CN104974798A - Control method for operation of pulverized coal burner of pulverized coal pressure gasification reaction device - Google Patents
Control method for operation of pulverized coal burner of pulverized coal pressure gasification reaction device Download PDFInfo
- Publication number
- CN104974798A CN104974798A CN201510395039.2A CN201510395039A CN104974798A CN 104974798 A CN104974798 A CN 104974798A CN 201510395039 A CN201510395039 A CN 201510395039A CN 104974798 A CN104974798 A CN 104974798A
- Authority
- CN
- China
- Prior art keywords
- valve
- group
- coal
- fine coal
- oxygen
- 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
- 239000003245 coal Substances 0.000 title claims abstract description 304
- 238000000034 method Methods 0.000 title claims abstract description 29
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 24
- 238000002309 gasification Methods 0.000 title claims abstract description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 121
- 239000001301 oxygen Substances 0.000 claims abstract description 121
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 121
- 238000010926 purge Methods 0.000 claims abstract description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- 239000007789 gas Substances 0.000 claims description 23
- 239000007788 liquid Substances 0.000 claims description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 16
- 239000002826 coolant Substances 0.000 claims description 12
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- 230000004224 protection Effects 0.000 claims description 8
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 7
- 230000008569 process Effects 0.000 claims description 7
- 229910001882 dioxygen Inorganic materials 0.000 claims description 6
- 231100001261 hazardous Toxicity 0.000 claims description 6
- 230000009467 reduction Effects 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 4
- 235000011089 carbon dioxide Nutrition 0.000 claims description 4
- 238000005520 cutting process Methods 0.000 claims description 4
- 230000004907 flux Effects 0.000 claims description 4
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen(.) Chemical compound [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 4
- 230000035939 shock Effects 0.000 claims description 4
- 238000010792 warming Methods 0.000 claims description 4
- 206010020852 Hypertonia Diseases 0.000 claims description 3
- 239000000498 cooling water Substances 0.000 claims description 3
- 238000005474 detonation Methods 0.000 claims description 3
- 238000007689 inspection Methods 0.000 claims description 3
- 230000007704 transition Effects 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 238000012423 maintenance Methods 0.000 abstract description 2
- 238000007600 charging Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- -1 olefin hydrocarbon Chemical class 0.000 description 2
- 230000008439 repair process Effects 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
Abstract
The invention provides a control method for operation of a pulverized coal burner of a pulverized coal pressure gasification reaction device, which is used for grouped control of a plurality of oxygen pipelines and a plurality of pulverized coal pipeline feeding of the pulverized coal burner of the pulverized coal pressure gasification reaction device and comprises start-up, operation, stop and purging of the pulverized coal burner. The invention can realize the simultaneous feeding or the grouped feeding of the multiple oxygen pipelines of the pulverized coal burner and the multiple pulverized coal pipelines, can also realize the simultaneous stopping or the grouped stopping of the multiple oxygen pipelines of the pulverized coal burner and the multiple pulverized coal pipelines, can realize the online maintenance of the oxygen pipelines and the pulverized coal pipelines, and ensures the long-period, continuous and stable safe operation and production of the pulverized coal pressure gasification device. The gasifier emergency safety system keeps the device running and enables the device to be started, stopped and purged safely.
Description
Technical field
The present invention relates to technical field of coal chemical industry, particularly relate to the control method that a kind of powdered coal pressuring gasified reaction unit fine coal burner runs.
Background technology
Powdered coal pressuring gasified technology is a kind of clean, efficiently all kinds of solid-state coal conversion is become the hydrogen of gaseous state and the modern technique of Co mixed gas, its ultimate principle coal is ground into dry coal dust, the vapourizing furnace with water wall is sent into continuously with rare gas element, under high-temperature and high-pressure conditions, by accurately controlling coal, ratio and the material of the raw material such as oxygen and water vapour are uniformly distributed, the raw gas containing co hydrogenation gas >=90% is generated through reaction, then, through Quench, be separated, the technological processs such as washing, isolate solid body, obtain pure saturated mode synthesis gas, the raw gas efficiency of carbon conversion generated is high, effective gas component content is high, methane content is low.The broken coal from feed coal bunker is characterized in join pulverize in coal pulverizer, by high temperature inert airflow drying, through positive delivery to vapourizing furnace, in stove, there is high-temp combustion with the pure oxygen divided from sky to react, generate crude synthesis gas, as the unstripped gas of follow-up workshop section, the field such as coal-based methanol, coal-based synthetic ammonia and coal preparing natural gas, coal synthetic oil, olefin hydrocarbon making by coal, coal hydrogen manufacturing, IGCC generating can be widely used in.
Traditional coal burner adopts single control method to be: no matter oxygen system or fine coal delivery system goes wrong, vapourizing furnace all wants parking maintenance.
Summary of the invention
(1) technical problem that will solve
The invention provides a set of level of automation high, control terse, safe and reliable single fire (spray) mouth polyoxy gas pipeline and the charging of many fine coal pipelines, the method and system that grouping controls, the on-bne repair of oxygen pipeline and fine coal pipeline can be realized, guarantee that the safe operation of powdered coal pressuring gasified device long period, continous-stable is produced.Present invention also offers a set of security interlocking protection method.
