CN105758123A - Method and device for preventing accumulative explosion of hydrocarbon compounds - Google Patents
Method and device for preventing accumulative explosion of hydrocarbon compounds Download PDFInfo
- Publication number
- CN105758123A CN105758123A CN201610253676.0A CN201610253676A CN105758123A CN 105758123 A CN105758123 A CN 105758123A CN 201610253676 A CN201610253676 A CN 201610253676A CN 105758123 A CN105758123 A CN 105758123A
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- Prior art keywords
- liquid oxygen
- oxygen
- pipeline
- liquid
- injector
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Links
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 17
- 238000000034 method Methods 0.000 title claims abstract description 13
- 238000004880 explosion Methods 0.000 title abstract description 13
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 87
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 39
- 239000001301 oxygen Substances 0.000 claims abstract description 39
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 39
- 238000010079 rubber tapping Methods 0.000 claims description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 239000007789 gas Substances 0.000 claims description 10
- 238000002347 injection Methods 0.000 claims description 9
- 239000007924 injection Substances 0.000 claims description 9
- 238000009825 accumulation Methods 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 239000003595 mist Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 229910000990 Ni alloy Inorganic materials 0.000 claims description 2
- 239000000956 alloy Substances 0.000 claims description 2
- 238000000889 atomisation Methods 0.000 claims description 2
- 238000004891 communication Methods 0.000 claims description 2
- 238000001914 filtration Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 claims description 2
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 abstract description 9
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 abstract description 9
- 238000000926 separation method Methods 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000004064 recycling Methods 0.000 abstract 1
- 238000004821 distillation Methods 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 239000006200 vaporizer Substances 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000009172 bursting Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
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
- F25J3/04406—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 using a dual pressure main column system
- F25J3/04412—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 using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high 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
- F25J3/04854—Safety aspects of operation
-
- 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
- F25J3/04854—Safety aspects of operation
- F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
-
- 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
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04896—Details of columns, e.g. internals, inlet/outlet devices
-
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/02—Mixing or blending of fluids to yield a certain product
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
-
- 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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/60—Expansion by ejector or injector, e.g. "Gasstrahlpumpe", "venturi mixing", "jet pumps"
-
- 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
- F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
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 discloses a method and device for preventing accumulative explosion of hydrocarbon compounds.A liquid oxygen continuous discharge device is arranged at the bottom of an upper tower body of an air separation two-stage rectifying tower, liquid oxygen accounting for 0.1-1.5% of a liquid oxygen product is continuously taken out from the bottom of the upper tower body, and the liquid oxygen is atomized through a liquid oxygen ejector and conveyed into an oxygen product pipeline after being mixed with oxygen.Temperature difference in the liquid oxygen ejector before and after liquid oxygen ejection is smaller than or equal to 4 DEG C, and the temperature after liquid oxygen ejection is larger than or equal to -5 DEG C.The device comprises the liquid oxygen ejector, a liquid oxygen pipeline communicated with the bottom of the upper tower body of the two-stage rectifying tower and the liquid oxygen ejector, a gaseous oxygen pipeline communicated with a gaseous oxygen inlet in the liquid oxygen ejector, and the oxygen product pipeline communicated with an oxygen product outlet in the liquid oxygen ejector.The method and device achieve continuous discharge of acetylene and other hydrocarbon compounds, prevent equipment explosion accidents, can be used for recycling oxygen, and generate economic benefits.
Description
Technical field
The invention belongs to technical field of coal chemical industry, relate to a kind of coal synthesis ammonia space division system, especially relate to a kind of method and device preventing the hydrocarbon compound accumulation such as acetylene in space division distillation system and cause equipment explosion accident to occur.
Background technology
Air separation unit is one of very important process units in chemical industry especially coal chemical industry enterprises, carries out the safe operation work of air separation unit, is to ensure that safe and stable, long period, a prerequisite of full production.For guaranteeing that the safety in production of air separation unit runs, it is necessary to reduce and eliminate acetylene and the gathering in space division distillation system of other hydrocarbon compound, otherwise there may be the danger that equipment explosion accident occurs.
