CN105444582B - A kind of combined and staged kiln exit gas processing unit and the process of burning of cement kiln bypass - Google Patents

A kind of combined and staged kiln exit gas processing unit and the process of burning of cement kiln bypass Download PDF

Info

Publication number
CN105444582B
CN105444582B CN201510946574.2A CN201510946574A CN105444582B CN 105444582 B CN105444582 B CN 105444582B CN 201510946574 A CN201510946574 A CN 201510946574A CN 105444582 B CN105444582 B CN 105444582B
Authority
CN
China
Prior art keywords
kiln
flue gas
air
dore furnace
desulfurizing tower
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201510946574.2A
Other languages
Chinese (zh)
Other versions
CN105444582A (en
Inventor
张雁忠
曾赐福
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shanghai Sancheng New Material Technology Co ltd
Shanghai Sanrong Environmental Protection Engineering Co ltd
Original Assignee
SHANGHAI SANRONG ENVIRONMENTAL PROTECTION ENGINEERING Co Ltd
Shanghai Sancheng Energy Technology Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by SHANGHAI SANRONG ENVIRONMENTAL PROTECTION ENGINEERING Co Ltd, Shanghai Sancheng Energy Technology Co Ltd filed Critical SHANGHAI SANRONG ENVIRONMENTAL PROTECTION ENGINEERING Co Ltd
Priority to CN201510946574.2A priority Critical patent/CN105444582B/en
Publication of CN105444582A publication Critical patent/CN105444582A/en
Application granted granted Critical
Publication of CN105444582B publication Critical patent/CN105444582B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/001—Extraction of waste gases, collection of fumes and hoods used therefor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C7/00—Combustion apparatus characterised by arrangements for air supply
    • F23C7/02—Disposition of air supply not passing through burner
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C9/00—Combustion apparatus characterised by arrangements for returning combustion products or flue gases to the combustion chamber
    • F23C9/003—Combustion apparatus characterised by arrangements for returning combustion products or flue gases to the combustion chamber for pulverulent fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/004—Systems for reclaiming waste heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2202/00—Fluegas recirculation
    • F23C2202/30—Premixing fluegas with combustion air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/004—Systems for reclaiming waste heat
    • F27D2017/005—Systems for reclaiming waste heat including pyrolising the waste gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/004—Systems for reclaiming waste heat
    • F27D2017/006—Systems for reclaiming waste heat using a boiler

Abstract

The invention discloses a kind of combined and staged burning kiln exit gas processing unit of cement kiln bypass, including the kiln tail smoke-box of rotary kiln, dore furnace, cyclone preheater, cyclone separator, layering cooling desulfurizing tower, bag filter；The kiln tail smoke-box of rotary kiln is connected with dore furnace；The kiln tail smoke-box of rotary kiln is connected by bypassing flue with cyclone separator；The hot raw material of tremie pipe of cyclone preheater are divided into two, and a part enters kiln tail smoke-box by former road, and another part enters the bypass flue gas extracted out from kiln tail smoke-box；Cyclone separator at the top of layering cooling desulfurizing tower with being connected；Layering cooling desulfurization tower bottom is connected with bag filter, and its middle part is connected by reducing airduct with dore furnace；Dore furnace sets burning-out zone, strong reducing zone, weak reducing zone respectively from top to bottom.In addition, invention additionally discloses the flue gas treating process method of said apparatus.Ammoniacal liquor reduced rate of the present invention reaches the effect of zero spray ammonia drop nitrogen, mitigates production cost and environmental pressure up to 80%.

