CN104293404B - Device and method for efficiently denitrifying natural gas - Google Patents

Device and method for efficiently denitrifying natural gas Download PDF

Info

Publication number
CN104293404B
CN104293404B CN201410462945.5A CN201410462945A CN104293404B CN 104293404 B CN104293404 B CN 104293404B CN 201410462945 A CN201410462945 A CN 201410462945A CN 104293404 B CN104293404 B CN 104293404B
Authority
CN
China
Prior art keywords
gas
pipeline
phase cryogen
export
port
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
CN201410462945.5A
Other languages
Chinese (zh)
Other versions
CN104293404A (en
Inventor
曹卫华
文向南
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.)
Sichuan Shudao Equipment Technology Co ltd
Original Assignee
Chengdu Shenleng Liquefaction Plant 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 Chengdu Shenleng Liquefaction Plant Co ltd filed Critical Chengdu Shenleng Liquefaction Plant Co ltd
Priority to CN201410462945.5A priority Critical patent/CN104293404B/en
Publication of CN104293404A publication Critical patent/CN104293404A/en
Application granted granted Critical
Publication of CN104293404B publication Critical patent/CN104293404B/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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
    • 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
    • F25J1/0002—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
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0219—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 in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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
    • F25J2210/02—Multiple feed streams, e.g. originating from different sources
    • 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
    • F25J2210/90—Boil-off gas from storage
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • 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
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • 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
    • F25J2270/18—External refrigeration with incorporated cascade loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons

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)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

The invention discloses a natural gas high-efficiency denitrification device, which comprises a heat exchanger (1), an LNG storage tank (2) and a washing tower (3), wherein a nitrogen-rich gas pipeline (4), a gas-liquid mixed phase refrigerant pipeline (7), a gas phase refrigerant pipeline I (8), a gas phase refrigerant pipeline II (9), a liquid phase refrigerant pipeline I (10) and a liquid phase refrigerant pipeline II (11) which are parallel to each other are arranged in the heat exchanger (1), a BOG heater (12), a BOG compressor (13), a BOG buffer tank (14) and a tail gas compressor (15) are sequentially connected from the outlet end of the LNG storage tank (2) to the inlet end of a pipeline I (5), and a fuel gas buffer tank (16) is connected between the outlet end of the BOG buffer tank (14) and the inlet end of the nitrogen-rich gas pipeline (4; it also discloses a denitrification method. The invention has the beneficial effects that: the method has the advantages of low production cost, low energy consumption, simple operation, good environmental protection benefit and economic benefit, and LNG with the nitrogen content less than 1.5 percent.

