CN108981286A - A kind of device and method of high nitrogenous two tower denitrogenation of natural gas - Google Patents
A kind of device and method of high nitrogenous two tower denitrogenation of natural gas Download PDFInfo
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- CN108981286A CN108981286A CN201810915597.0A CN201810915597A CN108981286A CN 108981286 A CN108981286 A CN 108981286A CN 201810915597 A CN201810915597 A CN 201810915597A CN 108981286 A CN108981286 A CN 108981286A
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- ice chest
- denitrification column
- denitrogenation
- throttle valve
- pressure denitrification
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
- F25J3/0214—Liquefied natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
-
- 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
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a kind of device and method of high nitrogenous two tower denitrogenation of natural gas, device includes liquefaction ice chest, first throttle valve, high pressure denitrification column, outer gas transmission compressor, denitrogenation ice chest, second throttle, separator, third throttle valve, low pressure denitrification column, the 4th throttle valve and the 5th throttle valve；Liquefaction ice chest, first throttle valve and high pressure denitrification column are sequentially connected, and high pressure denitrification column lower part outlet, liquefaction ice chest, high pressure denitrification column lower entrances are sequentially connected；High pressure denitrification column outlet at bottom, liquefaction ice chest, outer gas transmission compressor are sequentially connected；High pressure denitrification column top exit, denitrogenation ice chest, second throttle, separator are sequentially connected.The present invention effectively removes nitrogen with two tower rectifying for high nitrogenous Gas Exploitation, improves the calorific value of natural gas；Using the abundant exchange of liquefaction ice chest and denitrogenation ice chest realization device self-energy, additional cold source is not needed, plant energy consumption is reduced.
Description
Technical field
The present invention relates to natural gas processing technical field, in particular to a kind of dress of high nitrogenous two tower of natural gas removing nitrogen
It sets and method.
Background technique
With the development of Gas Industry, the nitrogen containing higher concentration in the natural gas of many oil gas field outputs, naturally
When nitrogen content is higher in gas, energy consumption increases during not only calorific value reduces, collects defeated, but also cannot be directly used as certain natural gas vapour
Vehicle and fuel chemical industry raw material.Deep cooling denitrification process is the current effective means for improving Gas Comprehensive utility value, and is had
The feature that treating capacity is big, nitrogen removal efficiency is high, technology is more mature.Chinese patent CN201010561795.5 discloses one kind and contains
Natural gas/liquefied natural gas method, Chinese patent 201611044602.2 are produced in the double tower cryogenic rectification denitrogenation of methane gas
Disclose nitrogen removing and purifying plant and method in a kind of gas deliquescence process.Lack at present for high nitrogenous natural gas
Remove the process unit and method of nitrogen.
Summary of the invention
The shortcomings that in order to overcome the prior art, the present invention provides a kind of device of high nitrogenous two tower denitrogenation of natural gas and sides
Method.
The technical scheme adopted by the invention is that: a kind of device of high nitrogenous two tower denitrogenation of natural gas, including liquefaction ice chest,
First throttle valve, high pressure denitrification column, outer gas transmission compressor, denitrogenation ice chest, second throttle, separator, third throttle valve, low pressure
Denitrification column, the 4th throttle valve and the 5th throttle valve；
Liquefaction ice chest, first throttle valve, high pressure denitrification column are sequentially connected；High pressure denitrification column lower part outlet, liquefaction ice chest, high pressure-off
Nitrogen tower lower entrances are sequentially connected；High pressure denitrification column outlet at bottom, liquefaction ice chest, outer gas transmission compressor are sequentially connected；High pressure-off
The outlet of nitrogen top of tower, denitrogenation ice chest, second throttle, separator are sequentially connected；Separator top exit, denitrogenation ice chest, third
Throttle valve, low pressure denitrification column upper entrance are sequentially connected；Separator bottom outlet, the 4th throttle valve, low pressure denitrification column middle part enter
Mouth is sequentially connected；Low pressure denitrification column top exit, denitrogenation ice chest, liquefaction ice chest are sequentially connected；Low pressure denitrification column lower part outlet takes off
Nitrogen ice chest, low pressure denitrification column lower entrances are sequentially connected；Low pressure denitrification column outlet at bottom, the 5th throttle valve, denitrogenation ice chest, liquefaction
Ice chest, outer gas transmission compressor are sequentially connected.
