CN102706098B - Hot start method of booster expander - Google Patents
Hot start method of booster expander Download PDFInfo
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- CN102706098B CN102706098B CN2012101588401A CN201210158840A CN102706098B CN 102706098 B CN102706098 B CN 102706098B CN 2012101588401 A CN2012101588401 A CN 2012101588401A CN 201210158840 A CN201210158840 A CN 201210158840A CN 102706098 B CN102706098 B CN 102706098B
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- decompressor
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- cold junction
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- 238000000034 method Methods 0.000 title claims abstract description 21
- 238000005057 refrigeration Methods 0.000 claims abstract description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000007789 gas Substances 0.000 claims abstract description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 7
- 230000007423 decrease Effects 0.000 claims description 9
- 230000000630 rising effect Effects 0.000 claims description 4
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract 1
- 238000000926 separation method Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—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 for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—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 for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—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 for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
- F25J3/04818—Start-up of the process
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to the field of a refrigeration process of a booster expander, in particular to a hot start method of the booster expander, which is characterized in that in the initial stage of hot start, all gas at the outlet of an expansion end enters a waste nitrogen channel of a main heat exchanger to be bypassed so as to accelerate the temperature reduction of the main heat exchanger, and simultaneously, air at the outlet of the cold end of the main heat exchanger is firstly introduced into the expansion end, and after the temperature of the air at the outlet of the expansion end is reduced to a designed value, air in the middle of the main heat exchanger is gradually introduced into the expansion end, so that the expander always runs at the designed highest safe rotating speed, and the maximum refrigeration capacity is fully exerted so as to shorten the air. Compared with the prior art, the invention has the beneficial effects that: by adopting the operation method, the hot start time of the expander can be shortened from the original 48 hours to 42 hours, the bypass operation period can be quickly passed in a relatively short time, the refrigerating capacity of the expander is fully exerted, and the power consumption for starting is further reduced.
Description
Technical field
The present invention relates to booster expansion machine refrigeration process field, particularly a kind of method of booster expansion machine thermal starting.
Background technology
Adopt in the refrigeration process flow process of booster expansion machine at present, compressed air is after molecular sieve purification, and one tunnel passage A through main heat exchanger enters Xia Ta; Another road is through the channel B of the laggard main heat exchanger of pressurized end supercharging of booster expansion machine, then after entering respectively the expanding end refrigeration from the middle part of main heat exchanger and cold junction, enters Shang Ta.
Above-mentioned air separation plant is when thermal starting, because the temperature of main heat exchanger middle part and cold side outlet progressively reduces, cause air themperature that initial start stage advances expanding end in the long period higher than nominal situation, pressurized end is in the bypass operating condition for a long time, refrigerating efficiency is had a greatly reduced quality, general thermal starting process needs about 48 hours consuming time, and power consumption is huge.
Summary of the invention
The purpose of this invention is to provide a kind of method of booster expansion machine thermal starting, overcome the deficiencies in the prior art, shorten the thermal starting time of air separation plant, reduce pressurized end bypass duration of runs, save reactive energy consumption.
For solving the problems of the technologies described above, technical scheme of the present invention is:
A kind of method of booster expansion machine thermal starting, the thermal starting initial stage, the dirty nitrogen passage bypass that the expanding end exit gas is all entered main heat exchanger is accelerated the decline of main heat exchanger temperature, first pass into main heat exchanger cold side outlet air to expanding end simultaneously, along with after the expanding end outlet air temperature drops to design load, pass into gradually main heat exchanger middle part air to expanding end again, shorten empty minute thermal starting time decompressor is turned round under the highest safe speed of rotation of design all the time for giving full play to maximum refrigerating capacity, concrete operation step is as follows:
1) standard-sized sheet expansion by-passing valve and supercharging by-passing valve make expanding end outlet cryogenic gas not advance upper tower but directly enter the dirty nitrogen passage of main heat exchanger, accelerate the decline of main heat exchanger temperature;
Cold junction air valve between while standard-sized sheet main heat exchanger cold junction and expanding end, the middle part air valve between complete shut-down main heat exchanger middle part and expanding end turns round expanding end under the main heat exchanger cold junction temperature;
2) make decompressor steady running under the highest safe speed of rotation of design;
3) cold junction temperature of main heat exchanger descends gradually, and the rotating speed of decompressor also decreases, and when its rotating speed is fallen 1800-2000rpm, closes the 8-10% of supercharging by-passing valve total kilometres, makes the rotating speed of decompressor again increase to the highest safe speed of rotation; Continue to descend with the main heat exchanger cold junction temperature, the rotating speed of decompressor continues to reduce, when its rotating speed is fallen 1800-2000rpm again, again close the 8-10% of supercharging by-passing valve total kilometres, make the rotating speed of decompressor again increase to the highest safe speed of rotation, operation so repeatedly is until supercharging by-passing valve complete shut-down;
4) when the decompressor inlet temperature reaches design load, open the 8-10% of middle part air valve total kilometres, make 8-10 ℃ of decompressor inlet temperature rising, along with the decompressor refrigeration that remains in operation, main heat exchanger centre exit temperature descends, and the decompressor inlet temperature drops to design load again, opens the 8-10% of middle part air valve total kilometres this moment again, so repeatedly, until middle part air valve standard-sized sheet;
5) along with the decompressor refrigeration that remains in operation, when the decompressor inlet temperature drops to design load again, close the 8-10% of cold junction air valve total kilometres, make 8-10 ℃ of decompressor inlet temperature rising, along with the decompressor refrigeration that remains in operation, when the decompressor inlet temperature drops to design load again, again close the 8-10% of cold junction air valve total kilometres, so repeatedly, until cold junction air valve complete shut-down, in whole process, decompressor intake air temperature is maintained between design load～(design load+10 ℃);
6) when the rotating speed of decompressor descends 1800-2000rpm again, close the 15-20% of expansion by-passing valve total kilometres, make the decompressor rise of rotational speed to the highest safe speed of rotation, along with the decompressor refrigeration that remains in operation, the rotating speed of decompressor descends after 1800-2000rpm again, then closes the 18-20% of expansion by-passing valve total kilometres, so repeatedly, until expansion by-passing valve complete shut-down begins to enter normal refrigerating operation.
Compared with prior art, the invention has the beneficial effects as follows: can make the thermal starting time of decompressor shorten to 42 hours by original 48 hours after adopting this method of operating, can cross fast the bypass on-stream period within the relatively short time, give full play to the refrigerating capacity of decompressor, and then reduce the startup power consumption.
Description of drawings
Fig. 1 is embodiment of the present invention process flow diagram.
The specific embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described further:
see Fig. 1, it is the embodiment of the method process flow diagram of a kind of booster expansion machine thermal starting of the present invention, the present invention is at the decompressor thermal starting initial stage, the expanding end exit gas is all accelerated the decline of main heat exchanger temperature with the dirty nitrogen passage bypass of main heat exchanger, first pass into main heat exchanger cold side outlet air to expanding end simultaneously, along with after the expanding end outlet air temperature drops to design load, pass into gradually main heat exchanger middle part air to expanding end again, shorten empty minute thermal starting time decompressor is turned round under the highest safe speed of rotation of design all the time for giving full play to maximum refrigerating capacity, concrete operation step is as follows:
1) standard-sized sheet expansion by-passing valve and supercharging by-passing valve make expanding end outlet cryogenic gas not advance upper tower but directly enter the dirty nitrogen passage of main heat exchanger, accelerate the decline of main heat exchanger temperature;
Cold junction air valve between while standard-sized sheet main heat exchanger cold junction and expanding end, the middle part air valve between complete shut-down main heat exchanger middle part and expanding end turns round expanding end under the main heat exchanger cold junction temperature;
2) make decompressor steady running under the highest safe speed of rotation 22000rpm of design;
3) along with the running of decompressor is freezed, the cold junction temperature of main heat exchanger descends gradually, and the rotating speed of decompressor also decreases, when its rotating speed drops to 20000rpm by 22000rpm, close the 8-10% of supercharging by-passing valve total kilometres, make the rotating speed of decompressor again increase to 22000rpm by 20000rpm; Continue to descend with the main heat exchanger cold junction temperature, the rotating speed of decompressor continues to reduce, when its rotating speed drops to 20000rpm by 22000rpm again, again close the 8-10% of supercharging by-passing valve total kilometres, make the rotating speed of decompressor again increase to 22000rpm by 20000rpm, operation so repeatedly is until supercharging by-passing valve complete shut-down;
4) when the decompressor inlet temperature reaches design load (110 ℃), open the 8-10% of middle part air valve total kilometres, make the decompressor inlet temperature rise to-100 ℃ by-110 ℃, along with the decompressor refrigeration that remains in operation, main heat exchanger centre exit temperature descends, and the decompressor inlet temperature drops to-110 ℃ again, opens the 8-10% of middle part air valve total kilometres this moment again, so repeatedly, until middle part air valve standard-sized sheet;
5) along with the decompressor refrigeration that remains in operation, when the decompressor inlet temperature drops to-110 ℃ again, close the 8-10% of cold junction air valve total kilometres, make the decompressor inlet temperature rise to-100 ℃ by-110 ℃, along with the decompressor refrigeration that remains in operation, when the decompressor inlet temperature drops to again-110 ℃, again close the 8-10% of cold junction air valve total kilometres, so repeatedly, until cold junction air valve complete shut-down, in whole process, guarantee as possible decompressor intake air temperature is maintained between-110 ℃～-100;
6) when the rotating speed of decompressor drops to 20000rpm by 22000rpm again, close the 15-20% of expansion by-passing valve total kilometres, make the decompressor rise of rotational speed to 22000rpm, along with the decompressor refrigeration that remains in operation, after the rotating speed of decompressor is down to 20000rpm again, then close the 18-20% of expansion by-passing valve total kilometres, so repeatedly, until expansion by-passing valve complete shut-down enters normal refrigerating operation program.
With 35000m
3/ h air separation plant is example, and after adopting hot start method operation of the present invention, the thermal starting time shortened to 42 hours by original 48 hours, but each thermal starting using electricity wisely 90000 kWh, and energy-saving effect is remarkable.
Claims (1)
1. the method for a booster expansion machine thermal starting, it is characterized in that, the thermal starting initial stage, the dirty nitrogen passage bypass that the expanding end exit gas is all entered main heat exchanger is accelerated the decline of main heat exchanger temperature, first pass into main heat exchanger cold side outlet air to expanding end simultaneously, along with after the expanding end outlet air temperature drops to design load, pass into gradually main heat exchanger middle part air to expanding end again, shorten empty minute thermal starting time decompressor is turned round under the highest safe speed of rotation of design all the time for giving full play to maximum refrigerating capacity, concrete operation step is as follows:
1) standard-sized sheet expansion by-passing valve and supercharging by-passing valve make expanding end outlet cryogenic gas not advance upper tower but directly enter the dirty nitrogen passage of main heat exchanger, accelerate the decline of main heat exchanger temperature;
Cold junction air valve between while standard-sized sheet main heat exchanger cold junction and expanding end, the middle part air valve between complete shut-down main heat exchanger middle part and expanding end turns round expanding end under the main heat exchanger cold junction temperature;
2) make decompressor steady running under the highest safe speed of rotation of design;
3) cold junction temperature of main heat exchanger descends gradually, and the rotating speed of decompressor also decreases, and when its rotating speed is fallen 1800-2000rpm, closes the 8-10% of supercharging by-passing valve total kilometres, makes the rotating speed of decompressor again increase to the highest safe speed of rotation; Continue to descend with the main heat exchanger cold junction temperature, the rotating speed of decompressor continues to reduce, when its rotating speed is fallen 1800-2000rpm again, again close the 8-10% of supercharging by-passing valve total kilometres, make the rotating speed of decompressor again increase to the highest safe speed of rotation, operation so repeatedly is until supercharging by-passing valve complete shut-down;
4) when the decompressor inlet temperature reaches design load, open the 8-10% of middle part air valve total kilometres, make 8-10 ℃ of decompressor inlet temperature rising, along with the decompressor refrigeration that remains in operation, main heat exchanger centre exit temperature descends, and the decompressor inlet temperature drops to design load again, opens the 8-10% of middle part air valve total kilometres this moment again, so repeatedly, until middle part air valve standard-sized sheet;
5) along with the decompressor refrigeration that remains in operation, when the decompressor inlet temperature drops to design load again, close the 8-10% of cold junction air valve total kilometres, make 8-10 ℃ of decompressor inlet temperature rising, along with the decompressor refrigeration that remains in operation, when the decompressor inlet temperature drops to design load again, again close the 8-10% of cold junction air valve total kilometres, so repeatedly, until cold junction air valve complete shut-down, in whole process, make decompressor intake air temperature maintain design load～higher than between 10 ℃ of design loads;
6) when the rotating speed of decompressor descends 1800-2000rpm again, close the 15-20% of expansion by-passing valve total kilometres, make the decompressor rise of rotational speed to the highest safe speed of rotation, along with the decompressor refrigeration that remains in operation, the rotating speed of decompressor descends after 1800-2000rpm again, then closes the 18-20% of expansion by-passing valve total kilometres, so repeatedly, until expansion by-passing valve complete shut-down begins to enter normal refrigerating operation.
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|---|---|---|---|
| CN2012101588401A CN102706098B (en) | 2012-05-21 | 2012-05-21 | Hot start method of booster expander |
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| CN2012101588401A CN102706098B (en) | 2012-05-21 | 2012-05-21 | Hot start method of booster expander |
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| CN102706098B true CN102706098B (en) | 2013-11-06 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107702431A (en) * | 2017-11-01 | 2018-02-16 | 西安交通大学 | A kind of cryogenic liquid expanding machine thermal starting system and method |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106338182B (en) * | 2016-08-25 | 2018-11-06 | 重庆朝阳气体有限公司 | A kind of energy-saving control method of air-seperation system |
| EP3438585A3 (en) * | 2017-08-03 | 2019-04-17 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for defrosting a device for air separation by cryogenic distillation and device adapted to be defrosted using this method |
| CN108240734B (en) * | 2018-03-08 | 2024-03-26 | 李佳晨 | Air supply system of booster expander and air separation equipment |
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| CN107702431A (en) * | 2017-11-01 | 2018-02-16 | 西安交通大学 | A kind of cryogenic liquid expanding machine thermal starting system and method |
| CN107702431B (en) * | 2017-11-01 | 2020-11-10 | 西安交通大学 | Hot start system and method for low-temperature liquid expansion machine |
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