Description

A kind of devices and methods therefor of High-efficiency Gas denitrogenation
Technical field
The present invention relates to the technical field of natural gas in low temperature denitrogenation, the devices and methods therefor of a kind of High-efficiency Gas denitrogenation.
Background technology
The unstripped gas being currently used for natural gas liquefaction device mainly has conventional gas (oil-gas reservoir) and Unconventional forage (coal bed gas, shale gas etc.), at least containing one or more the most liquescent light components, such as nitrogen, oxygen, argon, hydrogen and helium etc. in various natural gases.In gas deliquescence process, if these components not being removed, liquefy energy consumption increase, the reduction of LNG calorific value will be caused, and give the storage of LNG, transport and bring potential safety hazard.
Therefore, in natural gas, the removing of light component the most increasingly comes into one's own, and the above light component of cryogenic rectification method removing simultaneously has the advantages such as thorough, the dependable performance of removing.
United States Patent (USP) US6758060B2 describes and a kind of produces the method for separation of nitrogen during LNG.The method uses high-pressure rectification tower and low-pressure distillation tower, and each rectifying column is respectively provided with side boiling device, and lower pressure column tower top arranges decompressor and provides condensation for condenser simultaneously.Obtaining LNG at the bottom of the tower of high and low pressure tower, the tower top at lower pressure column obtains the methane content rich nitrogen less than 1%.
Being similar to therewith, Chinese invention patent CN201010561795 describes a kind of nitrogenous methane gas denitrogenation to the method for natural gas/liquefied natural gas.The method includes the precooling of unstripped gas, high-pressure tower (lower tower) rectifying, lower pressure column (upper tower) step such as stripping, product gas re-heat/mixed-refrigerant cycle.Obtain rich nitrogen at the top of lower pressure column (upper tower), the bottom of condenser/evaporator obtains LNG.
Chinese utility model patent CN201320809869 describes a kind of natural gas liquefaction co-producing high-purity nitrogen equipment, and the method includes compressor, heat exchanger, denitrogenation rectifying column, cold-producing medium knockout drum, LNG tank and denitrogenation rectifying column reboiler, condenser and phegma knockout drum etc..Obtain LNG in the bottom of reboiler, obtain High Purity Nitrogen at the top of condenser.
Process as described above is required to arrange evaporimeter at the bottom of overhead condenser and tower, substantially increases energy consumption and the complexity of natural gas liquefaction device, and reduces benefit and the competitiveness of liquefaction plant.
Summary of the invention
It is an object of the invention to overcome the shortcoming of prior art, it is provided that a kind of production cost is low, energy consumption is low, simple to operate, be obtained in that the devices and methods therefor of the High-efficiency Gas denitrogenation of good environmental benefit and economic benefit, the nitrogen content LNG less than 1.5%.
nullThe purpose of the present invention is achieved through the following technical solutions: the device of a kind of High-efficiency Gas denitrogenation，It includes heat exchanger、LNG storage tank and scrubbing tower，The rich nitrogen pipeline being parallel to each other it is provided with in described heat exchanger、Pipeline I、Pipeline II、Gas-liquid mixed phase cryogen pipeline、Gas phase cryogen pipeline I、Gas phase cryogen pipeline II、Liquid phase cryogen pipeline I and liquid phase cryogen pipeline II，The described port of export of rich nitrogen pipeline connects with the top of scrubbing tower，The bottom of scrubbing tower connects with LNG storage tank，And be connected between the bottom of scrubbing tower and the arrival end of LNG storage tank have regulation valve m，The port of export of LNG storage tank has been linked in sequence BOG heater to the arrival end of pipeline I、BOG compressor、BOG surge tank and tail-gas compressor，It is connected between the port of export of BOG surge tank and the arrival end of rich nitrogen pipeline and has fuel gas surge tank，
The port of export of described pipeline I is connected with the upper end entrance A of scrubbing tower, at the lower inlet B of scrubbing tower and the C being arranged on gas-liquid mixed phase cryogen pipeline, the port of export of outlet and gas-liquid mixed phase cryogen pipeline is connected, and be connected between outlet and gas-liquid mixed phase cryogen pipeline at C regulate valve a and regulation valve b
The arrival end of described gas-liquid mixed phase cryogen pipeline has been linked in sequence MR entrance separator, MR compressor, MR aftercooler and MR final stage separator to the arrival end of gas phase cryogen pipeline I, the port of export F of MR final stage separator is connected with the arrival end of liquid phase cryogen pipeline I
nullIt also includes MR Upper separator and MR Lower separator，The port of export of gas phase cryogen pipeline I is connected with the arrival end K of MR Upper separator，The port of export H of MR Upper separator is connected with the arrival end of gas phase cryogen pipeline II，The port of export of gas phase cryogen pipeline II is connected with the arrival end K of MR Lower separator，The port of export H and port of export J of MR Lower separator all ports of export with gas-liquid mixed phase cryogen pipeline are connected，The port of export J of described MR Upper separator is connected with the arrival end of liquid phase cryogen pipeline II，The port of export of liquid phase cryogen pipeline II is connected with one end of regulation valve c，The other end of regulation valve c and gas-liquid mixed phase cryogen pipeline communication，The port of export of described liquid phase cryogen pipeline I is connected with one end of regulation valve d，The other end of regulation valve d and gas-liquid mixed phase cryogen pipeline communication.
