CN203833612U - Nitrogen separation liquefaction system - Google Patents
Nitrogen separation liquefaction system Download PDFInfo
- Publication number
- CN203833612U CN203833612U CN201420092970.4U CN201420092970U CN203833612U CN 203833612 U CN203833612 U CN 203833612U CN 201420092970 U CN201420092970 U CN 201420092970U CN 203833612 U CN203833612 U CN 203833612U
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- China
- Prior art keywords
- nitrogen
- heat exchanger
- decompressor
- secondary heat
- loop
- 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.)
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 154
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 75
- 238000000926 separation method Methods 0.000 title claims abstract description 31
- 239000012528 membrane Substances 0.000 claims abstract description 29
- 239000007788 liquid Substances 0.000 claims abstract description 23
- 230000006835 compression Effects 0.000 claims abstract description 18
- 238000007906 compression Methods 0.000 claims abstract description 18
- 238000001914 filtration Methods 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims abstract description 10
- 239000000835 fiber Substances 0.000 claims description 10
- 238000003860 storage Methods 0.000 claims description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000012510 hollow fiber Substances 0.000 abstract 2
- 238000010586 diagram Methods 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 230000008595 infiltration Effects 0.000 description 1
- 238000001764 infiltration Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 150000002829 nitrogen Chemical class 0.000 description 1
- 239000003129 oil well Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The embodiment of the utility model provides a nitrogen separation liquefaction system which is simple in structure, relatively fast to generate a gas, relatively low in operation cost and capable of preparing liquid nitrogen at any place at any time. The nitrogen separation liquefactions system comprises membrane separation equipment and nitrogen expansion liquefaction equipment, wherein the membrane separation equipment is connected with the nitrogen expansion liquefaction equipment by virtue of a gas pipeline; the membrane separation equipment comprises a compression device, a filtering device, a hollow fiber membrane set and a generated gas output device; the compression device, the filtering device, the hollow fiber membrane set and the generated gas output device are connected in sequence; the nitrogen expansion liquefaction equipment comprises a cold source loop and a pressurizing liquefaction loop.
Description
Technical field
The utility model relates to gas generation field, particularly a kind of nitrogen separation liquefaction system.
Technical background
In order to improve output, in the production techniques such as oil, Sweet natural gas, coal-seam gas, shale gas the use of liquid nitrogen more and more frequent, along with the increase of liquid nitrogen consumption and the dispersiveness of oil well, the use cost of liquid nitrogen also starts significantly to increase.
In prior art, the preparation method of liquid nitrogen is mainly that its representative processes of method separating that first liquefies is again exactly cryogenic air separation unit, this is a kind of traditional liquid nitrogen preparation method, taking air as raw material, through overdraft, purification, recycling heat exchange makes liquefaction of air become liquid-air.Liquid-air is mainly the mixture of liquid oxygen and liquid nitrogen, then utilizes the boiling point of liquid oxygen and liquid nitrogen different (under 1 normal atmosphere, the boiling point of liquid oxygen is-183 DEG C, and the boiling point of liquid nitrogen is-196 DEG C), by the rectifying of liquid-air, makes them separate to obtain liquid nitrogen.Cryogenic air separation unit equipment is because it need to heat and higher to temperature control requirement liquified air, so its equipment complexity, floor space are large, capital cost is higher, be not suitable with in situ preparation liquid nitrogen, equipment one-time investment is larger, running cost is higher, and installation requirement is high, and the slow cycle of aerogenesis is longer.
Utility model content
The utility model embodiment provides a kind of nitrogen separation liquefaction system, and simple in structure, aerogenesis is very fast, and running cost is lower, is not subject to work point and environmental restraint can prepare liquid nitrogen whenever and wherever possible.
A kind of nitrogen separation liquefaction system that the utility model embodiment provides, comprising: membrane separation plant and nitrogen expansion liquefaction device, and described membrane separation plant is connected by gas piping with nitrogen expansion liquefaction device;
Described nitrogen expansion liquefaction device comprises low-temperature receiver circulation loop and pressurized liquefied loop;
Described low-temperature receiver circulation loop comprises at least two compressors, at least two first-class heat exchanger, decompressor and two secondary heat exchangers, described two secondary heat exchangers are connected in series, described at least two compressors intersect and are connected in series formation compression heat exchange unit with described at least two first-class heat exchanger order, described compression heat exchange machine set outlet is connected to decompressor entrance through a secondary heat exchanger, and described decompressor outlet is connected to compression heat exchange unit entrance through described two secondary heat exchangers;
Described pressurized liquefied loop comprises at least one compressor and the first-class heat exchanger being attached thereto, and described first-class heat exchanger is connected to liquid nitrogen storage tank through two secondary heat exchangers of described low-temperature receiver circulation loop.
Wherein, described compression set comprises: compressor and scatterer.
Wherein, described filtration unit comprises: the surge tank, low precision strainer, carbon bed filter, the high-precision filter that connect successively.
Wherein, described aerogenesis apparatus comprises: the under meter, purity variable valve and the check valve that connect successively.
Wherein, described filtration unit further comprises: well heater, described well heater is connected with described high-precision filter.
Wherein, described aerogenesis apparatus further comprises: oxygen cell, connects described check valve, for examining and determine nitrogen gas purity.
Wherein, when described at least one decompressor is two or more, described decompressor is connected in series.
Wherein, it is characterized in that, in described low-temperature receiver circulation loop, between secondary heat exchanger and described at least one decompressor, be provided with throttling valve.
Wherein, it is characterized in that, in described pressurized liquefied loop, between secondary heat exchanger and described liquid nitrogen storage tank, be provided with throttling valve.
A kind of nitrogen separation liquefaction system that the utility model embodiment provides, utilize tubular fibre membrane component from nitrogen, without being carried out to heat temperature raising, air separates, and adopt expansion cycles refrigeration techniques that low-temperature receiver liquefaction nitrogen is provided, simple in structure, aerogenesis is very fast, and the little running cost of volume is lower, can not be subject to work point and environmental restraint to prepare liquid nitrogen whenever and wherever possible.
Brief description of the drawings
Figure 1 shows that the nitrogen gas liquefaction system structural representation that the utility model embodiment provides.
Figure 2 shows that the concrete syndeton schematic diagram of nitrogen expansion liquefaction device that the utility model embodiment provides.
Figure 3 shows that the concrete syndeton schematic diagram of membrane separation plant that the utility model one embodiment provides.
Figure 4 shows that the concrete syndeton schematic diagram of expansion liquefaction device that the utility model one embodiment provides.
Embodiment
Below in conjunction with accompanying drawing, the embodiment of the utility model embodiment is clearly and completely described.
Figure 1 shows that the nitrogen separation liquefaction system structural representation that the utility model embodiment provides.As shown in Figure 1, this system comprises: membrane separation plant 100 and nitrogen expansion liquefaction device 200, membrane separation plant 100 is connected by gas piping with nitrogen expansion liquefaction device 200.
Wherein, membrane separation plant 100 comprises compression set 101, filtration unit 102, hollow-fibre membrane group 103 and aerogenesis take-off equipment 104, and this compression set 101, filtration unit 102, hollow-fibre membrane group 103 and aerogenesis take-off equipment 104 connect successively.
Figure 2 shows that the concrete syndeton schematic diagram of nitrogen expansion liquefaction device.As shown in Figure 2, nitrogen expansion liquefaction device 200 comprises low-temperature receiver circulation loop and pressurized liquefied loop, this low-temperature receiver circulation loop comprises at least two compressors (shown in figure two B1 and B2), at least two first-class heat exchanger (shown in figure two W1 and W2), at least one decompressor (shown in figure two ET1 and ET2) and two secondary heat exchanger E1 and E2, compressor B1, B2 and first-class heat exchanger W1, W2 order intersection is connected in series and forms compression heat exchange unit, be to be connected to compressor B2 entrance after compressor B1 is connected with first-class heat exchanger W1, compressor B2 outlet is connected with first-class heat exchanger W2 entrance, first-class heat exchanger W2 outlet is connected to decompressor ET1 through secondary heat exchanger E1, decompressor ET1 and decompressor ET2 are connected in series and pass through secondary heat exchanger E2 and E1 is connected to compressor B1 entrance, the first-class heat exchanger (a compressor B3 shown in figure and the first-class heat exchanger W3 being connected with B3) that pressurized liquefied loop comprises at least one compressor and is attached thereto, first-class heat exchanger W3 is connected to liquid nitrogen storage tank through secondary heat exchanger E1 and E2.
Air is exported pure nitrogen after membrane separation plant compresses, filters, separates, this nitrogen divides two portions to enter nitrogen expansion liquefaction device, a part enters low-temperature receiver circulation loop, for expansion cycles provides cold, a part enters pressurized liquefied loop, with the heat exchange of low-temperature receiver nitrogen liquefaction, export liquid nitrogen storage tank to.
In the utility model one embodiment, compression set comprises compressor and scatterer, filtration unit comprises the surge tank, low precision strainer, carbon bed filter, the high-precision filter that connect successively, and aerogenesis take-off equipment comprises the under meter, purity variable valve and the check valve that connect successively.
In the utility model one embodiment, before compressor, be connected with strainer, enter compression set at air and air is tentatively filtered before compressing; Between filtration unit and hollow-fibre membrane group, well heater is set, filtered nitrogen is heated and enter hollow-fibre membrane group to suitable temp, improve membrane sepn efficiency; After aerogenesis take-off equipment check valve, connect oxygen pond, for detection of nitrogen gas purity, the nitrogen flowing through through check valve reaches after corresponding purity through oxygen pond calibrating nitrogen, enters nitrogen expansion liquefaction device.
Figure 3 shows that the concrete syndeton schematic diagram of membrane separation plant that the utility model one embodiment provides.As shown in Figure 3, air first passes through filter 1 coarse filtration, then enter compressor 2, air is compressed into after certain pressure, enter rear-mounted radiator 3 cooling, and then enter filtration unit, entered successively surge tank 4 through the cooled pressurized air of scatterer 3, low precision strainer 5, carbon bed filter 6 and the airborne water of high-precision filter 7 elimination, wet goods impurity, and after being heated to applicable temperature, pure air heater via 8 after filtering enters hollow-fibre membrane group 103, utilize the infiltration rate difference of air composition in hollow-fibre membrane by nitrogen separation out, airborne oxygen enrichment is separated, discharge, the nitrogen that separation obtains passes through under meter 10 again, purity variable valve 11, check valve 12, and examine and determine nitrogen through oxygen pond 13 and reach after corresponding purity, enter nitrogen expansion liquefaction device.
Divide two portions to enter nitrogen expansion liquefaction device through the isolated nitrogen of membrane separation plant, a part is done low-temperature receiver, for expansion cycles provides cold; Another part pressurizes, and with the heat exchange of low-temperature receiver nitrogen, liquefaction, the nitrogen of liquefaction does not backflow and converges with raw nitrogen gas, circulation.
Figure 4 shows that the concrete syndeton schematic diagram of expansion liquefaction device that the utility model one embodiment provides.As shown in Figure 4, between secondary heat exchanger E1 and decompressor ET1 and between secondary heat exchanger E2 and liquid nitrogen storage tank, be respectively arranged with throttling valve V1 and V2, for controlling liquid nitrogen flow velocity.Wherein, part nitrogen is through two compressor B1 and B2 compression and to enter secondary heat exchanger E1 through two first-class heat exchanger W1 and W2 after cooling respectively cooling, cooled nitrogen is through two decompressor ET1 and the ET2 cooling of further expanding, and returns to compressor B1 and circulate from decompressor ET2 low-pressure low-temperature nitrogen out provides cold for two secondary heat exchanger E1 and E2.
The pure nitrogen of another part enters compressor B3, be compressed to after certain pressure, as 2.4MPa left and right, enter first-class heat exchanger W3, cooled nitrogen is through secondary heat exchanger E1 and the further cooling down liquefaction of E2, then enter liquid nitrogen storage tank, the nitrogen that do not liquefy reclaims cold through two secondary heat exchangers successively, converges and enters first-class heat exchanger W3 circulation with the isolated nitrogen of membrane separation plant.
A kind of nitrogen separation liquefaction system that the utility model embodiment provides, utilize tubular fibre membrane component from nitrogen, without being carried out to heat temperature raising, air separates, and adopt expansion cycles refrigeration techniques that low-temperature receiver liquefaction nitrogen is provided, simple in structure, aerogenesis is very fast, and the little running cost of volume is lower, can not be subject to work point and environmental restraint to prepare liquid nitrogen whenever and wherever possible.
Above-described embodiment is only explanation technical conceive of the present utility model and feature; not in order to limit the utility model; all within spirit of the present utility model and principle, any amendment of making, be equal to replacement etc., within all should being included in protection domain of the present utility model.
Claims (9)
1. a nitrogen separation liquefaction system, is characterized in that, comprising: membrane separation plant and nitrogen expansion liquefaction device, and described membrane separation plant is connected by gas piping with nitrogen expansion liquefaction device;
Membrane separation plant comprises compression set, filtration unit, hollow-fibre membrane group and aerogenesis take-off equipment, and described compression set, filtration unit, hollow-fibre membrane group and aerogenesis apparatus connect successively;
Described nitrogen expansion liquefaction device comprises low-temperature receiver circulation loop and pressurized liquefied loop;
Described low-temperature receiver circulation loop comprises at least two compressors, at least two first-class heat exchanger, decompressor and two secondary heat exchangers, described two secondary heat exchangers are connected in series, described at least two compressors intersect and are connected in series formation compression heat exchange unit with described at least two first-class heat exchanger order, described compression heat exchange machine set outlet is connected to decompressor entrance through a secondary heat exchanger, and described decompressor outlet is connected to compression heat exchange unit entrance through described two secondary heat exchangers;
Described pressurized liquefied loop comprises at least one compressor and the first-class heat exchanger being attached thereto, and described first-class heat exchanger is connected to liquid nitrogen storage tank through two secondary heat exchangers of described low-temperature receiver circulation loop.
2. system according to claim 1, is characterized in that, described compression set comprises: compressor and scatterer.
3. system according to claim 1, is characterized in that, described filtration unit comprises: the surge tank, low precision strainer, carbon bed filter, the high-precision filter that connect successively.
4. system according to claim 1, is characterized in that, described aerogenesis apparatus comprises: the under meter, purity variable valve and the check valve that connect successively.
5. system according to claim 3, is characterized in that, described filtration unit further comprises: well heater, described well heater is connected with described high-precision filter.
6. system according to claim 4, is characterized in that, described aerogenesis apparatus further comprises: oxygen cell, connects described check valve, for examining and determine nitrogen gas purity.
7. system according to claim 1, is characterized in that, when described decompressor number is two or more, described decompressor is connected in series.
8. system according to claim 1, is characterized in that, in described low-temperature receiver circulation loop, between secondary heat exchanger and described at least one decompressor, is provided with throttling valve.
9. system according to claim 1, is characterized in that, in described pressurized liquefied loop, between secondary heat exchanger and described liquid nitrogen storage tank, is provided with throttling valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420092970.4U CN203833612U (en) | 2014-03-03 | 2014-03-03 | Nitrogen separation liquefaction system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420092970.4U CN203833612U (en) | 2014-03-03 | 2014-03-03 | Nitrogen separation liquefaction system |
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| Publication Number | Publication Date |
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| CN203833612U true CN203833612U (en) | 2014-09-17 |
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| CN201420092970.4U Expired - Fee Related CN203833612U (en) | 2014-03-03 | 2014-03-03 | Nitrogen separation liquefaction system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103787286A (en) * | 2014-03-03 | 2014-05-14 | 天津凯德实业有限公司 | Nitrogen separation and liquefaction system |
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2014
- 2014-03-03 CN CN201420092970.4U patent/CN203833612U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103787286A (en) * | 2014-03-03 | 2014-05-14 | 天津凯德实业有限公司 | Nitrogen separation and liquefaction system |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140917 |
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| CF01 | Termination of patent right due to non-payment of annual fee |