CN104513680B - Technology and device for removing hydrogen and nitrogen from methane-rich gas through rectification and producing liquefied natural gas - Google Patents
Technology and device for removing hydrogen and nitrogen from methane-rich gas through rectification and producing liquefied natural gas Download PDFInfo
- Publication number
- CN104513680B CN104513680B CN201310461438.5A CN201310461438A CN104513680B CN 104513680 B CN104513680 B CN 104513680B CN 201310461438 A CN201310461438 A CN 201310461438A CN 104513680 B CN104513680 B CN 104513680B
- Authority
- CN
- China
- Prior art keywords
- gas
- nitrogen
- ice chest
- liquid
- rectifying column
- 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
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
- F25J3/0233—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
- 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
- F25J3/0257—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
- 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
-
- 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
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead 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
- 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising 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
- F25J2270/18—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
- F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
Abstract
A technology and a device for removing hydrogen and nitrogen from methane-rich gas through rectification and producing liquefied natural gas. The technology comprises two parts: low-temperature liquefaction and rectification separation, wherein the low-temperature liquefaction includes following steps: firstly feeding the methane-rich gas containing hydrogen and nitrogen into a refrigerating box and liquefying a methane component in the refrigerating box with a mixed refrigerant for providing cooling capacity; and the rectification separation includes: directly feeding the liquefied methane-rich gas containing hydrogen and nitrogen into a single rectifying column to perform rectification for removing the hydrogen, the nitrogen and a less amount of carbon monoxide, wherein a gas mixture containing the hydrogen, the nitrogen and the less amount of the carbon monoxide is obtained at the top of the rectifying column; passing the gas mixture through the refrigerating box for recycling the cooling capacity and discharging the gas mixture out from the refrigerating box; and feeding back a liquid phase at the bottom of the rectifying column to the refrigerating box for being supercooled and then discharging the liquid phase out from the system to obtain a liquefied natural gas product which is not more than 500 ppm in the content of the hydrogen, is not more than 2% in the content of the nitrogen and is not more than 2% in the content of carbon monoxide. The invention provides a technology in which liquefied natural gas is produced by liquefying the methane-rich gas and meanwhile the hydrogen, the nitrogen and the carbon monoxide are removed. The technology is simple in processes and is low in equipment investment cost.
Description
Technical field
The invention provides a kind of high methane gas rectifying dehydrogenation nitrogen and produce the technique and device of liquefied natural gas.Coal base is closed
Into gas after gas, oven gas and coke-oven gas methanation etc. in addition to containing methane, also contain nitrogen, hydrogen and a small amount of oxygen
Change carbon, to obtain liquefied natural gas, need to be removed to a certain extent, could be used as liquefied natural gas（LNG）Product output.
Background technology
Under the pressure of environmental protection and energy cost pressure, natural gas as primary energy in social every field proportion just gradually
Lifting, its application field be gradually expanded to generatings, automobile gas, industrial gas, city dweller with gas, chemical industry gas etc. just
Face, market demand increases sharply.The defeated method of supplying of traditional natural gas tube is still main flow, but by material condition and user distribution
Limitation, has quite a few resource to carry out pipe long-distance conveying, need to select liquefied mode, converts methane to liquid
User terminal is sent to using flexible means of transportation again.Also, liquefied natural gas（LNG）Volume only has same gas volume
1/625, storage and cost of transportation can be reduced after liquefaction, and the combustion value of unit volume can be improved.Liquefied natural gas industry
Continue to develop, requirement higher is proposed at aspects such as energy consumption, investment and efficiency to natural gas liquefaction and device.
Methane gas, such as synthetic natural gas obtained after coal based synthetic gas and coke-oven gas methanation are rich in for some
Deng, its composition in addition to methane, also containing nitrogen, hydrogen etc., to obtain the liquefied natural gas of high-purity, need to by nitrogen therein,
Hydrogen is removed to a certain extent, could be used as liquefied natural gas（LNG）Product output.
Conventional gas separating method typically has low-temperature liquefaction separation, pressure-variable adsorption and UF membrane etc., current low temperature at present
Liquefaction isolation technics is just gradually being applied to methane-rich gas purification and the production of liquefied natural gas.It is as shown in Figure 1 methane rich
Air lift is pure and liquefaction process, and the technique includes that low-temperature liquefaction and rectifying separate two parts；Low-temperature liquefaction part is provided by refrigerant
Cold realizes the liquefaction of natural gas in ice chest；Rectifying separate section uses two-tower rectification（High-pressure tower and lower pressure column）Flow is removed
Hydrogen, nitrogen, low-pressure distillation top of tower obtain rich nitrogen, and high-pressure rectification top of tower obtains hydrogen rich gas；Use this technique can be with
Obtain foreign gas and remove qualified liquefied natural gas product, but this technological process is complex, using two rectifying columns, if
Standby investment cost is higher, and is not easy to device driving operation.