Description

A kind of combined and staged kiln exit gas processing unit and the technique of burning of cement kiln bypass Method
Technical field
The present invention relates to manufacture of cement and cement kiln collaboration field of garbage disposal, more particularly, to one kind in manufacture of cement mistake Using the combined and staged burning kiln exit gas processing unit of bypass and process in journey.
Background technology
With the development of cement industry, original, it is becoming tight fuel source day, increasing cement plant needs to use waves containing height Hair property component (K2O、Na2O、SO3, Cl-) low-grade former, fuel calcination of cement clinker；Meanwhile increasing cement plant is adopted With alternative fuel and using kiln system processing discarded object, and institute is chloride in alternative fuel, discarded object, sulphur is all higher.
Municipal refuse is handled using new type nonaqueous cement rotary kiln, is one of mode of burning disposal rubbish, as cement Manufacturing enterprise, the disposal of discarded object must be premised on not influenceing manufacture of cement.From the perspective of controlling of production process, discard The harmful element (sulphur, chlorine and alkali metal) of thing belongs to volatile component, because raw material are fully suspended in hot gas, works as gas temperature When degree reaches the melting temperature of alkali, sulphur, chlorine, they are just condensate in raw meal powder particle surface, are returned to again in kiln with raw material, Height temperate zone is volatilized again, and volatile component is like this by repeatedly volatilization, condensation between kiln and preheater so that preheater, Raw material, which contain harmful ingredients, in kiln significantly improves, and from the point of view of nsp kiln test result, typically enters K in the hot raw material of kiln2O content is raw 2~4 times, Na of material2O is 1.5~2 times, Cl- is 20~30 times and SO3Mainly had a great influence by fuel, it can thus be seen that Volatile component circulates quite serious in preheater.The circulation collection of volatile component can often occur formation rings in a kiln or kiln tail smoke-box, The position such as cyclone cylinder cone skinning, be will be unable to normally be produced when serious, and Air Pollutant Emission is also had a certain impact.
Bypass system is that solve excessive potassium, sodium, the effective measures of chlorine discharge system in former, fuel, it is ensured that is System stable operation and product quality.However, current bypass technology, it is more using leak informaton mixed with cold wind by the way of carry out suddenly Cold, then cyclone separator or expansion chamber carry out dust and gas separation, and 200 DEG C or so of waste gas enters kiln tail afterheat generating system, Though there is partial heat recovery, but still substantial amounts of heat energy is wasted, and a large amount of dusts in flue gas can be to the fortune of waste heat boiler Row impacts, and does not also consider the processing of the pollutants such as nitrogen oxides of exhaust gas and sulfur dioxide, does not mitigate firing system really The pressure of fume treatment.
In addition, the denitration technology of domestic cement clinker production line is still based on SNCR SNCR methods, and divide Level combustion technology is in the starting stage, and denitration rate is less than 25%, and denitration effect is very unstable, easily causes the skinning of pre-heating system Block, it is impossible to adapt to various operating modes.It is strict to coal quality requirements, the high bituminous coal of volatile matter is only applicable to, to using anthracite conduct The cement production enterprise of fuel, then need to enter suitable reburning fuel outside, the staged combustion device of many enterprises is in idle state, no Can really it apply in production.And the denitration of SNCR ammonia method carries out the removing of nitrogen oxides by reducing agent ammoniacal liquor or urea, disappear Consume a large amount of reducing agents.No matter from the overall situation of national energy-saving emission reduction, or from manufacture of cement cost is saved, improve classification Combustion technology, ammoniacal liquor (or urea) discharge rate is reduced, all seems particularly urgent.
In view of the reason for above-mentioned, existing bypass technology and grading combustion technology all have much room for improvement.
The content of the invention
The technical problem to be solved in the present invention is to overcome deficiency of the prior art, there is provided a kind of cement bypass of kiln is put The combined and staged burning of wind carries out the process of kiln exit gas processing, and bypass technology and grading combustion technology are organically combined Get up, ammoniacal liquor reduced rate is up to 80%, it might even be possible to reach the effect of zero spray ammonia drop nitrogen, reduce harmful components in rotary kiln and wave Internal circulating load is sent out, improves clinker quality, lifts calcination equipment running rate, mitigates production cost and environmental pressure.Therefore, the present invention is also A kind of combined and staged burning of cement kiln bypass is provided and carries out kiln exit gas processing unit.
In order to solve the above-mentioned technical problem the present invention, adopts the following technical scheme that：
In one aspect of the invention, there is provided a kind of combined and staged burning kiln exit gas handling process side of cement kiln bypass Method, including cement kiln tail bypass wind discharging technique and cement kiln dore furnace fractional combustion technique；The cement kiln tail bypass is put Wind process following steps：
The first step, in the presence of exhaust blower, 1% is extracted out from the kiln tail smoke-box of rotary kiln by electric bypass vent valve Kiln exit gas to 15% is used as bypass flue gas；Flue gas is bypassed to lock through high temperature sub-material in increase in pipeline and from cyclone preheater The hot raw material in part of air-valve separation are sufficiently mixed, and enter the heat exchange of promoting the circulation of qi material；
Second step, the flue gas after the heat exchange of gas material is through cyclone separator, as desulfurizing agent after 90% hot raw material are separated Desulfurization tower bottom is cooled down into layering, flue gas then cools down in desulfurizing tower into layering and carries out layering cooling；
3rd step, the flue gas after layering cooling desulfurizing tower processing, according to production requirement, the flue gas less than 150 DEG C enters Enter and air is discharged into through chimney by exhaust blower after bag filter purifies；Flue gas higher than 300 DEG C then enters kiln tail waste heat boiler Generated electricity, or enter raw material drying workshop as hot blast source；Pass through after flue gas cool-down between 150 DEG C~300 DEG C Electric air valve enters bag filter；
