CN202116524U - Device for producing liquefied natural gas by coke oven gas through low-temperature rectification - Google Patents
Device for producing liquefied natural gas by coke oven gas through low-temperature rectification Download PDFInfo
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Abstract
The utility model relates to a device for producing liquefied natural gas by coke oven gas through low-temperature rectification, which comprises a first heat exchange device, a second heat exchange device and a set of rectifying tower, wherein heat exchange and throttling are carried out on the methanation mixture obtained through a coke oven gas methanation reaction device, then the processed methanation mixture directly goes into the rectifying tower to be rectified, and normal-pressure liquefied natural gas (LNG) with purity being higher than 99.5% can be directly obtained. In the utility model, the LNG can be directly produced through low-temperature rectification without reliquefaction, so that the energy consumption can be lowered, and the recovery rate of the methane is 99%; by adopting the utility model, the LNG with the normal pressure or a certain pressure grade can be produced; moreover, nitrogen is used for pressurization and expansion and step refrigeration and can be recycled, thereby further lowering the energy consumption.
Description
Technical field
The utility model relates to and belongs to environmental improvement and Energy production field, relates in particular to industrial gaseous waste and prepares the natural gas liquids technical field, and particularly a kind of coke-oven gas low temperature fractionation is produced the device of natural gas liquids.
Background technology
Coke-oven gas is the by product of process of coking, and the coke(oven)gas of the annual discharging of China's coal chemical enterprise is about 600 billion cubic meters, and it forms more complicated, and staple comprises: H
2, CH
4, CO
2, CO, N
2, O
2, H
2O and other hydro carbons and sulfide etc., coke-oven gas is taken off water, heavy hydrocarbon and trace impurity through pre-treatment usually, gets into the methanation cell processing, mainly obtains CH
4, H
2And N
2, wherein methane accounts for about 60% of mixed gas, and the preparation natural gas liquids need be isolated the methane gas of greater concn, final liquefaction, preparation natural gas liquids.
The methane separation technology (mainly is CH after the methanation at present
4, H
2And N
2) have membrane sepn, transformation to adsorb and low temperature fractionation.Simple to operate, the less energy consumption of membrane separation technique, but separating effect is poor, and pressure swing adsorption process is difficult to separation of C H
4And N
2, and investment cost is high, and the low temperature fractionation technology can direct separation go out highly purified methane.
Natural gas liquids (LNG) is the fastest-rising a kind of energy in the world today, and the production of natural gas liquids is in order to solve natural gas transportation and storage problem.Usually to be stored in temperature be that 112K, pressure are in the low temperature storage tank about 0.1MPa to natural gas liquids more, and its density is more than 600 times of methane under the standard state, and the volume energy force density is 72% of a gasoline, very helps transportation and storage.Natural gas liquids also is widely used on the natural gas peak-shaving device.Because the natural gas liquids critical temperature is low; Can't only depend on pressurization that it is liquefied; The natural gas liquefaction technology mainly is selection and the technical process configuration of heat-eliminating medium, and by the technical process branch: single mixed refrigeration process flow process and two formula refrigeration techniques flow processs that change are again arranged, and nitrogen expansion refrigeration cycle flow process is simple; Number of devices is few, and the plant area area is little; Propane/mixed refrigeration process flow process, technology are complicated, and number of devices is many, and the plant area area is bigger.
At present domestic have the coke-oven gas of Southwest Chemical Research and Design Institute application to prepare natural gas liquids patented technology (CN101709238A); It mainly comprises methanation reaction, rectifying separation and liquefaction step; This patented claim adopts first rectifying separation to go out highly purified methane gas; Liquefaction again, its conventional distillation methane recovery is merely 91.4%, also has only 97.1% and vacuumize the rectifying methane recovery.Methane belongs to the Class A Hazardous substances; Methane gas vacuumize not only equipment itself is required high, in case and methane vacuumizes leakage, very easily cause explosion hazard; Methane compression, throttling refrigeration are adopted in this patent liquefaction; The compressor anti-hazard classification is required high, and liquefaction process also needs extraneous a part of cold that replenishes, and could arrive the effect that liquefies.And do not see report as yet about coke-oven gas prepares the natural gas liquids technology abroad.
Therefore, prepare the technical process and the method that improves the natural gas liquids recovery that natural gas liquids just need provide safe and reliable long-term operation with coke-oven gas.
The utility model content
The utility model technical problem to be solved is to prepare the existing problem of natural gas liquids and provide a kind of with direct production natural gas liquids the mixture of low temperature fractionation behind gas employing methanation of coke oven to coke-oven gas; Need not to liquefy again; Produce the device of natural gas liquids through the coke-oven gas low temperature fractionation of cooling off, reduce pressure the natural gas liquids that can obtain different pressures; This device also can be produced natural gas liquids from contain methane, nitrogen and hydrogen mixed gas, and can effectively improve the recovery of methane, expands through adopting nitrogen supercharging; The properly distributed swell increment can effectively reduce the nitrogen circulation amount, reduces process energy consumption.