(2) technical scheme
The control method that a kind of powdered coal pressuring gasified reaction unit fine coal burner runs, method described in it comprises startup burner and runs and boost to 0.8MPaG-1.2MPaG and 600 DEG C-1000 DEG C, preferred 1.0MPaG and 800 DEG C, with satisfied throwing coal condition, now fine coal and oxygen are dropped into coal gasification reaction unit by first group of feed system and second group of feed system simultaneously or respectively, and startup burner is quit work, thus complete by startup burner to the transition of coal burner, and make described fine coal exit circulation, and boosting is proceeded to coal gasification reaction unit, warming temperature, it is made to work at the predetermined pressure and temperature, if first group of feed system goes wrong, then stop first group of feed system, start first group of feed system and purge program, and pass into protection gas, if second group of feed system goes wrong, then stop second group of feed system, start second group of feed system and purge program, and pass into protection gas, if other system of vapourizing furnace goes wrong, then two groups of feed systems stop simultaneously, start the purging program of two groups of feed systems simultaneously, and pass into shielding gas simultaneously.
First group of feed system comprises: oxygen pipeline, two to four fine coal pipelines and a superheated vapour pipeline.First group of feed system driving step is: (1) opens first group of fine coal circulation trip valve, opens first group of fine coal first trip valve, fine coal is circulated, (2) when first group of condition of feeding intake meets, open the by-pass valve of coal burner first group of oxygen first trip valve, when before and after first group of oxygen first trip valve, pressure reduction is lower than preset value, open coal burner first group of oxygen first trip valve, close the by-pass valve of coal burner first group of oxygen first trip valve, coal burner first group of oxygen flow rate adjusting valve is set to predetermined startup aperture, open first group of fine coal second trip valve and first group of fine coal the 3rd trip valve, open coal burner first group of oxygen eventually sever valve, described coal burner first group of oxygen flow rate adjusting valve and first group of fine coal flow control valve are started " oxygen/fine coal " rate control,
(3) close all first group of fine coal trip valves, open first group of fine coal circulation line blow down valve and purge, after purging after a predetermined time, close first group of fine coal circulation line blow down valve;
(4) all first group of superheated vapour trip valves are opened, first group of flow of superheated steam adjustable valve is set to startup aperture, starts described first group of flow of superheated steam adjustable valve and described first group of oxygen flow rate adjusting valve " steam/oxygen gas " ratio control.
Second group of feed system comprises: oxygen pipeline, one to three fine coal pipelines and a superheated vapour pipeline.Second group of feed system driving step is: (1) opens second group of fine coal circulation trip valve, opens second group of fine coal first trip valve, fine coal is circulated, (2) when second group of condition of feeding intake meets, open the by-pass valve of second group of oxygen first trip valve, when before and after second group of oxygen first trip valve, pressure reduction is lower than preset value, open coal burner second group of oxygen first trip valve, close the by-pass valve of coal burner second group of oxygen cutting valve, coal burner second group of oxygen flow rate adjusting valve is set to predetermined startup aperture, open second group of fine coal second trip valve and second group of fine coal the 3rd trip valve, open coal burner second group of oxygen eventually sever valve, described coal burner second group of oxygen flow rate adjusting valve and second group of fine coal flow control valve are started " oxygen/fine coal " rate control,
(3) close all second group of fine coal circulation trip valves, open second group of fine coal circulation line blow down valve and purge, after purging after a predetermined time, close second group of fine coal circulation line blow down valve;
(4) all second group of superheated vapour trip valves are opened, second group of flow of superheated steam adjustable valve is set to startup aperture, starts described second group of flow of superheated steam adjustable valve and described coal burner second group of oxygen flow rate adjusting valve " steam/oxygen gas " ratio control.
Other system of vapourizing furnace comprises: vapourizing furnace its own system; Synthetic gas system; Burner nozzle cooling water system, medium pressure boiler water system; The gasified water recycle system; Public engineer system.
The process variable triggering two cover feed system emergency protections simultaneously mainly contains: vapourizing furnace hypertonia, synthetic gas temperature is too high, coal burner water coolant total flux and each branch flow of coal burner water coolant too low, it is too low that burner water coolant fills with liquid level, liquid level of steam drum is too high or too low, boiler cycle pump is less than two normally work, boiler circulating water flow to coil pipe is too low, shock chamber's liquid level is too low, chilled water flow is too low, washing tower liquid level is too low, dreg-locking hopper recycle pump quits work, instrument air is too low, nitrogen or carbonic acid gas manifold pressure too low, fire inspection Loss Of Signal, stop button.
Wherein a set of feed system occurs that hazardous condition parking step is: (1) closes the first trip valve after the coal burner oxygen of described a set of feed system, the by-pass valve of coal burner oxygen first trip valve, coal burner oxygen flow rate adjusting valve, coal burner oxygen eventually sever valve, fine coal first trip valve, fine coal second trip valve and fine coal the 3rd trip valve, opens coal burner oxygen pipeline blow down valve and fine coal pipeline blow down valve; (2) all trip valves of superheated vapour pipeline and flow trip valve is closed; (3) open fine coal circulation trip valve, standard-sized sheet fine coal flow control valve, standard-sized sheet conveying high-pressure nitrogen flow variable valve, after a predetermined time, close fine coal circulation trip valve, open fine coal circulation line blow down valve; (4) after fine coal circulation line purges certain hour, close fine coal circulation line blow down valve and fine coal flow control valve, close the main blow down valve of coal burner oxygen pipeline, in vapourizing furnace, combustiblesubstance enters oxygen channel, cause oxygen pipeline detonation, coal burner oxygen pipeline low discharge blow down valve and fine coal pipeline blow down valve need be kept to be open mode.