Chinese patent 201210065876.5 disclose a kind of gas from methane rich in dehydrogenation, nitrogen, carbon monoxide
And the technique of liquefied natural gas is produced, as shown in Figure 2, the technique includes the rectifying separation of low-temperature liquefaction operation and preceding band flash distillation
Operation two parts；Wherein, the gaseous mixture of hydrogen, nitrogen, the methane rich of carbon monoxide is first through ice chest precooling, afterwards into essence
The tower bottom reboiler of tower is evaporated for rectifying column provides heat, is gone out in the postorder heat exchanger of mixed flow stock return ice chest of tower bottom reboiler
Cooling box enters in flash tank and flashes after cooling, and flash drum overhead obtains the hydrogen rich gas of part, returns to ice chest re-heat, flash tank bottom
Portion's liquid phase enters rectifying in rectifying column after being throttled through choke valve；Rectifying column top obtains the mixing of hydrogen, nitrogen, carbon monoxide
Gas, the hydrogen, nitrogen, carbon mono oxide mixture the cooling box system after ice chest recovery cold；The liquid phase of rectifier bottoms is returned
Go out system after being subcooled in ice chest, used as hydrogen content≤4000ppm, nitrogen content≤8%, the liquefaction of carbon monoxide≤9% is natural
Gas product is obtained.Though the technological process of the patent is relatively simple, contain as the hydrogen content of liquefied natural gas product, nitrogen
Amount, carbon monoxide content are still higher.Can inevitably cause to carry substantial amounts of first in flashed vapour using this process is flashed
Alkane, and its amount cannot precise control, the loss that methane component can be caused larger.Therefore, this flash distillation adds rectifying separating technology to use up
It is qualified that can be removed to for the impurity compositions such as hydrogen, nitrogen by pipe, also causes that methane component loss is larger, it is adaptable to the requirement of methane yield not
Occasion high.An object of the present invention is to research and develop a kind of new flow to improve methane content in LNG product, improves methane
Yield.
The content of the invention
The present inventor by by azeotrope it has surprisingly been found that provide cold by hydrogen, the richness of nitrogen in ice chest
Methane component liquefaction in methane gas；Then immediately proceed to single tower distillation tower rectifying, removing hydrogen, nitrogen and a small amount of carbon monoxide energy
Hydrogen content≤500ppm, nitrogen content≤2%, one are obtained while hydrogen, nitrogen and the carbon monoxide that may contain are removed
The liquefied natural gas of carbonoxide≤2%, flow is relatively simple and equipment investment expense is relatively low.Use the rectifying separating technology can be with essence
Methane component content in LNG product and tai gas of rectifying is really controlled, compared with flash distillation plus rectifying separating technology, methane in LNG product
Content at least improves 3%, and impurity composition content is lower.
Therefore, the present invention provides a kind of high methane gas rectifying dehydrogenation nitrogen and produces the technique of liquefied natural gas, the technique bag
Include low-temperature liquefaction and rectifying separates two parts；Low-temperature liquefaction includes that hydrogen, the high methane gas of nitrogen initially enter ice chest, by mixing
Cryogen offer cold is closed methane component liquefies in ice chest；Rectifying is separated to be included：The methane rich of hydrogen, nitrogen after liquefaction
Gas is directly entered single tower distillation tower rectifying, removing hydrogen, nitrogen and a small amount of carbon monoxide；Rectifying column top obtains hydrogen, nitrogen
And the gaseous mixture of a small amount of carbon monoxide, the hydrogen, nitrogen, carbon mono oxide mixture the cooling box system after ice chest recovery cold；
Go out system after being subcooled in the liquid phase return ice chest of rectifier bottoms, obtain hydrogen content≤500ppm, preferably≤300ppm, nitrogen
Content≤2%, preferably≤1%, carbon monoxide≤2%, liquefied natural gas product preferably≤1%.
Generally, in low-temperature liquefaction, the cold of ice chest and the heat of rectifying tower bottom reboiler are by mixed working fluid pressure
Compression system is provided or mainly provided by mixed working fluid compressibility；The mixed working fluid being made up of C1~C5 and N2 is by rational proportion
Afterwards（N2:5mol%~25mol%, preferably 10mol~15mol%, C1:10mol%~25mol%, preferably 15mol%~20mol, C2:
30mol%~55mol%, preferably 35mol%~45mol%, C3:10mol%~25mol%, preferably 15mol%~20mol%, C5:
10mol%~25mol%, preferably 15mol%~20mol%, the total mole number based on all gas）Into the entrance of compressor, warp
First paragraph is compressed to 0.6~1.8MPaA, and 30 DEG C~40 DEG C are cooled into first order cooler, enters back into first order gas-liquid point
Gas-liquid separation is carried out from device, the gas that first order gas-liquid separator top is isolated goes successively to the second segment entrance of compressor,
1.2~5.4MPaA is compressed to through two sections, after the liquid that first order gas-liquid separator bottom liquid phases end is isolated pressurizes through liquid pump
After converging with the hot gas of second segment compression outlet pipeline, enter back into and be cooled in second-stage cooler 30 DEG C~40 DEG C, it is cold
But the mixed working fluid after subsequently enters second level gas-liquid separator and carries out gas-liquid separation, and second level gas-liquid separator bottom is isolated
Liquid enter the first heat exchanger channels of ice chest and participate in heat exchange, the top gas of second level gas-liquid separator subsequently enter ice chest
Second heat exchanger channels participate in heat exchange；
The liquid drawn from the second level gas-liquid separator bottom of mixed working fluid compressibility initially enters the first of ice chest
Heat exchanger channels, are cooled to about -10 DEG C~-80 DEG C in advance wherein, preferably -20 DEG C~-60 DEG C, preferably -30 DEG C~-50 DEG C, through
One choke valve throttles to 0.2~0.8MPaA, with the mixed working fluid stream returned by second throttle after preferably 0.4~0.6MPaA
Stock converges and is redirected back into third level heat exchanger channels for ice chest provides cold and then returnes to the first compression section；By second level gas
The gas phase stream stock of the mixed working fluid that liquid/gas separator top is isolated is cooled to uniform temperature by the second heat exchanger channels of ice chest（One
As to -75 DEG C~-130 DEG C scopes, preferably -90 DEG C~-110 DEG C scopes）Cooling box afterwards, the tower bottom reboiler into rectifying column is
Rectifying column provides heat, goes out the stream stock of tower bottom reboiler（Own temperature is reduced to -80 DEG C~-133 DEG C）Return to ice chest（Such as
Eight heat exchanger channels）Continue cool to -140 DEG C~-165 DEG C, preferably -150 DEG C~-160 DEG C, then through second throttle throttle to
0.2~0.8MPaA, preferably 0.4~0.6MPaA, after be redirected back into the 3rd heat exchanger channels of ice chest for ice chest provides cold.