It is connected between the port of export and the arrival end of BOG heater of described LNG storage tank and has regulation valve e.
It is connected between the port of export and the arrival end of fuel gas surge tank of described BOG surge tank and has regulation valve f.
It is connected between upper end entrance A and the port of export of pipeline I of described scrubbing tower and has regulation valve h.
It is connected between the top of described scrubbing tower and the port of export of rich nitrogen pipeline and has regulation valve k.
A kind of method of High-efficiency Gas denitrogenation, it comprises the following steps:
S1, gas phase cryogen and the preparation of liquid phase cryogen, it is passed through Hydrocarbon Organic to the arrival end F of MR entrance separator, Hydrocarbon Organic is separated into gaseous state and liquid hydrocarbon and enters after MR compressor compresses in MR aftercooler by MR entrance separator, gaseous hydrocarbon and liquid hydrocarbon prepare gas phase cryogen and liquid phase cryogen after MR aftercooler condenses, it is achieved thereby that gas phase cryogen and the preparation of liquid phase cryogen；
S2, liquid phase cryogen enter MR final stage separator and separate, and liquid phase cryogen after separation enters liquid phase cryogen pipeline I, and prepare temperature after being adjusted valve d throttling and be the liquid phase cryogen of-50 DEG C ~-60 DEG C and enter gas-liquid mixed phase cryogen pipeline；
S3, gas phase cryogen enter MR final stage separator and separate, and the gas phase cryogen after separation enters gas phase cryogen pipeline I, and enters MR Upper separator, and gas phase cryogen is separated into gas phase cryogen A and liquid phase cryogen B by MR Upper separator；
Liquid phase cryogen B after S4, separation enters liquid phase cryogen pipeline II through the port of export J of MR Upper separator, liquid phase cryogen pipeline II flows out from heat exchanger after being adjusted valve c throttling and prepares the liquid phase cryogen B that temperature is-100 DEG C ~-120 DEG C, and enters gas-liquid mixed phase cryogen pipeline；
Gas phase cryogen A after S5, separation enters gas phase cryogen pipeline II, gas phase cryogen A through the port of export H of MR Upper separator and exits into MR Lower separator from heat exchanger, and gas phase cryogen A is separated into gas phase cryogen C and liquid phase cryogen D by MR Lower separator；
S6, separate after gas phase cryogen C and liquid phase cryogen D port of export H and port of export J through MR Lower separator respectively enter in gas-liquid mixed phase cryogen pipeline, in gas-liquid mixed phase cryogen pipeline, gas-liquid mixed phase cryogen is extracted out from heat exchanger, gas-liquid mixed phase cryogen is successively in MR entrance separator, MR compressor, MR aftercooler and MR final stage separator enter heat exchanger, it is achieved thereby that provide cold to heat exchanger；
The preparation of S7, LNG, it is passed through natural gas in pipeline II, natural gas backflowed in heat exchanger cold flow precooling, liquefy and be subcooled, temperature is that the natural gas of-100 ~-120 DEG C natural gas with-150 ~-160 DEG C flows out from the outlet C of pipeline II and outlet B respectively, and enter in scrubbing tower after being adjusted valve a and regulation valve b throttling respectively, in scrubbing tower, the nitrogen content LNG less than 1.5% is being prepared at the bottom of tower after natural gas and nitrogen heat exchange, obversion, the LNG prepared enters in LNG storage tank after being adjusted valve m throttling, it is achieved thereby that the LNG that nitrogen content is less than 1.5%；
S8, the process of rich nitrogen, the rich nitrogen produced in scrubbing tower is adjusted valve k and returns in rich nitrogen pipeline, and rich nitrogen is entered in fuel gas surge tank as fuel gas to normal temperature by natural gas and gas-liquid mixed phase cryogen re-heat；
The process of S9, BOG tail gas, after BOG heater, BOG compressor and BOG surge tank, divide into two strands of BOG tail gas successively at the BOG tail gas produced in LNG storage tank, it is interior as fuel gas that a portion BOG tail gas enters fuel gas surge tank, another part BOG tail gas enters in pipeline I after tail-gas compressor compresses, BOG tail gas backflowed cold flow precooling, liquefy and be subcooled after enter scrubbing tower, it is achieved thereby that the process of BOG tail gas.
The invention have the advantages that the nitrogen that (1) is contained by natural gas itself washs in scrubbing tower, the nitrogen content LNG less than 1.5% is being obtained at the bottom of tower, substitute evaporimeter and condenser owing to arranging rich solution nitrogen washing tower and be separately provided BOG heat exchanger channels to reduce compressor row pressure, liquefaction plant total energy consumption reduces by 5% ~ 10% compared with conventional rectification denitrification system, reduces cost of investment.(2) present invention can using in the BOG tail gas produced and rich nitrogen recycling to fuel gas surge tank as fuel treatment, make waste gas be recycled, not only economy and also protect environment.(3) present invention has that energy consumption is low, simple to operate, applied range, has the feature of good environmental benefit and economic benefit.
