped with the liquid outlet. The utility model discloses with heat transfer device and the integration of gas -liquid separation two parts structure to the cold volume of utilization that can be better reduces the waste of energy, make equipment area also reduce simultaneously thereupon, reduced investment cost.

Description

Flash vessel with heat exchange and methane gas recovery system
Technical field
The utility model relates to the technical field of gas recycling, refers in particular to the liquefaction again and recovery that are applied in boil-off gas (BOG) in liquefied natural gas (LNG) storage and transportation.
Background technology
Liquefied natural gas (LNG) main component is methane, being recognized is the energy the cleanest on the earth, colourless, tasteless, nontoxic and non-corrosiveness, its volume is about with amount gaseous natural gas volume 1/625, and the weight of liquefied natural gas is only about 45% of consubstantiality ponding.Liquefied natural gas is natural gas via compression, be cooled to its boiling temperature after become liquid, usual LNG storage subzero 161.5 degrees Celsius, in the low-temperature storage tank of about 0.1MPa, with special purpose ship or oil truck transport, again gasify during use.Very little to air pollution after liquefied natural gas burning, and liberated heat is large, so liquefied natural gas is a kind of more advanced energy.
But in LNG ship oceangoing ship, tank car transportation and LNG filling, uninstall process, due to the heat transmission that the huge temperature difference between environment temperature and low temperature LNG produces, the precooling of station system and other reason, the LNG of low temperature constantly can be heated and produce boil-off gas (being called for short BOG).Although the low-temperature (low temperature) vessel storing LNG has heat insulation layer; but still the impact of outer heat cannot be avoided, cause the increase producing BOG, BOG to make the pressure increase of system; once pressure exceedes the operating pressure that storage tank allows, need to start safety guard release BOG decompression.
Existing methane gas way of recycling comprise gasification methane gas out through with air heat-exchange after enter urban pipe network or use compressor that these methane gas are become the methane gas product that CNG(pressure is greater than 20MPa).To enter urban pipe network scheme need LNG filling station near urban pipe network, inapplicable to common LNG filling station; Make CNG product market value lower, accumulating is complicated, and compression power consumption is higher, and equipment takes up an area larger.Also the low-temperature receivers such as liquid nitrogen are utilized to cool methane, again the reuse of low temperature methane liquid is become, but the method need arrange separately cold generation device, investment and run power consumption higher, flow process is complicated and occupation of land is larger, the cost of the methane reclaimed is higher, and the rate of recovery is low, causes the waste of the energy to a certain extent.
In order to overcome the problems referred to above, there is the mounting structure of a kind of small-sized prizing liquefied natural gas boil-off gas recovery device of liquefied again in prior art, comprising: low-temperature storage tank, regenerating type low-temperature refrigerator, condensing heat exchanger; Condensing heat exchanger is arranged on the cold junction of regenerating type low-temperature refrigerator; Boil-off gas transfer passage and liquefied natural gas transfer passage is provided with between low-temperature storage tank and condensing heat exchanger; The liquefied natural gas at condensing heat exchanger place can enter low-temperature storage tank along liquefied natural gas transfer passage under gravity.Although above-mentioned document improves liquefaction efficiency again, ensure that equipment operational reliability and security, but described regenerating type low-temperature refrigerator and condensing heat exchanger must be arranged on the top of described low-temperature storage tank, therefore for equipment, certain requirement is installed, not easily realizes effectively reducing I&M cost; In addition, the rate of recovery of gas does not increase substantially.
Utility model content
For this reason, technical problem to be solved in the utility model is to overcome in prior art the problem that I&M cost is high and the rate of recovery is low that reclaims methane thus provides a kind of I&M cost of not only equipment low, and the flash vessel of the high band heat exchange of the rate of recovery and methane gas recovery system.
For solving the problems of the technologies described above, a kind of flash vessel with heat exchange described in the utility model, described flash vessel comprises tank body, be provided with the gas-liquid separation device being positioned at tank body lower part in described tank body and be positioned at the heat-exchanger rig on tank body top, described heat-exchanger rig comprises at least two passages, wherein first passage is communicated with the first air inlet for receiver gases on described tank body, second channel is connected with the second air inlet on described tank body, wherein said second air inlet is connected with compression set by first gas outlet on described tank body top, the bottom of described tank body is provided with liquid outlet.
In an embodiment of the present utility model, described heat-exchanger rig comprises cooling tube or tubulation, and forms first passage between the inwall of described cooling tube or tubulation and described tank body, and the inside of described cooling tube or tubulation forms second channel.
In an embodiment of the present utility model, described tank body top is provided with bracing frame along inwall, and described heat-exchanger rig is fixed on support frame as described above.
In an embodiment of the present utility model, in described gas-liquid separation device, be provided with dividing plate along inwall.
In an embodiment of the present utility model, the quantity of described dividing plate is multiple, and multiple dividing plate is crisscross arranged successively in the opposed inner walls of described tank body.
In an embodiment of the present utility model, the second channel of described heat-exchanger rig exports with the high-pressure material on described tank body and communicates, described gas-liquid separation device communicates with the low pressure material inlet on described tank body, and the outlet of described high-pressure material is connected to described low pressure material inlet by the decompressor being arranged on described tank body outside.
In an embodiment of the present utility model, the second channel of described heat-exchanger rig is communicated with described gas-liquid separation device by the decompressor being positioned at described tank body.
In an embodiment of the present utility model, the lower end of described tank body is respectively equipped with interface on liquid level gauge and is positioned at the liquid level gauge lower interface of interface lower end on described liquid level gauge.
In an embodiment of the present utility model, the top of described tank body is provided with the diffusion mouth for being vented.
The utility model additionally provides a kind of methane gas recovery system, comprise the above-mentioned flash vessel with heat exchange described in any one, described first gas outlet is connected to described second air inlet through described compression set, and described heat-exchanger rig is communicated with described gas-liquid separation device by decompressor.
Technique scheme of the present utility model has the following advantages compared to existing technology:
The flash vessel of band heat exchange described in the utility model and methane gas recovery system, integrate heat-exchanger rig and gas-liquid separation device two-part structure, thus can better utilize cold to reduce the waste of energy; Make occupation area of equipment also reduce simultaneously thereupon, reduce cost of investment.
Accompanying drawing explanation
In order to make content of the present utility model be more likely to be clearly understood, below according to specific embodiment of the utility model also by reference to the accompanying drawings, the utility model is described in further detail, wherein
Fig. 1 is the flash vessel with heat exchange described in the utility model embodiment one;
Fig. 2 is the flash vessel with heat exchange described in the utility model embodiment two;