Preferably, the distillation process uses a rectifying column, reboiler, the condenser of tower top of the rectifying column including bottom of towe
With a point flow container.
In situations where it is preferred, in the rectifying separation process, high methane gas is cooled to uniform temperature through ice chest first
（General extremely -140 DEG C~-165 DEG C scopes）Afterwards, the throttling arrangement of stream stock-traders' know-how one of cooling box（It is preferred that choke valve）Expenditure and pressure（One
As be decompressed to 0.6~3.5MPaA scopes, preferably 0.8~3.0MPaA scopes, more preferably 1.5~2.5MPaA scopes）Enter afterwards
Rectifying in rectifying column（Operating pressure in 0.6~3.5MPaA scopes, preferably 0.8~3.0MPaA scopes, more preferably 1.5~
2.5MPaA scopes）, overhead gas are hydrogen, nitrogen, carbon mono oxide mixture, cooling box system after reclaiming cold through ice chest；Rectifying column
Bottom liquid phases return ice chest（Such as the 9th heat exchanger channels）Middle mistake is cooled to a certain degree（General under-cooling is to -140 DEG C~-165 DEG C
Scope）, after as liquefied natural gas product draw, obtain LNG product.Gained LNG product has in scope defined above
Hydrogen content, nitrogen content.
As preferred mode, in rectifying column of the present invention during rectifying, enter from the gas phase of the Base top contact of rectifying column
Enter in overhead condenser, point flow container point liquid is entered after liquid nitrogen condensation, hydrogen, nitrogen, carbon monoxide are obtained from a point flow container top
Gaseous mixture, point flow container bottom liquid phases pass back into tower；Rectifying column bottom obtains LNG product, is then back to carry out supercooling behaviour in ice chest
Cooling box system after work, obtains LNG product.
It is preferred that, the overhead condenser of rectifying column provides cold using liquid nitrogen, from system outside gas nitrogen liquefied by ice chest
Liquid nitrogen is produced, the overhead condenser that rectifying column is entered after being throttled through choke valve carrys out cooling tower top gaseous stream, goes out after liquid nitrogen gasification
Condenser, cooling box system after reclaiming cold through ice chest.
According to another aspect of the present invention, there is provided a kind of high methane gas rectifying dehydrogenation nitrogen simultaneously produces the dress of liquefied natural gas
Put, the device includes：Ice chest, four throttling arrangements and rectifying column, the rectifying column include reboiler, the condenser of tower top of bottom of towe
With a point flow container,
Wherein, the ice chest includes：
Liquid phase azeotrope entrance, it is connected with the first heat exchanger channels of ice chest, and first heat exchanger channels are from ice chest
One specific level of heat exchanger（Such as first order, the second level, third level etc.）End draw a pipeline, via first throttle
Valve, is connected into ice chest with the 3rd heat exchanger channels of ice chest,
Gas phase cryogen entrance, it is connected with the second heat exchanger channels of ice chest, and second heat exchanger channels are from the another of heat exchanger
Individual specific level（Such as first order, the second level, third level etc.）End draw a pipeline, be connected to rectifying tower bottom reboiler
Arrival end, the port of export of rectifying tower bottom reboiler returns to ice chest（Such as the 8th heat exchanger channels）, another specific level from ice chest（Example
Such as first order, the second level, the third level）End draw a pipeline, via second throttle, the 3rd heat exchange with ice chest is logical
The arrival end connection in road, the port of export of the 3rd heat exchanger channels is azeotrope outlet,
The high methane gas import and a methane rich mixed flow stock outlet being connected with the 4th heat exchanger channels of ice chest, should
The stock outlet of methane rich mixed flow is connected via the 3rd choke valve with rectifying column centre entrance,
With the outlet of the gas nitrogen entrance that the 5th heat exchanger channels of ice chest are connected gentle nitrogen, the outlet of gas nitrogen draw a pipeline via
4th choke valve is connected with the liquid nitrogen entrance of rectifying column tower top condenser,
The gas nitrogen being connected with the 6th heat exchanger channels of ice chest exports gentle nitrogen entrance, and the gas nitrogen entrance is cold with rectifying column top
The gas nitrogen outlet connection of condenser,
The hydrogen nitrogen mixed gas outlet being connected with the 7th heat exchanger channels of ice chest and hydrogen nitrogen mixed gas entrance,
Rectifying column top introduction pipe connection overhead condenser, overhead condenser outlet is connected with the entrance of point flow container, point
The outlet of flow container bottom liquid phases is drawn return duct and is connected with rectifier, and a point flow container top gas phase outlet introduction pipe is changed with the 7th
The hydrogen nitrogen mixed gas entrance connection of the passage of heat,
The port of export of rectifier bottoms liquid phase returns to ice chest（Such as the 9th heat exchanger channels）, from the another specific level of ice chest
（Such as first order, the second level, third level etc.）End introduction pipe connection LNG tank.