Accompanying drawing explanation
Fig. 1 is the structural representation of embodiments of the invention one；
Fig. 2 is the structural representation of embodiments of the invention two；
Fig. 3 is the structural representation of embodiments of the invention three；
Fig. 4 is the structural representation of embodiments of the invention four；
nullIn figure，1-heat exchanger，2-LNG storage tank，3-scrubbing tower，4-richness nitrogen pipeline，5-pipeline I，6-pipeline II，7-gas-liquid mixed phase cryogen pipeline，8-gas phase cryogen pipeline I，9-gas phase cryogen pipeline II，10-liquid phase cryogen pipeline I，11-liquid phase cryogen pipeline II，12-BOG heater，13-BOG compressor，14-BOG surge tank，15-tail-gas compressor，16-fuel gas surge tank，17-MR entrance separator，18-MR compressor，19-MR aftercooler，20-MR final stage separator，21-MR Upper separator，22-MR Lower separator，23-regulates valve m，24-regulates valve a，25-regulates valve b，26-regulates valve c，27-regulates valve d，28-regulates valve e，29-regulates valve f，30-regulates valve h，31-regulates valve k，32-LNG technique pump.
Detailed description of the invention
The present invention will be further described below in conjunction with the accompanying drawings, and protection scope of the present invention is not limited to the following stated:
Embodiment one: as shown in Figure 1, a kind of device of High-efficiency Gas denitrogenation, it includes heat exchanger 1, LNG storage tank 2 and scrubbing tower 3, the rich nitrogen pipeline 4 being parallel to each other it is provided with in described heat exchanger 1, pipeline I5, pipeline II6, gas-liquid mixed phase cryogen pipeline 7, gas phase cryogen pipeline I8, gas phase cryogen pipeline II9, liquid phase cryogen pipeline I10 and liquid phase cryogen pipeline II11, the port of export of described rich nitrogen pipeline 4 connects with the top of scrubbing tower 3, the bottom of scrubbing tower 3 connects with LNG storage tank, and be connected between the bottom of scrubbing tower 3 and the arrival end of LNG storage tank 2 have regulation valve m23.As shown in Figure 1; the port of export of LNG storage tank 2 has been linked in sequence BOG heater 12, BOG compressor 13, BOG surge tank 14 and tail-gas compressor 15 to the arrival end of pipeline I5; it is connected between the port of export of BOG surge tank 14 and the arrival end of rich nitrogen pipeline 4 and has fuel gas surge tank 16; fuel gas surge tank 16 is used for collecting rich nitrogen and part BOG tail gas; use for fuel gas; therefore, save production cost, improve the economic benefit of enterprise, protect ecological environment.
As shown in Figure 1, the port of export of pipeline I5 is connected with the upper end entrance A of scrubbing tower 3, at the lower inlet B of the scrubbing tower 3 and C being arranged on gas-liquid mixed phase cryogen pipeline 7, the port of export of outlet and gas-liquid mixed phase cryogen pipeline 7 is connected, and is connected between outlet and gas-liquid mixed phase cryogen pipeline 7 at C regulate valve a24 and regulation valve b25.
As shown in Figure 1, the arrival end of gas-liquid mixed phase cryogen pipeline 7 has been linked in sequence MR entrance separator 17, MR compressor 18, MR aftercooler 19 and MR final stage separator 20 to the arrival end of gas phase cryogen pipeline I8, and the port of export F of MR final stage separator 20 is connected with the arrival end of liquid phase cryogen pipeline I10.
nullAs shown in Figure 1，It also includes MR Upper separator 21 and MR Lower separator 22，The port of export of gas phase cryogen pipeline I8 is connected with the arrival end K of MR Upper separator 21，The port of export H of MR Upper separator 21 is connected with the arrival end of gas phase cryogen pipeline II9，The port of export of gas phase cryogen pipeline II9 is connected with the arrival end K of MR Lower separator 22，The port of export H and port of export J of MR Lower separator 22 all ports of export with gas-liquid mixed phase cryogen pipeline 7 are connected，The port of export J of described MR Upper separator 21 is connected with the arrival end of liquid phase cryogen pipeline II11，The port of export of liquid phase cryogen pipeline II11 is connected with one end of regulation valve c26，The other end of regulation valve c26 connects with gas-liquid mixed phase cryogen pipeline 7，The port of export of described liquid phase cryogen pipeline I10 is connected with one end of regulation valve d27，The other end of regulation valve d27 connects with gas-liquid mixed phase cryogen pipeline 7，Gas phase cryogen is successively by MR Upper separator 21 and MR twice separation of Lower separator 22，Liquid phase cryogen and the temperature of gas phase cryogen after separation are the lowest，These gas phase cryogens and liquid phase cryogen are recycled again after entering gas-liquid mixed phase cryogen pipeline 7，Thus provide cold for heat exchanger 1，Denitrogenation for natural gas provides environment.
Regulation valve e28 is had as it is shown in figure 1, be connected between the port of export of LNG storage tank 2 and the arrival end of BOG heater 12；It is connected between the port of export of BOG surge tank 14 and the arrival end of fuel gas surge tank 16 and has regulation valve f29；It is connected between upper end entrance A and the port of export of pipeline I5 of scrubbing tower 3 and has regulation valve h30；It is connected between the top of scrubbing tower 3 and the port of export of rich nitrogen pipeline 4 and has regulation valve k31.