The utility model technical problem to be solved can realize through following technical scheme:
A kind of coke-oven gas low temperature fractionation is produced the device of natural gas liquids; Comprise at least one first heat-exchanger rig and one second heat-exchanger rig and a cover rectifying tower; Said first heat-exchanger rig is provided with first nitrogen inlet, first nitrogen outlet, first methane mixture inlet and the outlet of first methane mixture; Second heat-exchanger rig is provided with second nitrogen inlet, second nitrogen outlet, second methane mixture inlet, the outlet of second methane mixture, second natural gas liquids inlet and the outlet of second natural gas liquids; Be provided with the outlet of the tower bottom reboiler and first natural gas liquids at the bottom of the tower of said rectifying tower; The rectifying tower middle part is provided with inlet, and the rectifying tower top is provided with Waste gas outlet; First nitrogen inlet on said first heat-exchanger rig connects nitrogen through pipeline; First nitrogen outlet on first heat-exchanger rig connects second nitrogen inlet on said second heat-exchanger rig through pipeline, and second nitrogen outlet on said second heat-exchanger rig is discharged the nitrogen after the heat exchange; First methane mixture inlet on said first heat-exchanger rig connects the methane mixture outlet of methanation device; First methane mixture outlet on first heat-exchanger rig is connected through pipeline with the inlet of said tower bottom reboiler; The outlet of said tower bottom reboiler enters the mouth through second methane mixture on pipeline and said second heat-exchanger rig and is connected; Second methane mixture outlet on second heat-exchanger rig is connected with the inlet at said rectifying tower middle part through pipeline and first throttle valve; The outlet of first natural gas liquids at the bottom of the said rectifying Tata enters the mouth through the pipeline and second natural gas liquids on said second heat-exchanger rig and is connected; Second natural gas liquids outlet on second heat-exchanger rig is connected with natural gas liquids low temperature storage tank through pipeline and reducing valve, through the Waste gas outlet discharging of the waste gas after the rectifying tower rectifying by the rectifying tower top.
Another kind of coke-oven gas low temperature fractionation is produced the device of natural gas liquids; Comprise at least one first heat-exchanger rig and one second heat-exchanger rig, a cover rectifying tower and a cover tripping device; Said first heat-exchanger rig is provided with first nitrogen inlet, first nitrogen outlet, first methane mixture inlet and the outlet of first methane mixture; Second heat-exchanger rig is provided with second nitrogen inlet, second nitrogen outlet, second methane mixture inlet, the outlet of second methane mixture, second natural gas liquids inlet and the outlet of second natural gas liquids; Be provided with the outlet of the tower bottom reboiler and first natural gas liquids at the bottom of the tower of said rectifying tower; The rectifying tower middle part is provided with liquid inlet and gas inlet, and the rectifying tower top is provided with Waste gas outlet; Said tripping device comprises a separating tank and a gas expander, and the top of said separating tank is provided with pneumatic outlet, and the bottom of separating tank is provided with liquid exit, and the middle part of separating tank is provided with material inlet; First nitrogen inlet on said first heat-exchanger rig connects nitrogen through pipeline; First nitrogen outlet on first heat-exchanger rig connects second nitrogen inlet on said second heat-exchanger rig through pipeline, and second nitrogen outlet on said second heat-exchanger rig is discharged the nitrogen after the heat exchange; First methane mixture inlet on said first heat-exchanger rig connects the methane mixture outlet of methanation device; The outlet of first methane mixture on first heat-exchanger rig enters the mouth through the pipeline and second methane mixture on said second heat-exchanger rig and is connected; Second methane mixture outlet on second heat-exchanger rig is connected with the inlet of said tower bottom reboiler through pipeline; The outlet of tower bottom reboiler is connected through the material inlet of pipeline with said separating tank middle part; The liquid exit of separating tank bottom is connected with the liquid inlet at said rectifying tower middle part through pipeline and first throttle valve; The pneumatic outlet at separating tank top is connected with the inlet of gas expander through pipeline, and the outlet of gas expander is connected through the gas inlet of pipeline with said rectifying tower middle part; The outlet of first natural gas liquids at the bottom of the said rectifying Tata enters the mouth through the pipeline and second natural gas liquids on said second heat-exchanger rig and is connected; Second natural gas liquids outlet on second heat-exchanger rig is connected with natural gas liquids low temperature storage tank through pipeline and reducing valve, through the Waste gas outlet discharging of the waste gas after the rectifying tower rectifying by the rectifying tower top.
In the described device of the utility model; The first nitrogen supercharging machine, the second nitrogen supercharging machine and the 3rd heat-exchanger rig that also comprise parallel running; And said first heat-exchanger rig is provided with first nitrogen reflux inlet and the outlet of first nitrogen reflux; Said the 21 heat-exchanger rig is provided with second nitrogen reflux inlet and exports with second nitrogen reflux, is provided with condenser/evaporator at the cat head of said rectifying tower; The said first nitrogen supercharging machine is driven by the first nitrogen expansion machine; The second nitrogen supercharging machine is driven by the second nitrogen expansion machine; Inlet on first, second nitrogen supercharging machine connects nitrogen; Outlet on first, second nitrogen supercharging machine connects the inlet of the 3rd heat-exchanger rig through pipeline; The outlet of the 3rd heat-exchanger rig connects first nitrogen inlet of first heat-exchanger rig through pipeline, and the pipeline that is connected on first nitrogen inlet of first heat-exchanger rig is connected with the inlet of the said first nitrogen expansion machine through first arm, and the outlet of the first nitrogen expansion machine is passed through second arm and entered the mouth with first nitrogen reflux on first heat-exchanger rig and be connected; The pipeline that is connected on second nitrogen inlet of second heat-exchanger rig is connected with the inlet of the said second nitrogen expansion machine through the 3rd arm, and the outlet of the second nitrogen expansion machine is passed through the 4th arm and entered the mouth with second nitrogen reflux on second heat-exchanger rig and be connected; The outlet of second nitrogen reflux on second heat-exchanger rig enters the mouth through the pipeline and first nitrogen reflux on first heat-exchanger rig and is connected; Second nitrogen outlet on said second heat-exchanger rig is connected with the inlet of said condenser/evaporator through pipeline and throttling valve, and the outlet of condenser/evaporator is passed through pipeline and entered the mouth with second nitrogen reflux on said second heat-exchanger rig and be connected.
