CN114307413A - Calcium carbide purification and dedusting ash treatment system and method - Google Patents
Calcium carbide purification and dedusting ash treatment system and method Download PDFInfo
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- CN114307413A CN114307413A CN202111375839.XA CN202111375839A CN114307413A CN 114307413 A CN114307413 A CN 114307413A CN 202111375839 A CN202111375839 A CN 202111375839A CN 114307413 A CN114307413 A CN 114307413A
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- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000005997 Calcium carbide Substances 0.000 title claims description 45
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 title claims description 45
- 238000000746 purification Methods 0.000 title claims description 33
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 236
- 239000000428 dust Substances 0.000 claims abstract description 194
- 239000007789 gas Substances 0.000 claims abstract description 121
- 239000002893 slag Substances 0.000 claims abstract description 113
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 93
- 229910001873 dinitrogen Inorganic materials 0.000 claims abstract description 50
- 238000002485 combustion reaction Methods 0.000 claims abstract description 28
- 238000011084 recovery Methods 0.000 claims abstract description 22
- 239000002956 ash Substances 0.000 claims description 91
- 239000010881 fly ash Substances 0.000 claims description 28
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 14
- 239000001301 oxygen Substances 0.000 claims description 14
- 229910052760 oxygen Inorganic materials 0.000 claims description 14
- 238000007664 blowing Methods 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 6
- 230000001502 supplementing effect Effects 0.000 claims description 3
- 238000009835 boiling Methods 0.000 claims 2
- 230000000694 effects Effects 0.000 abstract description 6
- 238000003912 environmental pollution Methods 0.000 abstract description 4
- 230000009467 reduction Effects 0.000 abstract description 4
- 230000008569 process Effects 0.000 description 18
- 239000000571 coke Substances 0.000 description 12
- 239000004568 cement Substances 0.000 description 11
- 238000004519 manufacturing process Methods 0.000 description 10
- 230000008901 benefit Effects 0.000 description 8
- 239000000463 material Substances 0.000 description 8
- 239000000243 solution Substances 0.000 description 8
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- 239000007787 solid Substances 0.000 description 6
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- 238000010586 diagram Methods 0.000 description 4
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- 238000001816 cooling Methods 0.000 description 3
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- 238000010521 absorption reaction Methods 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000032258 transport Effects 0.000 description 2
- VZSRBBMJRBPUNF-UHFFFAOYSA-N 2-(2,3-dihydro-1H-inden-2-ylamino)-N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]pyrimidine-5-carboxamide Chemical compound C1C(CC2=CC=CC=C12)NC1=NC=C(C=N1)C(=O)NCCC(N1CC2=C(CC1)NN=N2)=O VZSRBBMJRBPUNF-UHFFFAOYSA-N 0.000 description 1
- YLZOPXRUQYQQID-UHFFFAOYSA-N 3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)-1-[4-[2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidin-5-yl]piperazin-1-yl]propan-1-one Chemical compound N1N=NC=2CN(CCC=21)CCC(=O)N1CCN(CC1)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F YLZOPXRUQYQQID-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
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- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
- Y02A50/2351—Atmospheric particulate matter [PM], e.g. carbon smoke microparticles, smog, aerosol particles, dust
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- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The system comprises a first gas storage tank, a nitrogen compressor, a second gas storage tank, a dust storage bin, a conveying pump, a collection bin, a first bag-type dust remover, a second bag-type dust remover, a fluidized bed furnace, a dust removal unit, a slag collection bin and a Roots blower; the method comprises the following steps: the nitrogen in the first gas storage tank is compressed and input into the second gas storage tank through the nitrogen compressor, the dust in the dust storage bin is conveyed to the collection bin through the nitrogen positive pressure by the conveying pump, then the nitrogen is recovered to the first gas storage tank through the first bag-type dust collector and the second bag-type dust collector to participate in the next circulation, the dust is blown to the fluidized bed furnace through the air conditioner to be combusted, and the slag obtained by combustion is discharged to the truck through the negative pressure slag suction. This application purifies the dust removal ash postcombustion with the carbide, has realized dust removal ash centralized processing, recycles through setting up nitrogen gas circulation recovery system and slag and has played energy saving and emission reduction effect, has reduced environmental pollution simultaneously, has improved the security that the dust removal ash was handled.
Description
Technical Field
The application relates to the technical field of calcium carbide production, in particular to a calcium carbide purification and dust removal treatment system and method.
Background
In order to protect the environment, the tail gas of the calcium carbide furnace is generally required to be dedusted and recycled. After the tail gas of the calcium carbide furnace is subjected to multi-stage cooling and dedusting, the collected solid dust is generally called calcium carbide purification dedusting ash. The purified ash has the characteristics of fine granularity, light specific gravity, low carbon content, high volatile content, low ignition point and easy dust emission, and because the components such as oxides and the like in the ash have the combustion-supporting effect, the ash is easy to spontaneously combust when meeting air. And dust is very easy to cause in the processes of loading, unloading and transportation, the surrounding working environment is polluted, and certain potential safety hazards of ignition exist in the transportation process.