Fig. 3 is the flash vessel with heat exchange described in the utility model embodiment three;
Fig. 4 is the schematic diagram of methane gas recovery system described in the utility model embodiment four;
Fig. 5 is the schematic diagram of methane gas recovery system described in the utility model embodiment five;
Fig. 6 is the schematic diagram of methane gas recovery system described in the utility model embodiment six;
Fig. 7 is the schematic diagram of methane gas recovery system described in the utility model embodiment seven;
Fig. 8 is a schematic diagram of methane gas recovery system described in the utility model embodiment eight;
Fig. 9 is another schematic diagram of methane gas recovery system described in the utility model embodiment eight.
Detailed description of the invention
Embodiment one:
As shown in Figure 1, present embodiments provide a kind of flash vessel with heat exchange, described flash vessel comprises tank body 30, the gas-liquid separation device 31 being positioned at tank body lower part and the heat-exchanger rig 32 being positioned at tank body top is provided with in described tank body 30, described heat-exchanger rig 32 comprises at least two passages, wherein first passage is communicated with the first air inlet 33A for receiver gases on described tank body 30, second channel is connected with the second air inlet 34A on described tank body 30, wherein said second air inlet 34A is connected with compression set 14 by the first gas outlet 34B on described tank body 30 top, the bottom of described tank body 30 is provided with liquid outlet 33B.
The flash vessel of band heat exchange described in the utility model, described flash vessel comprises tank body 30 and several different air inlets of being arranged on tank body 30 and gas outlet, wherein, the gas-liquid separation device 31 being positioned at tank body lower part and the heat-exchanger rig 32 being positioned at tank body top is provided with in described tank body 30, described heat-exchanger rig 32 and described gas-liquid separation device 31 two-part structure are integrated and are seated in tank body 30 by the utility model, thus can better utilize cold to reduce the waste of energy, make occupation area of equipment reduce simultaneously thereupon, reduce cost of investment, described tank body 30 is provided with the first air inlet 33A for receiver gases, methane gas enters in described tank body 30 by described first air inlet 33A, the top of described tank body 30 is respectively equipped with the second air inlet 34A and the first gas outlet 34B, described heat-exchanger rig 32 comprises at least two passages, wherein first passage is communicated with described first air inlet 33A, second channel is connected with described second air inlet 34A, described second air inlet 34A is connected with described first gas outlet 34B by described compression set 14, enter the high pressure methane gas heat exchange of methane gas after compressing in the first passage and second channel of heat-exchanger rig 32 in described tank body 30, described methane gas flows in described compression set 14 from described first gas outlet 34B, the high pressure methane gas formed after the compression process of described compression set 14 is back in described tank body 30 by described second air inlet 34A, high pressure low temperature methane gas is formed after heat exchange cooling in the second channel of described heat-exchanger rig 32, described high pressure low temperature methane gas forms the mixture of gaseous methane and liquid methane through reduced pressure treatment, the mixture of described methane gas and liquid methane enters the mixture being separated into low-temp low-pressure methane gas and methane liquid in described gas-liquid separation device 31, the bottom of described tank body 30 is provided with liquid outlet 33B, for described methane liquid is directly discharged, the first passage that described isolated methane gas enters described heat-exchanger rig 32 in the lump with the methane gas in described first air inlet 33A carries out circular treatment.The flash vessel of band heat exchange described in the utility model, methane gas can use at described tank body 30 Inner eycle, effectively improves energy utilization rate, avoids energy waste, reduce recovery power consumption; The setting of described liquid outlet 33B enables methane liquid finished product directly collect recycling, thus improves energy utilization rate; Moreover equipment described in the utility model, investment and to run power consumption little, reclaiming product is that liquefied natural gas can market goods locally, and reduce methane recovery power consumption, the efficiency therefore not only reclaiming methane gas increases substantially, and reduces I&M cost.
In the present embodiment, described heat-exchanger rig 32 comprises the multiple heat exchange structure such as cooling tube or tubulation, and form first passage between the inwall of described cooling tube or tubulation and described tank body 30, the inside of described cooling tube or tubulation forms second channel, can realize heating up to the heat exchange of described low temperature methane gas by described first passage, can realize lowering the temperature to the heat exchange of described middle temperature methane gas by described second channel.
In order to realize the mixture described high pressure low temperature methane gas being formed gaseous methane and liquid methane through reduced pressure treatment, described tank body 30 is respectively equipped with high-pressure material outlet 35B and low pressure material inlet 35A, second channel and the described high-pressure material of described heat-exchanger rig 32 export 35B and communicate, described gas-liquid separation device 31 communicates with described low pressure material inlet 35A, particularly, described high-pressure material outlet 35B is connected to described low pressure material inlet 35A by the decompressor 15 being arranged on described tank body 30 outside, after methane gas in described tank body 30 enters described decompressor 15, volumetric expansion becomes the gaseous methane of low-temp low-pressure, because methane can absorb most of heat in expansion process, thus make methane liquefy, form the mixture of gaseous methane and liquid methane.
Constantly can recycle in described tank body 30 to realize methane gas, described first air inlet 33A is positioned at the lower end of described heat-exchanger rig 32, and described tank body 30 top is provided with bracing frame 36 along inwall, and described heat-exchanger rig 32 is fixed on support frame as described above 36.
The lower end of described tank body is respectively equipped with interface 37A on liquid level gauge and is positioned at the liquid level gauge lower interface 37B of interface lower end on described liquid level gauge, in order to constantly improve the automatic recovery of methane gas, when the amount of liquid collected in described gas-liquid separation device 31 does not reach the position of described liquid level gauge lower interface 37B, controlling described liquid outlet 33B is closed state, once amount of liquid collected position between interface 37A and described liquid level gauge lower interface 37B on described liquid level gauge, open described liquid outlet 33B, liquid methane is discharged, thus be conducive to the separate run times of extension device, full liquid in described tank body 30 is avoided to note the problem of not air inlet body.
In the present embodiment, the liquid outlet 33B of described tank body 30 is connected with finished pot 16, the liquid outlet 33B of described tank body 30 is connected with described finished pot 16 and forms liquids recovery channel B, methane liquid finished product is directly back in described finished pot 16, thus avoids diffusing of finished pot 16 and cause reducing the problem of fluid temperature.
Described tank body 30 is axially arranged with the fixed support 38 for fixing described tank body 30 along outer wall, can be fixed on chassis by described tank body 30 entirety by described fixed support 38, easily forms skid integral structure, thus ensure that operational reliability and security.The top of described tank body 30 is also provided with the diffusion mouth 39 for being vented, if the gas pressure in described tank body 30 is too high, ensure that the safety of tank body thus avoid occurring the accidents such as destruction by gas purging in described diffusion mouth 39.
Embodiment two:
As shown in Figure 2, embodiment two is the improvement made on the basis of embodiment one, in order to the recycling of perfect recovery methane gas, the flash vessel of embodiment one adds the equipment of recycling, the following detailed description of:
In the present embodiment, dividing plate 40 is provided with along inwall in described gas-liquid separation device 31, because the temperature entering the methane gas in tank body 30 from described first air inlet 33A is higher than the temperature of the mixture from the gaseous methane formed through reduced pressure treatment and liquid methane, by the setting of described dividing plate 40, can prevent two kinds of gases from directly contacting, the time of effective prolongation two kinds of gas and vapor permeation, avoid liquid methane again to absorb heat and cause becoming the generation of methane gas, thus more methane liquid is separated from described gas-liquid separation device 31.In order to extend the time of two kinds of gas and vapor permeation, isolate more methane liquid to the full extent, the quantity of described dividing plate 40 is multiple, and multiple dividing plate 40 is crisscross arranged successively in the opposed inner walls of described tank body 30.In the present embodiment, the setting of described dividing plate 40 effectively can improve the liquefaction efficiency of methane, but needs to produce maintenance cost, suitably increases cost.
Embodiment three:
As shown in Figure 3, embodiment three is the improvement made on the basis of embodiment one or embodiment two, in order to the recycling of perfect recovery methane gas, is arranged on by described decompressor 15 in described tank body 30, the following detailed description of:
In the present embodiment, to form the mixture of gaseous methane and liquid methane through reduced pressure treatment in order to realize described high pressure low temperature methane gas, the second channel of described heat-exchanger rig 32 is communicated with described gas-liquid separation device 31 by the decompressor 15 being positioned at described tank body 30, methane gas after reduced pressure treatment directly flows in described gas-liquid separation device 31, the speed of recovery methane is not only made to accelerate, effective raising energy utilization rate, and the floor space of whole equipment is less, reduce cost of investment, if avoid the energy loss caused when the methane gas after heat exchange flows to the decompression of described tank body 30 outside.
Embodiment four
As shown in Figure 4, present embodiments provide a kind of methane gas recovery system, make use of embodiment one, embodiment two, the flash vessel of any one band heat exchange in embodiment three, particularly, described system comprises tank body 30, the gas-liquid separation device 31 being positioned at tank body 30 bottom and the heat-exchanger rig 32 being positioned at tank body top is provided with in described tank body 30, described heat-exchanger rig 32 comprises at least two passages, wherein first passage is communicated with the first air inlet 33A for receiver gases on described tank body 30, second channel is connected with the second air inlet 34A on described tank body 30, described second air inlet 34A is connected with compression set 14 by the first gas outlet 34B on described tank body 30 top, described heat-exchanger rig 32 is communicated with described gas-liquid separation device 31 by decompressor 15, the bottom liquid outlet 33B of described tank body 30 forms liquids recovery channel B.
Above-mentioned is core technology scheme described in the utility model, methane gas recovery system described in the utility model comprises tank body 30, with the interconnective compression set 14 of described tank body 30 and decompressor 15, described tank body 30 is provided with the first air inlet 33A for receiver gases, be provided with the gas-liquid separation device 31 being positioned at tank body lower part in described tank body 30 and be positioned at the heat-exchanger rig 32 on described tank body top, described methane gas enters after in described tank body 30, low pressure intensification methane gas is formed after the first passage heating of described heat-exchanger rig 32, first gas outlet 34B of described tank body 30 is connected to the second air inlet 34A of described tank body 30 through compression set 14, enter the low pressure intensification methane gas after heat exchange and flow to described compression set 14 by described first gas outlet 34B, low pressure intensification methane gas forms warm methane gas in high pressure after the pressurized treatments of described compression set 14, be back in described tank body 30 by described second air inlet 34A, in described high pressure, warm methane gas forms high pressure low temperature methane gas after described heat-exchanger rig 32 second channel heat exchange cooling, described high pressure low temperature methane gas forms the mixture of gaseous methane and liquid methane after the throttling process of described decompressor 15, the mixture of described gaseous methane and liquid methane is separated into low-temp low-pressure methane gas and methane liquid in described gas-liquid separation device 31, wherein, described heat-exchanger rig 32, described compression set 14 and described decompressor 15 form gas circulation channel A, in described gas-liquid separation device 31, isolated low-temp low-pressure methane gas and the methane gas from described first charging aperture 33A inflow tank body 30 constantly circulate in gas circulation channel A, the bottom liquid outlet 33B of described tank body 30 forms liquids recovery channel B, the methane liquid be separated in described tank body 30 flows out from liquids recovery channel B.Low temperature methane gas in tank body 30 described in the utility model can be recycled in gas circulation channel A, and methane gas is used at described tank body 30 Inner eycle to the full extent, effectively improves energy utilization rate, avoids energy waste, reduce recovery power consumption; The setting of described liquids recovery channel B enables methane liquid finished product directly collect recycling, thus improves energy utilization rate; Moreover the utility model technological process is simple, can make skid integral type, investment and to run power consumption little, reclaiming product is that liquefied natural gas can market goods locally, reduces methane recovery power consumption, therefore the efficiency not only reclaiming methane gas increases substantially, and reduces I&M cost.
The following describes the operation principle of methane gas recovery system:
Described methane gas enters in described tank body 30 by the first air inlet 33A, the operative liquid methane carried in methane gas can by initial gross separation in gas-liquid separation device 31, liquid methane flows out by liquids recovery channel B, and described methane gas and enter described heat-exchanger rig 32 from isolated low-temp low-pressure methane gas in described gas-liquid separation device 31, low pressure intensification methane gas is formed after the methane gas of low-temp low-pressure carries out heat exchange intensification in described heat-exchanger rig 32, low pressure intensification methane gas to enter in described compression set 14 and form warm methane gas in high pressure after the pressurized treatments of described compression set 14, in high pressure, warm methane gas enters described heat-exchanger rig 32 and lowers the temperature with the low-pressure low-temperature methane gas heat exchange entered in described tank body 30, high pressure low temperature methane gas is formed after abundant heat exchange, described high pressure low temperature methane gas forms the mixture of low-pressure low-temperature methane gas and methane liquid after the step-down process of described decompressor 15, wherein, described high pressure low temperature methane gas is when described decompressor 15, methane gas volumetric expansion becomes the gaseous methane of low-temp low-pressure, because methane can absorb most of heat in expansion process, thus make methane liquefy, form the mixture of gaseous methane and liquid methane.The mixture of described gaseous methane and liquid methane flows in described gas-liquid separation device 31, is separated into methane gas and methane liquid in described gas-liquid separation device 31, and described methane gas is in the process of described tank body 30 Inner eycle; Described isolated methane liquid is discharged from described liquid outlet 33B, is completed the recovery of methane liquid by liquids recovery channel B.