A kind of method of High-efficiency Gas denitrogenation, it comprises the following steps:
S1, gas phase cryogen and the preparation of liquid phase cryogen, it is passed through Hydrocarbon Organic to the arrival end F of MR entrance separator 17, Hydrocarbon Organic is separated into gaseous state and liquid hydrocarbon and enters after MR compressor 18 compresses in MR aftercooler 19 by MR entrance separator 17, gaseous hydrocarbon and liquid hydrocarbon prepare gas phase cryogen and liquid phase cryogen after MR aftercooler 19 condenses, it is achieved thereby that gas phase cryogen and the preparation of liquid phase cryogen；
S2, liquid phase cryogen enter MR final stage separator 20 and separate, and liquid phase cryogen after separation enters liquid phase cryogen pipeline I10, and prepare temperature after being adjusted valve d27 throttling and be the liquid phase cryogen of-50 DEG C ~-60 DEG C and enter gas-liquid mixed phase cryogen pipeline 7；
S3, gas phase cryogen enter MR final stage separator 20 and separate, and the gas phase cryogen after separation enters gas phase cryogen pipeline I8, and enters MR Upper separator 21, and gas phase cryogen is separated into gas phase cryogen A and liquid phase cryogen B by MR Upper separator 21；
Liquid phase cryogen B after S4, separation enters liquid phase cryogen pipeline II11 through the port of export J of MR Upper separator 21, liquid phase cryogen pipeline II11 flows out from heat exchanger 1 after being adjusted valve c26 throttling and prepares the liquid phase cryogen B that temperature is-100 DEG C ~-120 DEG C, and enters gas-liquid mixed phase cryogen pipeline 7；
Gas phase cryogen A after S5, separation enters gas phase cryogen pipeline II9 through the port of export H of MR Upper separator 21, gas phase cryogen A exits into MR Lower separator 22 from heat exchanger 1, and gas phase cryogen A is separated into gas phase cryogen C and liquid phase cryogen D by MR Lower separator 22；
S6, separate after gas phase cryogen C and liquid phase cryogen D port of export H and port of export J through MR Lower separator 22 respectively enter in gas-liquid mixed phase cryogen pipeline 7, in gas-liquid mixed phase cryogen pipeline 7, gas-liquid mixed phase cryogen is extracted out from heat exchanger 1, gas-liquid mixed phase cryogen enters in heat exchanger 1 through MR entrance separator 17, MR compressor 18, MR aftercooler 19 and MR final stage separator 20 successively, it is achieved thereby that provide cold to heat exchanger 1；
S7, the preparation of LNG, it is passed through natural gas in pipeline II6, natural gas is backflowed cold flow precooling in heat exchanger 1, liquefy and be subcooled, temperature is that the natural gas of-100 ~-120 DEG C natural gas with-150 ~-160 DEG C flows out from the outlet C of pipeline II6 and outlet B respectively, and enter in scrubbing tower 3 after being adjusted valve a24 and regulation valve b25 throttling respectively, in scrubbing tower 3, natural gas and nitrogen heat exchange, the nitrogen content LNG less than 1.5% is being prepared at the bottom of tower after obversion, the LNG prepared enters in LNG storage tank 2 after being adjusted valve m23 throttling, it is achieved thereby that the LNG that nitrogen content is less than 1.5%；
S8, the process of rich nitrogen; the rich nitrogen produced in scrubbing tower 3 is adjusted valve k31 and returns in rich nitrogen pipeline 4; rich nitrogen is entered in fuel gas surge tank 16 as fuel gas to normal temperature by natural gas and gas-liquid mixed phase cryogen re-heat; rich nitrogen is collected in fuel gas surge tank 16; not only save production cost; and need not be discharged in air, protect ecological environment；
S9, the process of BOG tail gas, the BOG tail gas produced in LNG storage tank 2 is successively through BOG heater 12, divide into two strands of BOG tail gas after BOG compressor 13 and BOG surge tank 14, it is interior as fuel gas that a portion BOG tail gas enters fuel gas surge tank 16, another part BOG tail gas enters in pipeline I5 after tail-gas compressor 15 compresses, BOG tail gas is backflowed cold flow precooling, scrubbing tower 3 is entered after liquefying and being subcooled, it is achieved thereby that the process of BOG tail gas, so BOG exhaust collection is risen and be used as fuel use, not only save production cost, and need not be discharged in air, protect ecological environment.
Embodiment 2: as shown in Figure 2, the present embodiment is with the difference of embodiment 1: when the storage pressure of LNG storage tank 2 is more than 0.08MPa (G), BOG compressor 13 can be cancelled, simultaneously in order to ensure that finished product LNG can enter LNG storage tank 2, need the pressure by governor valve control scrubbing tower at more than 0.18MPa (G), the nitrogen content LNG less than 1.5% can be prepared equally.
Embodiment 3: as shown in Figure 3, the present embodiment is with the difference of embodiment 1: when the storage pressure of LNG storage tank 2 is more than 0.08MPa (G), BOG compressor 13 can be cancelled, difference with embodiment 2 is: in order to ensure that finished product LNG can enter LNG storage tank 2, simultaneously control scrubbing tower 3 pressure at 0.1MPa (G) to guarantee higher detersive efficiency, increase LNG technique pump 32, the nitrogen content LNG less than 1.5% can be prepared equally.
Embodiment 4: as shown in Figure 4, the present embodiment is with the difference of embodiment 1: when using low temperature BOG compressor 13, cancel BOG heater 12, improve the row pressure of BOG compressor 13 to after 0.2 ~ 2.0MPa (G) simultaneously, cancel tail-gas compressor 15, the nitrogen content LNG less than 1.5% can be prepared equally.