4th step, the dry ash of layering cooling desulfurizing tower discharge, the is fallen into through the first FU conveyers and double-deck air locking valve with counter weight Three FU conveyers, wet slag then outer row's processing；The dust that bag filter is collected, the 2nd FU conveyings are fallen into through motoring blanking device Machine, the dry ash then discharged with layering cooling desulfurizing tower are delivered to mixing material storehouse by the 3rd FU conveyers together, are not suitable for mixing The material of cement then dispatches from the factory processing；
The cement kiln dore furnace fractional combustion technique comprises the following steps：The dore furnace sets after-flame respectively from top to bottom Area, strong reducing zone, weak reducing zone；
Step 1, the flue gas from rotary kiln, remove outside 1% to 15% bypass flue gas, it is most of to enter dore furnace, and After dore furnace tapering or lower prop converge with the tertiary air from tertiary-air pipe as dore furnace weak reducing zone combustion-supporting sky Gas；
Step 2, in the presence of centrifugal blower, by adjusting the aperture of Electric air valve, cool down in desulfurizing tower and take out from layering Rich steam-laden kiln tail bypass wind is taken, strong reducing zone is entered in the middle part of dore furnace, reduction wind mixes with flue gas in stove, is used as this The combustion air in area, coal dust divides equally two-way feeding reduction airduct and enters stove point top, and C4 raw material are sufficiently mixed；
Step 3, a part of fiery windward is drawn from tertiary-air pipe, tangentially enters burning-out zone at the top of dore furnace.
As currently preferred technical scheme, second step is specially：Flue gas is divided by entering at the top of layering cooling desulfurizing tower Layer cooling desulfurizing tower carries out the spray cooling of the first round to flue gas, and temperature control between 550 DEG C~650 DEG C, adopt by water injection system With automatic temperature-adjusting control system, injection flow rate is automatically adjusted according to flue gas exit temperature change；Flue gas continues traveling downwardly, and receives the second wheel Spray cooling, flue-gas temperature control between 150 DEG C~300 DEG C, then mixed with the hot raw material from cyclone separator, Alkaline atmosphere is formed, carrying out desulfurization to flue gas denitrogenates.
As currently preferred technical scheme, in the 3rd step, the flue gas for being higher than 300 DEG C to take air quantity to pass through electronic The aperture of air-valve is adjusted；Flue gas between described 150 DEG C~300 DEG C is cooled by adjusting the aperture of cold blast sliding valve.
As currently preferred technical scheme, in step 1, the air quantity of the tertiary air is entered by the aperture of tertiary air valve Row regulation, excess air coefficient are controlled 0.9；Coal consumption is then controlled 2/3rds of the total coal consumption of dore furnace, and coal dust is divided equally Two-way is sent into tertiary-air pipe and enters stove point top, and C4 raw material are sufficiently mixed；The C4 raw material amount of the weak reducing zone and dore furnace coal Ratio is mutually coordinated, and accounts for 2/3rds of C4 raw material total amounts.
As currently preferred technical scheme, in step 2, the excess air coefficient of the strong reducing zone is controlled 0.7； Coal consumption is then controlled 1/3rd of the total coal consumption of dore furnace；The C4 raw material amount and dore furnace coal ratio phase of the strong reducing zone Coordinate, account for 1/3rd of C4 raw material total amounts；When oxygen content is less than 5%, 1% vapor is added in mixed gas.
As currently preferred technical scheme, in step 3, the size of the air quantity of the fiery windward is entered by fiery upper air-valve Row regulation.
In another aspect of this invention, there is provided a kind of combined and staged burning kiln exit gas processing dress of cement kiln bypass Put, including：Kiln tail smoke-box, dore furnace, cyclone preheater, cyclone separator, layering cooling desulfurizing tower, the pocket type of rotary kiln are received Dirt device；The kiln tail smoke-box of the rotary kiln is connected with dore furnace；The kiln tail smoke-box of rotary kiln is by bypassing flue and bispin Wind separator connects；The hot raw material of the tremie pipe of cyclone preheater are divided into two, and a part is entered the kiln tail of rotary kiln by former road Smoke-box, another part enter the bypass flue gas extracted out from kiln tail smoke-box；Cyclone separator at the top of layering cooling desulfurizing tower with connecting Connect；Layering cooling desulfurization tower bottom is connected with bag filter；By reducing airduct and dore furnace in the middle part of layering cooling desulfurizing tower Connection；The dore furnace sets burning-out zone, strong reducing zone, weak reducing zone respectively from top to bottom.
As currently preferred technical scheme, the dore furnace lower prop is connected with tertiary-air pipe, on the dore furnace Cylinder is connected with fiery upcast ventilation pipe, is connected in the middle part of the dore furnace with reduction airduct, the reduction airduct other end and layering cooling desulfurization Tower connects；The reduction airduct is provided with Electric air valve and centrifugal blower；The tertiary-air pipe is provided with tertiary air valve；The fire Upcast ventilation pipe is provided with fiery upper air-valve.
As currently preferred technical scheme, the bypass flue is provided with electric bypass vent valve.
As currently preferred technical scheme, the layering cooling desulfurization tower bottom is provided with two cooling blowers；Institute State and two layers of water spray layer is provided with layering cooling desulfurizing tower；The dry ash of the layering cooling desulfurizing tower discharge, through the first FU conveyers The 3rd FU conveyers are fallen into double-deck air locking valve with counter weight；The dust that the bag filter is collected, falls through motoring blanking device Enter the 2nd FU conveyers, then the dry ash with layering cooling desulfurizing tower discharge is delivered to mixing material by the 3rd FU conveyers together Storehouse, the material for being not suitable for mixing cement then dispatch from the factory processing；On the connecting pipe of the layering cooling desulfurizing tower and bag filter Provided with cold blast sliding valve and Electric air valve；The bag filter is connected by exhaust blower with chimney；The layering cooling desulfurizing tower leads to The flue provided with Electric air valve is crossed to be connected with kiln tail waste heat boiler or raw material drying workshop；Under the cyclone preheater The hot raw material of expects pipe are divided into two by high temperature sub-material air valve.
Compared with prior art, the present invention has the advantages that：