Space division distillation system due to long-term operating, has acetylene and other hydrocarbon compound such as methane, ethane and assembles during production run in liquid oxygen, these aggregations spark that can generate static electricity by the rubbing action after accumulating finite concentration explodes, damage equipment.For preventing acetylene and the gathering of other hydrocarbon compound in liquid oxygen; system would generally arrange liquid oxygen purifier; but constantly bring in space division distillation system owing to including the air of the hydrocarbon compounds such as acetylene; when concentration reach one timing the most still can rub generation electrostatic spark explode; damage equipment, it is therefore necessary to discharge it in time.
Space division rectification is carried out in rectifying column, it is generally divided into single-stage rectification and twin-stage rectification, therefore having single rectification column and double rectification column, the air separation unit of large enterprise's overwhelming majority is all to use two-tower rectification tower, is made up of the condenser/evaporator between Xia Ta, upper tower and upper and lower tower.Air after compressing and cooling down enters from lower tower bottom, and coarse-fine through lower tower evaporates (initial gross separation), and the last rectification of upper tower, on double rectification column, top of tower and bottom obtain highly purified N respectively2And O2, and O2In have a certain amount of acetylene and other hydrocarbon compounds, it is easy to set off an explosion when the hydrocarbon compound gathered in space division distillation system reaches a certain amount of, once occur explosion accident to be necessary for parking to process, draw off pearlife, open ice chest inspection, not only need to check definite position of exploding, and need to clean the pipeline blocked by pearlife because of blast.Because the repair time is longer, very big to the Influence to operation of whole production line.
Summary of the invention
In order to solve problems of the prior art, the invention discloses a kind of method and device preventing hydrocarbon compound accumulation blast, by setting up the continuous tapping equipment of liquid oxygen at upper tower bottom, it is continuously withdrawn the liquid oxygen of trace, it is sent directly into oxygen product pipeline through liquid oxygen injector, had both achieved acetylene and other hydrocarbon compound discharges continuously, it is to avoid equipment explosion accident occurs, reclaim again oxygen, create economic benefit.
The present invention is achieved through the following technical solutions:
A kind of prevent hydrocarbon compound accumulation blast method, will through filtering, compressing, except mist, remove condensed water and CO2Air send into space division double rectification column be isolated to highly purified nitrogen, oxygen product, from space division double rectification column, the bottom of tower is continuously withdrawn the liquid oxygen accounting for liquid oxygen product 0.1-1.5%, liquid oxygen sends into oxygen product pipeline through liquid oxygen injector atomization and after oxygen mix, and before and after liquid oxygen injection, temperature difference≤4 DEG C in liquid oxygen injector, temperature >=-5 DEG C after liquid oxygen injection.
A kind of device for realizing described method, on space division double rectification column, the bottom of tower is provided with the continuous tapping equipment of liquid oxygen, the continuous tapping equipment of described liquid oxygen, including liquid oxygen injector, connect the liquid oxygen pipeline between bottom and the liquid oxygen injector of tower on double rectification column, with the gas oxygen pipeline of gas oxygen inlet communication on liquid oxygen injector, with the oxygen product pipeline of oxygen product outlet on liquid oxygen injector.
As a kind of preferred implementation, liquid oxygen pipeline is provided with manual operator, for the liquid oxygen amount taken out is regulated and controled.
Preferably, liquid oxygen sprayer body it is provided with in liquid oxygen injector, in liquid oxygen injector liquid oxygen sprayer body be respectively provided on two sides with thermometer, one of which thermometer is positioned at the respective side of the injection stream of liquid oxygen in liquid oxygen sprayer body, and another group thermometer is positioned at the opposition side of liquid oxygen sprayer body.
In order to ensure that this device is capable of discharge opeing when stopping or overhaul, and is provided with tapping valve on liquid oxygen pipeline；Preferably, tapping valve is on space division double rectification column on liquid oxygen pipeline between tower bottom and manual operator.
In order to prevent the oxide etch to pipeline, the material of described liquid oxygen pipeline, gas oxygen pipeline and oxygen product pipeline is nickel alloy material.
The method and device preventing hydrocarbon compound accumulation blast provided by the present invention, since putting into operation, not only effectively prevent the danger that equipment explosion accident occurs, and reclaimed oxygen and created good economic benefit, solve because equipment explosion affects the bottleneck that system normally produces.