The original calcium carbide purification dust removal ash is piled up after being transported to a slag yard by a vehicle, but due to the spontaneous combustion characteristic of the calcium carbide purification dust removal ash, spraying is needed after piling. Because the particle size is small, the temperature is high, and the dust comes all around in the spraying process, the environmental protection pressure is extremely high. And because of the high-temperature environment, the danger to the operators who spray and the like is great. Today with increasingly strict environmental requirements, the treatment of calcium carbide purification dedusting ash has several difficulties as follows: large dust, large environmental pollution, large potential safety hazard, high energy consumption, high cost, large occupied area of treatment equipment and the like.
Disclosure of Invention
The application provides a carbide purifies dust removal ash processing system and method for solve above-mentioned carbide and purify the problem that the dust removal ash processing in-process easily spontaneous combustion, raise dust and to environmental pollution are big, realized dust removal ash centralized processing, solve the secondary pollution that unloads ash, fortune ash caused, greatly reduced intensity of labour, reduced raise dust and the manpower and materials and the expense that sprinkle dust fall and transport, improved the production environment simultaneously.
In a first aspect, the present application provides a calcium carbide purifies dust removal ash processing system, includes: the device comprises a first gas storage tank, a nitrogen compressor, a second gas storage tank, an ash storage bin, a delivery pump, a collection bin, a first bag-type dust remover, a second bag-type dust remover, a fluidized bed furnace, a dust removal unit, a slag collection bin and a Roots blower.
The top of the first gas storage tank is provided with a nitrogen gas inlet, the nitrogen gas inlet is connected with a public nitrogen pipe network through a nitrogen gas conveying pipeline and used for inputting nitrogen gas into the system, a gas outlet of the first gas storage tank is fixedly connected with a gas inlet of a nitrogen gas compressor through the nitrogen gas conveying pipeline, a gas outlet of the nitrogen gas compressor is fixedly connected with a gas inlet of a second gas storage tank through the nitrogen gas conveying pipeline, a discharge port of the ash storage bin and a gas outlet of the second gas storage tank are respectively fixedly connected with a feed port of a conveying pump, and a discharge port of the collection bin and a discharge port of the conveying pump are fixedly connected through a dedusting ash conveying pipeline.
The top of the collecting bin is fixedly provided with a first bag-type dust remover, a clean gas outlet of the first bag-type dust remover is fixedly connected with a dust gas inlet of a second bag-type dust remover, and a clean gas outlet of the second bag-type dust remover is fixedly connected with a gas inlet of a first gas storage tank through a nitrogen recovery pipeline.
The feed inlet of the fluidized bed furnace is fixedly connected with the collection bin, the fluidized bed furnace is fixedly connected with the dust gas inlet of the dust removal unit, the ash outlet of the dust removal unit is fixedly connected with the feed inlet of the slag collection bin, and the purified gas outlet of the dust removal unit is fixedly connected with the Roots blower.
Optionally, a back pressure device is arranged between the delivery pump and the calcium carbide furnace to prevent negative pressure of the ash storage bin, and an emergency ash discharge port is arranged on the lower portion of the ash storage bin to facilitate dust removal during system failure.
Optionally, an oxygen content analyzer is arranged on the nitrogen recovery pipeline between the second bag-type dust collector and the first gas storage tank, and the oxygen content analyzer is used for detecting oxygen content in recovered nitrogen.
Optionally, the lower part of the collection bin is provided with a compressed nitrogen inlet and an ash discharge port, the compressed nitrogen inlet is used for supplementing compressed nitrogen to keep the internal pressure difference of the collection bin, and a dome valve is arranged on a discharge pipeline at the bottom of the collection bin.
Optionally, after the outlet of the dome valve is connected with the air outlet of the air conditioner, the outlet is fixedly connected with the feed inlet of the distributor arranged on the fly ash conveying pipeline, so that the fly ash is conveyed to the distributor through positive pressure air flow, and the air inlet of the air conditioner is compressed air.
Optionally, a discharge port of the distributor is fixedly connected with a feed port of the fluidized bed furnace, the distributor is used for distributing the fly ash to the fluidized bed furnace, and the fluidized bed furnace is used for burning the fly ash.
Optionally, a coarse slag hopper and a fine slag hopper are arranged at the bottom of the fluidized bed furnace and used for collecting slag obtained after combustion of the fluidized bed furnace, the coarse slag hopper and the fine slag hopper are connected to the same slag suction pipeline through a switching valve to discharge the slag, and a feed inlet of the dust removal unit is fixedly connected with the slag suction pipeline and used for removing dust from the slag discharged from the slag suction pipeline.
Optionally, the dust removal unit includes: the device comprises a first cyclone dust collector, a second cyclone dust collector and a third bag-type dust collector, wherein the first cyclone dust collector, the second cyclone dust collector and the third bag-type dust collector are sequentially connected in series along the gas conveying direction; the ash outlet of the third bag-type dust collector is fixedly connected with the feed inlet of the slag collecting bin.
Optionally, the pressure of the compressed nitrogen for the system is greater than or equal to 0.6MPa, and the pressure of the compressed air is greater than or equal to 0.4 MPa.