In the said device of the utility model; Also comprise a compressor and the 4th heat-exchanger rig; First nitrogen reflux outlet on said first heat-exchanger rig connects the inlet of said compressor through pipeline; The outlet of said compressor connects the inlet of the 4th heat-exchanger rig, and the outlet of the 4th heat-exchanger rig is connected with inlet on said first, second nitrogen supercharging machine through pipeline.
In the described device of the utility model; Said first heat-exchanger rig is provided with first exhaust gas entrance, first waste gas outlet; Said second heat-exchanger rig is provided with second exhaust gas entrance, second waste gas outlet; The Waste gas outlet at said rectifying tower top is connected with second exhaust gas entrance on said second heat-exchanger rig through pipeline; Second waste gas outlet on second heat-exchanger rig is connected with first exhaust gas entrance on said first heat-exchanger rig through pipeline, and first waste gas outlet that is provided with on first heat-exchanger rig connects factory's combustion gas.
Said first heat-exchanger rig and second heat-exchanger rig are plate-fin heat exchanger.
Owing to adopted technical scheme as above, the utility model need not to liquefy through low temperature fractionation direct production natural gas liquids again, and capable of reducing energy consumption, methane recovery is 99%; The utility model can be produced the natural gas liquids of normal pressure or certain pressure grade; Adopt nitrogen supercharging expansion, ladder refrigeration, recycle has further reduced energy consumption.
Description of drawings
Fig. 1 is the schematic flow sheet that the coke-oven gas low temperature fractionation of the utility model embodiment 1 and 2 is produced the device of natural gas liquids.
Fig. 2 is the schematic flow sheet that the coke-oven gas low temperature fractionation of the utility model embodiment 3 is produced the device of natural gas liquids.
Embodiment
For the technique means, the creation characteristic that make the utility model, reach purpose and effect and be easy to understand and understand, further set forth the utility model in conjunction with embodiment.
Embodiment 1
Referring to Fig. 1; Coke-oven gas low temperature fractionation shown in the figure is produced the device of natural gas liquids; Comprise that two nitrogen supercharging machine ZP01, ZP02, two nitrogen expansion machine X01, X02, two interchanger E03, E04, two platen fin heat exchanger E01, E02, compressor P01 and overlap rectifying tower T01; Plate-fin heat exchanger E01 is provided with nitrogen inlet 011, nitrogen outlet 012, methane mixture inlet 013, methane mixture outlet 014, nitrogen reflux inlet 015, nitrogen reflux gangway 016, exhaust gas entrance 017, waste gas outlet 018; Plate-fin heat exchanger E02 is provided with nitrogen inlet 021, nitrogen outlet 022, methane mixture inlet 023, methane mixture outlet 024, nitrogen reflux inlet 025, nitrogen reflux outlet 026, exhaust gas entrance 027, waste gas outlet 028, natural gas liquids inlet 029 and natural gas liquids outlet 029a; Be provided with tower bottom reboiler T011 and natural gas liquids outlet T012 at the bottom of the tower of rectifying tower T01; The middle part is provided with inlet T013, and the rectifying tower top is provided with Waste gas outlet T014 and condenser/evaporator T015.
The outlet of nitrogen supercharging machine ZP01, ZP02 connects the inlet of interchanger E03 after through pipeline 11,12 parallel connections again through pipeline 10; The outlet of interchanger E03 is through the nitrogen inlet 011 on the pipeline 13 fishplate bar fin heat exchanger E01; Pipeline 13 is told the inlet that an arm 14 meets nitrogen expansion machine X01 simultaneously, and nitrogen expansion machine X01 drives nitrogen supercharging machine ZP01.Nitrogen outlet 012 on the plate-fin heat exchanger E01 is through the nitrogen inlet 021 on the pipeline 15 fishplate bar fin heat exchanger E02, and pipeline 15 is told the inlet that an arm 16 meets nitrogen expansion machine X02 simultaneously, and nitrogen expansion machine X02 drives nitrogen supercharging machine ZP01.