1st, bypass by cyclone dust removal and flue gas humidification two procedures circulate the collection of volatile matter in the present invention, And enter from cyclone preheater tremie pipe sub-material and bypass the separation that flue gas circulate volatile matter, effectively reduce harmful element Circulation collection in firing system, the possibility of smoke-box, dore furnace and preheater skinning is alleviated from root, it is low to produce Alkali cement is laid a good foundation, and is escort for the stabilization of clinker burning system.
2nd, undecomposed CaCO in cyclone preheater tremie pipe is utilized in the present invention3The flue gas that leaks informaton to kiln tail carries out heat absorption drop Temperature, the CaCO then decomposed using height3The CaO of generation carries out desulfurization process to bypass flue gas, and it is cold can to reduce flue gas But the thermal loss in, and can reduce the discharge of dusty gas.
3rd, the combustion air in the present invention using the bypass flue gas after humidification as " strong reducing zone " in fractional combustion, utilizes water The occurring principle of coal gas strengthens the reducing atmosphere in the area, and powerful guarantee is provided for denitration and reduction ammoniacal liquor discharge rate, will Bypass technology and grading combustion technology combine, and break through reburning technology to the rigors of reburning fuel, make With denitration efficiency in the case of anthracitic still up to more than 90%, ammoniacal liquor reduced rate is up to 80%.In the requirement of existing environment protection emission Under, it might even be possible to reach the effect of zero spray ammonia drop nitrogen.
Brief description of the drawings
The invention will be further described below in conjunction with the accompanying drawings：
Fig. 1 is a kind of process chart of the combined and staged burning kiln exit gas processing of cement kiln bypass of the present invention；
In Fig. 1：1 is rotary kiln, and 2 be kiln tail smoke-box, and 3 be dore furnace, and 4 be electric bypass vent valve, and 5 be cyclone separation Device, 6 be layering cooling desulfurizing tower, and 7 be cooling blower, and 8 be the first FU conveyers, and 9 be double-deck air locking valve with counter weight, and 10 be electronic wind Valve, 11 be bag filter, and 12 be motoring blanking device, and 13 be the 2nd FU conveyers, and 14 be the 3rd FU conveyers, and 15 be row Blower fan, 16 be chimney, and 17 be Electric air valve, and 18 be Electric air valve, and 19 be centrifugal blower, and 20 be high temperature sub-material air valve, and 21 are Tertiary air valve, 22 be fiery upper air-valve, and 23 be tertiary-air pipe, and 24 be fiery upcast ventilation pipe, and 25 be reduction airduct, and 26 be cold blast sliding valve, and C5 is Cyclone preheater.
Embodiment
The present invention is described in further detail with reference to the accompanying drawings and examples：
As shown in figure 1, a kind of technique of the combined and staged burning kiln exit gas processing of cement kiln bypass, in exhaust blower 15 In the presence of, by electric bypass vent valve 4 from the connecting portion of rotary kiln 1 and dore furnace 3 be to extract 1% out in kiln tail smoke-box 2 Kiln exit gas to 15% is used as bypass flue gas.Flue gas is bypassed in flue is risen and from cyclone preheater C5 through high temperature The hot raw material in part that sub-material air valve 20 separates are sufficiently mixed, and enter the heat exchange of promoting the circulation of qi material.
Flue gas after the heat exchange of gas material divides through cyclone separator 5 using entering after 90% hot raw material separation as desulfurizing agent The bottom of layer cooling desulfurizing tower 6, flue gas then cool down in desulfurizing tower 6 into layering and carry out layering cooling.
Flue gas is entered by the top of layering cooling desulfurizing tower 6, and the water spray that layering cooling desulfurizing tower 6 carries out the first round to flue gas drops Temperature, temperature control is between 550 DEG C~650 DEG C.Water injection system uses automatic temperature-adjusting control system, is become according to flue gas exit temperature Change automatically adjusts injection flow rate.Flue gas is continued traveling downwardly, and receives the spray cooling of the second wheel, and flue-gas temperature is controlled at 150 DEG C~300 DEG C Between, then mixed with the hot raw material from cyclone separator 5, form alkaline atmosphere, carrying out desulfurization to flue gas denitrogenates.Layering Cooling desulfurizing tower 6 bottom is provided with two cooling blowers 7, on the one hand supplements cold wind with auxiliary temperature-reducing, on the one hand strengthens flue gas, steams Vapour and hot raw material three's is sufficiently mixed.Kiln tail is leaked informaton by the way of multi-level water spray the middle and upper part of layering cooling desulfurizing tower 6 Flue gas carries out layering cooling, and bottom aqueous vapor mixes with the supplied materials of cyclone separator 5, forms alkaline atmosphere, and bottom sets cooling wind Machine 7 and dry and wet material transfer equipment.
Flue gas after layering cooling desulfurizing tower 6 is handled, according to production requirement, the flue gas less than 150 DEG C enters pocket type Air is discharged into through chimney 16 by exhaust blower 15 after the purification of dust-precipitator 11；Flue gas higher than 300 DEG C can then enter kiln tail waste heat Boiler is generated electricity, or enters raw material drying workshop as hot blast source, takes aperture of the air quantity then by Electric air valve 17 It is adjusted；Flue gas between 150 DEG C~300 DEG C then can pass through Electric air valve by adjusting the aperture of cold blast sliding valve 26 after cooling 10 enter bag filter 11.
The dry ash that layering cooling desulfurizing tower 6 is discharged, the 3rd FU is fallen into through the first FU conveyers 8 and double-deck air locking valve with counter weight 9 Conveyer 14, wet slag then outer row's processing.The dust that bag filter 11 is collected, it is defeated to fall into the 2nd FU through motoring blanking device 12 Machine 13 is sent, the dry ash then discharged with layering cooling desulfurizing tower 6 is delivered to mixing material storehouse by the 3rd FU conveyers 14 together, uncomfortable The material for preferably mixing cement then dispatches from the factory processing.
As shown in figure 1, flue gas trend and dust handling process of the above section for cement kiln tail bypass wind discharging.
As shown in figure 1, using lower part as the fractional combustion fume treatment process of cement kiln dore furnace：
As shown in figure 1, kiln tail power transportation pipe is transformed, using the mode for dividing wind to divide coal sub-material, in dore furnace 3 Three combustion zones are established from bottom to top in inside, i.e., " weak reducing zone ", " strong reducing zone " and " burning-out zone ".It is de- from layering cooling Sulphur tower 6 introduces 650 DEG C or so of rich steam-laden bypass wind, into " strong reducing zone ", is formed using water-gas occurring principle Reducibility gas CO and H2, and then NOXIt is reduced into N2；The layered cooling desulfurizing tower 6 layering cooling of kiln tail bypass flue gas Afterwards, it is partly into cogeneration or is discharged into air after being purified by bag filter 11 as drying thermal source, a part, collection Material then selects outer row or as the mixing material for producing cement according to dry and wet situation.The tool of three combustion zones in dore furnace 3 Body fractional combustion step includes as follows：