On the other hand, the application provides a calcium carbide purification and dust removal ash treatment method, which applies the calcium carbide purification and dust removal ash treatment system and comprises the following steps:
s401, collecting nitrogen into a first gas storage tank, and inputting the nitrogen collected by the first gas storage tank into a nitrogen compressor;
s402, pressurizing nitrogen by a nitrogen compressor, and inputting the nitrogen into a second gas storage tank;
s403, conveying the dust in the dust storage bin to a collection bin through a conveying pump through positive pressure of nitrogen in a second gas storage tank;
s404, removing dust of the nitrogen through a first bag-type dust remover and a second bag-type dust remover, and conveying the nitrogen to a first gas storage tank through a nitrogen recovery pipeline so as to participate in the next calcium carbide purification and dust removal treatment cycle;
s405, blowing the dust removal ash to a fluidized bed furnace for combustion through an air conditioner at the bottom of the collection bin;
and S406, discharging the slag obtained by combustion out of the furnace through negative pressure slag absorption and loading, and finishing secondary combustion treatment of calcium carbide purification dust removal ash.
According to the calcium carbide purification and dedusting ash treatment system and method, the nitrogen conveying system is adopted to convey the calcium carbide purification and dedusting ash, so that the dedusting ash is prevented from spontaneous combustion in the conveying process, the safety of the treatment environment is improved, and the environmental protection pressure is reduced; meanwhile, nitrogen is recycled, and collected dedusting ash is sprayed into a hearth of the fluidized bed furnace by compressed air to be used as fuel for combustion, so that the combustion usage amount of the semi coke is reduced, the combusted fluidized bed furnace slag can be directly sent into a cement plant to produce cement, the effects of energy conservation and emission reduction are achieved, the purpose of centralized treatment of the dedusting ash is also achieved, and the labor intensity is greatly reduced.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present application, and other drawings can be obtained by those skilled in the art without creative efforts.
Fig. 1 is a schematic structural diagram of a calcium carbide purification and dust removal treatment system according to an embodiment of the present application;
fig. 2 is a schematic structural view of a calcium carbide purification and dust removal treatment system according to another embodiment of the present application;
FIG. 3 is a schematic structural diagram of a dust removal unit according to another embodiment of the present disclosure;
fig. 4 is a process flow chart of a calcium carbide purification and dust removal treatment method according to another embodiment of the present application.
Description of reference numerals:
1: a first gas storage tank;
101: an air inlet;
2: a nitrogen compressor;
3: a second gas tank;
4: an ash storage bin;
41: a delivery pump;
42: a back pressure device;
43: an emergency ash discharge port;
44: a calcium carbide furnace;
5: a collection bin;
51: a compressed nitrogen inlet;
52: an ash discharge port;
6: dome valve
7: a first bag-type dust collector;
8: a second bag-type dust collector;
9: an oxygen analyzer;
10: an air conditioner (AMS);
11: a dispenser;
12: a fluidized bed furnace;
121: a coarse slag hopper;
122: a fine slag hopper;
13: a dust removal unit;
131: a first cyclone;
132: a second cyclone;
133: a third bag-type dust collector;
14: a slag collecting bin;
15: roots blower.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present application clearer, the technical solutions in the embodiments of the present application are clearly and completely described below, and it is obvious that the described embodiments are a part of the embodiments of the present application, but not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
Fig. 1 is a process flow diagram of a calcium carbide purification and dust removal treatment system according to an embodiment of the present application, and as shown in fig. 1, the embodiment includes:
the device comprises a first gas storage tank 1, a nitrogen compressor 2, a second gas storage tank 3, an ash storage bin 4, a conveying pump 41, a collection bin 5, a first bag-type dust remover 7, a second bag-type dust remover 8, a fluidized bed furnace 12, a dust removal unit 13, a slag collection bin 14 and a Roots blower 15.
1 top of first gas holder is provided with nitrogen gas air inlet 101, nitrogen gas air inlet 101 passes through nitrogen gas pipeline and is connected with public nitrogen gas pipe network, be used for to system internal input nitrogen gas, nitrogen gas pipeline and nitrogen compressor 2's air inlet fixed connection is passed through to first gas holder 1's gas outlet, nitrogen gas pipeline fixed connection is passed through with second gas holder 3's air inlet to nitrogen compressor 2's gas outlet, the discharge gate of ash storage storehouse 4 and second gas holder 3's gas outlet respectively with delivery pump 41's feed inlet fixed connection, collect and pass through dust removal conveying pipeline fixed connection between storehouse 5's the feed inlet and delivery pump 41's the discharge gate.