The invention also discloses a kind of methods of high nitrogenous two tower denitrogenation of natural gas, include the following steps:
The first step, by pressure 3500kPa.a ~ 5000kPa.a, 30 ~ 50 DEG C of temperature, 25mol% containing nitrogen ~ 75mol% natural gas
Input liquefaction ice chest is cooled to -110 ~ -130 DEG C in advance, and high pressure is entered after first throttle valve throttles to 2700kPa.a ~ 3500kPa.a
Denitrification column top carries out gas-liquid separation；Liquid phase enters liquefaction ice chest re-heat to after -70 ~ -95 DEG C from high pressure denitrification column lower part outlet
It returns to high pressure denitrification column lower entrances and carries out gas-liquid separation；Liquid phase from high pressure denitrification column outlet at bottom enter liquefaction ice chest re-heat to
Enter outer gas transmission compressor boost after 25 ~ 45 DEG C to 3700kPa.a ~ 5200kPa.a；
Second step, gas phase enters denitrogenation ice chest from high pressure denitrification column top exit and is cooled to -140 ~ -160 DEG C, through second throttle
Throttling carries out gas-liquid separation to entering separator after 800kPa.a ~ 1500kPa.a, in which: liquid phase through the 4th throttle valve throttle to
Enter in the middle part of low pressure denitrification column after 500kPa.a ~ 2000kPa.a；Gas phase enters denitrogenation ice chest and condenses to after -140 ~ -160 DEG C, warp
Third throttle valve, which throttles, enters the progress gas-liquid separation of low pressure denitrification column top to 500kPa.a ~ 2000kPa.a；Liquid phase is de- from low pressure
Nitrogen tower lower part outlet enters denitrogenation ice chest re-heat to return low pressure denitrification column lower entrances after -130 ~ -145 DEG C and carries out gas-liquid point
From；Liquid phase is throttled by the 5th throttle valve to 350kPa.a ~ 500kPa.a from low pressure denitrification column outlet at bottom, sequentially enters denitrogenation
Ice chest re-heat to -120 ~ -145 DEG C, liquefaction ice chest re-heat to after 25 ~ 45 DEG C, through outer gas transmission compressor boost to 3700kPa.a ~
5200kPa.a to subsequent processing；The nitrogen of removing successively passes through the re-heat of denitrogenation ice chest to -120 from low pressure denitrification column top exit
It is ~ -145 DEG C, rear to enter liquefaction ice chest re-heat to 25 ~ 45 DEG C to subsequent processing.
Basic principle of the invention is: the condensation temperature using natural gas and nitrogen is different, by high pressure denitrification column, low
The rectifying separation for pressing denitrification column, the nitrogen in high nitrogenous natural gas is removed.It will predominantly contain nitrogen 25mol% ~ 75mol%'s
Natural gas through supercooling enter high pressure denitrification column carry out gas-liquid separation, realize the Nitrogen in Natural Gases Gas content of tower top improve to
60mol% ~ 85mol% carries out gas-liquid separation into low pressure denitrification column, by nitrogen concentrate to 97mol% then using cooling
More than.
Compared with prior art, the positive effect of the present invention is: effectively de- with two tower rectifying for high nitrogenous Gas Exploitation
Except nitrogen, the calorific value of natural gas is improved；Using the abundant exchange of liquefaction ice chest and denitrogenation ice chest realization device self-energy, do not need
Additional cold source, reduces plant energy consumption.
Detailed description of the invention
Fig. 1 is the system principle schematic diagram of the device of high nitrogenous two tower denitrogenation of natural gas of the invention；
In figure: 1, pipeline；2, liquefy ice chest；3, pipeline；4, first throttle valve；5, pipeline；6, high pressure denitrification column；7, pipeline；8,
Pipeline；9, pipeline；10, outer gas transmission compressor；11, pipeline；12, pipeline；13, denitrogenation ice chest；14, pipeline；15, the second throttling
Valve；16, pipeline；17, separator；18, pipeline；19, pipeline；20, third throttle valve；21, pipeline；22, low pressure denitrification column；23,
Pipeline；24, the 4th throttle valve；25, pipeline；26, pipeline；27, pipeline；28, pipeline；29, pipeline；30, pipeline；31, pipeline；
32, the 5th throttle valve；33, pipeline；34, pipeline；35, pipeline；36, pipeline.