Flue gas from rotary kiln 1, remove outside 1% to 15% bypass flue gas, it is most of to enter dore furnace 3, and dividing Solve the combustion-supporting sky as dore furnace 3 " weak reducing zone " after the tapering of stove 3 or lower prop converge with the tertiary air from tertiary-air pipe 23 Gas.The air quantity of tertiary air can be adjusted by the aperture of tertiary air valve 21, and excess air coefficient is controlled 0.9 or so.With Coal amount (i.e. main coal in Fig. 1) is then controlled 2/3rds of 3 total coal consumption of dore furnace, and coal dust divides equally two-way and is sent into tertiary-air pipe 23 enter stove point top, and C4 raw material (i.e. C4 materials in Fig. 1) are sufficiently mixed.The C4 lifes in the area (i.e. weak reducing zone in Fig. 1) Doses and dore furnace 3 are mutually coordinated with coal ratio, account for 2/3rds of C4 raw material total amounts.
In the presence of centrifugal blower 19, by adjusting the aperture of Electric air valve 18, cool down in desulfurizing tower 6 and extract from layering 650 DEG C or so of rich steam-laden kiln tail bypass wind, enters " strong reducing zone ", reduction wind and cigarette in stove at the middle part of dore furnace 3 Gas is mixed, and as the combustion air in the area, excess air coefficient is controlled 0.7 or so.Coal consumption (i.e. main coal in Fig. 1) is then controlled For system 1/3rd of 3 total coal consumption of dore furnace, coal dust, which divides equally two-way and is sent into reduction airduct 25, enters stove point top, and C4 raw material (i.e. C4 materials in Fig. 1) is sufficiently mixed.The C4 raw material amount and the coal ratio of dore furnace 3 in the area (i.e. strong reducing zone in Fig. 1) Mutually coordinate, account for 1/3rd of C4 raw material total amounts.When oxygen content is less than 5%, the water that 1% or so is added in mixed gas steams Gas, NO generation can be suppressed, and can shortens the tail-off time of coal dust, while utilizes a large amount of caused by the occurring principle of water-gas CO and H2And the reducing substances in coal-fired volatile matter again, caused thermal NO in rotary kiln is reduced, while suppress reducing zone Fuel type NO formation.
In order to ensure the elimination of the after-flame and CO of dore furnace 3 " strong reducing zone " coal dust, ensure the calorific capacity of dore furnace, from A part of wind (i.e. fiery windward in Fig. 1) is drawn in tertiary-air pipe 23, tangentially enters " burning-out zone " in the top of dore furnace 3, on fire The size of air quantity can be adjusted by fiery upper air-valve 22.
As shown in figure 1, by way of setting and reducing airduct 25, bypass and fractional combustion two systems is organic System gets up.On the one hand the thermal loss of traditional bypass quenching technology is reduced, on the one hand the reduction wind as dore furnace 3 is carried out Denitrating flue gas.
As shown in figure 1, a kind of combined and staged burning kiln exit gas processing unit of cement kiln bypass of the present invention, including： Kiln tail smoke-box 2, dore furnace 3, cyclone preheater C5, cyclone separator 5, layering cooling desulfurizing tower 6, the pocket type of rotary kiln 1 are received Dirt device 11.Wherein, the kiln tail smoke-box 2 of rotary kiln 1 is connected (the connecting portion i.e. kiln tail of rotary kiln 1 and dore furnace 3 with dore furnace 3 Smoke-box 2)；The kiln tail smoke-box 2 of rotary kiln 1 is connected by bypassing flue with cyclone separator 5；Under cyclone preheater C5 The hot raw material of expects pipe are divided into two, and a part is entered the kiln tail smoke-box 2 of rotary kiln 1 by former road, and another part enters from kiln tail cigarette The bypass flue gas that room 2 is extracted out, the layering cooling bottom of desulfurizing tower 6 and gas-vapor mix are entered after heat exchange is decomposed, utilizes the alkali of formation Property atmosphere carry out drop nitrogen desulfurization remove alkali；Cyclone separator 5 is connected with the top of layering cooling desulfurizing tower 6；Layering cooling desulfurizing tower 6 Bottom is connected with bag filter 11；The middle part of layering cooling desulfurizing tower 6 is connected by reducing airduct 25 with dore furnace 3；
The dore furnace 3 sets burning-out zone, strong reducing zone, weak reducing zone respectively from top to bottom；Tertiary-air pipe 23 and dore furnace 3 Lower prop connects；Fiery upcast ventilation pipe 24 is connected with the column body of dore furnace 3；Reduction one end of airduct 25 is connected with the middle part of dore furnace 3, another End is connected with layering cooling desulfurizing tower 6.Electric air valve 18 and centrifugal blower 19 are provided with reduction airduct 25.In tertiary-air pipe 23 Provided with tertiary air valve 21.Fiery upcast ventilation pipe 24 is provided with fiery upper air-valve 22.
The bypass flue is provided with electric bypass vent valve 4.Layering cooling desulfurizing tower 6 bottom be provided with two it is cold But blower fan 7, cold wind is on the one hand supplemented with auxiliary temperature-reducing, on the one hand strengthens being sufficiently mixed for flue gas, steam and hot raw material three.Point Two layers of water spray layer is provided with layer cooling desulfurizing tower 6；The dry ash that layering cooling desulfurizing tower 6 is discharged, through the first FU conveyers 8 and bilayer Air locking valve with counter weight 9 falls into the 3rd FU conveyers 14.The dust that bag filter 11 is collected, the is fallen into through motoring blanking device 12 Two FU conveyers 13, the dry ash then discharged with layering cooling desulfurizing tower 6 are delivered to mixing material by the 3rd FU conveyers 14 together Storehouse, the material for being not suitable for mixing cement then dispatch from the factory processing.Set on the connecting pipe of layering cooling desulfurizing tower 6 and bag filter 11 There are cold blast sliding valve 26 and Electric air valve 10.Bag filter 11 is connected by exhaust blower 15 with chimney 16.Layering cooling desulfurizing tower 6 is logical The flue provided with Electric air valve 17 is crossed to be connected with kiln tail waste heat boiler or raw material drying workshop.The cyclone preheater C5 The hot raw material of tremie pipe be divided into two by high temperature sub-material air valve 20.
Above-described embodiment, the purpose of the present invention, technical scheme and beneficial effect are carried out further Detailed description, should be understood that the foregoing is only the present invention embodiment, be not used to the present invention Protection domain, hair within the spirit and principles in the present invention, any modification, equal replacement and improvement for being made etc., all should include Within protection scope of the present invention.