Above-mentioned high pressure low temperature methane gas is when described decompressor 15, described decompressor 15 can be arranged on the outside of described tank body 30, now the second channel of described heat-exchanger rig 32 exports 35B with the high-pressure material on described tank body 30 and communicates, described gas-liquid separation device 31 communicates with the low pressure material inlet 35A on described tank body 30, and described high-pressure material outlet 35B is connected to described low pressure material inlet 35A by described decompressor 15, the mixture that high pressure low temperature methane gas in described tank body 30 forms low-pressure low-temperature methane gas and methane liquid after the step-down process of described decompressor 15 is back in described tank body 30, methane gas and methane liquid is separated into by described gas-liquid separation device 31.
In the present embodiment, described heat-exchanger rig 32 can be heat exchanger, and described compression set 14 can be compressor, and described decompressor 15 can be pressure-reducing valve.
Embodiment five:
As shown in Figure 5, embodiment five is the improvement made on the basis of embodiment four, in order to the system of perfect recovery methane gas, the system of embodiment four adds the equipment of recycling, the following detailed description of:
In the present embodiment, first air inlet 33A of described tank body 30 is connected with surge tank 11 by pipeline, described tank body 30 receives described methane gas 10 by described surge tank 11, the methane gas 10 flowed in it collected by described surge tank 11 by pipeline, when the methane gas that surge tank 11 is collected reaches a certain amount of, low-temp low-pressure methane gas in described surge tank 11 enters in described tank body 30, the utility model diffuses the recovery of methane owing to can be applied to LNG filling station, make use of the pressure feature that LNG filling station diffuses methane gas, described surge tank 11 the unstability that can overcome LNG filling station source of release is set, increase the time of this system each run.
Valve is provided with between described surge tank 11 and described tank body 30, this valve is pressure-regulating valve 17, be preferably pressure-reducing valve, thus temperature can be reduced further after methane gas is reduced pressure, the cold methane gas of high-quality is supplied to described gas-liquid separation device 31, be conducive to the separation of methane gas in described gas-liquid separation device 31, obtain more methane liquid.
The bottom liquid outlet 33B of described tank body 30 is connected with finished pot 16 and forms liquids recovery channel B, and methane liquid finished product is directly back in described finished pot 16, thus avoids diffusing of finished pot and cause reducing the problem of fluid temperature.
Be provided with force (forcing) pump 18 between described liquid outlet 33B and described finished pot 16, for methane liquid in described gas-liquid separation device 31 is evacuated in described finished pot 16, thus is conducive to described methane liquid and flows in described finished pot 16, be convenient to recycle.
In the present embodiment, described decompressor 15 is arranged on the inside of described tank body 30, the second channel of described heat-exchanger rig 32 directly connects described decompressor 15, high pressure low temperature methane gas in described tank body 30 directly forms the mixture of low-pressure low-temperature methane gas and methane liquid through the step-down process of decompressor 15, thus the speed of recovery methane is accelerated, effective raising energy utilization rate, is conducive to saving energy; And the floor space of whole equipment is less, reduces cost of investment, decrease the loss of energy.
Embodiment six:
As shown in Figure 6, embodiment six is the distortion made on the basis of embodiment five, in order to the system of perfect recovery methane gas, the system of embodiment five adds the equipment of recycling, the following detailed description of:
When the methane gas of collecting in described tank body 30 in the present embodiment arrives a certain amount of in possibility adverse current to described surge tank 11, stop valve 50 is provided with between described surge tank 11 and described pressure-regulating valve 17, described stop valve 50 is opened when the gas in described surge tank 11 arrives scheduled volume, the methane gas of described surge tank 11 is flow in described tank body 30 after the adjustment of described pressure-regulating valve 17 and carries out gas-liquid separation, effectively prevent the situation that in described surge tank 11, pressure is excessive.
Embodiment seven:
As shown in Figure 7, embodiment seven is distortion that the basis of any one embodiment in embodiment four, embodiment five, embodiment six is made, and in order to the system of perfect recovery methane gas, turn increases the equipment of recycling, the following detailed description of:
In the present embodiment, described compression set 14 has multiple, and multiple described compression set is parallel with one another, and particularly, the first gas outlet 33A of described tank body 30 is connected to the second air inlet 34A of described tank body 30 through the compression set 14 of multiple parallel connection.After the methane tolerance reclaimed in described tank body 30 increases gradually, in order to ensure methane gas constantly to be reclaimed fast when not increasing methane gas flask volume, multiple stage compression set 14 can be opened, multiple stage compression set 14 is worked simultaneously, constantly the methane gas after heat exchange is inputed in described compression set 14, thus increase substantially the organic efficiency of methane gas; When the methane tolerance reclaimed reduces gradually, reduce the working quantity of described compression set 14, make Partial shrinkage device be responsible for groundwork, other compression set can be done for subsequent use.
The present embodiment for the outside that described decompressor 15 is arranged on described tank body 30 describe in detail there is multiple compression set 14 time system operation principle, equally the inside of described tank body 30 is arranged on for described decompressor 15 applicable equally.
Embodiment eight:
As shown in Figure 8, embodiment eight is the distortion made on the basis of embodiment seven, in order to the system of perfect recovery methane gas, the system of embodiment seven adds the monitoring equipment for controlling gas the automatic recovery, the following detailed description of:
Surge tank 11 described in the present embodiment and be provided with pressure-regulating valve 17 between described tank body 30, be provided with the first pressure monitoring device 171 controlling described compression set 14 and open and close between described surge tank 11 and described pressure-regulating valve 17, described pressure-regulating valve 17 is provided with the second pressure monitoring device 172 controlling described pressure-regulating valve 17 flow.Particularly, utilize described first pressure monitoring device 171 to monitor the pressure of described surge tank 11, when the pressure of described surge tank 11 is pressure low-value, described compression set 14 is in closed condition; When the pressure of described surge tank 11 reaches pressure high-value, start described compression set 14, described compression set 14 brings into operation, and flows in described tank body 30 after the adjustment of the methane gas in described surge tank 11 by pressure-regulating valve 17.
In the present embodiment, the pressure requirements that the setting of described pressure low-value runs based on follow-up system is considered, if hypotony, the methane gas in described surge tank 11 will be difficult to flow in described tank body 30, easily feel suffocated; The pressure in methane gas 10 source is diffused in the setting of described pressure high-value based on leading portion, when described pressure high-value is higher than when diffusing the pressure of methane source gas, can collect in described surge tank 11 and abundant diffuse methane gas, to ensure that described surge tank 11 storage capacity is for being more than or equal to system hour recovery ability, make system as far as possible a running time longer, avoid frequent unlatching.If when the pressure of described surge tank 11 is lower than pressure low-value, whole system is closed, if when the pressure of described surge tank 11 is higher than pressure high-value, whole system is opened, particularly, when the pressure of described surge tank 11 is lower than 0.1Mpa-0.3Mpa, halt system runs, being preferably described pressure low-value is 0.2Mpa, and halt system runs; When the pressure of surge tank 11 is higher than open system during 0.5Mpa-0.7Mpa, being preferably described pressure high-value is 0.6Mpa open system.