Preferably, the heat of the cold of ice chest and rectifying tower bottom reboiler provided by mixed working fluid compressibility or it is main by
Mixed working fluid compressibility is provided, and the mixed working fluid compressibility includes that the refrigerant compression systems include that two-period form mixes work
Matter compressor, the first order cooler being connected with the first paragraph and second segment of the two-period form mixed working fluid compressor respectively and
Secondary coolers, the first order gas-liquid separator being connected with the first order cooler and second-stage cooler respectively and the second level
Gas-liquid separator and a liquid pump being connected with first order gas-liquid separator,
The liquid phase end and gas phase end of the second level gas-liquid separator in the refrigerant compression systems are respectively with described first
The arrival end of the arrival end of heat exchanger channels and the second heat exchanger channels is connected via two pipelines, the port of export warp of the 3rd heat exchanger channels
The cryogen access road of the first compression section is connected to by pipeline；
The gas phase end of the first order gas-liquid separator in wherein two gas-liquid separators and two-period form mixed working fluid compressor
The second compression section connection, the liquid phase end of first order gas-liquid separator is converged via liquid pump with the outlet conduit of the second compression section
The second-stage cooler in two coolers is connected to afterwards.
Advantages of the present invention：
1st, of the invention to separate hydrogen, the process route of nitrogen using brand-new, will liquefy and separate synchronously is carried out, and economy can
Lean on；
2nd, single tower distillation flow is relatively simple compared with two-tower rectification flow, the reduction of equipment investment maintenance cost；The double tower essence
The low-pressure distillation bottom of towe for evaporating flow provides thermal source in itself using the natural gas of partial liquefaction, and single tower distillation flow of the present invention is then
Thermal source is provided using mix refrigerant；This be due to：Rectification column pressure is compared with single column flow mesolow Rectification column pressure in the present invention
Height, corresponding operating temperature is also higher, and the natural gas under this kind of operating condition as thermal source may be pure gas phase, then pass in and out bottom of towe again
The natural air Temperature Difference for boiling device will be larger, cannot bear larger during using the good plate-fin of heat transfer effect as tower bottom reboiler
The temperature difference, the present invention solves this problem, and this is one of the difference of the present invention compared with two-tower rectification flow；
3rd, can accurately be controlled by controlling the operating pressure and tower top of rectifying column, bottom of towe thermic load using rectifying separating technology
Methane component content in LNG product processed and tai gas of rectifying, compared with flash distillation plus rectifying separating technology, methane content in LNG product
3% is at least improved, impurity composition content is lower, methane yield is higher.
Brief description of the drawings
Fig. 1 is a kind of process chart of prior art；Wherein, E1 ' is ice chest, and V1 ', V2 ', V3 ', V4 ', V5 ' are section
Stream valve, T1 ' is high-pressure rectification tower, and T2 ' is low-pressure distillation tower, and T3 ', T4 ' are flash tank.
Fig. 2 is another process chart of prior art；Wherein E1 is ice chest, and V1, V2, V3, V4 are choke valve, and T1 is
Rectifying column, T2 is flash tank, and E2 is tower bottom reboiler, and E3 is overhead condenser.
Fig. 3 is process chart of the invention；Wherein, X1 is ice chest, and C1 is compressor, and E3 is first order cooler, E4
It is second-stage cooler, V2 is first order gas-liquid separator, and V3 is second level gas-liquid separator, and P1 is liquid pump, and T1 is rectifying
Tower, V1 is a point flow container, and E2 is overhead condenser, and E1 is tower bottom reboiler, and V-1, V-2, V-3, V-4 are choke valve.
Specific embodiment
Technique of the invention includes that low-temperature liquefaction and rectifying separate two parts；Low-temperature liquefaction includes hydrogen, the richness of nitrogen
Methane gas initially enter ice chest, and providing cold by azeotrope liquefies methane component in ice chest；Rectifying is separated to be included：Liquefaction
Hydrogen afterwards, the high methane gas of nitrogen are directly entered single tower distillation tower rectifying, removing hydrogen, nitrogen and a small amount of carbon monoxide；
Rectifying column top obtains the gaseous mixture of hydrogen, nitrogen and a small amount of carbon monoxide, and the hydrogen, nitrogen, carbon mono oxide mixture are through cold
Case reclaims cooling box system after cold；The liquid phase of rectifier bottoms being returned after be subcooled in ice chest and goes out system, obtain hydrogen content≤
500ppm, nitrogen content≤2%, the liquefied natural gas product of carbon monoxide≤2%.