Specifically, nitrogen gas conveying is adopted in the conveying process because calcium carbide purified ash has the risk of spontaneous combustion and the danger can occur if air is mixed in during the conveying process and the storage process. Nitrogen enters the first gas storage tank 1 through the gas inlet 101 arranged at the top of the first gas storage tank 1 for collection, and is connected with a public nitrogen pipe network through a nitrogen conveying pipeline, and the public nitrogen pipe network is a public nitrogen conveying pipe network in the whole production plant area and is used for inputting nitrogen into the system. The gas outlet of first gas holder 1 passes through nitrogen gas conveying line and nitrogen compressor 2's air inlet fixed connection, and nitrogen compressor 2 also can set up two according to the operating mode, and two nitrogen compressor one is equipped with one, carries out the pressure boost with nitrogen gas reserve to satisfy the nitrogen gas quantity that carries the dust removal ash in the system, nitrogen compressor is screw compressor. Gas outlet and the air inlet fixed connection of second gas holder 3 of nitrogen gas compressor 2, second gas holder 3 is used for saving compressed nitrogen, play the effect of buffering simultaneously, the feed inlet of delivery pump 41 respectively with the discharge gate in storage ash bin 4 and the gas outlet fixed connection of second gas holder 3, open delivery pump 41, the fly ash in storage ash bin 4 is carried to collecting bin 5 through the nitrogen gas malleation, adopt nitrogen gas to carry the loss of having avoided the fly ash in transportation process, the potential safety hazard has been reduced simultaneously.
The top of the collection bin 5 is fixedly provided with a first bag-type dust remover 7, a clean gas outlet of the first bag-type dust remover 7 is fixedly connected with a dust gas inlet of a second bag-type dust remover 8, and a clean gas outlet of the second bag-type dust remover 8 is fixedly connected with a gas inlet of the first gas storage tank 1 through a nitrogen recovery pipeline.
Specifically, the dust of the fine particles in the collection bin 5 enters the first bag-type dust collector 7, and is filtered through the first bag-type dust collector 7, the first bag-type dust collector 7 can be designed to be a plurality of according to the working conditions of the dust collection amount, the filtered dust of the fine particles falls into the collection bin 5 again, and the dust collection is filtered and the nitrogen gas is purified for the first time. The nitrogen gas after will purifying lets in the dirt gas entry of second sack cleaner 8 through the net gas export of first sack cleaner 7, second sack cleaner 8 filters the nitrogen gas after the first time purifies once more, the net gas export of passing through second sack cleaner 8 with the nitrogen gas after filtering is imported to first gas holder 1 through nitrogen gas recovery pipeline, the nitrogen gas that will retrieve is in first gas holder 1 storage, be used for carrying out next cycle, the nitrogen gas rate of recovery reaches more than 90%, the nitrogen gas use amount has been practiced thrift, the production cost is reduced, adopt nitrogen gas closed loop circulation to avoid the spontaneous combustion that the entering of air arouses in the dust removal ash transportation process simultaneously.
The feed inlet of the fluidized bed furnace 12 is fixedly connected with the collection bin 5, the fluidized bed furnace 12 is fixedly connected with the dust gas inlet of the dust removal unit 13, the ash outlet of the dust removal unit 13 is fixedly connected with the feed inlet of the slag collection bin 14, and the clean gas outlet of the dust removal unit 13 is fixedly connected with the Roots blower 15.
Specifically, the fly ash in the collection bin 5 is conveyed to the fluidized bed furnace 12 through a fly ash conveying pipeline, and part of the blue charcoal is replaced in the fluidized bed furnace 12 for incineration, so that heat is provided for production, the utilization rate of the blue charcoal is saved, and the production cost is reduced. The slag obtained after the fly ash is combusted in the fluidized bed furnace 12 is subjected to negative pressure slag suction to a dust removal unit for dust removal and then is discharged into a slag collection bin 14, and the gas generated after the slag is subjected to dust removal by the dust removal unit is discharged through a Roots blower 15, wherein the slag obtained after the fly ash is combusted can be loaded and conveyed to a cement plant to serve as a raw material or an outer pin for producing cement, so that waste recycling is achieved, and the resource utilization rate is improved.
This embodiment has reached the purpose to carbide purification dust removal ash centralized processing through adopting nitrogen gas to carry the dust removal ash through above-mentioned scheme, compares and transports in direct loading, has avoided the dust removal ash to take place vehicle damage, personnel incident such as be injured because of spontaneous combustion in the air in transportation process, has solved the raise dust that unloads ash, fortune ash and has caused and to the big problem of environmental pollution. And finally, negative-pressure slag suction is carried out on the slag, the slag is used as a raw material for producing cement, the resource recycling is realized, the labor intensity is greatly reduced, and good environmental benefit and economic benefit are achieved.
Optionally, a back pressure device 42 is arranged between the delivery pump 41 and the calcium carbide furnace 44 to prevent negative pressure of the ash storage bin 4, and an emergency ash discharge port 43 is arranged at the lower part of the ash storage bin 4 to facilitate dust discharge when a system fails.
Specifically, fig. 2 is a schematic structural view of a calcium carbide purification and dust removal treatment system provided by another embodiment of the present application, as shown in fig. 2, a back pressure device 42 is connected between a delivery pump 41 and a calcium carbide furnace 44, so as to prevent negative pressure in the ash storage bin 4, so that the dust removal is more smoothly conveyed, and an emergency ash discharge port 43 is arranged at the lower part of the ash storage bin 4, so that the dust removal in the ash storage bin 4 can be conveniently discharged through the emergency ash discharge port 43 when the system fails and needs emergency parking.
Optionally, an oxygen analyzer 9 is arranged on the nitrogen recovery pipeline between the second bag-type dust collector 8 and the first gas storage tank 1, and the oxygen analyzer 9 is used for detecting the oxygen content in the recovered nitrogen.