Described tank body 30 is provided with the level monitoring device 121 controlling force (forcing) pump 18 and open and close, liquid level self-adjusting valve 122 is provided with between described force (forcing) pump 18 and described finished pot 16, described level monitoring device 121 controls the unlatching of described force (forcing) pump 18 and described liquid level self-adjusting valve 122 or closes, particularly, when described liquid level monitoring arrangement 121 detects that the liquid height inside described flash vessel 12 exceedes preset value, described liquid level self-adjusting valve 122 and described force (forcing) pump 18 will be opened, utilize described force (forcing) pump 18 to be entered by liquid pressing in described finished pot 16.
In the present embodiment, in order to improve the automatic recovery of methane gas, first gas outlet 34B and the described compression set 14 inlet duct place of described tank body 30 are provided with device for detecting temperature 20, and wherein, described device for detecting temperature 20 is provided with temperature alarming high-value and temperature parking high-value.When the temperature of the methane gas between described tank body 30 and described compression set 14 being detected higher than temperature alarming high-value, system automatic alarm, whether detection system is normally run; When the temperature of the methane gas between described tank body 30 and described compression set 14 being detected higher than parking high-value, close described stop valve 50 and described compression set 14, system automatic stopping.Described device for detecting temperature 20 is for carrying out interlocked control to the motor of described stop valve 50 and described compression set 14, be conducive to monitoring described tank body 30 and described compression set 14 whether normal operation, not only can effective monitoring running situation, and can essential safety be accomplished.Wherein, design temperature warning high-value object is the temperature by monitoring described compression set 14 entrance methane gas, as too high in temperature may show as described in tank body 30 break down or as described in compression set 14 to export methane gas temperature too high, affect overall operation.
In the present embodiment, as shown in Figure 9, when the methane gas of collecting in described tank body 30 arrives a certain amount of in possibility adverse current to described surge tank 11, stop valve 50 is provided with between described surge tank 11 and described pressure-regulating valve 17, the first pressure monitoring device 171 controlling described compression set 14 and open and close is provided with between described surge tank 11 and described stop valve 50, particularly, described stop valve 50 is provided with the first pressure monitoring device 171 controlling described compression set 14 and open and close, when the pressure of described surge tank 11 is pressure low-value, described stop valve 50 is in closed condition, when the pressure of described surge tank 11 is higher than scheduled volume, open described stop valve 50, low-temp low-pressure methane gas in described surge tank 11 enters in described tank body 30 after the decompression of described pressure-regulating valve 17, thus is conducive to the separation of methane gas in described flash vessel 12 and obtains more methane liquid.
In the present embodiment, if described compression set 14 has multiple, described surge tank 11 arranges Stress control interlock, determines according to the size of pressure in described surge tank 11 compression set starting varying number, thus increase substantially the organic efficiency reclaiming methane.
Embodiment nine:
As shown in Fig. 4, Fig. 5 and Fig. 6 and Fig. 7, the present embodiment provides a kind of methane gas recovery method, utilize embodiment four, embodiment five, embodiment six, embodiment seven any one described in methane gas recovery system reclaim methane gas and collect methane liquid, its step is as follows: step S1: be delivered in tank body 30 by described methane gas by the first air inlet 33A; Step S2: enter described compression set 14 after described methane gas is carried out heat exchange intensification in described tank body 30 and carry out compression process; Step S3: be again delivered to compressing the rear high pressure methane gas formed of process in tank body 30, and in described tank body 30, carry out heat exchange cooling formation high pressure low temperature methane gas; Step S4: described high pressure low temperature methane gas is carried out step-down, forms the mixture of gaseous methane and liquid methane; Step S5: described gaseous methane be separated in tank body 30 with the mixture of liquid methane, returns by gaseous methane to step S2 and carries out circular treatment; Liquid methane is reclaimed.
In methane gas recovery method described in the present embodiment, described low temperature methane gas can use at tank body Inner eycle, effectively improves energy utilization rate, avoids energy waste, reduce recovery power consumption; Described methane liquid finished product can directly be recycled, and recovery process is simple, and cost is low, and recovery product is that liquefied natural gas can market goods locally.
In the present embodiment, also step S0 is comprised: the methane gas that will reclaim carries out collection buffering before described step S1, when the methane gas collected reaches the first predetermined amount, open compression set 14, perform described step S1-S5, ensure system as far as possible a running time longer, avoid frequent unlatching, particularly, when described first predetermined amount is pressure high-value, open described compression set 14 by described first pressure monitoring device 171; If when the methane gas collected is lower than the second predetermined amount, stop performing described step S1-S5, effectively prevent in described tank body 30 problem of feeling suffocated, particularly, when described second predetermined amount is pressure lower position, close described compression set 14 by described first pressure monitoring device 171.
In the present embodiment, the methane gas that will reclaim carries out collection buffering, when the methane gas collected reaches the 3rd predetermined amount, when performing step S2, enter multiple compression set 14 after described methane gas heat exchange respectively and carry out compression process, wherein said multiple compression set is in parallel, determines the number starting described compression set 14, thus while saving efficiency, ensure that the quick recovery of methane gas according to the amount of the methane gas collected.Illustrate to arrange two compression sets below, when the pressure of described surge tank 11 is higher than pressure high-value, whole system is opened, and particularly, when the pressure of surge tank 11 is higher than open system during 0.5Mpa-0.7Mpa, a compression set starts; When the pressure of surge tank 11 is higher than 0.8Mpa-1.0MPa, another compression set for subsequent use starts; When the pressure of surge tank 11 is lower than 0.5Mpa-0.7Mpa, another compression set for subsequent use stops; When the pressure of surge tank 11 is lower than 0.1Mpa-0.3Mpa, main compressor is out of service.
In described step S3, the methane gas before compressing is carried out heat exchange to complete cooling, not only effectively can improve energy utilization rate in described high pressure-temperature methane gas and described step S2, and be conducive to reducing energy loss.In described step S4, described high pressure low temperature methane gas is carried out step-down process in described tank body 30, not only can effective economize energy, and accelerate the organic efficiency of methane gas.
In the present embodiment, in described step S1, if carry liquid methane in methane gas, initial gross separation can be carried out in described tank body 30, isolated liquid methane is delivered to finished pot 16, methane gas is performed step S2.
Described surge tank 11 storage capacity can make methane gas continuous the automatic recovery when being more than or equal to system hour disposal ability, thus is easy to the market goods locally realizing liquefied natural gas.
Embodiment ten:
As shown in Figure 8, the present embodiment provides a kind of methane gas recycling and control method, utilize embodiment four, embodiment five, embodiment six, embodiment seven, embodiment eight any one described in methane gas recovery system reclaim methane gas and collect methane liquid, comprising:
Step S1: the methane gas that will reclaim carries out collection buffering, the first pressure monitoring device 171 is utilized to control the keying of described compression set 14, when the methane gas collected arrives the first predetermined amount, open described compression set, enter step S2, when the methane gas collected is lower than the second predetermined amount, close described compression set 14; Step S2: the flow utilizing the second pressure monitoring device 172 controlled pressure control valve 17, makes methane gas enter in described tank body; Step S3: described methane gas is carried out in described tank body 30 complete the entering of heat exchange intensification and compress process formation high pressure methane gas; Step S4: described high pressure methane gas to be delivered to again in tank body 30 and to carry out heat exchange cooling and form high pressure low temperature methane gas; Step S5: described high pressure low temperature methane gas is carried out throttling, forms the mixture of gaseous methane and liquid methane; Step S6: described gaseous methane is separated with the mixture of liquid methane in described tank body 30, gaseous methane is returned step S3 and carry out circular treatment; Liquid methane is reclaimed.
Methane gas recycling and control method described in the present embodiment, the first pressure-detecting device 171 and the second pressure monitoring device 172 is provided with between described surge tank 11 and described tank body 30, described first pressure-detecting device 171 is for carrying out interlocked control to the motor switch of described compression set 14, described second pressure monitoring device 172, for carrying out interlocked control to the motor switch of described pressure-regulating valve 17, is conducive to prolongation system separate run times.This method judges whether to open described compression set 14 by the pressure of monitoring described surge tank 11, pressure high-value is reached once the pressure of being monitored out in described surge tank 11 by described first pressure-detecting device 171, start described compression set 14, when the methane gas collected is higher than described scheduled volume, open stop valve 50, the methane gas in described surge tank 11 enters in described gas circulation channel A and described liquids recovery channel B by described pressure-regulating valve 17 respectively; If when the pressure of described surge tank 11 is lower than the second predetermined amount and pressure low-value, described compression set 14 is in closed condition, continue in described surge tank 11 to collect methane gas until when pressure reaches pressure high-value.Moreover, control method described in the utility model, by the keying of pressure interlock control system, is conducive to prolongation system separate run times, avoids using manpower to control, solve the Automated condtrol problem of methane recovery, so both saved human cost to additionally reduce inoperative power cost.
In the present embodiment, in system operation, if when the methane gas collected in described surge tank 11 reaches the 3rd predetermined amount, in order to improve the rate of recovery of methane, when performing step S3, enter multiple compression set after described methane gas heat exchange respectively and carry out compression process, wherein said multiple compression set is in parallel, determines according to the amount of the methane gas collected the number starting described compression set 14.
In order to constantly improve the automatic recovery of methane gas, in the present embodiment, described tank body 30 is provided with liquid level detection device 121, is provided with liquid level self-adjusting valve 122 between described force (forcing) pump 18 and described finished pot 16.Described liquid level detection device 121 is provided with liquid level high-value and liquid level low-value, after in described flash vessel 12, described methane gas is separated into methane liquid, the liquid level of methane liquid is detected by liquid level detection device 121, when the liquid level of the methane liquid detected is higher than liquid level high-value, namely liquid level is higher than on liquid level gauge during interface 37A, start force (forcing) pump 18, methane liquid is transported in finished pot 16; When the liquid level of the methane liquid detected is lower than liquid level low-value, namely when liquid level is lower than liquid level gauge lower interface 37B, close force (forcing) pump 18, the present embodiment is by carrying out interlocked control to motor switch on described force (forcing) pump 18 and described liquid level self-adjusting valve 122, thus be conducive to the separate run times extending described force (forcing) pump 18, avoid full liquid in described tank body 30 to note problem or the too low problem causing gas to seal in described force (forcing) pump 18 of liquid level of not air inlet body.
In the present embodiment, methane gas continuous the automatic recovery can be made when described surge tank 11 storage capacity is more than or equal to system hour disposal ability, thus be easy to the market goods locally realizing liquefied natural gas.
In the utility model, in order to increase the uptake of methane gas in described surge tank 11, sorbing material can be provided with in described surge tank 11, described sorbing material is used for absorbing methane gas in a large number, as materials such as active carbons, not only make the buffering capacity of system increase, and the occupation area of equipment of described surge tank 11 reduced, described surge tank 11 source of the gas is LNG filling process, LNG finished pot diffuse process, LNG cistern car decompression process etc. produce methane gas.
To sum up, above technical scheme described in the utility model has the following advantages:
1. the flash vessel of band heat exchange described in the utility model, methane gas can use at described tank body Inner eycle, effectively improves energy utilization rate, avoids energy waste, reduce recovery power consumption; The setting of described liquid outlet enables methane liquid finished product directly collect recycling, thus improves energy utilization rate; Moreover equipment described in the utility model, investment and to run power consumption little, reclaiming product is that liquefied natural gas can market goods locally, and reduce methane recovery power consumption, the efficiency therefore not only reclaiming methane gas increases substantially, and reduces I&M cost.
2. be provided with dividing plate along inwall in gas-liquid separation device described in the utility model, because the temperature entering the methane gas in tank body from described first air inlet is higher than the temperature of the mixture from the gaseous methane formed through reduced pressure treatment and liquid methane, by the setting of described dividing plate, can prevent two kinds of gases from directly contacting, the time of effective prolongation two kinds of gas and vapor permeation, avoid liquid methane again to absorb heat and cause becoming the generation of methane gas, thus more methane liquid is separated from described gas-liquid separation device.In order to extend the time of two kinds of gas and vapor permeation, isolate more methane liquid to the full extent, the quantity of described dividing plate is multiple, and multiple dividing plate is crisscross arranged successively in the opposed inner walls of described tank body.
3. the second channel of heat-exchanger rig described in the utility model is communicated with described gas-liquid separation device by the decompressor being positioned at described tank body, methane gas after reduced pressure treatment directly flows in described gas-liquid separation device, the speed of recovery methane is not only made to accelerate, effective raising energy utilization rate, and the floor space of whole equipment is less, reduce cost of investment, if avoid the energy loss caused when the methane gas after heat exchange flows to the decompression of described tank body outside.
Obviously, above-described embodiment is only for clearly example being described, the restriction not to embodiment.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here exhaustive without the need to also giving all embodiments.And thus the apparent change of extending out or variation be still in the protection domain that the utility model creates.