Claims (2)

  1. null1. the device of a High-efficiency Gas denitrogenation，It is characterized in that: it includes heat exchanger (1)、LNG storage tank (2) and scrubbing tower (3)，The rich nitrogen pipeline (4) being parallel to each other it is provided with in described heat exchanger (1)、Pipeline I(5)、Pipeline II(6)、Gas-liquid mixed phase cryogen pipeline (7)、Gas phase cryogen pipeline I(8)、Gas phase cryogen pipeline II(9)、Liquid phase cryogen pipeline I(10) and liquid phase cryogen pipeline II(11)，The port of export of described rich nitrogen pipeline (4) connects with the top of scrubbing tower (3)，The bottom of scrubbing tower (3) connects with LNG storage tank，And be connected between the bottom of scrubbing tower (3) and the arrival end of LNG storage tank (2) have regulation valve m(23)，The port of export of LNG storage tank (2) is to pipeline I(5) arrival end be linked in sequence BOG heater (12)、BOG compressor (13)、BOG surge tank (14) and tail-gas compressor (15)，It is connected between the port of export of BOG surge tank (14) and the port of export of rich nitrogen pipeline (4) and has fuel gas surge tank (16)，
    Described pipeline I(5) the port of export be connected with the upper end entrance A of scrubbing tower (3), the lower inlet B of scrubbing tower (3) be arranged on pipeline II(6) on C at outlet and pipeline II(6) port of export B be connected, pipeline II(6) on C at outlet and the lower inlet B of port of export B and scrubbing tower (3) between be connected to regulation valve a(24) and regulate valve b(25)
    The port of export of described gas-liquid mixed phase cryogen pipeline (7) is to gas phase cryogen pipeline I(8) arrival end be linked in sequence MR entrance separator (17), MR compressor (18), MR aftercooler (19) and MR final stage separator (20), the port of export F of MR final stage separator (20) and liquid phase cryogen pipeline I(10) arrival end be connected
    nullIt also includes MR Upper separator (21) and MR Lower separator (22)，Gas phase cryogen pipeline I(8) the port of export be connected with the arrival end K of MR Upper separator (21)，The port of export Ha of MR Upper separator (21) and gas phase cryogen pipeline II(9) arrival end be connected，Gas phase cryogen pipeline II(9) the port of export be connected with the arrival end K of MR Lower separator (22)，The port of export Hb and port of export Jb of MR Lower separator (22) all arrival ends with gas-liquid mixed phase cryogen pipeline (7) are connected，The port of export Ja of described MR Upper separator (21) and liquid phase cryogen pipeline II(11) arrival end be connected，Liquid phase cryogen pipeline II(11) the port of export and regulation valve c(26) one end be connected，Regulation valve c(26) the other end connect with gas-liquid mixed phase cryogen pipeline (7)，Described liquid phase cryogen pipeline I(10) the port of export and regulation valve d(27) one end be connected，Regulation valve d(27) the other end connect with gas-liquid mixed phase cryogen pipeline (7)；
    It is connected between the port of export and the arrival end of BOG heater (12) of described LNG storage tank (2) and has regulation valve e(28)；
    It is connected between the port of export and the arrival end of fuel gas surge tank (16) of described BOG surge tank (14) and has regulation valve f(29)；
    Upper end entrance A and the pipeline I(5 of described scrubbing tower (3)) the port of export between be connected have regulation valve h(30)；
    It is connected between the top of described scrubbing tower (3) and the arrival end of rich nitrogen pipeline (4) and has regulation valve k(31).
  2. The method of device High-efficiency Gas denitrogenation the most according to claim 1, it is characterised in that: it comprises the following steps:
    S1, gas phase cryogen and the preparation of liquid phase cryogen, it is passed through Hydrocarbon Organic to the arrival end F of MR entrance separator (17), Hydrocarbon Organic is separated into gaseous state and liquid hydrocarbon and enters after MR compressor (18) compresses in MR aftercooler (19) by MR entrance separator (17), gaseous hydrocarbon and liquid hydrocarbon prepare gas phase cryogen and liquid phase cryogen after MR aftercooler (19) condenses, it is achieved thereby that gas phase cryogen and the preparation of liquid phase cryogen；
    S2, liquid phase cryogen enter MR final stage separator (20) and separate, liquid phase cryogen after separation enters liquid phase cryogen pipeline I(10), and it is adjusted valve d(27) prepare temperature after throttling and be the liquid phase cryogen of-50 DEG C ~-60 DEG C and enter gas-liquid mixed phase cryogen pipeline (7)；
    S3, gas phase cryogen enter MR final stage separator (20) and separate, gas phase cryogen after separation enters gas phase cryogen pipeline I(8), and entering MR Upper separator (21), gas phase cryogen is separated into gas phase cryogen A and liquid phase cryogen B by MR Upper separator (21)；
    Liquid phase cryogen B after S4, separation enters liquid phase cryogen pipeline II(11 through the port of export Ja of MR Upper separator (21)), liquid phase cryogen pipeline II(11) flow out from heat exchanger (1) be adjusted valve c(26) to prepare temperature after throttling be the liquid phase cryogen B of-100 DEG C ~-120 DEG C, and enters gas-liquid mixed phase cryogen pipeline (7)；
    Gas phase cryogen A after S5, separation enters gas phase cryogen pipeline II(9 through the port of export Ha of MR Upper separator (21)), gas phase cryogen A exits into MR Lower separator (22) from heat exchanger (1), and gas phase cryogen A is separated into gas phase cryogen C and liquid phase cryogen D by MR Lower separator (22)；
    S6, separate after gas phase cryogen C and liquid phase cryogen D port of export Hb and port of export Jb through MR Lower separator (22) respectively enter in gas-liquid mixed phase cryogen pipeline (7), in gas-liquid mixed phase cryogen pipeline (7), gas-liquid mixed phase cryogen is extracted out from heat exchanger (1), gas-liquid mixed phase cryogen is successively in MR entrance separator (17), MR compressor (18), MR aftercooler (19) and MR final stage separator (20) enter heat exchanger (1), it is achieved thereby that provide cold to heat exchanger (1)；
    S7, the preparation of LNG, to pipeline II(6) in be passed through natural gas, natural gas is backflowed cold flow precooling in heat exchanger (1), liquefy and be subcooled, temperature is that the natural gas of the natural gas of-100 ~-120 DEG C and-150 ~-160 DEG C is respectively from pipeline II(6) outlet C and outlet B flow out, and it is adjusted valve a(24 respectively) and regulation valve b(25) enter in scrubbing tower (3) after throttling, in scrubbing tower (3), natural gas and nitrogen heat exchange, the nitrogen content LNG less than 1.5% is being prepared at the bottom of tower after obversion, the LNG prepared is adjusted valve m(23) enter in LNG storage tank (2) after throttling, it is achieved thereby that the LNG that nitrogen content is less than 1.5%；
    S8, the process of rich nitrogen, the rich nitrogen produced in scrubbing tower (3) is adjusted valve k(31) return in rich nitrogen pipeline (4), rich nitrogen is entered in fuel gas surge tank (16) as fuel gas to normal temperature by natural gas and gas-liquid mixed phase cryogen re-heat；
    The process of S9, BOG tail gas, after BOG heater (12), BOG compressor (13) and BOG surge tank (14), divide into two strands of BOG tail gas successively at the BOG tail gas produced in LNG storage tank (2), it is interior as fuel gas that a portion BOG tail gas enters fuel gas surge tank (16), another part BOG tail gas enters pipeline I(5 after tail-gas compressor (15) compresses) in, BOG tail gas backflowed cold flow precooling, liquefy and be subcooled after enter scrubbing tower (3), it is achieved thereby that the process of BOG tail gas.
CN201410462945.5A 2014-09-12 2014-09-12 Device and method for efficiently denitrifying natural gas Active CN104293404B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201410462945.5A CN104293404B (en) 2014-09-12 2014-09-12 Device and method for efficiently denitrifying natural gas