The step of two cover feed system emergency work simultaneously: all trip valves of coal burner oxygen and oxygen flow rate adjusting valve, all trip valves of fine coal, all trip valves of superheated vapour pipeline and the flow control valve of simultaneously closing two feed systems, opens coal burner oxygen pipeline blow down valve and fine coal pipeline blow down valve; Open fine coal circulation trip valve, standard-sized sheet fine coal flow control valve, standard-sized sheet conveying high-pressure nitrogen flow variable valve, after a predetermined time, close fine coal circulation trip valve, open fine coal circulation line blow down valve; After fine coal circulation line purges certain hour, close fine coal circulation line blow down valve and fine coal flow control valve, close coal burner oxygen pipeline blow down valve and fine coal pipeline blow down valve.
(3) beneficial effect
The invention provides a set of level of automation high, control terse, safe and reliable single fire mouth many groups charging, the method and system that grouping controls, the on-bne repair of oxygen pipeline and fine coal pipeline can be realized, guarantee that the safe operation of powdered coal pressuring gasified device long period, continous-stable is produced.
Accompanying drawing explanation
Fig. 1 is present system frame diagram.
Fig. 2 is present invention process schema.
Fig. 3 is that the present invention drives sequence control process figure.
Fig. 4 is that the present invention is stopped sequence control process figure.
In figure, A1 is that vapourizing furnace purges, lights a fire, go into operation system; A2 is first group of fine coal burner feed system; A3 is second group of fine coal burner feed system; A4 is other system of vapourizing furnace; A5 is coal gasification reaction unit.
Embodiment
Below by specific embodiment accompanying drawing in addition, describe the present invention.
Embodiment 1
As shown in Figure 1, startup burner runs and after boosting to 1.0MPaG and 800 DEG C, two cover feed system A2 and A3 enable simultaneously or enable respectively fine coal circulation, when throwing coal condition and meeting, A2 and A3 enables simultaneously or respectively fine coal and oxygen is dropped into coal gasification reaction unit A5, and startup burner is quit work, and makes described fine coal exit circulation, and boosting, warming temperature are proceeded to coal gasification reaction unit, make it work at the predetermined pressure and temperature.If two cover feed systems are when feeding intake respectively, then the oxygen pipeline of the second cover feed system and fine coal pipeline will pass into shielding gas before first set feed system feeds intake.
As shown in Figure 2: first group of feed system A2 comprises: oxygen pipeline, two to four fine coal pipelines and a superheated vapour pipeline.First group of feed system A2 driving step is: A21, open described fine coal circulation trip valve, opens first group of fine coal first trip valve, fine coal is circulated, A22, when first group of condition of feeding intake meets, open the by-pass valve of coal burner first group of oxygen first trip valve, when before and after first group of oxygen first trip valve, pressure reduction is lower than preset value, open coal burner first group of oxygen first trip valve, close the by-pass valve of coal burner first group of oxygen first trip valve, coal burner first group of oxygen flow rate adjusting valve is set to predetermined startup aperture, open first group of fine coal second trip valve and first group of fine coal the 3rd trip valve, open coal burner first group of oxygen eventually sever valve, described coal burner first group of oxygen flow rate adjusting valve and first group of fine coal flow control valve are started " oxygen/fine coal " rate control, A23, close all first group of fine coal trip valves, open first group of fine coal circulation line blow down valve and purge, after purging after a predetermined time, close first group of fine coal circulation line blow down valve, A24, open all first group of superheated vapour trip valves, first group of flow of superheated steam adjustable valve is set to startup aperture, starts described first group of flow of superheated steam adjustable valve and described first group of oxygen flow rate adjusting valve " steam/oxygen gas " ratio control.
Second group of feed system A3 comprises: oxygen pipeline, one to three fine coal pipelines.Second group of feed system A3 driving step is: A31, open described fine coal circulation trip valve, opens second group of fine coal first trip valve, fine coal is circulated, A32, when second group of condition of feeding intake meets, open the by-pass valve of second group of oxygen first trip valve, when before and after second group of oxygen first trip valve, pressure reduction is lower than preset value, open coal burner second group of oxygen first trip valve, close the by-pass valve of coal burner second group of oxygen cutting valve, coal burner second group of oxygen flow rate adjusting valve is set to predetermined startup aperture, open second group of fine coal second trip valve and second group of fine coal the 3rd trip valve, open coal burner second group of oxygen eventually sever valve, described coal burner second group of oxygen flow rate adjusting valve and second group of fine coal flow control valve are started " oxygen/fine coal " rate control, A33, close all second group of fine coal circulation trip valves, open second group of fine coal circulation line blow down valve and purge, after purging after a predetermined time, close second group of fine coal circulation line blow down valve, A34, open all second group of superheated vapour trip valves, second group of flow of superheated steam adjustable valve is set to startup aperture, starts described second group of flow of superheated steam adjustable valve and described coal burner second group of oxygen flow rate adjusting valve " steam/oxygen gas " ratio control.