Claims (10)

1. the flash vessel with heat exchange, it is characterized in that: described flash vessel comprises tank body, be provided with the gas-liquid separation device being positioned at tank body lower part in described tank body and be positioned at the heat-exchanger rig on tank body top, described heat-exchanger rig comprises at least two passages, wherein first passage is communicated with the first air inlet for receiver gases on described tank body, second channel is connected with the second air inlet on described tank body, wherein said second air inlet is connected with compression set by first gas outlet on described tank body top, and the bottom of described tank body is provided with liquid outlet.
2. the flash vessel of band heat exchange according to claim 1, it is characterized in that: described heat-exchanger rig comprises cooling tube or tubulation, and forming first passage between the inwall of described cooling tube or tubulation and described tank body, the inside of described cooling tube or tubulation forms second channel.
3. the flash vessel of band heat exchange according to claim 2, is characterized in that: described tank body top is provided with bracing frame along inwall, and described heat-exchanger rig is fixed on support frame as described above.
4. the flash vessel of band heat exchange according to claim 1, is characterized in that: be provided with dividing plate along inwall in described gas-liquid separation device.
5. the flash vessel of band heat exchange according to claim 4, is characterized in that: the quantity of described dividing plate is multiple, and multiple dividing plate is crisscross arranged successively in the opposed inner walls of described tank body.
6. the flash vessel of band heat exchange according to claim 1, it is characterized in that: the second channel of described heat-exchanger rig exports with the high-pressure material on described tank body and communicates, described gas-liquid separation device communicates with the low pressure material inlet on described tank body, and the outlet of described high-pressure material is connected to described low pressure material inlet by the decompressor being arranged on described tank body outside.
7. the flash vessel of band heat exchange according to claim 1, is characterized in that: the second channel of described heat-exchanger rig is communicated with described gas-liquid separation device by the decompressor being positioned at described tank body.
8. the flash vessel of band heat exchange according to claim 7, is characterized in that: the lower end of described tank body is respectively equipped with interface on liquid level gauge and is positioned at the liquid level gauge lower interface of interface lower end on described liquid level gauge.
9. the flash vessel of band heat exchange according to claim 1, is characterized in that: the top of described tank body is provided with the diffusion mouth for being vented.
10. a methane gas recovery system, it is characterized in that: comprise the flash vessel with heat exchange described in any one in claim 1-9, described first gas outlet is connected to described second air inlet through described compression set, and described heat-exchanger rig is communicated with described gas-liquid separation device by decompressor.
CN201520244116.XU 2015-04-21 2015-04-21 Take flash vessel and methane gas recovery system of heat transfer Active CN205002518U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201520244116.XU CN205002518U (en) 2015-04-21 2015-04-21 Take flash vessel and methane gas recovery system of heat transfer