Claims (8)

  1. A kind of 1. combined and staged burning kiln exit gas handling process method of cement kiln bypass, it is characterised in that including cement Kiln kiln tail bypass technique and cement kiln dore furnace fractional combustion technique；The cement kiln tail bypass wind discharging technique walks as follows Suddenly：
    The first step, in the presence of exhaust blower, extracted out by electric bypass vent valve from the kiln tail smoke-box of rotary kiln 1% to 15% kiln exit gas is as bypass flue gas；Bypass flue gas and lock wind through high temperature sub-material in increase in pipeline and from cyclone preheater The hot raw material in part of valve separation are sufficiently mixed, and enter the heat exchange of promoting the circulation of qi material；
    Second step, the flue gas after the heat exchange of gas material enter through cyclone separator using after 90% hot raw material separation as desulfurizing agent Layering cooling desulfurization tower bottom, flue gas then cool down in desulfurizing tower into layering and carry out layering cooling；
    3rd step, the flue gas after layering cooling desulfurizing tower processing, according to production requirement, the flue gas less than 150 DEG C enters bag Air is discharged into through chimney by exhaust blower after the purification of formula dust-precipitator；Flue gas higher than 300 DEG C, which then enters kiln tail waste heat boiler, to be carried out Generate electricity, or enter raw material drying workshop as hot blast source；By electronic after flue gas cool-down between 150 DEG C~300 DEG C Air-valve enters bag filter；
    4th step, the dry ash of layering cooling desulfurizing tower discharge, the 3rd FU is fallen into through the first FU conveyers and double-deck air locking valve with counter weight Conveyer, wet slag then outer row's processing；The dust that bag filter is collected, the 2nd FU conveyers are fallen into through motoring blanking device, Then the dry ash with layering cooling desulfurizing tower discharge is delivered to mixing material storehouse by the 3rd FU conveyers together, is not suitable for mixing cement Material then dispatch from the factory processing；
    The cement kiln dore furnace fractional combustion technique comprises the following steps：The dore furnace set respectively from top to bottom burning-out zone, Strong reducing zone, weak reducing zone；
    Step 1, the flue gas from rotary kiln, remove outside 1% to 15% bypass flue gas, it is most of to enter dore furnace, and dividing Solution stove tapering or lower prop and the tertiary air from tertiary-air pipe converge after as dore furnace weak reducing zone combustion air；
    Step 2, in the presence of centrifugal blower, by adjusting the aperture of Electric air valve, cooled down from layering and richness is extracted in desulfurizing tower Steam-laden kiln tail bypasses wind, strong reducing zone is entered in the middle part of dore furnace, reduction wind mixes with flue gas in stove, as the area Combustion air, coal dust divides equally two-way feeding reduction airduct and enters stove point top, and C4 raw material are sufficiently mixed；
    Step 3, a part of fiery windward is drawn from tertiary-air pipe, tangentially enters burning-out zone at the top of dore furnace.
  2. 2. the method as described in claim 1, it is characterised in that second step is specially：Flue gas is by layering cooling desulfurizing tower top Into layering cooling desulfurizing tower carries out the spray cooling of the first round to flue gas, and temperature control is between 550 DEG C~650 DEG C, water spray System uses automatic temperature-adjusting control system, and injection flow rate is automatically adjusted according to flue gas exit temperature change；Flue gas continues traveling downwardly, and receives The spray cooling of second wheel, flue-gas temperature are controlled between 150 DEG C~300 DEG C, then raw with the heat from cyclone separator Material mixing, forms alkaline atmosphere, and carrying out desulfurization to flue gas denitrogenates.
  3. 3. the method as described in claim 1, it is characterised in that in the 3rd step, the flue gas for being higher than 300 DEG C takes air quantity to lead to The aperture for crossing Electric air valve is adjusted；Flue gas between described 150 DEG C~300 DEG C is cooled by adjusting the aperture of cold blast sliding valve.
  4. 4. the method as described in claim 1, it is characterised in that in step 1, the air quantity of the tertiary air passes through tertiary air valve Aperture is adjusted, and excess air coefficient is controlled 0.9；Coal consumption is then controlled 2/3rds of the total coal consumption of dore furnace, coal Powder divides equally two-way feeding tertiary-air pipe and enters stove point top, and C4 raw material are sufficiently mixed；The C4 raw material amount of the weak reducing zone is with decomposing Stove coal ratio is mutually coordinated, and accounts for 2/3rds of C4 raw material total amounts.
  5. 5. the method as described in claim 1, it is characterised in that in step 2, the excess air coefficient control of the strong reducing zone 0.7；Coal consumption is then controlled 1/3rd of the total coal consumption of dore furnace；The C4 raw material amount of the strong reducing zone and dore furnace coal Ratio is mutually coordinated, and accounts for 1/3rd of C4 raw material total amounts；When oxygen content is less than 5%, the water that 1% is added in mixed gas steams Gas.
  6. 6. the method as described in claim 1, it is characterised in that in step 3, the size of the air quantity of the fiery windward passes through on fire Air-valve is adjusted.
  7. A kind of 7. combined and staged burning kiln exit gas processing unit of cement kiln bypass, it is characterised in that including：Rotary kiln Kiln tail smoke-box, dore furnace, cyclone preheater, cyclone separator, layering cooling desulfurizing tower, bag filter；The rotary kiln Kiln tail smoke-box be connected with dore furnace；The kiln tail smoke-box of rotary kiln is connected by bypassing flue with cyclone separator；Rotation The hot raw material of the tremie pipe of wind preheater are divided into two, and a part is entered the kiln tail smoke-box of rotary kiln by former road, and another part enters Enter the bypass flue gas extracted out from kiln tail smoke-box；Cyclone separator at the top of layering cooling desulfurizing tower with being connected；Layering cooling desulfurization Tower bottom is connected with bag filter；It is connected in the middle part of layering cooling desulfurizing tower by reducing airduct with dore furnace；The dore furnace Set burning-out zone, strong reducing zone, weak reducing zone respectively from top to bottom；
    The dore furnace lower prop is connected with tertiary-air pipe, and the dore furnace column body is connected with fiery upcast ventilation pipe, the dore furnace Middle part is connected with reduction airduct, and the reduction airduct other end is connected with layering cooling desulfurizing tower；The reduction airduct is provided with electronic Air-valve and centrifugal blower；The tertiary-air pipe is provided with tertiary air valve；The fiery upcast ventilation pipe is provided with fiery upper air-valve；
    The bypass flue is provided with electric bypass vent valve.
  8. 8. device as claimed in claim 7, it is characterised in that the layering cooling desulfurization tower bottom is provided with two cooling wind Machine；Two layers of water spray layer is provided with the layering cooling desulfurizing tower；The dry ash of the layering cooling desulfurizing tower discharge, it is defeated through the first FU Machine and double-deck air locking valve with counter weight is sent to fall into the 3rd FU conveyers；The dust that the bag filter is collected, through motoring blanking Device falls into the 2nd FU conveyers, and then the dry ash with layering cooling desulfurizing tower discharge is delivered to mixing by the 3rd FU conveyers together Material storehouse；The connecting pipe of the layering cooling desulfurizing tower and bag filter is provided with cold blast sliding valve and Electric air valve；The pocket type Dust-precipitator is connected by exhaust blower with chimney；The layering cooling desulfurizing tower passes through flue and kiln tail provided with Electric air valve Waste heat boiler or raw material drying workshop connection；The hot raw material of the tremie pipe of the cyclone preheater pass through high temperature sub-material air valve It is divided into two.
CN201510946574.2A 2015-12-16 2015-12-16 A kind of combined and staged kiln exit gas processing unit and the process of burning of cement kiln bypass Active CN105444582B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201510946574.2A CN105444582B (en) 2015-12-16 2015-12-16 A kind of combined and staged kiln exit gas processing unit and the process of burning of cement kiln bypass