Other system A4 of vapourizing furnace comprises:
A41, vapourizing furnace its own system (vapourizing furnace pressure, fire box temperature, vapourizing furnace upper cone section outside wall temperature); A42, synthetic gas system (outlet syngas temperatures); A43, burner nozzle cooling water system (coal burner water coolant total flux, each branch flow of coal burner water coolant, burner water coolant fill with liquid level); A44, medium pressure boiler water system (liquid level of steam drum, boiler cycle pump, boiler circulating water flow) to coil pipe; A45, the gasified water recycle system (shock chamber's liquid level, washing tower liquid level, chilled water flow, dreg-locking hopper recycle pump); A46, public engineer system (instrument air pressure, nitrogen or carbonic acid gas manifold pressure).The process variable that the present invention triggers the emergency protection simultaneously of two cover feed systems mainly contains: vapourizing furnace hypertonia, synthetic gas temperature is too high, coal burner water coolant total flux and each branch flow of coal burner water coolant too low, it is too low that burner water coolant fills with liquid level, liquid level of steam drum is too high or too low, boiler cycle pump is less than two normally work, boiler circulating water flow to coil pipe is too low, shock chamber's liquid level is too low, chilled water flow is too low, washing tower liquid level is too low, dreg-locking hopper recycle pump quits work, instrument air is too low, nitrogen or carbonic acid gas manifold pressure too low, fire inspection Loss Of Signal, stop button.
As shown in Figure 3: coal burner drives to operate: fine coal is circulated, when throwing coal condition and meeting, oxygen and fine coal are dropped into described powdered coal pressuring gasified device stably, so far, coal burner feeds intake successfully, and described startup burner is quit work, thus complete by startup burner to the transition of coal burner, make described fine coal exit circulation, and boosting, warming temperature are proceeded to described powdered coal pressuring gasified device, make its safe operation production at full capacity at the predetermined pressure and temperature.
As shown in Figure 4: when wherein hazardous condition appears in set of system oxygen pipeline or fine coal pipeline in two cover feed system A2 and A3 systems, only need stop the set of system occurring hazardous condition, another set ofly still on-line operation can be continued.Wherein set of system occurs that hazardous condition parking step is: (1) closes the first trip valve after the coal burner oxygen of described a set of feed system, the by-pass valve of coal burner oxygen first trip valve, coal burner oxygen flow rate adjusting valve, coal burner oxygen eventually sever valve, fine coal first trip valve, fine coal second trip valve and fine coal the 3rd trip valve, opens coal burner oxygen pipeline blow down valve and fine coal pipeline blow down valve; (2) all trip valves of superheated vapour pipeline and flow trip valve is closed; (3) open fine coal circulation trip valve, standard-sized sheet fine coal flow control valve, standard-sized sheet conveying high-pressure nitrogen flow variable valve, after a predetermined time, close fine coal circulation trip valve, open fine coal circulation line blow down valve; (4) after fine coal circulation line purges certain hour, close fine coal circulation line blow down valve and fine coal flow control valve, close the main blow down valve of coal burner oxygen pipeline, in vapourizing furnace, combustiblesubstance enters oxygen channel, cause oxygen pipeline detonation, coal burner oxygen pipeline low discharge blow down valve and fine coal pipeline blow down valve need be kept to be open mode.
The present invention triggers set of system oxygen pipeline or fine coal pipeline occurs that hazardous condition has: the coal flow velocity to burner is too low, fine coal density to coal burner is too low, too low to coal burner oxygen flow, too high to burner oxygen flow, single cover system oxygen coal is higher than too, fine coal is too little to batch can and " oxygen/vapor mixing pipe " positive pressure differential, oxygen and vapourizing furnace positive pressure differential too little, oxygen pipeline blow-off valve does not cut out, fine coal end trip valve fails to open completely, coal reversing valve fails to open completely, oxygen cutting valve fails to open completely.
The step of two cover feed system emergency work simultaneously: all trip valves of coal burner oxygen and oxygen flow rate adjusting valve, all trip valves of fine coal, all trip valves of superheated vapour pipeline and the flow control valve of simultaneously closing two feed systems, opens coal burner oxygen pipeline blow down valve and fine coal pipeline blow down valve; Open fine coal circulation trip valve, standard-sized sheet fine coal flow control valve, standard-sized sheet conveying high-pressure nitrogen flow variable valve, after a predetermined time, close fine coal circulation trip valve, open fine coal circulation line blow down valve, after fine coal circulation line purges certain hour, close fine coal circulation line blow down valve and fine coal flow control valve, close coal burner oxygen pipeline blow down valve and fine coal pipeline blow down valve.
It should be noted that: in the above-described embodiments, in two groups of chargings, all add superheated vapour, but, also can add superheated vapour in one group of charging wherein.
Embodiment 2
According to the method that embodiment 1 is identical, just startup burner runs and boosts to 0.8MPaG and 1000 DEG C.
Embodiment 3
According to the method that embodiment 1 is identical, just startup burner runs and boosts to 1.2MPaG and 600 DEG C.
Above-listed detailed description is illustrating for possible embodiments of the present invention, and this embodiment is also not used to limit the scope of the claims of the present invention, and the equivalence that all the present invention of disengaging do is implemented or changed, and all should be contained in the scope of the claims of this case.