Specifically, the nitrogen recovery pipeline is provided with an oxygen analyzer 9, the oxygen analyzer 9 is provided with output feedback, when the oxygen content in the nitrogen in the recovery pipeline exceeds a set value by 3%, the alarm feedback is carried out, and nitrogen supplement operation is required until the oxygen content is reduced to the set value.
Optionally, the lower part of the collecting bin 5 is provided with a compressed nitrogen inlet 51 and an ash discharge port 52, the compressed nitrogen inlet 51 is used for supplementing compressed nitrogen to maintain the internal pressure difference of the collecting bin 5, and a dome valve 6 is arranged on a discharge pipeline at the bottom of the collecting bin 5.
Specifically, gather storehouse 5 through compression nitrogen gas entry 51 and supply nitrogen gas to keep gathering the interior pressure differential of storehouse 5, make the dust removal carry more smoothly, be provided with dome valve 6 on gathering 5 bottom discharging pipes for the dust removal in the storehouse 5 is collected in the discharge has prevented that the material is difficult to drop and takes place the bridge in 5 cone portions of gathering the storehouse.
Optionally, after the outlet of the dome valve 6 is connected with the air outlet of the air conditioner 10, the outlet is fixedly connected with the feed inlet of the distributor 11 arranged on the fly ash conveying pipeline, so that the fly ash is conveyed to the distributor 11 through positive pressure air flow, and the air inlet of the air conditioner 10 is compressed air.
Specifically, the outlet of the dome valve 6 is connected to the air outlet of the air conditioner 10, and the fly ash discharged from the outlet of the dome valve 6 is blown from the dome valve 6 to the distributor 11 by adjusting the air flow rate of the air conditioner 10, and the distributor 11 may be provided in one or more number. The air source blown by the air conditioner 10 uses compressed air to continuously and stably blow the fly ash into the fluidized bed furnace.
Optionally, a discharge port of the distributor 11 is fixedly connected with a feed port of the fluidized bed furnace 12, the distributor 11 is used for distributing the fly ash to the fluidized bed furnace 12, and the fluidized bed furnace 12 is used for incinerating the fly ash.
Specifically, carry the fly ash to distributor 11 through air conditioner 10, spout and burn to fluidized bed furnace 12 the inside after being distributed by distributor 11 again, the fly ash burns in fluidized bed furnace 12, provide the heat source for the system, wherein, because according to the difference of season and production load, the quantity of the fluidized bed furnace of putting into operation is also different, fluidized bed furnace 12 can set up one or more, the quantity of fluidized bed furnace 12 corresponds with the quantity of distributor 11, realized the concentrated utilization to the fly ash, adopt the fly ash to carry the jetting mode of being responsible for + distributor + branch pipe, can satisfy 3 fluidized bed furnaces of at most jetting simultaneously, also can satisfy only 1 fluidized bed furnace jetting.
Wherein, during the injection process, the amount of the injected gas can be adjusted by the air conditioner 10 according to the amount of the injected gas and the amount of the fluidized bed boiler 12 and the distributor 11The blowing air quantity is controlled to be 0.08-0.12Nm3And min, so that the pipeline is prevented from being worn by overlarge air quantity, the pipeline blockage caused by the undersize air quantity is also avoided, the equipment utilization rate is realized more efficiently, and single-outlet multipoint spraying is realized.
Optionally, the bottom of the fluidized bed furnace 12 is provided with a coarse slag hopper 121 and a fine slag hopper 122 for collecting slag obtained after combustion of the fluidized bed furnace 12, the coarse slag hopper 121 and the fine slag hopper 122 are connected to the same slag suction pipeline through a switching valve to discharge the slag, and a feed inlet of the dust removal unit 13 is fixedly connected with the slag suction pipeline for removing dust from the slag discharged from the slag suction pipeline.
Specifically, the coarse slag hopper 121 and the fine slag hopper 122 are used for collecting slag obtained after combustion of the fluidized bed furnace 12, and the collecting hopper is made as large as possible according to field conditions so as to adjust the operation efficiency of slag discharge pneumatic transmission. Wherein, the slag charge particle diameter in the coarse slag hopper 121 is thicker, smash the slag charge in the coarse slag hopper 121 to particle diameter 1-2mm, convenient follow-up cement manufacture that is used for, be connected to same root through the diverter valve with coarse slag hopper 121 and thin slag hopper 122 afterwards and inhale the slag pipe way, pass through negative pressure suction to dust removal unit 13 with the slag, every fluidized bed furnace corresponds one and inhales the slag pipeline, dust removal unit 13 not only removes dust to inhaling slag pipeline exhaust slag, can play the effect to the slag cooling simultaneously, make things convenient for the slag to discharge after the loading.
Optionally, the dust removing unit 13 includes: the dust collector comprises a first cyclone dust collector 131, a second cyclone dust collector 132 and a third bag-type dust collector 133, wherein the first cyclone dust collector 131, the second cyclone dust collector 132 and the third bag-type dust collector 133 are sequentially connected in series along the gas conveying direction, a dust gas inlet of the first cyclone dust collector 131 is fixedly connected with a slag suction pipeline, a clean gas outlet of the third bag-type dust collector 133 is fixedly connected with a Roots blower 15, and an ash outlet of the third bag-type dust collector 133 is fixedly connected with a feed inlet of a slag collecting bin 14.