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201410462945.5A CN104293404B (en) 2014-09-12 2014-09-12 Device and method for efficiently denitrifying natural gas

Publications (2)

Publication Number Publication Date
CN104293404A CN104293404A (en) 2015-01-21
CN104293404B true CN104293404B (en) 2016-08-24

Family

ID=52313367

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201410462945.5A Active CN104293404B (en) 2014-09-12 2014-09-12 Device and method for efficiently denitrifying natural gas

Country Status (1)

Country Link
CN (1) CN104293404B (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021028068A1 (en) * 2019-08-13 2021-02-18 Linde Gmbh Method and unit for processing a gas mixture containing nitrogen and methane

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105695015B (en) * 2016-03-31 2018-09-25 成都深冷液化设备股份有限公司 A kind of novel natural gas de-heavy hydrocarbon apparatus and method
GB2571946A (en) * 2018-03-13 2019-09-18 Linde Ag Method for operating a feed gas processing plant
US11221176B2 (en) * 2018-08-14 2022-01-11 Air Products And Chemicals, Inc. Natural gas liquefaction with integrated nitrogen removal
CN110540882A (en) * 2019-08-28 2019-12-06 四川杰瑞恒日天然气工程有限公司 Denitrification method for natural gas liquefaction device
CN113776278B (en) * 2021-09-06 2024-05-14 四川蜀道装备科技股份有限公司 Nitrogen-containing natural gas denitrification liquefying device and process