Low-temperature liquefaction is completed in ice chest X1, and the cold of ice chest and the heat of rectifying tower bottom reboiler are compressed by mixed working fluid
System is provided or mainly provided by mixed working fluid compressibility.Referring to the drawings 3, the mixed working fluid being made up of C1~C5 and N2 passes through
After rational proportion（N2:5mol%~25mol%, preferably 10mol~15mol%, C1:10mol%~25mol%, preferably 15mol%~
20mol, C2:30mol%~55mol%, preferably 35mol%~45mol%, C3:10mol%~25mol%, preferably 15mol%~
20mol%, C5:10mol%~25mol%, preferably 15mol%~20mol%, the total mole number based on all gas）Into compressor
The entrance of C1,0.6~1.8MPaA is compressed to through first paragraph, and 30 DEG C~40 DEG C are cooled into first order cooler E3, is entered back into
First order gas-liquid separator V2 carries out gas-liquid separation, and the gas that first order gas-liquid separator V2 is isolated at top goes successively to compression
The second segment entrance of machine, 1.2~5.4MPaA is compressed to through two sections, and first order gas-liquid separator V2 bottom liquid phases end is isolated
After liquid converges after being pressurizeed through liquid pump P1 with the hot gas of second segment compression outlet pipeline, in entering back into second-stage cooler E4
30 DEG C~40 DEG C are cooled to, the mixed working fluid after cooling subsequently enters second level gas-liquid separator V3 and carries out gas-liquid separation, the
The first heat exchanger channels that the liquid that two grades of gas-liquid separator V3 bottoms are isolated enters ice chest X1 participate in heat exchange, second level gas-liquid point
The second heat exchanger channels for subsequently entering ice chest X1 from the top gas of device V3 participate in heat exchange.
The liquid drawn from the second level gas-liquid separator V3 bottoms of mixed working fluid compressibility initially enters ice chest X1's
First heat exchanger channels, are cooled to about -10 DEG C~-80 DEG C in advance wherein, preferably -20 DEG C~-60 DEG C, preferably -30 DEG C~-50 DEG C,
Throttle to 0.2~0.8MPaA through first throttle valve V-1, after preferably 0.4~0.6MPaA with returned by second throttle V-2
Mixed working fluid stream stock converges and is redirected back into third level heat exchanger channels for ice chest X1 provides cold and then returnes to the first compression
Section；The second heat exchanger channels that the gas phase stream stock of the mixed working fluid isolated by second level gas-liquid separator V3 tops passes through ice chest X1
It is cooled to uniform temperature（General extremely -75 DEG C~-130 DEG C scopes, preferably -90 DEG C~-110 DEG C scopes）Cooling box X1, enters afterwards
The tower bottom reboiler E1 of rectifying column T1 provides heat for rectifying column T1, goes out the stream stock of tower bottom reboiler E1（Own temperature is reduced to-
80 DEG C~-133 DEG C）Return to the heat exchanger channels of ice chest X1 the 8th and continue cool to -140 DEG C~-165 DEG C, preferably -150 DEG C~-160
DEG C, then throttled to 0.2~0.8MPaA through second throttle V-2, the 3rd of ice chest X1 the is redirected back into after preferably 0.4~0.6MPaA
Heat exchanger channels provide cold for ice chest X1.
Referring to accompanying drawing 3, illustrate that rectifying separation process is as follows：
After high methane gas is cooled to -140 DEG C~-165 DEG C through ice chest X1 first, the choke valve V- of stream stock-traders' know-how one of cooling box X1
3 expenditure and pressures to 0.6~3.5MPaA, preferably 0.8~3.0MPaA scopes enter essence after more preferably 1.5~2.5MPaA scopes
Evaporate rectifying in tower T1（Operating pressure in 0.6~3.5MPaA scopes, preferably 0.8~3.0MPaA scopes, more preferably 1.5~
2.5MPaA scopes）；The bottom liquid phases of rectifying column T1 are returned in the heat exchanger channels of ice chest the 9th, continue to be cooled to -140 DEG C~-165
Drawn as liquefied natural gas product after DEG C, obtain LNG product.Gained LNG product hydrogen content≤500ppm, nitrogen content≤
2%, carbon monoxide≤2%.
From the gas phase of the Base top contact of rectifying column T1（Overhead gas are hydrogen, nitrogen, carbon mono oxide mixture）It is cold into tower top
In condenser E2, through liquid nitrogen condensation, subsequently into gas-liquid separation in point flow container V1, a point flow container V1 tops obtain hydrogen, nitrogen, carbon monoxide
Gaseous mixture, a point flow container V1 bottom liquid phases pass back into tower；Rectifying column T1 bottom of towe obtains LNG product, is then back to be carried out in ice chest X1
Cooling box system after supercooling operation, obtains LNG product.