Specifically, fig. 3 is a schematic structural diagram of the dust removal unit, as shown in fig. 3, a dust-gas inlet of the first cyclone 131 is fixedly connected to a slag suction pipeline, the slag is subjected to gas-solid separation in the first cyclone 131, the solid slag is discharged into the slag collection bin 14, the gas is air and slag with a small particle size, the gas is input into the second cyclone 132 for gas-solid separation again, the solid slag separated again by the second cyclone 132 is discharged into the slag collection bin 14, the gas separated again is input into the third bag-type dust collector 133 for filtration, the filtered solid particles are discharged into the slag collection bin 14, the filtered gas is discharged through the roots blower 15, and the pressure of the roots blower 15 is-49 KPa-0 KPa. The slag materials of the slag suction pipeline are dedusted by the first cyclone dust collector 131, the second cyclone dust collector 132 and the third bag-type dust collector 133, so that the slag materials are completely collected to the slag collecting bin for reutilization, the temperature of the slag materials is reduced, and the influence on subsequent external discharge loading vehicles due to overhigh temperature of the slag materials is avoided.
Wherein, because in the slag transportation process, all pipe-line system are closed system, and only a small amount of air, can lead to getting into to inhale the slag pipeline and the slag storehouse slag is in a higher temperature all the time, leads to pipeline and slag storehouse outer wall high temperature, can inhale the slag pipeline according to the operating mode increase. And the air needs to be sucked in the conveying process, the temperature of the slag can be greatly reduced under the influence of the temperature of the external air, the temperature of a slag sucking pipeline and a slag bin is ensured not to be too high, the temperature of the slag outlet of the fluidized bed furnace 12 is more than or equal to 700 ℃, the conveying principle of large air intake and small-batch material sucking quantity is adopted, and the first cyclone dust collector 131, the second cyclone dust collector 132 and the third bag dust collector 133 are adopted, so that the temperature of the slag can be quickly reduced, and the temperature of the slag can be reduced to about 55 ℃.
Optionally, the pressure of the compressed nitrogen for the system is greater than or equal to 0.6MPa, and the pressure of the compressed air is greater than or equal to 0.4 MPa.
Specifically, the pressure of compressed nitrogen in the system is more than or equal to 0.6MPa so as to meet the requirement of conveying the dust, the pressure in the system is kept stable, and the pressure of compressed air is controlled to be more than or equal to 0.4MPa so as to control the dust not to generate spontaneous combustion or a small amount of spontaneous combustion in the blowing incineration process.
Fig. 4 is a process flow chart of a calcium carbide purification and dust removal ash treatment method provided in an embodiment of the present application, and as shown in fig. 4, the method is applied to the calcium carbide purification and dust removal ash treatment system in any one of the embodiments, and the method in this embodiment includes:
s401, collecting the nitrogen into a first gas storage tank, and inputting the nitrogen collected by the first gas storage tank into a nitrogen compressor.
And S402, pressurizing the nitrogen by a nitrogen compressor, and inputting the nitrogen into a second gas storage tank.
And S403, conveying the dust in the dust storage bin to a collection bin through a conveying pump through positive pressure of nitrogen in a second gas storage tank.
S404, removing dust of the nitrogen through the first bag-type dust remover and the second bag-type dust remover, and inputting the nitrogen into the first gas storage tank through the nitrogen recovery pipeline to participate in the next calcium carbide purification and dust removal treatment cycle.
And S405, blowing the dust removal ash to a fluidized bed furnace for combustion through an air conditioner at the bottom of the collection bin.
And S406, discharging the slag obtained by combustion out of the furnace through negative pressure slag absorption and loading, and finishing secondary combustion treatment of calcium carbide purification dust removal ash.
Wherein, nitrogen enters a first gas storage tank through a gas inlet arranged at the top of the first gas storage tank for collection, the collected nitrogen is pressurized by a nitrogen compressor and then is input into a second gas storage tank for storage, the dust in an ash storage bin is conveyed to a collection bin through a conveying pump by positive pressure of compressed nitrogen in the second gas storage tank, the dust is filtered by a first bag-type dust collector arranged at the top of the collection bin and a second bag-type dust collector arranged on a nitrogen recovery pipeline, the filtered nitrogen is conveyed to the first gas storage tank through the recovery pipeline to participate in the next cycle, meanwhile, the dust is conveyed to a distributor by adjusting the pressure of compressed air through an air regulator at the bottom of the collection bin, and then is blown to a fluidized bed furnace for combustion by the distributor, finally, slag obtained by combustion is sucked to a dust removal unit through negative pressure for dust removal and temperature reduction, and is discharged to an external pin or conveyed to a cement plant for reuse as a raw material for producing cement, the centralized treatment of the calcium carbide purification dedusting ash is completed, the effects of energy conservation and emission reduction are achieved, the production cost is also saved, the consumption of manpower and material resources is reduced, and the environmental protection pressure is reduced.