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5036671A (en) * 1990-02-06 1991-08-06 Liquid Air Engineering Company Method of liquefying natural gas
NZ582507A (en) * 2007-07-09 2012-08-31 Lng Technology Pty Ltd A method and system for production of liquid natural gas
CN202254637U (en) * 2011-08-03 2012-05-30 成都蜀远煤基能源科技有限公司 Gas deep-cooling separated liquefying device for methanated coal gas
CN103033025B (en) * 2011-09-30 2015-02-18 新地能源工程技术有限公司 Industrial arts for dehydrogenation and denitrogen and de-carbon monoxide from high methane gas and liquefied natural gas production
CN103075868B (en) * 2011-10-25 2015-09-23 中国石油天然气股份有限公司 Natural gas liquefaction system and method
US20130269386A1 (en) * 2012-04-11 2013-10-17 Air Products And Chemicals, Inc. Natural Gas Liquefaction With Feed Water Removal
CN103031169B (en) * 2012-12-13 2014-05-07 新地能源工程技术有限公司 Method and device for carrying out liquefaction and heavy hydrocarbon treatment on natural gas
CN204058408U (en) * 2014-09-12 2014-12-31 成都深冷液化设备股份有限公司 A kind of device of High-efficiency Gas denitrogenation

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021028068A1 (en) * 2019-08-13 2021-02-18 Linde Gmbh Method and unit for processing a gas mixture containing nitrogen and methane

Also Published As

Publication number Publication date
CN104293404A (en) 2015-01-21

Similar Documents

Publication Publication Date Title
CN104293404B (en) Device and method for efficiently denitrifying natural gas
CN103697659B (en) The device and method of liquefied natural gas and rich hydrogen production is produced from high methane gas
CN104528647B (en) The method and apparatus that a kind of synthesis gas separates hydrogen making and high-purity CO
CN212747065U (en) High-nitrogen and helium-containing natural gas liquefaction and crude helium and nitrogen extraction system
CN102435044A (en) Cryogenic separating system for preparing liquefied natural gas with oven gas
CN112066642A (en) High-nitrogen and helium-containing natural gas liquefaction and crude helium and nitrogen extraction system
CN102435045A (en) Liquid nitrogen washing purified synthetic gas and device for cryogenically separating and recovering LNG (liquefied natural gas) thereof
CN204058408U (en) A kind of device of High-efficiency Gas denitrogenation
CN109631494A (en) A kind of helium production system and production method
CN204981793U (en) Processing apparatus of associated gas is applied to to LNG cold energy
CN103868324B (en) The natural gas liquefaction of small-sized skid-mounted type mix refrigerant and NGL reclaim integrated system
CN206858511U (en) BOG recovery liquefaction removing Nitrogen in Natural Gases gas process systems
CN202382517U (en) Cryogenic separation system of using coke-oven gas to produce liquefied natural gas
CN204508803U (en) The device of a kind of high efficiency separation synthetic gas hydrogen making and carbon monoxide
CN214371298U (en) Carbon dioxide gathering liquefaction recovery device
CN212299662U (en) Natural gas low-temperature throttling helium extraction device
CN202382518U (en) Device for washing and purifying synthesis gas with liquid nitrogen and cryogenically separating and recovering LNG (liquefied natural gas)
CN103175380A (en) Device for preparing LNG (liquefied natural gas) by low-concentration coal bed gas oxygen-containing cryogenic liquefaction
CN204702504U (en) A kind of synthetic gas is separated hydrogen making and high-purity CO device
CN206094746U (en) Extract novel device of liquid methane in follow high methane gas
CN103773529B (en) Pry-mounted associated gas liquefaction system
CN114518016A (en) Carbon dioxide capturing, liquefying and recycling device and method
CN204693949U (en) A kind of separation high methane gas device with n-formyl sarcolysine alkane refrigerating function
CN106500460B (en) Nitrogen removing and purifying plant and method in gas deliquescence process
CN216898061U (en) Nitrogen-containing natural gas denitrification liquefaction device

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant
PE01 Entry into force of the registration of the contract for pledge of patent right
PE01 Entry into force of the registration of the contract for pledge of patent right

Denomination of invention: High-efficiency natural gas denitriding device and method

Effective date of registration: 20200107

Granted publication date: 20160824

Pledgee: China Minsheng Banking Corp Chengdu branch

Pledgor: Chengdu Shenleng Liquefaction Plant Co., Ltd.

Registration number: Y2020510000003

PC01 Cancellation of the registration of the contract for pledge of patent right
PC01 Cancellation of the registration of the contract for pledge of patent right

Date of cancellation: 20210825

Granted publication date: 20160824

Pledgee: China Minsheng Banking Corp Chengdu branch

Pledgor: CHENGDU SHENLENG LIQUEFACTION PLANT Co.,Ltd.

Registration number: Y2020510000003

CP01 Change in the name or title of a patent holder
CP01 Change in the name or title of a patent holder

Address after: 611700 north area of Chengdu modern industrial port, Pixian County, Chengdu City, Sichuan Province

Patentee after: Sichuan Shudao Equipment Technology Co.,Ltd.

Address before: 611700 north area of Chengdu modern industrial port, Pixian County, Chengdu City, Sichuan Province

Patentee before: CHENGDU SHENLENG LIQUEFACTION PLANT Co.,Ltd.