Claims (8)
1. the control method of a powdered coal pressuring gasified reaction unit fine coal burner operation, described in it, method comprises: startup burner runs and boosts to 0.8MPaG-1.2MPaG and 600 DEG C-1000 DEG C, with satisfied throwing coal condition, now fine coal and oxygen are dropped into coal gasification reaction unit by first group of feed system and second group of feed system simultaneously or respectively, and startup burner is quit work, thus complete by startup burner to the transition of coal burner, and make described fine coal exit circulation, and boosting is proceeded to coal gasification reaction unit, warming temperature, it is made to work at the predetermined pressure and temperature, if first group of feed system goes wrong, then stop first group of feed system, start first group of feed system and purge program, and pass into protection gas, if second group of feed system goes wrong, then stop second group of feed system, start second group of feed system and purge program, and pass into protection gas, if other system of vapourizing furnace goes wrong, then two groups of feed systems stop simultaneously, start the purging program of two groups of feed systems simultaneously, and pass into shielding gas simultaneously.
2. the control method of powdered coal pressuring gasified reaction unit fine coal burner operation according to claim 1, is characterized in that: first group of feed system comprises: oxygen pipeline, two to four fine coal pipelines and a superheated vapour pipeline; First group of feed system driving step is:
(1) open fine coal circulation trip valve, open first group of fine coal first trip valve, fine coal is circulated;
(2) when first group of condition of feeding intake meets, open the by-pass valve of coal burner first group of oxygen first trip valve, when before and after first group of oxygen first trip valve, pressure reduction is lower than preset value, open coal burner first group of oxygen first trip valve, close the by-pass valve of coal burner first group of oxygen first trip valve, coal burner first group of oxygen flow rate adjusting valve is set to predetermined startup aperture, open first group of fine coal second trip valve and first group of fine coal the 3rd trip valve, open coal burner first group of oxygen eventually sever valve, described coal burner first group of oxygen flow rate adjusting valve and first group of fine coal flow control valve are started " oxygen/fine coal " rate control,
(3) close all first group of fine coal trip valves, open first group of fine coal circulation line blow down valve and purge, after purging after a predetermined time, close first group of fine coal circulation line blow down valve;
(4) all first group of superheated vapour trip valves are opened, first group of flow of superheated steam adjustable valve is set to startup aperture, starts described first group of flow of superheated steam adjustable valve and described first group of oxygen flow rate adjusting valve " steam/oxygen gas " ratio control.
3. the control method of powdered coal pressuring gasified reaction unit fine coal burner operation according to claim 2, is characterized in that: second group of feed system comprises: oxygen pipeline, one to three fine coal pipelines and a superheated vapour pipeline; Second group of feed system driving step is: (1) opens fine coal circulation trip valve, opens second group of fine coal first trip valve, fine coal is circulated;
(2) when second group of condition of feeding intake meets, open the by-pass valve of second group of oxygen first trip valve, when before and after second group of oxygen first trip valve, pressure reduction is lower than preset value, open coal burner second group of oxygen first trip valve, close the by-pass valve of coal burner second group of oxygen cutting valve, coal burner second group of oxygen flow rate adjusting valve is set to predetermined startup aperture, open second group of fine coal second trip valve and second group of fine coal the 3rd trip valve, open coal burner second group of oxygen eventually sever valve, described coal burner second group of oxygen flow rate adjusting valve and second group of fine coal flow control valve are started " oxygen/fine coal " rate control,
(3) close all second group of fine coal circulation trip valves, open second group of fine coal circulation line blow down valve and purge, after purging after a predetermined time, close second group of fine coal circulation line blow down valve;
(4) all second group of superheated vapour trip valves are opened, second group of flow of superheated steam adjustable valve is set to startup aperture, starts described second group of flow of superheated steam adjustable valve and described coal burner second group of oxygen flow rate adjusting valve " steam/oxygen gas " ratio control.
4. the control method that the powdered coal pressuring gasified reaction unit fine coal burner according to claim 1 or 3 runs, is characterized in that: other system of gasification burner comprises: vapourizing furnace its own system; Synthetic gas system; Burner nozzle cooling water system; Medium pressure boiler water system; The gasified water recycle system and public engineer system.
5. the control method of powdered coal pressuring gasified reaction unit fine coal burner operation according to claim 4, it is characterized in that: the process variable triggering two cover feed system emergency protections simultaneously mainly contains: vapourizing furnace hypertonia, synthetic gas temperature is too high, coal burner water coolant total flux and each branch flow of coal burner water coolant too low, it is too low that burner water coolant fills with liquid level, liquid level of steam drum is too high or too low, boiler cycle pump is less than two normally work, boiler circulating water flow to coil pipe is too low, shock chamber's liquid level is too low, chilled water flow is too low, washing tower liquid level is too low, dreg-locking hopper recycle pump quits work, instrument air is too low, nitrogen or carbonic acid gas manifold pressure too low, fire inspection Loss Of Signal, stop button.