The technical solution of the present application is illustrated in detail by the following specific examples.
Example 1
The calcium carbide purification dedusting ash is treated by adopting the following steps and systems:
s401, enabling nitrogen to enter a first gas storage tank through a gas inlet formed in the top of the first gas storage tank for collection, and compressing the collected nitrogen through a nitrogen compressor.
And S402, after being compressed by a nitrogen compressor, the nitrogen is input into a second gas storage tank for storage.
And S403, conveying the dust in the dust storage bin to a collection bin through a conveying pump by positive pressure of compressed nitrogen in a second gas storage tank.
S404, filtering the dust through a first bag-type dust collector arranged at the top of the collecting bin and a second bag-type dust collector arranged on the nitrogen recovery pipeline, and delivering the filtered nitrogen to a first gas storage tank through the recovery pipeline to participate in next circulation.
S405, blowing the filtered dust removal ash to a fluidized bed furnace through compressed air for combustion, wherein the number of the fluidized bed furnaces is 1.
And S406, finally, sucking the slag obtained by combustion to a dust removal unit through negative pressure, removing dust and cooling, and discharging the slag to a truck for external sale or conveying the slag to a cement plant for reutilization as a raw material for producing cement.
Example 2
The calcium carbide purification dedusting ash is treated by adopting the following steps and systems: the only difference from example 1 is that: the number of the fluidized bed furnaces is 2.
Example 3
The calcium carbide purification dedusting ash is treated by adopting the following steps and systems: the only difference from example 1 is that: the number of the fluidized bed furnaces is 3.
Comparative example 1
The calcium carbide purification dedusting ash is treated by adopting the following steps and systems: and (3) directly loading and discharging calcium carbide purification dedusting ash at the calcium carbide furnace outlet.
Experimental example 1
Compared with the amount of the semi-coke used, the nitrogen recovery rate and the generated economic benefits in the comparative example 1, the method for burning the semi-coke in the practical operation process can be used for calculating the use amount, the nitrogen recovery rate and the generated economic benefits of the semi-coke in the examples 1 to 3, 80% of the fly ash can be burned at the highest time, only 20% of the semi-coke needs to be burned, and the semi-coke can be stably operated. The calorific value of the semi-coke is 5600kcal/kg, the lower calorific value of the fly ash is 4.27MJ/kg, which is about 1017kcal/kg, therefore, 1kg of purified ash can be calculated to be equivalent to saving 0.18kg of the semi-coke when being burnt. According to 60T of dust removal ash generated every day, 8-10T of semi-coke powder is saved, about 500 yuan per ton of semi-coke powder is saved, 5000 yuan per day is generated, about 30-40T of slag generated after burning of dust removal ash is saved, about 40-50 yuan per ton is generated, 2000 yuan per day is generated, 7000 yuan per day is generated, and 3600 yuan per day is generated, and the results shown in the table I are obtained according to the maximum calculation of annual economic benefits.
Watch 1
| Number of fluidized bed furnaces | Utilization rate of semi coke | Recovery rate of nitrogen | Economic benefit/ten thousand | |
| Example 1 | 1 | 20％ | 90％ | 85.2 |
| Example 2 | 2 | 23％ | 92％ | 107.3 |
| Example 3 | 3 | 30％ | 95％ | 255.5 |
| Comparative example 1 | 0 | 0 | - | - |
As can be seen from the table I, the calcium carbide purified dedusting ash is conveyed to a fluidized bed furnace for incineration, so that the concentrated treatment of the calcium carbide purified dedusting ash is realized, the incineration usage amount of the semi-coke is reduced, and the incineration usage amount of the semi-coke is equivalent to 20% -30% of the incineration usage amount of the semi-coke when the dedusting ash is not added; the nitrogen is recycled, the recovery rate is up to more than 90%, the cost is greatly saved, and the production intensity of workers is reduced; meanwhile, furnace slag obtained by burning the fly ash is reused as a raw material for producing cement, so that great economic benefits are brought to enterprises.
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present application, and not for limiting the same; although the present application has been described in detail with reference to the foregoing embodiments, it will be understood by those skilled in the art; the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present application.