It is preferred that, the overhead condenser E2 of rectifying column provides cold using liquid nitrogen, from system outside gas nitrogen pass through ice chest X1
Liquefaction produces liquid nitrogen, and the overhead condenser E2 that rectifying column T1 is entered after being throttled through choke valve V-4 comes cooling tower top gaseous stream, liquid
Go out condenser E2 after nitrogen, cooling box after reclaiming cold through ice chest X1.
Claims (9)
1. a kind of high methane gas rectifying dehydrogenation nitrogen and the technique of liquefied natural gas is produced, the technique includes low-temperature liquefaction and rectifying point
From two parts；Low-temperature liquefaction includes that hydrogen, the high methane gas of nitrogen initially enter ice chest, and cold is provided cold by azeotrope
Methane component is liquefied in case；Rectifying is separated to be included：The high methane gas of hydrogen, nitrogen after liquefaction is directly entered single tower distillation
Tower rectifying, removing hydrogen, nitrogen and a small amount of carbon monoxide；Rectifying column top obtains the mixed of hydrogen, nitrogen and a small amount of carbon monoxide
Close gas, the hydrogen, nitrogen, carbon mono oxide mixture the cooling box system after ice chest recovery cold；The liquid phase of rectifier bottoms is returned
Return after being subcooled in ice chest and go out system, obtain hydrogen content≤500ppm, nitrogen content≤2%, the liquefaction of carbon monoxide≤2% is natural
Gas product, wherein single tower distillation flow provide thermal source using mix refrigerant；
Wherein, in low-temperature liquefaction part, the cold of ice chest and the heat of rectifying tower bottom reboiler are by mixed working fluid compressibility
There is provided or mainly provided by mixed working fluid compressibility；The mixed working fluid being made up of C1~C5 and N2 is by after rational proportion, entering
Enter the entrance of compressor, 0.6~1.8MPaA is compressed to through first paragraph, 30 DEG C~40 DEG C are cooled into first order cooler, then
Gas-liquid separation is carried out into first order gas-liquid separator, the gas that first order gas-liquid separator top is isolated goes successively to compression
The second segment entrance of machine, 1.2~5.4MPaA, the liquid that first order gas-liquid separator bottom liquid phases end is isolated are compressed to through two sections
After body converges after being pressurizeed through liquid pump with the hot gas of second segment compression outlet pipeline, enter back into second-stage cooler and be cooled
To 30 DEG C~40 DEG C, the mixed working fluid after cooling subsequently enters second level gas-liquid separator and carries out gas-liquid separation, second level gas-liquid
The first heat exchanger channels that the liquid that separator bottom is isolated enters ice chest participate in heat exchange, the top gas of second level gas-liquid separator
The second heat exchanger channels that body subsequently enters ice chest participate in heat exchange；
The liquid drawn from the second level gas-liquid separator bottom of mixed working fluid compressibility initially enters the first heat exchange of ice chest
Passage, is cooled to -10 DEG C~-80 DEG C in advance wherein, throttled to 0.2~0.8MPaA through first throttle valve with by second section
The mixed working fluid stream stock that stream valve is returned converges and is redirected back into third level heat exchanger channels for ice chest provides cold and then returnes to
First compression section；The second heat exchange that the gas phase stream stock of the mixed working fluid isolated by second level gas-liquid separator top passes through ice chest
Passage is cooled to cooling box after -75 DEG C~-130 DEG C scopes, and the tower bottom reboiler into rectifying column provides heat for rectifying column, goes out
The stream stock own temperature of tower bottom reboiler is reduced to -80 DEG C~-133 DEG C, returns to ice chest and continues cool to -140 DEG C~-165 DEG C,
Threeth heat exchanger channels that are redirected back into ice chest are throttled to 0.2~0.8MPaA through second throttle again for ice chest provides cold.
2. technique according to claim 1, it is characterised in that：Wherein in the distillation process of rectifying column, rectifying column top
Gas phase enters point liquid in point flow container in overhead condenser after liquid nitrogen condensation, and a point flow container top obtains hydrogen, nitrogen, an oxidation
The gaseous mixture of carbon, a point flow container bottom liquid phases pass back into tower, and rectifying column bottom liquid phase carries out cooling box after supercooling operation in returning to ice chest
System, obtains liquefied natural gas product.
3. technique according to claim 1 and 2, wherein crosses in the liquid phase return ice chest of rectifier bottoms and is cooled to -140 DEG C
Go out system after to -165 DEG C, obtained as liquefied natural gas product.
4. technique according to claim 1 and 2, the wherein overhead condenser of rectifying column provide cold using liquid nitrogen, come from
Nitrogen outside system is liquefied by ice chest and produces liquid nitrogen, and the overhead condenser that rectifying column is entered after being throttled through choke valve carrys out cooling tower
Top gaseous stream, leaves overhead condenser and the cooling box system after ice chest recovery cold after liquid nitrogen gasification.
5. technique according to claim 3, the wherein overhead condenser of rectifying column provide cold using liquid nitrogen, from system
Outer nitrogen is liquefied by ice chest and produces liquid nitrogen, and the overhead condenser that rectifying column is entered after being throttled through choke valve carrys out cooling tower top gas
Phase logistics, leaves overhead condenser and the cooling box system after ice chest recovery cold after liquid nitrogen gasification.