Nitrogen outlet 022 on the plate-fin heat exchanger E02 connects the inlet of condenser/evaporator T015 through pipeline 17 and throttling valve 17a; The outlet of condenser/evaporator T015 is through the nitrogen reflux inlet 025 of pipeline 18 fishplate bar fin heat exchanger E02, and the outlet of nitrogen expansion machine X02 is taken over line 18 through arm 19.The nitrogen reflux outlet 026 of plate-fin heat exchanger E02 is through the nitrogen reflux inlet 015 of pipeline 20 fishplate bar fin heat exchanger E01, and the outlet of nitrogen expansion machine X01 is taken over line 20 through arm 19a.The outlet 016 of the nitrogen reflux of plate-fin heat exchanger E01 connects the inlet of compressor P01 through pipeline 21, and the outlet of compressor P01 connects the inlet of interchanger E04 through pipeline 22, and the outlet of interchanger E04 connects the inlet of nitrogen supercharging machine ZP01, ZP02 through pipeline 23.
The methane mixture COG that is come by methanation device is through the methane mixture inlet 013 of pipeline 24 fishplate bar fin heat exchanger E01; Methane mixture outlet 014 connects the inlet of tower bottom reboiler T011 through pipeline 25; The outlet of tower bottom reboiler T011 is through the methane mixture inlet 023 of pipeline 26 fishplate bar fin heat exchanger E02; The methane mixture outlet 024 of plate-fin heat exchanger E02 meets the inlet T013 at rectifying tower T01 middle part through pipeline 27 and throttling valve 28; The natural gas liquids outlet T012 of rectifying tower T01 bottom is through the inlet of the natural gas liquids on the pipeline 29 fishplate bar fin heat exchanger E02 029, and the natural gas liquids outlet 029a on the plate-fin heat exchanger E02 connects natural gas liquids low temperature storage tank through pipeline 30 and reducing valve.
The Waste gas outlet T014 at rectifying tower T01 top is through the exhaust gas entrance 027 on the pipeline 31 fishplate bar fin heat exchanger E02; Waste gas outlet 028 on the plate-fin heat exchanger E02 is through the exhaust gas entrance 017 of pipeline 32 fishplate bar fin heat exchanger E01, and the waste gas outlet 018 of plate-fin heat exchanger E01 connects factory's combustion gas.
The methane mixture COG composition that the present embodiment methanation device is brought: CH4,63.76%, N2,7.65%, H2,28.59%, T=40 ℃, P=30bar
Through the nitrogen after two nitrogen supercharging machine ZP01, the ZP02 supercharging, before getting into plate-fin heat exchanger E01, divide two strands, one directly gets into plate-fin heat exchanger E01 through pipeline 13, and another strand directly gets into nitrogen expansion machine X01 through arm 14 and expands.Nitrogen through plate-fin heat exchanger E01 heat exchange; Divide two strands; One directly gets into plate-fin heat exchanger E02 through pipeline 15, and another strand gets into nitrogen expansion machine X02 through arm 16 and expand, and nitrogen expansion machine X01, X02 drive nitrogen supercharging machine ZP01, ZP02 respectively.
The nitrogen that comes out from plate-fin heat exchanger E02 gets into condenser/evaporator T015 through pipeline 17 and after passing through throttling valve 17a throttling to certain pressure; The nitrogen that comes out from condenser/evaporator T015 mixes with the nitrogen of bringing through arm 19 that expand into certain pressure through nitrogen expansion machine X02, sends among the plate-fin heat exchanger E02.Nitrogen after plate-fin heat exchanger E02 re-heat mixes with the nitrogen of bringing through arm 19a that expand into certain pressure through nitrogen expansion machine X01, sends into re-heat among the plate-fin heat exchanger E01.After plate-fin heat exchanger E01 re-heat, send into compressor P01 compression through pipeline 21, after the nitrogen after the compressor P01 compression is sent into interchanger E04 heat exchange through pipeline 22, again through pipeline 23 send into nitrogen supercharging machine ZP01, ZP02 recycles.
Methane mixture COG sends among the plate-fin heat exchanger E01 after plate-fin heat exchanger E01 heat exchange; Get into tower bottom reboiler T011 through pipeline 25 and carry out heat exchange; Methane mixture after plate-fin heat exchanger E01 heat exchange is as rectifying tower T01 reboiler thermal source; T01 provides heat for rectifying tower, further cools off self.Getting into plate-fin heat exchanger E02 through the cooled gas of tower bottom reboiler T011 through pipeline 26 further cools off; Cooled gas gets into rectifying tower T01 operation through pipeline 27 and through throttling valve 28 throttlings; That come out at the bottom of the tower of rectifying tower T01 is natural gas liquids LNG; Natural gas liquids is sent into plate-fin heat exchanger E02 through pipeline 29 at the bottom of the tower; Further cool off and be decompressed to 1.5bar through plate-fin heat exchanger E02, obtain purity and be 99.5%, pressure is the natural gas liquids of 1.5bar, input low temperature storage tank.Cat head comes out mainly is to contain H2 and the N2 gas mixture is sent among the plate-fin heat exchanger E02 through pipeline 31, after plate-fin heat exchanger E02 heat exchange, sends among the plate-fin heat exchanger E01 through pipeline 32 again, after plate-fin heat exchanger E01 heat exchange, send factory's combustion gas.
The methane recovery of the rectifying tower T01 of present embodiment is more than 99%, and the energy consumption of this explained hereafter natural gas liquids is 0.93KWh/Nm
3
Embodiment 2
The schema of whole device is referring to Fig. 1, the methane mixture COG composition that methanation device is brought among this embodiment: CH4,63.76%, N2,7.65%, H2,28.59%, T=40 ℃, P=30bar.