Claims (10)
1. The utility model provides a carbide purifies dust removal ash processing system which characterized in that includes: the device comprises a first gas storage tank (1), a nitrogen compressor (2), a second gas storage tank (3), an ash storage bin (4), a conveying pump (41), a collection bin (5), a first bag-type dust remover (7), a second bag-type dust remover (8), a fluidized bed furnace (12), a dust removal unit (13), a slag collection bin (14) and a Roots blower (15);
the system is characterized in that a nitrogen gas inlet (101) is formed in the top of the first gas storage tank (1), the nitrogen gas inlet (101) is connected with a public nitrogen gas pipe network through a nitrogen gas conveying pipeline and used for inputting nitrogen gas into the system, a gas outlet of the first gas storage tank (1) is fixedly connected with a gas inlet of the nitrogen gas compressor (2) through the nitrogen gas conveying pipeline, a gas outlet of the nitrogen gas compressor (2) is fixedly connected with a gas inlet of the second gas storage tank (3) through the nitrogen gas conveying pipeline, a discharge hole of the ash storage bin (4) and a gas outlet of the second gas storage tank (3) are respectively fixedly connected with a feed inlet of the conveying pump (41), and a feed inlet of the collection bin (5) is fixedly connected with a discharge hole of the conveying pump (41) through a dedusting ash conveying pipeline;
the first bag-type dust collector (7) is fixedly mounted at the top of the collection bin (5), a clean gas outlet of the first bag-type dust collector (7) is fixedly connected with a dust gas inlet of the second bag-type dust collector (8), and a clean gas outlet of the second bag-type dust collector (8) is fixedly connected with a gas inlet of the first gas storage tank (1) through a nitrogen recovery pipeline;
the feeding port of the fluidized bed furnace (12) is fixedly connected with the collecting bin (5), the fluidized bed furnace (12) is fixedly connected with the dust and gas inlet of the dust removing unit (13), the ash outlet of the dust removing unit (13) is fixedly connected with the feeding port of the slag collecting bin (14), and the clean gas outlet of the dust removing unit (13) is fixedly connected with the Roots blower (15).
2. The system according to claim 1, characterized in that a back pressure device (42) is arranged between the delivery pump (41) and the calcium carbide furnace (44) to prevent negative pressure of the ash storage bin (4); the lower part of the ash storage bin (4) is provided with an emergency ash discharge port (43), so that the ash can be discharged conveniently when the system fails.
3. The system according to claim 1, wherein an oxygen analyzer (9) is arranged on a nitrogen recovery pipeline between the second bag-type dust collector (8) and the first gas storage tank (1), and the oxygen analyzer (9) is used for detecting the oxygen content in the recovered nitrogen.
4. The system according to claim 1, characterized in that the collecting bin (5) is provided with a compressed nitrogen inlet (51) and an ash discharge port (52) at the lower part, the compressed nitrogen inlet (51) is used for supplementing compressed nitrogen to maintain the internal pressure difference of the collecting bin (5), and a dome valve (6) is arranged on a discharge pipeline at the bottom of the collecting bin (5).
5. The system according to claim 4, characterized in that the outlet of the dome valve (6) is connected with the outlet of the air conditioner (10) and then fixedly connected with the inlet of the distributor (11) arranged on the conveying pipeline of the fly ash, so as to convey the fly ash to the distributor (11) through positive pressure airflow, and the inlet air of the air conditioner (10) is compressed air.
6. The system according to claim 5, characterized in that the discharge port of the distributor (11) is fixedly connected with the feed port of a fluidized bed furnace (12), the distributor (11) is used for distributing the fly ash to the fluidized bed furnace (12), and the fluidized bed furnace (12) is used for incinerating the fly ash.
7. The system according to claim 1, characterized in that the bottom of the boiling furnace (12) is provided with a coarse slag hopper (121) and a fine slag hopper (122) for collecting slag obtained after combustion of the boiling furnace (12); the coarse slag hopper (121) and the fine slag hopper (122) are connected to the same slag suction pipeline through a switching valve to discharge the slag, and a feed inlet of the dust removal unit (13) is fixedly connected with the slag suction pipeline and used for removing dust from the slag discharged from the slag suction pipeline.
8. The system according to claim 1, wherein the dust removal unit (13) comprises: the device comprises a first cyclone dust collector (131), a second cyclone dust collector (132) and a third bag-type dust collector (133), wherein the first cyclone dust collector (131), the second cyclone dust collector (132) and the third bag-type dust collector (133) are sequentially connected in series along the gas conveying direction, a dust gas inlet of the first cyclone dust collector (131) is fixedly connected with a slag suction pipeline, and a clean gas outlet of the third bag-type dust collector (133) is fixedly connected with a Roots blower (15); and an ash outlet of the third bag-type dust collector (133) is fixedly connected with a feed inlet of the slag collecting bin (14).
9. The system of claim 4 or 5, wherein the pressure of the compressed nitrogen for the system is 0.6MPa or more, and the pressure of the compressed air is 0.4MPa or more.
10. A calcium carbide purification and dust removal ash treatment method is applied to the calcium carbide purification and dust removal ash treatment system of any one of claims 1 to 9, and the method comprises the following steps:
collecting nitrogen gas into the first gas storage tank, and inputting the nitrogen gas collected by the first gas storage tank to the nitrogen gas compressor;
after the nitrogen is pressurized by the nitrogen compressor, inputting the nitrogen into the second gas storage tank;
conveying the dust removed in the dust storage bin to the collection bin through the conveying pump by the positive pressure of the nitrogen in the second gas storage tank;
dedusting the nitrogen gas by the first bag-type dust remover and the second bag-type dust remover, and conveying the nitrogen gas to the first gas storage tank through a nitrogen gas recovery pipeline so as to participate in the next calcium carbide purification dedusting ash treatment cycle;
blowing the fly ash to a fluidized bed furnace for combustion through an air conditioner at the bottom of the collection bin;
and (4) discharging the slag obtained by combustion out of the truck through negative pressure slag suction, and finishing secondary combustion treatment of the calcium carbide purification dedusting ash.
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