Specific embodiment
As shown in Figure 1, the device of the high nitrogenous two tower denitrogenation of natural gas of the present invention, including liquefaction ice chest 2, first throttle valve 4,
High pressure denitrification column 6, outer gas transmission compressor 10, denitrogenation ice chest 13, second throttle 15, separator 17, third throttle valve 20, low pressure
Denitrification column 22, the 4th throttle valve 24, the 5th throttle valve 32；
The liquefaction ice chest 2 inputs natural gas by connecting a process outside pipeline 1, by pipeline 1；The liquefaction ice chest 2 passes through
The external subsequent processing of pipeline 30；
The liquefaction ice chest 2, first throttle valve 4, high pressure denitrification column 6 pass sequentially through the connection of pipeline 3,5；
6 lower part outlet of high pressure denitrification column, liquefaction ice chest 2,6 lower entrances of high pressure denitrification column pass sequentially through the company of pipeline 11,12
It connects；6 outlet at bottom of high pressure denitrification column, liquefaction ice chest 2, outer gas transmission compressor 10 pass sequentially through the connection of pipeline 8,9；
6 top exit of high pressure denitrification column, denitrogenation ice chest 13, second throttle 15, separator 17 pass sequentially through pipeline 7,14,
16 connections；
17 top exit of separator, denitrogenation ice chest 13, third throttle valve 20,22 upper entrance of low pressure denitrification column pass sequentially through
Pipeline 18,19,21 connects；
17 outlet at bottom of separator, the 4th throttle valve 24,22 centre entrance of low pressure denitrification column pass sequentially through the company of pipeline 23,25
It connects；
22 top exit of low pressure denitrification column, denitrogenation ice chest 13, liquefaction ice chest 2 pass sequentially through the connection of pipeline 28,29；
22 lower part outlet of low pressure denitrification column, denitrogenation ice chest 13,22 lower entrances of low pressure denitrification column pass sequentially through pipeline 26,27
Connection；
22 outlet at bottom of low pressure denitrification column, the 5th throttle valve 32, denitrogenation ice chest 13, liquefaction ice chest 2, outer gas transmission compressor 10
Pass sequentially through the connection of pipeline 31,33,34,35；Outer gas transmission press 10 is used by the external gas distributing system of pipeline 36 or natural gas
Family.
The invention also discloses the processes of high nitrogenous two tower deep cooling denitrogenation of natural gas, include the following steps:
The first step, will from 1 25mol% containing nitrogen of pipeline ~ 75mol% natural gas (3500kPa.a ~ 5000kPa.a, 30 ~ 50
DEG C) input liquefaction ice chest 2 be cooled to -110 ~ -130 DEG C in advance, pass sequentially through pipeline 3, first throttle valve 4 throttle to 2700kPa.a ~
3500kPa.a enters 6 top of high pressure denitrification column by pipeline 5 and carries out gas-liquid separation；Liquid phase is from 6 lower part outlet of high pressure denitrification column
Enter liquefaction 2 re-heat of ice chest to -70 ~ -95 DEG C through pipeline 11, returns to 6 lower entrances of high pressure denitrification column through pipeline 12 and carry out gas-liquid
Separation；Liquid phase from 6 outlet at bottom of high pressure denitrification column through pipeline 8 enter liquefaction 2 re-heat of ice chest to after 25 ~ 45 DEG C by pipeline 9 into
Enter outer gas transmission compressor 10 and is pressurized to 3700kPa.a ~ 5200kPa.a；
Second step, gas phase are cooled to -140 ~ -160 DEG C into denitrogenation ice chest 13 by pipeline 7 from 6 top exit of high pressure denitrification column,
Separator 17 is entered by pipeline 16 through pipeline 14, the throttling of second throttle 15 to 800kPa.a ~ 1500kPa.a and carries out gas-liquid point
From, in which: liquid phase is throttled through the 4th throttle valve 24 to 500kPa.a ~ 2000kPa.a by pipeline 23, and it is de- that pipeline 25 enters low pressure
22 middle part of nitrogen tower；Gas phase is throttled by pipeline 19 through third after pipeline 18 enters extremely -140 ~ -160 DEG C of the condensation of denitrogenation ice chest 13
The throttling of valve 20 enters 22 top of low pressure denitrification column through pipeline 25 and carries out gas-liquid separation to 500kPa.a ~ 2000kPa.a；Liquid phase from
22 lower part outlet of low pressure denitrification column enters 13 re-heat of denitrogenation ice chest to -130 ~ -145 DEG C through pipeline 26, returns to low pressure through pipeline 27
22 lower entrances of denitrification column carry out gas-liquid separation；Liquid phase is from 22 outlet at bottom of low pressure denitrification column by pipeline 31 through the 5th throttle valve
After 32 throttlings to 350kPa.a ~ 500kPa.a, 13 re-heat of denitrogenation ice chest is entered to -120 ~ -145 DEG C by pipeline 33, passes through pipe
Road 34 enter liquefaction 2 re-heat of ice chest to 25 ~ 45 DEG C, by pipeline 35 into outer gas transmission compressor 10 be pressurized to 3700kPa.a ~
5200kPa.a passes through pipeline 36 to subsequent processing；The nitrogen of removing passes sequentially through pipeline 28 from 22 tower top outlet of low pressure denitrification column
Into 13 re-heat of denitrogenation ice chest to -120 ~ -145 DEG C, by pipeline 29 enter liquefaction 2 re-heat of ice chest to 25 ~ 45 DEG C, pass through pipeline
30 to subsequent processing.