Through the nitrogen after two nitrogen supercharging machine ZP01, the ZP02 supercharging, before getting into plate-fin heat exchanger E01, divide two strands, one directly gets into plate-fin heat exchanger E01 through pipeline 13, and another strand directly gets into nitrogen expansion machine X01 through arm 14 and expands.Nitrogen through plate-fin heat exchanger E01 heat exchange; Divide two strands; One directly gets into plate-fin heat exchanger E02 through pipeline 15, and another strand gets into nitrogen expansion machine X02 through arm 16 and expand, and nitrogen expansion machine X01, X02 drive nitrogen supercharging machine ZP01, ZP02 respectively.
The nitrogen that comes out from plate-fin heat exchanger E02 gets into condenser/evaporator T015 through pipeline 17 and after passing through throttling valve 17a throttling to certain pressure; The nitrogen that comes out from condenser/evaporator T015 mixes with the nitrogen of bringing through arm 19 that expand into certain pressure through nitrogen expansion machine X02, sends among the plate-fin heat exchanger E02.Nitrogen after plate-fin heat exchanger E02 re-heat mixes with the nitrogen of bringing through arm 19a that expand into certain pressure through nitrogen expansion machine X01, sends into re-heat among the plate-fin heat exchanger E01.After plate-fin heat exchanger E01 re-heat, send into compressor P01 compression through pipeline 21, after the nitrogen after the compressor P01 compression is sent into interchanger E04 heat exchange through pipeline 22, again through pipeline 23 send into nitrogen supercharging machine ZP01, ZP02 recycles.
Methane mixture COG sends among the plate-fin heat exchanger E01 after plate-fin heat exchanger E01 heat exchange; Get into tower bottom reboiler T011 through pipeline 25 and carry out heat exchange; Methane mixture after plate-fin heat exchanger E01 heat exchange is as rectifying tower T01 reboiler thermal source; T01 provides heat for rectifying tower, further cools off self.Getting into plate-fin heat exchanger E02 through the cooled gas of tower bottom reboiler T011 through pipeline 26 further cools off; Cooled gas gets into rectifying tower T01 operation through pipeline 27 and through throttling valve 28 throttlings; That come out at the bottom of the tower of rectifying tower T01 is natural gas liquids LNG; Natural gas liquids is sent into plate-fin heat exchanger E02 through pipeline 29 at the bottom of the tower; Further cool off and be decompressed to 4bar through plate-fin heat exchanger E02, obtain purity and be 99.5%, pressure is the natural gas liquids of 4bar, input low temperature storage tank.Cat head comes out mainly is to contain H2 and the N2 gas mixture is sent among the plate-fin heat exchanger E02 through pipeline 31, after plate-fin heat exchanger E02 heat exchange, sends among the plate-fin heat exchanger E01 through pipeline 32 again, after plate-fin heat exchanger E01 heat exchange, send factory's combustion gas.
The methane recovery of the rectifying tower T01 of present embodiment is more than 99%, and the energy consumption of this explained hereafter natural gas liquids is 0.93KWh/Nm
3
Embodiment 3
Referring to Fig. 2; Coke-oven gas low temperature fractionation shown in the figure is produced the device of natural gas liquids; Comprise two nitrogen supercharging machine ZP01, ZP02, two nitrogen expansion machine X01, X02, two interchanger E03, E04, two platen fin heat exchanger E01, E02, a compressor P01, a cover separating tank T02, gas expander X03 and a cover rectifying tower T01, plate-fin heat exchanger E01 is provided with nitrogen inlet 011, nitrogen outlet 012, methane mixture inlet 013, methane mixture outlet 014, nitrogen reflux inlet 015, nitrogen reflux gangway 016, exhaust gas entrance 017, waste gas outlet 018.Plate-fin heat exchanger E02 is provided with nitrogen inlet 021, nitrogen outlet 022, methane mixture inlet 023, methane mixture outlet 024, nitrogen reflux inlet 025, nitrogen reflux gangway 026, exhaust gas entrance 027, waste gas outlet 028, natural gas liquids inlet 029 and natural gas liquids outlet 029a; Be provided with tower bottom reboiler T011 and natural gas liquids outlet T012 at the bottom of the tower of rectifying tower T01; The middle part is provided with liquid inlet T013 and gas inlet T016; The rectifying tower top is provided with Waste gas outlet T014 and condenser/evaporator T015; The top of separating tank T02 is provided with pneumatic outlet T021; The bottom is provided with liquid exit T022, and the middle part is provided with material inlet T023.
The outlet of nitrogen supercharging machine ZP01, ZP02 connects the inlet of interchanger E03 after through pipeline 11,12 parallel connections again through pipeline 10; The outlet of interchanger E03 is through the nitrogen inlet 011 on the pipeline 13 fishplate bar fin heat exchanger E01; Pipeline 13 is told the inlet that an arm 14 meets nitrogen expansion machine X01 simultaneously, and nitrogen expansion machine X01 drives nitrogen supercharging machine ZP01.Nitrogen outlet 012 on the plate-fin heat exchanger E01 is through the nitrogen inlet 021 on the pipeline 15 fishplate bar fin heat exchanger E02, and pipeline 15 is told the inlet that an arm 16 meets nitrogen expansion machine X02 simultaneously, and nitrogen expansion machine X02 drives nitrogen supercharging machine ZP01.