6. the control method of powdered coal pressuring gasified reaction unit fine coal burner operation according to claim 5, it is characterized in that: wherein a set of feed system occurs that hazardous condition parking step is: (1) closes the first trip valve after the coal burner oxygen of described a set of feed system, the by-pass valve of coal burner oxygen first trip valve, coal burner oxygen flow rate adjusting valve, coal burner oxygen eventually sever valve, fine coal first trip valve, fine coal second trip valve and fine coal the 3rd trip valve, opens coal burner oxygen pipeline blow down valve and fine coal pipeline blow down valve; (2) all trip valves of superheated vapour pipeline and flow trip valve is closed; (3) open fine coal circulation trip valve, standard-sized sheet fine coal flow control valve, standard-sized sheet conveying high-pressure nitrogen flow variable valve, after a predetermined time, close fine coal circulation trip valve, open fine coal circulation line blow down valve; (4) after fine coal circulation line purges certain hour, close fine coal circulation line blow down valve and fine coal flow control valve, close the main blow down valve of coal burner oxygen pipeline, in vapourizing furnace, combustiblesubstance enters oxygen channel, cause oxygen pipeline detonation, coal burner oxygen pipeline low discharge blow down valve and fine coal pipeline blow down valve need be kept to be open mode.
7. the control method of powdered coal pressuring gasified reaction unit fine coal burner operation according to claim 5, it is characterized in that: the step of two cover feed system emergency work simultaneously: all trip valves of coal burner oxygen and oxygen flow rate adjusting valve, all trip valves of fine coal, all trip valves of superheated vapour pipeline and the flow control valve of simultaneously closing two feed systems, open coal burner oxygen pipeline blow down valve and fine coal pipeline blow down valve; Open fine coal circulation trip valve, standard-sized sheet fine coal flow control valve, standard-sized sheet conveying high-pressure nitrogen flow variable valve, after a predetermined time, close fine coal circulation trip valve, open fine coal circulation line blow down valve, after fine coal circulation line purges certain hour, close fine coal circulation line blow down valve and fine coal flow control valve, close coal burner oxygen pipeline blow down valve and fine coal pipeline blow down valve.
8. the control method of powdered coal pressuring gasified reaction unit fine coal burner operation according to claim 1, is characterized in that startup burner runs and boosts to 1.0MPaG and 800 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510395039.2A CN104974798B (en) | 2015-07-07 | 2015-07-07 | Control method for operation of pulverized coal burner of pulverized coal pressure gasification reaction device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510395039.2A CN104974798B (en) | 2015-07-07 | 2015-07-07 | Control method for operation of pulverized coal burner of pulverized coal pressure gasification reaction device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104974798A true CN104974798A (en) | 2015-10-14 |
| CN104974798B CN104974798B (en) | 2019-02-22 |
Family
ID=54271769
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510395039.2A Active CN104974798B (en) | 2015-07-07 | 2015-07-07 | Control method for operation of pulverized coal burner of pulverized coal pressure gasification reaction device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104974798B (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106635172A (en) * | 2015-11-04 | 2017-05-10 | 神华集团有限责任公司 | Jet assembly, multi-burner gasifier and feeding system thereof |
| CN106906004A (en) * | 2017-03-23 | 2017-06-30 | 山东晋煤明水化工集团有限公司 | Pulverized coal gasification control method and pulverized coal gasification device |
| CN107118805A (en) * | 2017-06-15 | 2017-09-01 | 航天长征化学工程股份有限公司 | Gasification system and method for pulverized coal-doped combustible |
| CN107937036A (en) * | 2017-11-30 | 2018-04-20 | 陕西延长石油（集团）有限责任公司 | The system and method for oxygen concentration in a kind of circle fluidized-bed gasification furnace control gasifying agent |
| CN107954218A (en) * | 2017-12-13 | 2018-04-24 | 航天长征化学工程股份有限公司 | Coal grinding and pulverized coal conveying system |
| CN108753362A (en) * | 2018-06-22 | 2018-11-06 | 鲁西化工集团股份有限公司 | A kind of clean type gasifying powder coal device of processing waste water opens/control method for stopping and system |
| CN108951367A (en) * | 2018-09-04 | 2018-12-07 | 中交公局海威工程建设有限公司 | A kind of method that asphalt mixing plant coal changes gas heating |
| CN110173626A (en) * | 2019-06-28 | 2019-08-27 | 恒力石化（大连）有限公司 | A kind of PTA refining plant paste system through transport and mutually for control system |
| CN110760342A (en) * | 2018-07-25 | 2020-02-07 | 新能能源有限公司 | Boiler starting method of circulating fluidized bed boiler |
| CN112592740A (en) * | 2020-12-07 | 2021-04-02 | 新奥科技发展有限公司 | Control method of gasification furnace |
| US20210356933A1 (en) * | 2020-05-12 | 2021-11-18 | Kepco Engineering & Construction Company, Inc. | Method, computer program, and device for determining variable setpoints of plant protection system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20050256592A1 (en) * | 2002-04-05 | 2005-11-17 | Martens Franciscus Johanna A | Method to control a process |