6. technique according to claim 1, it is characterised in that：The distillation process uses a rectifying column, rectifying column bag
Include the reboiler of bottom of towe, the condenser of tower top and point flow container.
7. technique according to claim 1, wherein, the mixed working fluid being made up of C1~C5 and N2 by after rational proportion,
So that the total mole number based on all gas, N2:5 mol%~25mol%, C1:10mol %~25mol%, C2:30mol %~
55 mol%, C3:10mol%~25mol%, C5:10mol%~25mol%.
8. a kind of high methane gas rectifying dehydrogenation nitrogen and the device of liquefied natural gas is produced, the device includes：Ice chest, four throttling dresses
Put and rectifying column, the rectifying column includes reboiler, the condenser of tower top and point flow container of bottom of towe,
Wherein, the ice chest includes：
Liquid phase azeotrope entrance, it is connected with the first heat exchanger channels of ice chest, and first heat exchanger channels are from the heat exchange in ice chest
A pipeline is drawn in the end of one specific level of device, via first throttle valve, into ice chest and the 3rd heat exchanger channels of ice chest
Connection,
Gas phase cryogen entrance, it is connected with the second heat exchanger channels of ice chest, another spy of second heat exchanger channels from heat exchanger
A pipeline is drawn in the end of deciding grade and level, is connected to the arrival end of rectifying tower bottom reboiler, and the port of export of rectifying tower bottom reboiler is returned
Ice chest is returned, a pipeline is drawn in the end of another specific level from ice chest, via second throttle, the 3rd heat exchange with ice chest is logical
The arrival end connection in road, the port of export of the 3rd heat exchanger channels is azeotrope outlet,
The high methane gas import and a methane rich mixed flow stock outlet being connected with the 4th heat exchanger channels of ice chest, this is the richest in
The stock outlet of alkane mixed flow is connected via the 3rd choke valve with rectifying column centre entrance,
With the gentle nitrogen outlet of the gas nitrogen entrance that the 5th heat exchanger channels of ice chest are connected, a gas nitrogen outlet piece pipeline of extraction is via the 4th
Choke valve is connected with the liquid nitrogen entrance of rectifying column tower top condenser,
The gas nitrogen being connected with the 6th heat exchanger channels of ice chest exports gentle nitrogen entrance, the gas nitrogen entrance and rectifying column evaporator overhead condenser
Gas nitrogen outlet connection,
The hydrogen nitrogen mixed gas outlet being connected with the 7th heat exchanger channels of ice chest and hydrogen nitrogen mixed gas entrance,
Rectifying column top introduction pipe connection overhead condenser, overhead condenser outlet is connected with the entrance of point flow container, point flow container
Bottom liquid phases outlet is drawn return duct and is connected with rectifier, and point flow container top gas phase outlet introduction pipe and the 7th heat exchange are logical
The hydrogen nitrogen mixed gas entrance connection in road,
The port of export of rectifier bottoms liquid phase returns to ice chest, and the another specific level end introduction pipe connection liquefaction from ice chest is natural
Gas storage tank.
9. device according to claim 8, it is characterised in that the cold of ice chest and the heat of rectifying tower bottom reboiler are by mixing
Close working medium compression system to provide or mainly provided by mixed working fluid compressibility, the mixed working fluid compressibility includes two-period form
Mixed working fluid compressor, the first order being connected with the first paragraph and second segment of the two-period form mixed working fluid compressor respectively cooling
Device and second-stage cooler, the first order gas-liquid separator being connected with the first order cooler and second-stage cooler respectively and
Second level gas-liquid separator and a liquid pump being connected with first order gas-liquid separator,
The liquid phase end and gas phase end of the second level gas-liquid separator in the mixed working fluid compressibility are changed with described first respectively
The arrival end of the arrival end of the passage of heat and the second heat exchanger channels is connected via two pipelines, the port of export of the 3rd heat exchanger channels via
Pipeline is connected to the cryogen access road of the first compression section；
The of the gas phase end of the first order gas-liquid separator in wherein two gas-liquid separators and two-period form mixed working fluid compressor
Two compression sections connect, and the liquid phase end of first order gas-liquid separator connects after converging with the outlet conduit of the second compression section via liquid pump
It is connected to the second-stage cooler in two coolers.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310461438.5A CN104513680B (en) | 2013-09-30 | 2013-09-30 | Technology and device for removing hydrogen and nitrogen from methane-rich gas through rectification and producing liquefied natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310461438.5A CN104513680B (en) | 2013-09-30 | 2013-09-30 | Technology and device for removing hydrogen and nitrogen from methane-rich gas through rectification and producing liquefied natural gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104513680A CN104513680A (en) | 2015-04-15 |
| CN104513680B true CN104513680B (en) | 2017-05-24 |
Family
ID=52789553