Nitrogen outlet 022 on the plate-fin heat exchanger E02 connects the inlet of condenser/evaporator T015 through pipeline 17 and throttling valve 17a; The outlet of condenser/evaporator T015 is through the nitrogen reflux inlet 025 of pipeline 18 fishplate bar fin heat exchanger E02, and the outlet of nitrogen expansion machine X02 is taken over line 18 through arm 19.The nitrogen reflux outlet 026 of plate-fin heat exchanger E02 is through the nitrogen reflux inlet 015 of pipeline 20 fishplate bar fin heat exchanger E01, and the outlet of nitrogen expansion machine X01 is taken over line 20 through arm 19a.The outlet 016 of the nitrogen reflux of plate-fin heat exchanger E01 connects the inlet of compressor P01 through pipeline 21, and the outlet of compressor P01 connects the inlet of interchanger E04 through pipeline 22, and the outlet of interchanger E04 connects the inlet of nitrogen supercharging machine ZP01, ZP02 through pipeline 23.
The methane mixture COG that is come by methanation device is through the methane mixture inlet 013 of pipeline 24 fishplate bar fin heat exchanger E01; Methane mixture outlet 014 is through the methane mixture inlet 023 of pipeline 25 fishplate bar fin heat exchanger E02; Methane mixture outlet 024 connects the inlet of tower bottom reboiler T011 through pipeline 29; The outlet of tower bottom reboiler T011 meets the material inlet T023 at separating tank T02 middle part through pipeline 26; The liquid exit T022 of separating tank T02 bottom meets the liquid inlet T013 at rectifying tower T01 middle part through pipeline 27 and throttling valve 28; The pneumatic outlet T021 of separating tank T02 bottom connects the inlet of gas compressor X03 through pipeline 27a, and the outlet of gas compressor X03 meets the gas inlet T016 at rectifying tower T01 middle part through pipeline 27b.
The natural gas liquids outlet T012 of rectifying tower T01 bottom is through the inlet of the natural gas liquids on the pipeline 33 fishplate bar fin heat exchanger E02 029, and the natural gas liquids outlet 029a on the plate-fin heat exchanger E02 connects natural gas liquids low temperature storage tank through pipeline 30 and reducing valve.
The Waste gas outlet T014 at rectifying tower T01 top is through the exhaust gas entrance 027 on the pipeline 31 fishplate bar fin heat exchanger E02; Waste gas outlet 028 on the plate-fin heat exchanger E02 is through the exhaust gas entrance 017 of pipeline 32 fishplate bar fin heat exchanger E01, and the waste gas outlet 018 of plate-fin heat exchanger E01 connects factory's combustion gas.
The methane mixture COG composition that the present embodiment methanation device is brought: CH4,63.76%, N2,7.65%, H2,28.59%, T=40 ℃, P=30bar.
Through the nitrogen after two nitrogen supercharging machine ZP01, the ZP02 supercharging, before getting into plate-fin heat exchanger E01, divide two strands, one directly gets into plate-fin heat exchanger E01 through pipeline 13, and another strand directly gets into nitrogen expansion machine X01 through arm 14 and expands.Nitrogen through plate-fin heat exchanger E01 heat exchange; Divide two strands; One directly gets into plate-fin heat exchanger E02 through pipeline 15, and another strand gets into nitrogen expansion machine X02 through arm 16 and expand, and nitrogen expansion machine X01, X02 drive nitrogen supercharging machine ZP01, ZP02 respectively.
The nitrogen that comes out from plate-fin heat exchanger E02 gets into condenser/evaporator T015 through pipeline 17 and behind throttling valve 17a throttling to certain pressure; The nitrogen that comes out from condenser/evaporator T015 mixes with the nitrogen of bringing through arm 19 that expand into certain pressure through nitrogen expansion machine X02, sends among the plate-fin heat exchanger E02.Nitrogen after plate-fin heat exchanger E02 re-heat mixes with the nitrogen of bringing through arm 19a that expand into certain pressure through nitrogen expansion machine X01, sends into re-heat among the plate-fin heat exchanger E01.After plate-fin heat exchanger E01 re-heat, send into compressor P01 compression through pipeline 21, after the nitrogen after the compressor P01 compression is sent into interchanger E04 heat exchange through pipeline 22, again through pipeline 23 send into nitrogen supercharging machine ZP01, ZP02 recycles.
Methane mixture COG sends among the plate-fin heat exchanger E01 after plate-fin heat exchanger E01 and E02 heat exchange; Get into tower bottom reboiler T011 through pipeline 29 and carry out heat exchange; Methane mixture after heat exchange is as rectifying tower T01 reboiler thermal source; T01 provides heat for rectifying tower, further cools off self.Get into separating tank T02 through the cooled gas of tower bottom reboiler T011 through pipeline 26 and carry out vapor-liquid separation; Liquid after the vapor-liquid separation gets into rectifying tower T01 through pipeline 27 and through throttling valve 28 throttlings, and the gas after the vapor-liquid separation is sent into gas expander X03 expansion entering rectifying tower T01 through pipeline 27a and moved with the liquid that gets into rectifying tower T01.That come out at the bottom of the tower of rectifying tower T01 is natural gas liquids LNG; Natural gas liquids is sent into plate-fin heat exchanger E02 through pipeline 33 at the bottom of the tower; Further cool off and be decompressed to 1.5bar through plate-fin heat exchanger E02; Obtain purity and be 99.5%, pressure is the natural gas liquids of 1.5bar, input low temperature storage tank.Cat head comes out mainly is to contain H2 and the N2 gas mixture is sent among the plate-fin heat exchanger E02 through pipeline 31, after plate-fin heat exchanger E02 heat exchange, sends among the plate-fin heat exchanger E01 through pipeline 32 again, after plate-fin heat exchanger E01 heat exchange, send factory's combustion gas.