| CN101050386A (en) * | 2007-02-14 | 2007-10-10 | 兖矿集团有限公司 | Method for online lowering of charge for gasification burner tip |
| CN102618332A (en) * | 2011-12-23 | 2012-08-01 | 航天长征化学工程股份有限公司 | Starting/stopping control method and system for powdered coal pressure gasification device |
| CN102618331A (en) * | 2011-12-12 | 2012-08-01 | 航天长征化学工程股份有限公司 | Safety interlocking protection system used for powdered coal pressure gasification process and method |
| CN104449867A (en) * | 2014-11-20 | 2015-03-25 | 水煤浆气化及煤化工国家工程研究中心 | Method for controlling igniter burner of powdered coal pressurized gasifier |
-
2015
- 2015-07-07 CN CN201510395039.2A patent/CN104974798B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20050256592A1 (en) * | 2002-04-05 | 2005-11-17 | Martens Franciscus Johanna A | Method to control a process |
| CN101050386A (en) * | 2007-02-14 | 2007-10-10 | 兖矿集团有限公司 | Method for online lowering of charge for gasification burner tip |
| CN102618331A (en) * | 2011-12-12 | 2012-08-01 | 航天长征化学工程股份有限公司 | Safety interlocking protection system used for powdered coal pressure gasification process and method |
| CN102618332A (en) * | 2011-12-23 | 2012-08-01 | 航天长征化学工程股份有限公司 | Starting/stopping control method and system for powdered coal pressure gasification device |
| CN104449867A (en) * | 2014-11-20 | 2015-03-25 | 水煤浆气化及煤化工国家工程研究中心 | Method for controlling igniter burner of powdered coal pressurized gasifier |
Non-Patent Citations (1)
| Title |
|---|
| 孔德升等: "《四喷嘴水煤浆气工艺关键设备的在线检修》", 《煤炭加工与综合利用》 * |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106635172A (en) * | 2015-11-04 | 2017-05-10 | 神华集团有限责任公司 | Jet assembly, multi-burner gasifier and feeding system thereof |
| CN106906004B (en) * | 2017-03-23 | 2022-08-02 | 山东明泉新材料科技有限公司 | Pulverized coal gasification control method and pulverized coal gasification device |
| CN106906004A (en) * | 2017-03-23 | 2017-06-30 | 山东晋煤明水化工集团有限公司 | Pulverized coal gasification control method and pulverized coal gasification device |
| CN107118805A (en) * | 2017-06-15 | 2017-09-01 | 航天长征化学工程股份有限公司 | Gasification system and method for pulverized coal-doped combustible |
| CN107937036A (en) * | 2017-11-30 | 2018-04-20 | 陕西延长石油（集团）有限责任公司 | The system and method for oxygen concentration in a kind of circle fluidized-bed gasification furnace control gasifying agent |
| CN107937036B (en) * | 2017-11-30 | 2023-08-04 | 陕西延长石油（集团）有限责任公司 | System and method for controlling oxygen concentration in gasifying agent by circulating fluidized bed gasifier |
| CN107954218A (en) * | 2017-12-13 | 2018-04-24 | 航天长征化学工程股份有限公司 | Coal grinding and pulverized coal conveying system |
| CN108753362B (en) * | 2018-06-22 | 2023-08-01 | 鲁西化工集团股份有限公司 | Method and system for controlling start/stop of clean pulverized coal gasification device for treating wastewater |
| CN108753362A (en) * | 2018-06-22 | 2018-11-06 | 鲁西化工集团股份有限公司 | A kind of clean type gasifying powder coal device of processing waste water opens/control method for stopping and system |
| CN110760342A (en) * | 2018-07-25 | 2020-02-07 | 新能能源有限公司 | Boiler starting method of circulating fluidized bed boiler |
| CN110760342B (en) * | 2018-07-25 | 2021-02-19 | 新能能源有限公司 | Boiler starting method of circulating fluidized bed boiler |
| CN108951367A (en) * | 2018-09-04 | 2018-12-07 | 中交公局海威工程建设有限公司 | A kind of method that asphalt mixing plant coal changes gas heating |
| CN110173626A (en) * | 2019-06-28 | 2019-08-27 | 恒力石化（大连）有限公司 | A kind of PTA refining plant paste system through transport and mutually for control system |
| CN110173626B (en) * | 2019-06-28 | 2024-02-13 | 恒力石化（大连）有限公司 | Slurry system intermodal transportation and mutual supply control system of PTA refining device |
| US20210356933A1 (en) * | 2020-05-12 | 2021-11-18 | Kepco Engineering & Construction Company, Inc. | Method, computer program, and device for determining variable setpoints of plant protection system |
| US11698621B2 (en) * | 2020-05-12 | 2023-07-11 | Kepco Engineering & Construction Company, Inc. | Method, non-transitory computer-readable recording medium, and device for determining variable setpoints of a plant protection system |
| CN112592740A (en) * | 2020-12-07 | 2021-04-02 | 新奥科技发展有限公司 | Control method of gasification furnace |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104974798B (en) | 2019-02-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104974798A (en) | Control method for operation of pulverized coal burner of pulverized coal pressure gasification reaction device | |
| CN102618332B (en) | Starting/stopping control method and system for powdered coal pressure gasification device | |
| CN101050386B (en) | Method for online lowering of charge for gasification burner tip | |
| CN101899329B (en) | Systems and methods for treating a stream comprising an undesirable emission gas | |
| CN101096605A (en) | Operation of a high capacity transport gassing reactor | |
| US9399587B2 (en) | System and method for slurry preparation | |
| CN101967406A (en) | Control system and method to operate a quench scrubber system under high entrainment | |
| CN106906004B (en) | Pulverized coal gasification control method and pulverized coal gasification device | |
| CN103452538A (en) | Pure oxygen and natural gas combined heat carrier generator system | |
| SU981348A1 (en) | Method for operating dust fuel gasification plants | |