The above is only a preferred embodiment of the present invention, it is noted that for the ordinary skill people of the art
For member, several improvement can also be made without departing from the principle of the present invention, these improvement also should be regarded as of the invention
Protection scope.
Claims (2)
1. a kind of device of high nitrogenous two tower denitrogenation of natural gas, it is characterised in that: including ice chest (2), first throttle valve of liquefying
(4), high pressure denitrification column (6), outer gas transmission compressor (10), denitrogenation ice chest (13), second throttle (15), separator (17),
Three throttle valves (20), low pressure denitrification column (22), the 4th throttle valve (24) and the 5th throttle valve (32)；
The liquefaction ice chest (2), first throttle valve (4), high pressure denitrification column (6) are sequentially connected；High pressure denitrification column (6) lower part
Outlet, liquefaction ice chest (2), high pressure denitrification column (6) lower entrances are sequentially connected；High pressure denitrification column (6) outlet at bottom, liquefaction
Ice chest (2), outer gas transmission compressor (10) are sequentially connected；High pressure denitrification column (6) top exit, denitrogenation ice chest (13), second
Throttle valve (15), separator (17) are sequentially connected；Separator (17) top exit, denitrogenation ice chest (13), third throttle valve
(20), low pressure denitrification column (22) upper entrance is sequentially connected；It is separator (17) outlet at bottom, the 4th throttle valve (24), low
Pressure denitrification column (22) centre entrance is sequentially connected；Low pressure denitrification column (22) top exit, denitrogenation ice chest (13), liquefaction ice chest
(2) it is sequentially connected；Low pressure denitrification column (22) lower part outlet, denitrogenation ice chest (13), low pressure denitrification column (22) lower entrances according to
Secondary connection；Low pressure denitrification column (22) outlet at bottom, denitrogenation ice chest (13), liquefies ice chest (2), is outer at the 5th throttle valve (32)
Gas transmission compressor (10) is sequentially connected.
2. a kind of denitrogenation method based on claim 1 described device, characterized by the following steps:
The first step, pressure 3500kPa.a ~ 5000kPa.a, 30 ~ 50 DEG C of temperature, 25mol% containing nitrogen ~ 75mol% is natural
Gas input liquefaction ice chest (2) is cooled to -110 ~ -130 DEG C in advance, after first throttle valve (4) throttling to 2700kPa.a ~ 3500kPa.a
Gas-liquid separation is carried out into high pressure denitrification column (6) top；Liquid phase enters liquefaction ice chest (2) from high pressure denitrification column (6) lower part outlet
Re-heat to return high pressure denitrification column (6) lower entrances after -70 ~ -95 DEG C carry out gas-liquid separation；Liquid phase is from high pressure denitrification column tower (6)
Outlet at bottom enter liquefaction ice chest (2) re-heat to enter after 25 ~ 45 DEG C outer gas transmission compressor (10) be pressurized to 3700kPa.a ~
5200kPa.a；
Second step, gas phase enter denitrogenation ice chest (13) from high pressure denitrification column (6) top exit and are cooled to -140 ~ -160 DEG C, through
Enter separator (17) after two throttle valves (15) throttling to 800kPa.a ~ 1500kPa.a and carry out gas-liquid separation, in which: liquid phase warp
Enter in the middle part of low pressure denitrification column (22) after the throttling to 500kPa.a ~ 2000kPa.a of 4th throttle valve (24)；It is cold that gas phase enters denitrogenation
After extremely -140 ~ -160 DEG C of case (13) condensation, it is de- to enter low pressure through third throttle valve (20) throttling to 500kPa.a ~ 2000kPa.a
Nitrogen tower (22) top carries out gas-liquid separation；Liquid phase from low pressure denitrification column (22) lower part outlet enter denitrogenation ice chest (13) re-heat to-