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201510946574.2A CN105444582B (en) 2015-12-16 2015-12-16 A kind of combined and staged kiln exit gas processing unit and the process of burning of cement kiln bypass

Publications (2)

Publication Number Publication Date
CN105444582A CN105444582A (en) 2016-03-30
CN105444582B true CN105444582B (en) 2017-11-10

Family

ID=55555065

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201510946574.2A Active CN105444582B (en) 2015-12-16 2015-12-16 A kind of combined and staged kiln exit gas processing unit and the process of burning of cement kiln bypass

Country Status (1)

Country Link
CN (1) CN105444582B (en)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106247791B (en) * 2016-09-29 2018-07-24 济南裕兴化工有限责任公司 Titanium workshop rotary kiln with waste heat from tail gas reuse function and method
CN106675650B (en) * 2017-03-06 2022-09-27 上海三融环保工程有限公司 ERD (activated carbon reduction) and fire coal saturated steam catalytic combustion denitration device and process method
JP2020521630A (en) * 2017-05-26 2020-07-27 ノベリス・インコーポレイテッドＮｏｖｅｌｉｓ Ｉｎｃ． Cyclone temperature control for decoating system
CN108443713A (en) * 2018-04-04 2018-08-24 江苏苏亚迪炭材有限公司 Pot type burner gas bypass valve device for preventing leakage
CN108298844A (en) * 2018-04-08 2018-07-20 天津健威泽节能环保科技股份有限公司 A kind of clinker drop alkali device and implementation method
CN108525508A (en) * 2018-05-11 2018-09-14 中国建筑材料科学研究总院有限公司 The method for carrying out flue gas desulfurization using cement slurry
CN108534543A (en) * 2018-06-07 2018-09-14 天津水泥工业设计研究院有限公司 A kind of bypass technique and its equipment
CN111689704B (en) * 2019-03-12 2021-10-08 中国科学院工程热物理研究所 Multistage suspension preheating cement kiln system and control method thereof
CN109985500A (en) * 2019-04-23 2019-07-09 天津朝阳环保科技集团有限公司 A kind of hot carbon reduction NO_x Reduction by Effective system of modified precalcining dry-process cement rotary kiln
CN110282889B (en) * 2019-05-17 2021-09-28 中国建筑材料科学研究总院有限公司 Cement self-desulfurization device and method
CN110360843A (en) * 2019-07-31 2019-10-22 中国科学院力学研究所 A kind of cement decomposing furnace coal dust high-efficiency gasification low-NO_x combustion technology device