Accompanying drawing explanation
In order to be illustrated more clearly that the embodiment of the present invention or technical scheme of the prior art, the accompanying drawing used required in embodiment or description of the prior art will be briefly described below, apparently, accompanying drawing in describing below is only some embodiments of the present invention, for those of ordinary skill in the art, on the premise of not paying creative work, it is also possible to obtain other accompanying drawing according to these accompanying drawings.
Fig. 1 is that the liquid oxygen of the embodiment of the present invention discharges schematic flow sheet continuously.
Fig. 2 is the structural representation of liquid oxygen injector in Fig. 1.
In Fig. 1: 1. the upper tower of space division double rectification column, 2. lead cold vaporizer, 3. lead cold tank gage, the 4. lower tower of space division double rectification column, 5. tapping valve, 6. manual operator, 7. thermodetector before liquid oxygen injection, 8. liquid oxygen injector, 9. thermodetector after liquid oxygen injection.
Detailed description of the invention
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is clearly and completely described, it is clear that described embodiment is only a part of embodiment of the present invention rather than whole embodiments.Based on the embodiment in the present invention, the every other embodiment that those of ordinary skill in the art are obtained under not making creative work premise, broadly fall into the scope of protection of the invention.
Embodiment
During present system work, air is successively filtered, air compressor machine compresses, water cooler cooling is except mist, condensed water removed by ammonia evaporator, adsorber removing moisture content and carbon dioxide, its temperature is made to be down to-172 DEG C through heat exchanger cooling again, pressure reaches 0.55MPa, air close to saturation enters space division rectifying column, in tower, uprising gas repeatedly partial condensation is realized by main cold vaporizer 2 with the evaporation of dropping liq many second part, first gas carry out coarse-fine evaporating in the lower tower 4 of space division double rectification column, again through upper tower 1 rectification of space division double rectification column, oxygen is obtained in upper tower, double high purity products of nitrogen, bottom the upper tower 1 of space division double rectification column, i.e. obtain the product oxygen that concentration is 90%, its top further rectification of dirt nitrogen obtains final products nitrogen.
It is 0.055MPa because operating pressure bottom the upper tower 1 of space division double rectification column, oxygen product line pressure is 0.11MPa, there is 55KPa pressure differential in both, the continuous tapping equipment of liquid oxygen is to meet main cold tank gage 3 >=82% bottom the upper tower 1 of space division double rectification column, as the oxygen withdrawal amount >=15000Nm of the upper tower 1 of space division double rectification column3Under conditions of/h, manual operator 6 comes into operation.1% liquid oxygen controls flow through manual operator 6, because pressure differential is drawn continuously by bottom the upper tower 1 of space division double rectification column, after liquid oxygen Pipeline transport to liquid oxygen injector 8, after liquid oxygen is sufficiently mixed with the gas oxygen that mist and gas oxygen Pipeline transport come, by oxygen product Pipeline transport to oxygen compressor.
It should be noted that (1) valve opening slowly to be carried out when manual operator 6 operates, each aperture answers ＜ 1%, prevents from causing main cold tank gage 3 to fluctuate widely；(2) after valve opening, it should be noted that main cold tank gage 3 changes, and adjust the load of decompressor on space division double rectification column in time, prevent main cold level fluctuation；(3) control the temperature difference≤4 DEG C before and after the injection of liquid oxygen injector 8 liquid oxygen, if front and back the temperature difference is little, should suitably open big manual operator 6；Otherwise, turn down manual operator 6；(4) temperature >=-5 DEG C of thermodetector 9 after liquid oxygen sprays after strict control liquid oxygen injector 8, to prevent bursting by freezing oxygen product pipeline；(5) noting cold regulation, main cold tank gage 3 controls 82 ~ 85%；(6) because air is wanted before entering air separation column first to compress through air compressor, when air compressor stops, or oxygen withdrawal amount≤10000Nm3During/h, manual operator 6 interlocked valve closes；(7), when needing discharge opeing, close manual operator 6, then tapping valve 5 is opened and carry out discharge opeing.
