CN1031499C - Outer decomposition technology and device for plaster kiln - Google Patents
Outer decomposition technology and device for plaster kiln Download PDFInfo
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- CN1031499C CN1031499C CN 93111274 CN93111274A CN1031499C CN 1031499 C CN1031499 C CN 1031499C CN 93111274 CN93111274 CN 93111274 CN 93111274 A CN93111274 A CN 93111274A CN 1031499 C CN1031499 C CN 1031499C
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- cyclonic separator
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- 238000000354 decomposition reaction Methods 0.000 title claims abstract description 22
- 239000011505 plaster Substances 0.000 title claims description 4
- 238000005516 engineering process Methods 0.000 title abstract description 8
- 229910052602 gypsum Inorganic materials 0.000 claims abstract description 51
- 239000010440 gypsum Substances 0.000 claims abstract description 51
- 239000000463 material Substances 0.000 claims abstract description 50
- 239000007787 solid Substances 0.000 claims abstract description 28
- 239000000843 powder Substances 0.000 claims abstract description 21
- 238000000034 method Methods 0.000 claims abstract description 16
- 239000004568 cement Substances 0.000 claims abstract description 15
- 239000011343 solid material Substances 0.000 claims abstract description 10
- 238000007254 oxidation reaction Methods 0.000 claims description 17
- 230000009467 reduction Effects 0.000 claims description 17
- 239000000470 constituent Substances 0.000 claims description 15
- 230000003647 oxidation Effects 0.000 claims description 15
- 238000004519 manufacturing process Methods 0.000 claims description 13
- 239000000446 fuel Substances 0.000 claims description 11
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 3
- 230000015556 catabolic process Effects 0.000 claims description 2
- 238000006731 degradation reaction Methods 0.000 claims description 2
- 239000000376 reactant Substances 0.000 claims description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 abstract description 12
- 230000008569 process Effects 0.000 abstract description 6
- 239000012530 fluid Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 25
- 238000006722 reduction reaction Methods 0.000 description 14
- 238000000926 separation method Methods 0.000 description 10
- 230000000694 effects Effects 0.000 description 8
- 239000002994 raw material Substances 0.000 description 7
- 239000002912 waste gas Substances 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000001354 calcination Methods 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B11/00—Calcium sulfate cements
- C04B11/02—Methods and apparatus for dehydrating gypsum
- C04B11/028—Devices therefor characterised by the type of calcining devices used therefor or by the type of hemihydrate obtained
- C04B11/036—Devices therefor characterised by the type of calcining devices used therefor or by the type of hemihydrate obtained for the dry process, e.g. dehydrating in a fluidised bed or in a rotary kiln, i.e. to obtain beta-hemihydrate
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Ceramic Engineering (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Organic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention relates to an improved outer decomposition technique of a gypsum kiln. A circulating fluid bed technique is applied to the making process of sulfuric acid and cement clinker with gypsum decomposing, and the gypsum has no need of entering the kiln to be decomposed, but is circularly decomposed in a fluid-bed drier reactor of a decomposing furnace. The device of the present invention comprises a decomposing furnace main body and a cyclone preheating system, wherein the decomposing furnace main body is composed of a main body reactor, a deflective tapering shape cyclone separator with no inner cylinder and a solid material distributor. The technology of the present invention has the characteristic that the gypsum powder stays for 20 to 60 seconds in the main body reactor; the returned amount of the solid decomposing material returning back to the main body reactor from the material distributor is from 70 to 90%, etc.
Description
The present invention relates to the improvement that gypsum is processed into a kind of precal cination technique of sulfuric acid and cement clinker.
Circulating fluidized bed technique is applied to gypsum decomposition system sulfuric acid and the cement clinker aspect is a new technology, and gypsum needn't add in the kiln again and decompose, but decomposes in the decomposing furnace of circulating fluidized bed, and the gypsum raw material after the preheating add in the decomposing furnace of fluidized-bed, with CO or H
2Decompose, decompositions that circulate again of the intact material of unreacted, the material that reacts completely discharge enters rotary calciner calcining cement clinker, the SO that concentration is higher
2Tail gas is sent to manufacturing sulfuric acid.