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6023781A (en) * 1983-07-18 1985-02-06 石川島播磨重工業株式会社 Denitrating device for furnace
WO1999006778A1 (en) * 1997-07-30 1999-02-11 Southdown, Inc. Oxygen enrichment of cement kiln system combustion
US6228143B1 (en) * 2000-01-18 2001-05-08 The International Metals Reclamation Company, Inc. Rotary thermal oxidizer for battery recycling and process
CN102636038A (en) * 2012-03-30 2012-08-15 中信重工机械股份有限公司 Bypass ventilating process flow
WO2013113664A1 (en) * 2012-01-31 2013-08-08 Italcementi S.P.A. Integrated process for the production of clinker with treatment of bypass dusts produced by the kiln
CN203494378U (en) * 2013-08-30 2014-03-26 安徽省元琛环保科技有限公司 SCR (Selective Catalytic Reduction) denitration device for controlling NOx of rotary cement kiln
CN204619708U (en) * 2015-04-10 2015-09-09 无锡华光新动力环保科技股份有限公司 A kind of cement rotary kiln kiln gas combined denitration device
CN205425856U (en) * 2015-12-16 2016-08-03 上海三橙能源科技有限公司 Cement kiln bypass joint fractional combustion kiln tail smoke treatment device that leaks informaton

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6023781A (en) * 1983-07-18 1985-02-06 石川島播磨重工業株式会社 Denitrating device for furnace
WO1999006778A1 (en) * 1997-07-30 1999-02-11 Southdown, Inc. Oxygen enrichment of cement kiln system combustion
US6228143B1 (en) * 2000-01-18 2001-05-08 The International Metals Reclamation Company, Inc. Rotary thermal oxidizer for battery recycling and process
WO2013113664A1 (en) * 2012-01-31 2013-08-08 Italcementi S.P.A. Integrated process for the production of clinker with treatment of bypass dusts produced by the kiln
CN102636038A (en) * 2012-03-30 2012-08-15 中信重工机械股份有限公司 Bypass ventilating process flow
CN203494378U (en) * 2013-08-30 2014-03-26 安徽省元琛环保科技有限公司 SCR (Selective Catalytic Reduction) denitration device for controlling NOx of rotary cement kiln
CN204619708U (en) * 2015-04-10 2015-09-09 无锡华光新动力环保科技股份有限公司 A kind of cement rotary kiln kiln gas combined denitration device
CN205425856U (en) * 2015-12-16 2016-08-03 上海三橙能源科技有限公司 Cement kiln bypass joint fractional combustion kiln tail smoke treatment device that leaks informaton

Also Published As

Publication number Publication date
CN105444582A (en) 2016-03-30

Similar Documents

Publication Publication Date Title
CN105444582B (en) A kind of combined and staged kiln exit gas processing unit and the process of burning of cement kiln bypass
CN104748567B (en) Sintering flue gas waste heat staged cyclic utilization and pollutant emission reducing process and system
CN105091615B (en) A kind of integrated conduct method of agglomeration for iron mine flue gas pollutant
CN205425856U (en) Cement kiln bypass joint fractional combustion kiln tail smoke treatment device that leaks informaton
CN104132550A (en) Energy-saving environment-friendly sintering waste gas waste-heat utilization and pollutant purification process and system
CN106215695A (en) A kind of sinter the out of stock system of flue gas simultaneous desulfurization and its implementation
CN110273065A (en) A kind of iron ore microwave sintering method
CN106969641A (en) One kind sintering flue gas decomposes bioxin desulphurization denitration recovery waste heat system and method from combustion-supporting
CN102607043B (en) Method and device for synergetic stable incineration of sludge and solid waste and dioxin emission suppression
CN201715522U (en) Hazardous waste incineration deacidification equipment
CN110513693B (en) Sludge incineration method
CN105042575A (en) Fuel and gas-fired boiler oxygen-enriched combustion smoke nearly-zero-emission power generation system
CN107131770B (en) A kind of agglomeration for iron mine waste heat recycling collaboration emission reduction SOxAnd NOxMethod
CN109573955B (en) Device and process for preparing sulfur and recovering desulfurizer through sulfate carbon thermal reduction
CN105066113A (en) Coal-powder boiler oxygen-enriched combustion smoke near-zero emission and power generation system
CN109569183A (en) A kind of bi serie sintering system smoke comprehensive circulation process method and processing unit
CN106287771B (en) A kind of coal-fired power station boiler fume afterheat utilizes system with moisture combined recovery
CN106610230A (en) Sintering flue gas reduction and waste heat comprehensive utilization method and device
CN206944178U (en) A kind of smoke processing system
CN106861412B (en) System and method for sharing and recycling high-calcium fly ash of multi-unit power station
CN200975664Y (en) Oxygen-enriched combustion circulating fluid bed boiler system
CN110274463A (en) A kind of pure sintering system and method based on fuel formulations and roasting control
CN102350211B (en) Three-stage desulfurization device for circulating fluidized bed boiler
CN102777921B (en) System and method for carrying out mercury removal and sulfur fixation on pulverized coal boiler by using white mud
CN202315697U (en) Three-segment desulfurizer for boiler of circulating fluidized bed

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
CP01 Change in the name or title of a patent holder

Address after: Room A241, Building 1, No. 1628 Suzhao Road, Minhang District, Shanghai, 201100

Patentee after: Shanghai Sancheng New Material Technology Co.,Ltd.

Patentee after: SHANGHAI SANRONG ENVIRONMENTAL PROTECTION ENGINEERING Co.,Ltd.

Address before: Room A241, Building 1, No. 1628 Suzhao Road, Minhang District, Shanghai, 201100

Patentee before: SHANGHAI SANCHENG ENERGY TECHNOLOGY Co.,Ltd.

Patentee before: SHANGHAI SANRONG ENVIRONMENTAL PROTECTION ENGINEERING Co.,Ltd.

CP01 Change in the name or title of a patent holder