A lot of explosion accident was there is on space division double rectification column before setting up the continuous tapping equipment of liquid oxygen, after setting up the continuous tapping equipment of liquid oxygen, the excessive acetylene gathered in space division double rectification column and hydrocarbon compound can be dredged removing in time, effectively prevent the danger that equipment explosion accident occurs, and reclaimed oxygen and created good economic benefit, solve because equipment explosion affects the bottleneck that system normally produces.
The foregoing is only presently preferred embodiments of the present invention, not in order to limit the present invention, all within the spirit and principles in the present invention, any modification, equivalent substitution and improvement etc. made, should be included within the scope of the present invention.
Claims (7)
1. prevent hydrocarbon compound accumulation blast a method, will through filtering, compressing, except mist, remove condensed water and CO2Air send into space division double rectification column obtain highly purified nitrogen, oxygen product, it is characterized in that: from space division double rectification column, the bottom of tower is continuously withdrawn the liquid oxygen accounting for liquid oxygen product 0.1-1.5%, liquid oxygen sends into oxygen product pipeline through liquid oxygen injector atomization and after oxygen mix, and before and after liquid oxygen injection, temperature difference≤4 DEG C in liquid oxygen injector, temperature >=-5 DEG C after liquid oxygen injection.
2. the device being used for the method described in claim 1 that realizes, it is characterized in that: on space division double rectification column, the bottom of tower is provided with the continuous tapping equipment of liquid oxygen, the continuous tapping equipment of described liquid oxygen, including liquid oxygen injector, connect the liquid oxygen pipeline between bottom and the liquid oxygen injector of tower on double rectification column, with the gas oxygen pipeline of gas oxygen inlet communication on liquid oxygen injector, with the oxygen product pipeline of oxygen product outlet on liquid oxygen injector.
3. device as claimed in claim 2, it is characterised in that: on liquid oxygen pipeline, it is provided with manual operator, for the liquid oxygen amount taken out is regulated and controled.
4. device as claimed in claim 3, it is characterized in that: in liquid oxygen injector, be provided with liquid oxygen sprayer body, in liquid oxygen injector, liquid oxygen sprayer body is respectively provided on two sides with thermometer, one of which thermometer is positioned at the respective side of liquid oxygen injection stream in liquid oxygen sprayer body, and another group thermometer is positioned at the opposition side of liquid oxygen sprayer body.
5. the device as described in claim 3 or 4, it is characterised in that: on liquid oxygen pipeline, it is provided with tapping valve.
6. device as claimed in claim 5, it is characterised in that: tapping valve is on space division double rectification column on liquid oxygen pipeline between tower bottom and manual operator.
7. device as claimed in claim 6, it is characterised in that: the material of liquid oxygen pipeline, gas oxygen pipeline and oxygen product pipeline is nickel alloy material.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610253676.0A CN105758123B (en) | 2016-04-22 | 2016-04-22 | A kind of method and device for preventing hydrocarbon compound accumulation blast |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610253676.0A CN105758123B (en) | 2016-04-22 | 2016-04-22 | A kind of method and device for preventing hydrocarbon compound accumulation blast |
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| Publication Number | Publication Date |
|---|---|
| CN105758123A true CN105758123A (en) | 2016-07-13 |
| CN105758123B CN105758123B (en) | 2018-02-23 |
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| CN201610253676.0A Active CN105758123B (en) | 2016-04-22 | 2016-04-22 | A kind of method and device for preventing hydrocarbon compound accumulation blast |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113154799A (en) * | 2021-03-09 | 2021-07-23 | 杭州杭氧低温液化设备有限公司 | Liquid oxygen jet evaporator of air separation equipment |
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|---|---|---|---|---|
| JPH11132654A (en) * | 1997-10-31 | 1999-05-21 | Liquid Gas Co Ltd | Air separating method and air separating device |
| US5996373A (en) * | 1998-02-04 | 1999-12-07 | L'air Liquide, Societe Ananyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Cryogenic air separation process and apparatus |
| CN102607239A (en) * | 2012-03-20 | 2012-07-25 | 中煤能源黑龙江煤化工有限公司 | Liquid oxygen system |
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| CN105758123B (en) | 2018-02-23 |
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