United States Patent (USP) 4102989 discloses the technology of " carrying out the reduction and the oxygenolysis of calcium sulfate on fluidized-bed ", is characterized in hydrogenous carbon element fuel and primary air are imported reduction zone---the bottom of fluidized-bed, makes the reduction zone effectively CaSO
4Change the mixture of CaO and CaS into, draw secondary air again and enter fluidized-bed top (and on this horizontal plane, importing fuel), make top form oxidation zone, change CaS into CaO.CaO and SO that reaction generates
2All discharge by fluidized-bed top.This fluidized-bed can be the top sectional area greater than the long-pending cone of lower section.Primary air is the required O of fuel combustion
220～90%, secondary air is for importing 10～60% of air total amount.Temperature range is 1195～1250 ℃.This patent specification discloses, CaSO
4Entered in the reactor by reactor head, powder enters the top of fluidized-bed by a pipe; Cyclonic separator is located in the reactor, on fluidized-bed, is communicated with the fluidized-bed top by pipe; Primary air and secondary air all enter (indivedual embodiment secondary airs enter fluidized-bed by the top) by the fluidized-bed bottom, and the secondary air pipe is long slightly, air is imported the top of fluidized-bed conical part.Fluidisation is supported by gas distribution grid.
United States Patent (USP) 4102989 disclosed technology, secondary air pipe stretch into the fluidized-bed middle part, and pipe is longer, wants long term maintenance indeformable in the high flame of thousands of degree, and this is to be difficult to carry out and grasp aborning.Simultaneously, reactor volume is huge, and cyclonic separation and fluidized-bed etc. is included in the reactor, and this is also reasonable inadequately.This patented technology is in fact very difficult in a word, and does not in fact also use aborning.The improvement technology of German patent DE 3622688A1 then connects cyclonic separator and tripper and forms the outer loop decomposing system outside the main body reactor; Remedied the defective of United States Patent (USP); But the raw material of its new input drops into reactor after the preheating of cement rotary kiln tail gas, " waste gas " heat energy of reactor fails to be fully used, and has used the level Four preheater, and facility investment is bigger.
The object of the present invention is to provide a kind of heat energy utilization rate height, outer decomposition technique of the plaster kiln that technical process is more simplified and device.
In circulating fluidized bed, decompose gypsum and become solid CaO and gas SO
2Production technique, be to carry out in the recycle system formed of main body reactor, cyclonic separator, tripper and return line in fluidised bed decomposition furnace main body part and finish.Gypsum powder, fuel are dropped into the cylindrical bodies reactor, and import primary air wind as fluidized wind, make powder and fuel combustion produce CO or H from the main body reactor bottom
2, make Ca-SO
4Reduction.Feed secondary air wind controlled oxidation atmosphere on reactor top, make
CaSOxidation, for the atmosphere in the controlling reactor, also can on reactor, feed tertiary air wind in the middle part, like this, in the main body reactor, form a reduction zone and an oxidation zone, the gypsum particulate constantly circulates decomposition, gypsum degradation production CaO, SO at a wind between reduction zone and oxidation zone under the secondary air effect
2And other reactant gasess, discharge from the top of reactor simultaneously, through cyclonic separator and tripper, the solid materials that gypsum is decomposed partly turns back in the reactor, mixes with the gypsum powder of new input, realizes kiln outer circulation decomposition reaction.An important feature of the present invention be the new gypsum powder that drops into second stage cyclone preheater 2 in expellant gas enter first step cyclone preheater 1 after directly mixing, separated solid materials mixes for expellant gas in the cyclonic separator 5 of one with gas reactor 4 again, again after second stage cyclone preheater 2 separates, in pipeline investment subject reactor 4, mix with the decomposing materials that from decomposing furnace solids constituent glassware 6, returns and to proceed the decomposition reaction that circulates.The ratio of the decomposing materials that returns in new gypsum powder that drops into and the solids constituent glassware is 1: 2.5～6.0.The residence time of gypsum powder in the main body reactor is 20-60 seconds, the temperature of control reduction zone is 850～1080 ℃ in the main body reactor, the temperature of oxidation zone is 1000-1150 ℃, and cross section, reduction zone wind speed is 1.6-5 meter per seconds, and oxidation zone cross section wind speed is 3.4-6 meter per seconds.