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201520244116.XU CN205002518U (en) 2015-04-21 2015-04-21 Take flash vessel and methane gas recovery system of heat transfer

Publications (1)

Publication Number Publication Date
CN205002518U true CN205002518U (en) 2016-01-27

Family

ID=55159403

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201520244116.XU Active CN205002518U (en) 2015-04-21 2015-04-21 Take flash vessel and methane gas recovery system of heat transfer

Country Status (1)

Country Link
CN (1) CN205002518U (en)

Similar Documents

Publication Publication Date Title
CN104713310B (en) Methane gas recovery system and recycling and control method
CN105318190B (en) BOG liquefaction recovery system and method
CN201964142U (en) LNG (liquefied natural gas) pump-free aeration equipment with function of BOG (boil off gas) recovery
CN202675796U (en) Device utilizing liquefied Natural Gas (LNG) cold energy to produce liquid air separation products
CN102913752B (en) Unloading and liquid adding device for skid-type liquid adding station and unloading and liquid adding method
CN104033727A (en) Technique and device for treating BOG by using recycled cold energy at LNG receiving station
CN204647843U (en) LNGV (liquefied natural gas vehicle) liquid-adding device
CN104819379A (en) Methane gas recovery system and recovery control method
CN102425725B (en) System and method for reclaiming boil off gas (BOG) in liquefied natural gas (LNG) storage tank
CN109027660A (en) Supercritical hydrogen storage method and application thereof
CN105674056A (en) Methane recovering system and recovering method
CN104482396B (en) BOG recovery system with cold storage function
CN205002518U (en) Take flash vessel and methane gas recovery system of heat transfer
CN104696700B (en) methane gas recovery system and recovery method
CN105042327B (en) methane gas recovery system and recovery method
CN104833173A (en) Methane gas recovery system and recovery method
CN204718304U (en) Flash vessel with heat exchange and methane gas recovery system
CN104832783A (en) Methane gas recovery system and recovery method
CN204611334U (en) Methane gas reclaiming system
CN114893719A (en) BOG gas recovery system and method for hydrogenation and liquefied natural gas combined station
CN104819378B (en) Liquefied natural gas (LNG) automobile liquid adding device
CN105486030B (en) Methane gas recovery system and recycling and control method
CN205209071U (en) Flash vessel
CN204403773U (en) A kind of LNG refueling gas recovery system
CN218720604U (en) Liquid hydrogen supply hydrogen station

Legal Events

Date Code Title Description
C14 Grant of patent or utility model
GR01 Patent grant
TR01 Transfer of patent right

Effective date of registration: 20170208

Address after: 065001 Hebei economic and Technological Development Zone, Langfang science and Technology Park in the Southern District of B building, room 522

Patentee after: ENN SCIENCE & TECHNOLOGY DEVELOPMENT Co.,Ltd.

Address before: The 065001 Hebei economic and Technological Development Zone of Langfang Huaxiang Xinyuan host new Austrian Science and Technology Park in Southern District

Patentee before: ENN Coal Gasification Co., Ltd.

TR01 Transfer of patent right

Effective date of registration: 20170605

Address after: Building software No. 662 410006 Hunan province Yuelu District City Lugu Avenue (Changsha professional building No. 539)

Patentee after: New Austrian Gas Engineering Company Limited

Address before: 065001 Hebei economic and Technological Development Zone, Langfang science and Technology Park in the Southern District of B building, room 522

Patentee before: ENN SCIENCE & TECHNOLOGY DEVELOPMENT Co.,Ltd.

TR01 Transfer of patent right
CP01 Change in the name or title of a patent holder

Address after: Building software No. 662 410006 Hunan province Yuelu District City Lugu Avenue (Changsha professional building No. 539)

Patentee after: The new Austrian Energy Engineering Technology Co., Ltd.

Address before: Building software No. 662 410006 Hunan province Yuelu District City Lugu Avenue (Changsha professional building No. 539)

Patentee before: New Austrian Gas Engineering Company Limited

CP01 Change in the name or title of a patent holder