The methane recovery of the rectifying tower T01 of present embodiment is more than 99%, and the energy consumption of this explained hereafter natural gas liquids is 0.88KWh/Nm
3
More than show and described the advantage of ultimate principle, principal character and the utility model of utility model.The technician of the industry should understand; The utility model is not restricted to the described embodiments; The principle of describing in the foregoing description and the specification sheets that the utility model just is described; The utility model also has various changes and modifications under the prerequisite that does not break away from the utility model spirit and scope, and these variations and improvement all fall in the utility model scope that requires protection.The utility model requires protection domain to be defined by appending claims and equivalent thereof.
Claims (6)
1. a coke-oven gas low temperature fractionation is produced the device of natural gas liquids; It is characterized in that comprising one first heat-exchanger rig and one second heat-exchanger rig and a cover rectifying tower; Said first heat-exchanger rig is provided with first nitrogen inlet, first nitrogen outlet, first methane mixture inlet and the outlet of first methane mixture; Second heat-exchanger rig is provided with second nitrogen inlet, second nitrogen outlet, second methane mixture inlet, the outlet of second methane mixture, second natural gas liquids inlet and the outlet of second natural gas liquids; Be provided with the outlet of the tower bottom reboiler and first natural gas liquids at the bottom of the tower of said rectifying tower; The rectifying tower middle part is provided with the liquid inlet, and the rectifying tower top is provided with Waste gas outlet; First nitrogen inlet on said first heat-exchanger rig connects liquefaction nitrogen through pipeline; First nitrogen outlet on first heat-exchanger rig connects second nitrogen inlet on said second heat-exchanger rig through pipeline, and second nitrogen outlet on said second heat-exchanger rig is discharged the nitrogen after the heat exchange; First methane mixture inlet on said first heat-exchanger rig connects the methane mixture outlet of methanation device; First methane mixture outlet on first heat-exchanger rig is connected through pipeline with the inlet of said tower bottom reboiler; The outlet of said tower bottom reboiler enters the mouth through second methane mixture on pipeline and said second heat-exchanger rig and is connected; Second methane mixture outlet on second heat-exchanger rig is connected with the inlet at said rectifying tower middle part through pipeline and first throttle valve; The outlet of first natural gas liquids at the bottom of the said rectifying Tata enters the mouth through the pipeline and second natural gas liquids on said second heat-exchanger rig and is connected; Second natural gas liquids outlet on second heat-exchanger rig is connected with natural gas liquids low temperature storage tank through pipeline and reducing valve, through the Waste gas outlet discharging of the waste gas after the rectifying tower rectifying by the rectifying tower top.
2. a coke-oven gas low temperature fractionation is produced the device of natural gas liquids; It is characterized in that; Comprise at least one first heat-exchanger rig and one second heat-exchanger rig, a cover rectifying tower and a cover tripping device; Said first heat-exchanger rig is provided with first nitrogen inlet, first nitrogen outlet, first methane mixture inlet and the outlet of first methane mixture; Second heat-exchanger rig is provided with second nitrogen inlet, second nitrogen outlet, second methane mixture inlet, the outlet of second methane mixture, second natural gas liquids inlet and the outlet of second natural gas liquids; Be provided with the outlet of the tower bottom reboiler and first natural gas liquids at the bottom of the tower of said rectifying tower, the rectifying tower middle part is provided with liquid inlet and gas inlet, and the rectifying tower top is provided with Waste gas outlet; Said tripping device comprises a separating tank and a gas expander, and the top of said separating tank is provided with pneumatic outlet, and the bottom of separating tank is provided with liquid exit, and the middle part of separating tank is provided with material inlet; First nitrogen inlet on said first heat-exchanger rig connects liquefaction nitrogen through pipeline; First nitrogen outlet on first heat-exchanger rig connects second nitrogen inlet on said second heat-exchanger rig through pipeline, and second nitrogen outlet on said second heat-exchanger rig is discharged the nitrogen after the heat exchange; First methane mixture inlet on said first heat-exchanger rig connects the methane mixture outlet of methanation device; The outlet of first methane mixture on first heat-exchanger rig enters the mouth through the pipeline and second methane mixture on said second heat-exchanger rig and is connected; Second methane mixture outlet on second heat-exchanger rig is connected with the inlet of said tower bottom reboiler through pipeline; The outlet of tower bottom reboiler is connected through the material inlet of pipeline with said separating tank middle part; The liquid exit of separating tank bottom is connected with the liquid inlet at said rectifying tower middle part through pipeline and first throttle valve; The pneumatic outlet at separating tank top is connected with the inlet of gas expander through pipeline, and the outlet of gas expander is connected through the gas inlet of pipeline with said rectifying tower middle part; The outlet of first natural gas liquids at the bottom of the said rectifying Tata enters the mouth through the pipeline and second natural gas liquids on said second heat-exchanger rig and is connected; Second natural gas liquids outlet on second heat-exchanger rig is connected with natural gas liquids low temperature storage tank through pipeline and reducing valve, through the Waste gas outlet discharging of the waste gas after the rectifying tower rectifying by the rectifying tower top.
3. according to claim 1 or claim 2 device; It is characterized in that; The first nitrogen supercharging machine, the second nitrogen supercharging machine and the 3rd heat-exchanger rig that also comprise parallel running; And said first heat-exchanger rig is provided with first nitrogen reflux inlet and the outlet of first nitrogen reflux, and said second heat-exchanger rig is provided with second nitrogen reflux inlet and second nitrogen reflux exports, and is provided with condenser/evaporator at the cat head of said rectifying tower; The said first nitrogen supercharging machine is driven by the first nitrogen expansion machine; The second nitrogen supercharging machine is driven by the second nitrogen expansion machine; Inlet on first, second nitrogen supercharging machine connects nitrogen; Outlet on first, second nitrogen supercharging machine connects the inlet of the 3rd heat-exchanger rig through pipeline; The outlet of the 3rd heat-exchanger rig connects first nitrogen inlet of first heat-exchanger rig through pipeline, and the pipeline that is connected on first nitrogen inlet of first heat-exchanger rig is connected with the inlet of the said first nitrogen expansion machine through first arm, and the outlet of the first nitrogen expansion machine is passed through second arm and entered the mouth with first nitrogen reflux on first heat-exchanger rig and be connected; The pipeline that is connected on second nitrogen inlet of second heat-exchanger rig is connected with the inlet of the said second nitrogen expansion machine through the 3rd arm, and the outlet of the second nitrogen expansion machine is passed through the 4th arm and entered the mouth with first nitrogen reflux on second heat-exchanger rig and be connected; The outlet of second nitrogen reflux on second heat-exchanger rig enters the mouth through the pipeline and first nitrogen reflux on first heat-exchanger rig and is connected; Second nitrogen outlet on said second heat-exchanger rig connects the inlet of said condenser/evaporator through pipeline, and the outlet of condenser/evaporator enters the mouth through the pipeline and second nitrogen reflux on said second heat-exchanger rig and is connected.
4. device as claimed in claim 3; It is characterized in that; Also comprise a compressor and the 4th heat-exchanger rig; The outlet of first nitrogen reflux on said first heat-exchanger rig connects the inlet of said compressor through pipeline, and the outlet of said compressor connects the inlet of the 4th heat-exchanger rig, and the outlet of the 4th heat-exchanger rig is connected with inlet on said first, second nitrogen supercharging machine through pipeline.
5. device as claimed in claim 3; It is characterized in that; Said first heat-exchanger rig is provided with first exhaust gas entrance, first waste gas outlet; Said second heat-exchanger rig is provided with second exhaust gas entrance, second waste gas outlet; The Waste gas outlet at said rectifying tower top is connected with second exhaust gas entrance on said second heat-exchanger rig through pipeline, and second waste gas outlet on second heat-exchanger rig passes through pipeline and is connected with first exhaust gas entrance on said first heat-exchanger rig, and first waste gas outlet that is provided with on first heat-exchanger rig connects factory's combustion gas.
6. device as claimed in claim 3 is characterized in that, said first heat-exchanger rig and second heat-exchanger rig are plate-fin heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011202464587U CN202116524U (en) | 2011-07-13 | 2011-07-13 | Device for producing liquefied natural gas by coke oven gas through low-temperature rectification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011202464587U CN202116524U (en) | 2011-07-13 | 2011-07-13 | Device for producing liquefied natural gas by coke oven gas through low-temperature rectification |
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| Publication Number | Publication Date |
|---|---|
| CN202116524U true CN202116524U (en) | 2012-01-18 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011202464587U Expired - Fee Related CN202116524U (en) | 2011-07-13 | 2011-07-13 | Device for producing liquefied natural gas by coke oven gas through low-temperature rectification |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103673502A (en) * | 2013-12-10 | 2014-03-26 | 新奥科技发展有限公司 | Natural gas purification liquidation method |
| CN108826830A (en) * | 2018-07-12 | 2018-11-16 | 北京拓首能源科技股份有限公司 | A kind of intermediate feed coke-stove gas recovery system using cold energy of liquefied natural gas |
-
2011
- 2011-07-13 CN CN2011202464587U patent/CN202116524U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103673502A (en) * | 2013-12-10 | 2014-03-26 | 新奥科技发展有限公司 | Natural gas purification liquidation method |
| CN108826830A (en) * | 2018-07-12 | 2018-11-16 | 北京拓首能源科技股份有限公司 | A kind of intermediate feed coke-stove gas recovery system using cold energy of liquefied natural gas |
| CN108826830B (en) * | 2018-07-12 | 2024-01-09 | 北京拓首能源科技股份有限公司 | Intermediate feeding coke oven gas recovery system utilizing liquefied natural gas cold energy |
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