The fluidized bed type decomposer that is used for the gypsum decomposition provided by the present invention is made up of main part and a whirlwind preheating system of a decomposing furnace, the principal feature of invention is the main part of said decomposing furnace: have one to become the inclined to one side bevel-type of integral body not have the inner core cyclonic separator with it above a cylindrical bodies reactor, below cyclonic separator, connect a box solids constituent glassware, said box solids constituent glassware becomes the fluidized bed type blowdown valve of integral body to be made up of the sub-material chamber with one with it, make solid powder when the solids constituent glassware is distributed, solid powder is shunted between the returning charge mouth of blowdown valve and sub-material chamber in proportion.Above cyclonic separator, be connected with the two stage cyclone preheater.
The cyclonic separator that uses in the prior art is cartridge type cyclonic separator in the right cone, in this gypsum decomposing system, use, because temperature of charge height, contain the higher sulfur dioxide gas of concentration in the system, the inner core of cyclonic separator easily is corroded, and damages distortion, thereby has reduced the separating effect of separator, often repair and replacement involve great expense.The present invention has adopted cartridge type cyclonic separator in a kind of nothing according to desired separation efficiency, in order to overcome the difficult problem of gypsum material high temperature current downflow difference, taked inclined to one side tapered, awl has changed the trend of air-flow and streams partially, promote the slippage of material, thereby improved gas-solid body separation efficiency, reached effective gas-solid separating effect, solved in the prior art damage that easily is corroded of cyclonic separator inner core, the problem that separation efficiency descends.Inclined to one side bevel-type used in the present invention does not have the inner core cyclonic separator, and the eccentric angle of cone (the minimum angle of cylindrical shell bus and cone generatrices) can be selected in 0～30 ° of scope.Can certainly select the inclined to one side bevel-type cyclonic separation of inner core for use, such problem that still exists inner core easily to be corroded, if select corrosion resistant material inner core for use, facility investment will be much higher.Positive bevel-type cyclonic separator cone angle increase also can be used, but effect is not as inclined to one side bevel-type.
Adopted the said box solids constituent glassware of CN92240256.6 patent in the present invention, it is a kind of fluidized bed type tripper, comprises sub-material chamber 24 and blowdown valve 30 two portions.Blowdown valve 30 is made an integral body with sub-material chamber 24, also is fluidized bed type, as shown in Figure 3.An opening for feed 25 is arranged above sub-material chamber 24, and it is relative with the valve opening 31 of the blowdown valve 30 of being located at 24 bottoms, sub-material chamber; The other end of sub-material chamber 24, top are provided with discharge gate 27, i.e. returning charge mouth, and the major part of the solid materials after the separation is from returning main body reactor 4 here.Bottom, sub-material chamber is provided with two blast inlets 28, and pressing close to bottom, sub-material chamber above blast inlet 28 has one deck dispersion plate 29, constitutes a wind box with sub-material chamber base plate.There is the lock aerofoil 26 of an adjustment height centre of sub-material chamber, and the sub-material chamber is divided into two portions.The control of lock aerofoil 26 height is by the pressure reduction decision of tripper 24 into and out of the material mouth, and generally its height is 1.5～3 times of both pressure differences.The up-down adjustment of lock aerofoil 26 is in order to control the size of passage between the separated two portions of tripper, to play the effect of lock wind, avoiding producing between pressure bigger import 25 and the discharge gate 27 and scurry the wind phenomenon.Fluidized bed type blowdown valve 30 bottoms are provided with a blast inlet 28, and blowdown valve 30 bottoms of pressing close to blast inlet 28 also are provided with one deck dispersion plate 29.One side of valve is provided with discharge port 34, and the small portion solid materials enters rotary kiln thus and produces cement clinker; A spool 32 is arranged in the blowdown valve 30, reached in the blowdown valve 30 by center at the bottom of the valve, spool 32 is aimed at valve opening 31, can regulate height by setter 33.By the height of regulating spool 32, size that can control valve bore 31, thus regulate the materials flow ratio that the tripper branch is expected sub-material chamber 24 and blowdown valve 30 and is discharged to main body reactor 4 and rotary kiln 14 respectively.To return the amount of main body reactor from the solids constituent glassware be to enter 70-90% of tripper inventory to the solid decomposer material in the present invention.Because the fluidized bed type structure is all adopted with blowdown valve 30 in sub-material chamber 24, material remains active state in the tripper, make solid materials in tripper, be able to quantitatively shunt uniformly and stably, like this, rationally controlled, to reach the abundant decomposition of gypsum the residence time of material in circulating fluidized bed.
Introduce technical process of the present invention below in conjunction with accompanying drawing in detail with an example.