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310461438.5A Active CN104513680B (en) | 2013-09-30 | 2013-09-30 | Technology and device for removing hydrogen and nitrogen from methane-rich gas through rectification and producing liquefied natural gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104513680B (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105482861A (en) * | 2015-11-19 | 2016-04-13 | 辽宁中集哈深冷气体液化设备有限公司 | Method for preparing LNG by utilizing low-pressure tower refluxing liquid as high-pressure tower washing liquid |
| CN106979665B (en) * | 2017-04-13 | 2023-03-24 | 成都赛普瑞兴科技有限公司 | Method and equipment for purifying synthetic gas |
| CN107024074B (en) * | 2017-05-19 | 2022-08-16 | 河南开元空分集团有限公司 | Device and method for preparing LNG (liquefied Natural gas) by recovering methane in methanol synthesis tail gas through nitrogen single-stage expansion refrigeration |
| US10976103B2 (en) * | 2017-12-15 | 2021-04-13 | Saudi Arabian Oil Company | Process integration for natural gas liquid recovery |
| CN110195962A (en) * | 2019-06-05 | 2019-09-03 | 杭州凯德空分设备有限公司 | Rubbish landfill gas, biogas or chemical industry tail gas extract high-purity carbon dioxide process equipment |
| RU2720813C1 (en) * | 2019-12-10 | 2020-05-13 | Игорь Анатольевич Мнушкин | Gas processing cluster |
| CN115371355B (en) * | 2022-08-16 | 2023-10-20 | 中海石油气电集团有限责任公司 | Natural gas liquefaction system and method suitable for standard modularization |
| CN115790076B (en) * | 2023-02-08 | 2023-05-23 | 杭氧集团股份有限公司 | Device and method for recycling carbon dioxide and nitrogen in flue gas |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1293232A (en) * | 1999-10-15 | 2001-05-02 | 余庆发 | Process for preparing liquefied natural gas |
| CN103033025A (en) * | 2011-09-30 | 2013-04-10 | 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 |
| CN203513622U (en) * | 2013-09-30 | 2014-04-02 | 新地能源工程技术有限公司 | Device for removing hydrogen and nitrogen from methane-rich gas by rectifying and producing liquefied natural gas (LNG) |
-
2013
- 2013-09-30 CN CN201310461438.5A patent/CN104513680B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1293232A (en) * | 1999-10-15 | 2001-05-02 | 余庆发 | Process for preparing liquefied natural gas |
| CN103033025A (en) * | 2011-09-30 | 2013-04-10 | 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 |
| CN203513622U (en) * | 2013-09-30 | 2014-04-02 | 新地能源工程技术有限公司 | Device for removing hydrogen and nitrogen from methane-rich gas by rectifying and producing liquefied natural gas (LNG) |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104513680A (en) | 2015-04-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104513680B (en) | Technology and device for removing hydrogen and nitrogen from methane-rich gas through rectification and producing liquefied natural gas | |
| CN104061757B (en) | A kind of liquid oxygen and liquid nitrogen device for making and method | |
| CN107560319B (en) | A kind of natural gas ethane recovery device and method using cascade refrigeration | |
| CN103697659B (en) | The device and method of liquefied natural gas and rich hydrogen production is produced from high methane gas | |
| RU2668303C1 (en) | System and method for liquefying of natural gas (options) | |
| CN107228526B (en) | Helium extraction, denitrification and reliquefaction device for LNG flash gas | |
| CN105486034B (en) | A kind of natural gas liquefaction and lighter hydrocarbons isolation integral integrated technique system and technique | |
| US20080016909A1 (en) | Flexible hydrocarbon gas separation process and apparatus | |
| CN110470102B (en) | Modular LNG separator and flash gas heat exchanger | |
| WO2013135037A1 (en) | Apparatus and method for liquefying natural gas by refrigerating single mixed working medium | |
| CN102620521B (en) | Technology and device for removing hydrogen and nitrogen from methane rich gas and producing liquefied natural gas | |
| CN101392983B (en) | Process for liquefying high methane gas | |
| CN203513622U (en) | Device for removing hydrogen and nitrogen from methane-rich gas by rectifying and producing liquefied natural gas (LNG) | |
| CN102374754A (en) | Equipment and method for preparing liquid natural gas and carbon oxide from coke oven gas | |
| US20040069015A1 (en) | Method for ethane recovery, using a refrigeration cycle with a mixture of at least two coolants, gases obtained by said method, and installation therefor | |
| CN202297535U (en) | Device for removing hydrogen, nitrogen and carbon monoxide from high methane gas and producing liquefied natural gas | |
| CN113959176B (en) | System and method for separating helium from liquefied natural gas flash gas | |
| CN205747680U (en) | A kind of natural gas liquefaction and lighter hydrocarbons isolation integral integrated technique system | |
| CN105066586B (en) | Device for preparing raw material gas for synthetic ammonia and L NG by liquid nitrogen washing and preparation method thereof | |
| RU2580453C1 (en) | Method of processing natural hydrocarbon gas | |
| CN203949440U (en) | A kind of system of two-stage pre-cooling type azeotrope refrigeration liquefying natural gas | |
| CN104019626B (en) | The cold method and device preparing liquefied natural gas of a kind of azeotrope two-stage system | |
| CN103697660B (en) | The device and method of LNG and rich hydrogen production is produced from high methane gas | |
| CN202924980U (en) | Natural gas liquefaction and heavy hydrocarbon treatment device | |
| CN114777418B (en) | System for extracting helium from natural gas BOG by condensation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |