CN102022893A - Cold-state starting method of air separation equipment - Google Patents
Cold-state starting method of air separation equipment Download PDFInfo
- Publication number
- CN102022893A CN102022893A CN2009101874670A CN200910187467A CN102022893A CN 102022893 A CN102022893 A CN 102022893A CN 2009101874670 A CN2009101874670 A CN 2009101874670A CN 200910187467 A CN200910187467 A CN 200910187467A CN 102022893 A CN102022893 A CN 102022893A
- Authority
- CN
- China
- Prior art keywords
- crude argon
- argon column
- oxygen
- air
- tower
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 18
- 238000000926 separation method Methods 0.000 title claims abstract description 16
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims abstract description 186
- 229910052786 argon Inorganic materials 0.000 claims abstract description 93
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 55
- 239000001301 oxygen Substances 0.000 claims abstract description 55
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 55
- 239000007788 liquid Substances 0.000 claims description 54
- 238000001704 evaporation Methods 0.000 claims description 22
- 230000008020 evaporation Effects 0.000 claims description 22
- 238000011084 recovery Methods 0.000 claims description 11
- 239000002808 molecular sieve Substances 0.000 claims description 6
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 10
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 5
- 238000009792 diffusion process Methods 0.000 abstract 1
- 230000002950 deficient Effects 0.000 description 5
- 238000010992 reflux Methods 0.000 description 5
- 230000007812 deficiency Effects 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- VVTSZOCINPYFDP-UHFFFAOYSA-N [O].[Ar] Chemical compound [O].[Ar] VVTSZOCINPYFDP-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—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
Landscapes
- 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 a cold-state starting method of an air separation plant, which is characterized in that when the air separation plant is started in a cold state, the oxygen purity can not generate large fluctuation by controlling the set value of an air compressor emptying valve, opening an air compressor inlet guide vane, increasing the air quantity entering a tower, reducing the set value of oxygen diffusion quantity and the like, the time for sending out qualified products such as oxygen, nitrogen, argon and the like is reduced, the consumption of electric energy is reduced, and the enterprise benefit is improved.
Description
Technical field
The present invention relates to a kind of equipment starting method, particularly relate to a kind of air separation plant cold start method.
Background technology
Crude argon column was long recovery time when steel plant's air separation plant started at cold state, can cause oxygen purity fluctuation in crude argon column recovery process, and it is defective that oxygen purity is occurred after qualified once more, and oxygen is sent and interrupted about 2h once more, and the company that influences produces.
The main cause of oxygen purity fluctuation:
(1) in the process of resuming production, advances PID adjustment modules such as tower air mass flow, argon cut oxygen content, swell increment and can't realize automatic adjusting, in case molecular sieve adsorber switches, the fluctuation of oxygen pipe network causes crude argon column nitrogen plug easily and oxygen purity is defective.
(2) in throwing the crude argon column process, cold concentrates on crude argon column, and main cold liquid level is low, main cooling and heating load deficiency, and entering tower air capacity reduces, and last tower rising steam reduces, and last tower reflux ratio increases, and causes oxygen purity defective; For guaranteeing to lead cold liquid level, the liquid that crude argon column is got back to tower by the last tower control valve of crude argon column bottom liquid backflow is too much, and the stripping section reflux ratio increases, and causes oxygen purity defective.
Summary of the invention
The present invention has overcome deficiency of the prior art, provides a kind of and can effectively guarantee the impregnable air separation plant cold start of oxygen purity method.
In order to address the above problem, the present invention by the following technical solutions:
A kind of air separation plant cold start method is characterized in that this method is carried out as follows:
(1) after air separation plant stops, complete shut-down crude argon column condenser argon side drain valve;
(2) air compressor machine atmospheric valve pressure set points is brought up to 0.49～0.52MPa after the air guide of empty branch, opens big air compressor machine inlet guide vane, and going into the tower air mass flow increases by 4000～8000m than calculated value
3/ h;
(3) before oxygen purity is qualified, the oxygen amount of diffusing setting value reduces by 1500～2500m than calculated value
3/ h;
(4) start the crude argon pump in advance to main cold-patch topping up body, the backflow of crude argon column bottom liquid is gone up the tower control valve and is reached 6%～8%, guarantees that the crude argon column liquid level slowly descends;
(5) when switching, molecular sieve adsorber increases entering tower air capacity 3000～5000m
3/ h, manual adjustments oxygen is sent valve during the fluctuation of oxygen pipe network, guarantees that the oxygen sendout is constant;
(6) reach more than 98% at oxygen purity, argon cut oxygen content reaches more than 89%, on the pressure reduction of tower bottom pressure and last top of tower pressure reach more than the 10kPa, the crude argon column condenser pressure is set 100kPa, liquid air evaporation capacity control valve opening is at 10% crude argon column of startup when above;
(7) along with the increase of crude argon column liquid air evaporation capacity, open big crude argon column liquid backflow synchronously and go up the tower control valve, the crude argon column liquid level is slowly descended, after liquid level was reduced to normal value, control valve transferred automatic adjusting to;
(8) the liquid air evaporation capacity increases by 1500～3000m than calculated value in crude argon column recovery process
3/ h drops to normal value again after liquid argon purity is qualified;
(9) swell increment increases by 1500～4000m on the calculated value basis in operating mode recovery process
3/ h, swell increment drops to normal value again after crude argon column liquid air evaporation capacity is increased to normal value.
Compared with prior art, the invention has the beneficial effects as follows:
By utilization aforesaid operations method, when air separation plant starts, shortened effectively that liquid argon purity is qualified sends the time under cold state, fluctuation no longer appears after oxygen purity is qualified, reduced power consumption greatly, improved the performance of enterprises.
The specific embodiment
A kind of air separation plant cold start method, this method is carried out as follows:
(1) after air separation plant stops, complete shut-down crude argon column condenser argon side drain valve;
(2) air compressor machine atmospheric valve pressure set points is brought up to 0.49～0.52MPa after the air guide of empty branch, opens big air compressor machine inlet guide vane, and going into the tower air mass flow increases by 4000～8000m than calculated value
3/ h;
(3) before oxygen purity is qualified, the oxygen amount of diffusing setting value reduces by 1500～2500m than calculated value
3/ h;
(4) start the crude argon pump in advance to main cold-patch topping up body, the backflow of crude argon column bottom liquid is gone up the tower control valve and is reached 6%～8%, guarantees that the crude argon column liquid level slowly descends;
(5) when switching, molecular sieve adsorber increases entering tower air capacity 3000～5000m
3/ h, manual adjustments oxygen is sent valve during the fluctuation of oxygen pipe network, guarantees that the oxygen sendout is constant;
(6) reach more than 98% at oxygen purity, argon cut oxygen content reaches more than 89%, on the pressure reduction of tower bottom pressure and last top of tower pressure reach more than the 10kPa, the crude argon column condenser pressure is set 100kPa, liquid air evaporation capacity control valve opening is at 10% crude argon column of startup when above;
(7) along with the increase of crude argon column liquid air evaporation capacity, open big crude argon column liquid backflow synchronously and go up the tower control valve, the crude argon column liquid level is slowly descended, after liquid level was reduced to normal value, control valve transferred automatic adjusting to;
(8) the liquid air evaporation capacity increases by 1500～3000m than calculated value in crude argon column recovery process
3/ h drops to normal value again after liquid argon purity is qualified;
(9) swell increment increases by 1500～4000m on the calculated value basis in operating mode recovery process
3/ h, swell increment drops to normal value again after crude argon column liquid air evaporation capacity is increased to normal value.
Embodiment one
Below with 35000m
3/ h air separation plant is an example, specifically sets forth the inventive method.
The inventive method is carried out as follows:
1, at 35000m
3After/h air separation plant stopped, complete shut-down crude argon column condenser argon side drain valve HV1720 avoided the high argon cut of tower parking back nitrogen content to enter crude argon column.
2, after the air guide of empty branch the pressure set points of air compressor machine atmospheric valve is brought up to 0.52MPa, open big air compressor machine inlet guide vane, going into tower air mass flow FIC1294 increases 5000m than calculated value
3/ h increases entering tower air capacity, strengthens the anti-fluctuation ability of operating mode, shortens the oxygen purity qualified time.
3, before oxygen purity is qualified, the setting value of the oxygen amount of diffusing reduces 2000m than calculated value
3/ h strengthens the anti-fluctuation ability of operating mode, shortens the oxygen purity qualified time.
4, start the crude argon pump in advance to main cold-patch topping up body, the backflow of crude argon column bottom liquid is gone up tower control valve LV1701 and is reached 6%～8%, guarantees that the LV1701 liquid level slowly descends, and avoids main cold liquid level to cross the low heat loads deficiency.Because this moment, the main cold temperature difference was big, the condensation evaporation process is violent, and main cold liquid oxygen purity will reach normal value again in the short time.After crude argon column puts into operation, along with crude argon column liquid air evaporation capacity increases, the argon cut phegma that flows to the crude argon column bottom after crude argon column rectifying contains oxygen more than 90%, opens big LV1701 gradually, can not impact main cold liquid oxygen purity, send oxygen just purity can not occur repeatedly again.
5, when molecular sieve adsorber switching, the fluctuation of oxygen pipe network, by increasing entering tower air capacity 4000m
3/ h and manual adjustments oxygen are sent valve and are prevented that the fluctuation of argon cut oxygen content from causing the crude argon column fluctuation of operating conditions, increases entering tower air capacity 4000m when molecular sieve adsorber switches
3/ h, manual adjustments oxygen is sent valve during the fluctuation of oxygen pipe network, guarantees that the oxygen sendout is constant.
6, grasp the startup opportunity of crude argon column, determine that according to oxygen purity, argon cut oxygen content, the pressure reduction of going up tower bottom pressure P I1622 and last top of tower pressure P I1626 and crude argon column liquid air evaporation capacity crude argon column starts and HV1720 opens opportunity.Reach more than 98% at oxygen purity, argon cut oxygen content reaches more than 89%, the pressure reduction of PI1622 and PI1626 reaches more than the 10kPa, the crude argon column condenser pressure is set 100kPa liquid air evaporation capacity control valve PIC1712 aperture at 10% crude argon column of startup when above.If HV1720 opens early, last tower argon cut nitrogen content height, nitrogen enter the crude argon column condenser and cause condenser heat load to reduce, and phegma reduces, and influences the crude argon column operating mode; If HV1720 opens late, crude argon column prolongs recovery time, and the argon amount of staying the tower stripping section increases, and causes oxygen purity to reduce.
7, along with big LV1701 is opened in the increase of crude argon column liquid air evaporation capacity FIC1712 synchronously, guarantee that crude argon column liquid level LI1701 liquid level slowly descends, LV1701 transfers automatic adjusting to after liquid level is reduced to normal value, avoid cold to concentrate on crude argon column, main cold liquid level is low, main cooling and heating load deficiency, and entering tower air capacity reduces, last tower reflux ratio increases, and causes oxygen purity defective.
8, liquid air evaporation capacity FIC1712 increases 2000m than calculated value in crude argon column recovery process
3/ h to make full use of the rectifying potentiality of crude argon column, drops to normal value again after liquid argon purity is qualified.Increase the liquid air evaporation capacity, can shorten the crude argon oxygen content and reach the qualified time, this be because: (1) liquid air evaporation capacity increases, and the argon cut amount of suction increases, and the crude argon amount of staying in the crude argon column increases; (2) the liquid air evaporation capacity increases, and the crude argon column reflux ratio increases, and helps crude argon purity and improves.
9, suitably increase swell increment in operating mode recovery process, swell increment increases 2000m on the calculated value basis
3/ h avoids owing to throw crude argon column, and cold concentrates on crude argon column, causes main cold liquid level low excessively; Swell increment drops to normal value again after crude argon column liquid air evaporation capacity is increased to normal value, avoids the excessive tower reflux ratio that causes of amount of liquid big, prevents that the reduction of argon cut oxygen content from causing crude argon column fluctuation of operating conditions and oxygen purity to reduce.
Claims (1)
1. air separation plant cold start method is characterized in that this method is carried out as follows:
(1) after air separation plant stops, complete shut-down crude argon column condenser argon side drain valve;
(2) air compressor machine atmospheric valve pressure set points is brought up to 0.49～0.52MPa after the air guide of empty branch, opens big air compressor machine inlet guide vane, and going into the tower air mass flow increases by 4000～8000m than calculated value
3/ h;
(3) before oxygen purity is qualified, the oxygen amount of diffusing setting value reduces by 1500～2500m than calculated value
3/ h;
(4) start the crude argon pump in advance to main cold-patch topping up body, the backflow of crude argon column bottom liquid is gone up the tower control valve and is reached 6%～8%, guarantees that the crude argon column liquid level slowly descends;
(5) when switching, molecular sieve adsorber increases entering tower air capacity 3000～5000m
3/ h, manual adjustments oxygen is sent valve during the fluctuation of oxygen pipe network, guarantees that the oxygen sendout is constant;
(6) reach more than 98% at oxygen purity, argon cut oxygen content reaches more than 89%, on the pressure reduction of tower bottom pressure and last top of tower pressure reach more than the 10kPa, the crude argon column condenser pressure is set 100kPa, liquid air evaporation capacity control valve opening is at 10% crude argon column of startup when above;
(7) along with the increase of crude argon column liquid air evaporation capacity, open big crude argon column liquid backflow synchronously and go up the tower control valve, the crude argon column liquid level is slowly descended, after liquid level was reduced to normal value, control valve transferred automatic adjusting to;
(8) the liquid air evaporation capacity increases by 1500～3000m than calculated value in crude argon column recovery process
3/ h drops to normal value again after liquid argon purity is qualified;
(9) swell increment increases by 1500～4000m on the calculated value basis in operating mode recovery process
3/ h, swell increment drops to normal value again after crude argon column liquid air evaporation capacity is increased to normal value.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009101874670A CN102022893B (en) | 2009-09-18 | 2009-09-18 | Cold-state starting method of air separation equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009101874670A CN102022893B (en) | 2009-09-18 | 2009-09-18 | Cold-state starting method of air separation equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102022893A true CN102022893A (en) | 2011-04-20 |
| CN102022893B CN102022893B (en) | 2013-10-16 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009101874670A Active CN102022893B (en) | 2009-09-18 | 2009-09-18 | Cold-state starting method of air separation equipment |
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| Country | Link |
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| CN (1) | CN102022893B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102654350A (en) * | 2012-04-24 | 2012-09-05 | 本钢板材股份有限公司 | Method for starting oxygen making unit |
| CN102997616A (en) * | 2011-09-10 | 2013-03-27 | 鞍钢股份有限公司 | Method for quickly preparing oxygen and argon |
| CN103344091A (en) * | 2013-07-26 | 2013-10-09 | 四川德胜集团钢铁有限公司 | Method for shortening time from effusion to oxygen generation for industrial oxygen generator |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6272884B1 (en) * | 1998-04-08 | 2001-08-14 | Praxair Technology, Inc. | Rapid restart system for cryogenic air separation plant |
-
2009
- 2009-09-18 CN CN2009101874670A patent/CN102022893B/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102997616A (en) * | 2011-09-10 | 2013-03-27 | 鞍钢股份有限公司 | Method for quickly preparing oxygen and argon |
| CN102654350A (en) * | 2012-04-24 | 2012-09-05 | 本钢板材股份有限公司 | Method for starting oxygen making unit |
| CN102654350B (en) * | 2012-04-24 | 2015-03-11 | 本钢板材股份有限公司 | Method for starting oxygen making unit |
| CN103344091A (en) * | 2013-07-26 | 2013-10-09 | 四川德胜集团钢铁有限公司 | Method for shortening time from effusion to oxygen generation for industrial oxygen generator |
| CN103344091B (en) * | 2013-07-26 | 2015-08-19 | 四川德胜集团钒钛有限公司 | A kind of industrial oxygenerating machine that shortens is from hydrops to the method for time going out oxygen |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102022893B (en) | 2013-10-16 |
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