Low pressure denitrification column (22) lower entrances are returned after 130 ~ -145 DEG C carries out gas-liquid separation；Liquid phase goes out from low pressure denitrification column (22) bottom
Mouthful by the throttling of the 5th throttle valve (32) to 350kPa.a ~ 500kPa.a, sequentially enter denitrogenation ice chest (13) re-heat to -120 ~ -
145 DEG C, liquefaction ice chest (2) re-heat to after 25 ~ 45 DEG C, be pressurized to 3700kPa.a ~ 5200kPa.a through outer gas transmission compressor (10)
To subsequent processing；The nitrogen of removing from low pressure denitrification column (22) top exit successively pass through denitrogenation ice chest (13) re-heat to -120 ~ -
It is 145 DEG C, rear to enter liquefaction ice chest (2) re-heat to 25 ~ 45 DEG C to subsequent processing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810915597.0A CN108981286B (en) | 2018-08-13 | 2018-08-13 | Device and method for two-tower denitrification of high-nitrogen-content natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810915597.0A CN108981286B (en) | 2018-08-13 | 2018-08-13 | Device and method for two-tower denitrification of high-nitrogen-content natural gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108981286A true CN108981286A (en) | 2018-12-11 |
| CN108981286B CN108981286B (en) | 2020-03-24 |
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| CN201810915597.0A Active CN108981286B (en) | 2018-08-13 | 2018-08-13 | Device and method for two-tower denitrification of high-nitrogen-content natural gas |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1301943C (en) * | 2001-07-11 | 2007-02-28 | 英国氧气集团有限公司 | Denitrogenation method and appts. |
| CN102021056A (en) * | 2010-11-26 | 2011-04-20 | 成都赛普瑞兴科技有限公司 | Method for preparing natural gas/liquefied natural gas by denitrifying nitrogen-containing methane gas |
| CN102767936A (en) * | 2012-07-18 | 2012-11-07 | 重庆耐德工业股份有限公司 | Process for producing gas-phase natural gas and liquid-phase natural gas through nitrogen-methane separation in nitrogen-containing natural gas |
| CN205279605U (en) * | 2015-11-17 | 2016-06-01 | 辽宁中集哈深冷气体液化设备有限公司 | Preparation synthetic natural gas's coke oven gas cryogenic separation system |
| CN206207884U (en) * | 2016-10-27 | 2017-05-31 | 杭州中泰深冷技术股份有限公司 | A kind of oven gas LNG coproducing synthetic ammonia devices |
| CN107228526A (en) * | 2017-07-03 | 2017-10-03 | 成都深冷液化设备股份有限公司 | A kind of LNG flashed vapours carry helium, denitrogenation and reliquefaction installation |
| CN108384593A (en) * | 2018-05-11 | 2018-08-10 | 中国石油工程建设有限公司 | A kind of process unit and method of nitrogenous natural gas double tower deep cooling denitrogenation |
-
2018
- 2018-08-13 CN CN201810915597.0A patent/CN108981286B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1301943C (en) * | 2001-07-11 | 2007-02-28 | 英国氧气集团有限公司 | Denitrogenation method and appts. |
| CN102021056A (en) * | 2010-11-26 | 2011-04-20 | 成都赛普瑞兴科技有限公司 | Method for preparing natural gas/liquefied natural gas by denitrifying nitrogen-containing methane gas |
| CN102767936A (en) * | 2012-07-18 | 2012-11-07 | 重庆耐德工业股份有限公司 | Process for producing gas-phase natural gas and liquid-phase natural gas through nitrogen-methane separation in nitrogen-containing natural gas |
| CN205279605U (en) * | 2015-11-17 | 2016-06-01 | 辽宁中集哈深冷气体液化设备有限公司 | Preparation synthetic natural gas's coke oven gas cryogenic separation system |
| CN206207884U (en) * | 2016-10-27 | 2017-05-31 | 杭州中泰深冷技术股份有限公司 | A kind of oven gas LNG coproducing synthetic ammonia devices |
| CN107228526A (en) * | 2017-07-03 | 2017-10-03 | 成都深冷液化设备股份有限公司 | A kind of LNG flashed vapours carry helium, denitrogenation and reliquefaction installation |
| CN108384593A (en) * | 2018-05-11 | 2018-08-10 | 中国石油工程建设有限公司 | A kind of process unit and method of nitrogenous natural gas double tower deep cooling denitrogenation |
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