| CN103897740A (en) | Coal co-gasification method | |
| CA2807985C (en) | Biomass gasifier | |
| CA3155211A1 (en) | Control schemes for thermal management of power production systems and methods | |
| CN209602473U (en) | A kind of low energy consumption coal water slurry gasification system | |
| CN201810401U (en) | Gas caloric value allocation device in underground coal deployment combined-cycle power plant system | |
| WO2013136868A1 (en) | Circulation type gasification furnace | |
| CN106459789B (en) | The starting method of gasification furnace apparatus, integrated gasification combined cycle plant and the furnace apparatus that gasifies | |
| US20200080011A1 (en) | Enriched Air Gasifier | |
| CN105861064A (en) | Coal slurry preheater and coal gasification system and method using the device | |
| US8739549B2 (en) | Systems and methods for feedstock injection | |
| KR101634594B1 (en) | An apparatus for cooling gasification burner using circulation water system cooling facilities of integrated gasification combined cycle by circulating boiler feed water | |
| CN103374419A (en) | System and method for changing pumps for feedstock supply system | |
| CN100494659C (en) | Coal powder gas turbine generation system and process for producing coal powder two-phase flow fuel | |
| CN203395584U (en) | Nitrogen purging system for large medium-low calorific value synthesis-gas gas turbine for integrated gasification combined cycle (IGCC) power station | |
| US9138708B2 (en) | System and method for removing residual gas from a gasification system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20151014 Assignee: Inner Mongolia Baofeng Coal-based New Materials Co.,Ltd. Assignor: CHANGZHENG ENGINEERING Co.,Ltd. Contract record no.: X2023990000054 Denomination of invention: A control method for operation of pulverized coal burner in pulverized coal pressurized gasification reactor Granted publication date: 20190222 License type: Common License Record date: 20230106 |
|
| EE01 | Entry into force of recordation of patent licensing contract | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20151014 Assignee: ANHUI DEBANG CHEMICAL Co.,Ltd. Assignor: CHANGZHENG ENGINEERING Co.,Ltd. Contract record no.: X2023990000607 Denomination of invention: A control method for operation of pulverized coal burner in pulverized coal pressurized gasification reaction device Granted publication date: 20190222 License type: Common License Record date: 20230614 |
|
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20151014 Assignee: ANHUI JINMEI ZHONGNENG CHEMICAL INDUSTRIAL Co.,Ltd. Assignor: CHANGZHENG ENGINEERING Co.,Ltd. Contract record no.: X2023990000838 Denomination of invention: A Control Method for the Operation of Pulverized Coal Burner in a Pulverized Coal Pressurized Gasification Reaction Device Granted publication date: 20190222 License type: Common License Record date: 20230926 |
|
| EE01 | Entry into force of recordation of patent licensing contract | ||
| EE01 | Entry into force of recordation of patent licensing contract | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20151014 Assignee: ANHUI QUANSHENG CHEMICAL Co.,Ltd. Assignor: CHANGZHENG ENGINEERING Co.,Ltd. Contract record no.: X2023990000918 Denomination of invention: A Control Method for the Operation of Coal Burner in a Pulverized Coal Pressurized Gasification Reaction Device Granted publication date: 20190222 License type: Common License Record date: 20231205 |
|
| EE01 | Entry into force of recordation of patent licensing contract | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20151014 Assignee: Anhui Jinhe Industrial Co.,Ltd. Assignor: CHANGZHENG ENGINEERING Co.,Ltd. Contract record no.: X2024980002102 Denomination of invention: A Control Method for the Operation of Coal Burner in a Pulverized Coal Pressurized Gasification Reaction Device Granted publication date: 20190222 License type: Common License Record date: 20240220 |
|
| EE01 | Entry into force of recordation of patent licensing contract | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20151014 Assignee: Xinjiang Zhongneng Lvyuan Chemical Co.,Ltd. Assignor: CHANGZHENG ENGINEERING Co.,Ltd. Contract record no.: X2024980002193 Denomination of invention: A Control Method for the Operation of Coal Burner in a Pulverized Coal Pressurized Gasification Reaction Device Granted publication date: 20190222 License type: Common License Record date: 20240223 |
|
| EE01 | Entry into force of recordation of patent licensing contract | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20151014 Assignee: Inner Mongolia Zhuozheng Coal Chemical Co.,Ltd. Assignor: CHANGZHENG ENGINEERING Co.,Ltd. Contract record no.: X2024980002255 Denomination of invention: A Control Method for the Operation of Coal Burner in a Pulverized Coal Pressurized Gasification Reaction Device Granted publication date: 20190222 License type: Common License Record date: 20240227 |
|
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20151014 Assignee: Fujian Haichen Chemical Co.,Ltd. Assignor: CHANGZHENG ENGINEERING Co.,Ltd. Contract record no.: X2024980007800 Denomination of invention: A Control Method for the Operation of Coal Burner in a Pulverized Coal Pressurized Gasification Reaction Device Granted publication date: 20190222 License type: Common License Record date: 20240624 |