Fig. 1 is that gypsum decomposes agent set and process flow diagram.
Fig. 2 decomposes and producing cement clinker device technique schematic flow sheet for gypsum.
Fig. 3 is the cross-sectional view of solids constituent glassware.
Fig. 4 does not have inner core cyclonic separator cross-sectional view for inclined to one side bevel-type.
Fig. 5 does not have inner core cyclonic separator vertical view for inclined to one side bevel-type.
Among the figure, 1. one-level cyclone preheater, 2. secondary cyclone preheater, 3. gypsum powder pipeline system, 4. main body reactor (fluidized-bed), 5. cyclonic separator, 6. solids constituent glassware 7. enters the solid material pipelines system of rotary kiln, 8. fluidized wind (primary air wind), 9. secondary air wind, 10. fuel delivery system, 11. pipelines from cyclonic separator to the secondary cyclone preheater.12. pipeline from the secondary cyclone preheater to the one-level cyclone preheater.13. with SO
2Gas is sent to the pipeline of relieving haperacidity.14. rotary kiln, 15. cement clinker coolers, 16. Pulverized Coal Bin, 17. raw material silo, 18. raw mills, 19. gypsum storehouses, 20. the subsidiary material storehouse, 21. dryers, 22. dust-precipitators, 23. chimney, sub-material chambers 24., 25. opening for feeds, 26. the lock aerofoil, 27. discharges (returning charge) mouth, 28. blast inlets, 29. gas distribution grid, 30. blowdown valves, 31. valve openings, 32. spool, 33. spool setters, 34. discharge ports, 35. gas feed, the minimum angle of 36. cylindrical shell buses and cone generatrices, 37. material outlets, 38. cone, 39. cylindrical shell bus and cone generatrices angle, 40. cylindrical shells, 41. pneumatic outlets.Fig. 1, Fig. 2 arrow solid line are represented the material direction, and the arrow dotted line is represented gas direction.
As shown in Figure 1 and Figure 2, the gypsum powder that has carried out the grinding batching through raw mill 18 adds pipeline 12 from raw material silo 17, by the SO that discharges from secondary cyclone preheater 2
2Air-flow is brought the one-level cyclone preheater into, and after one-level preheating and gas solid separation, gypsum powder enters pipeline 11, accompanys or follow the SO that contains of cyclonic separator 5 discharges
2Air-flow is sent in the secondary cyclone preheater 2, by the secondary preheating and send into the bottom of main body reactor 4 by pipeline system 3 through gas solid separation, fuel (can be kerosene or Sweet natural gas etc.) also is admitted to reactor lower part from delivery system 10, and gypsum raw material and fuel all are added on the interior grid distributor of reactor.Expect that from the cement heat of rotary kiln the fluidized wind 8 that cooler 15 draws enters reactor as primary air wind from main body reactor 4 bottoms, CO or H that non-complete combustion of fuel is generated
2Carry out reduction reaction Deng reducing medium and gypsum powder, generate CaO, SO
2With a small amount of CaS, at this moment temperature of reaction is at 850-950 ℃, and reduction zone atmosphere is CO1.5～4%, and primary air wind is 3～3.5 meter per seconds at the cross section of reduction zone wind speed.The waste gas that comes out from rotary kiln enters the middle part of going up of main body reactor 4 as secondary air wind 9 by annular passage, and the middle and upper part of control main body reactor is an oxidation zone, keeps micro-oxidizing atmosphere to contain O
20.5～2%, make the CaS oxidation, accelerated the gas velocity in the fluidized-bed simultaneously, the material after decomposing is taken out of, enter cyclonic separator 5.Secondary air is 4～4.5 meter per seconds in the cross section of oxidation zone speed, and the oxidation zone temperature is 1000～1050 ℃.The reduction zone accounts for 2/3rds of reactor volume, the reduction and oxidizing atmosphere be by fuel add-on, once adjust with secondary air flow.
The effect of cyclonic separator 5 is that the feed separation of recirculation is got off.Because the temperature of charge height is hung at the conical part knot easily, causes cone and the pipeline below it (dipleg) to stop up, inclined to one side bevel-type of the present invention does not have the inner core cyclonic separator and has solved this difficult problem preferably.
In main body reactor 4, all material suspended in air-flow, the density of suspensoid is successively decreased to the top by reactor bottom, gas flow rate increases progressively, material approximately stopped 20-60 seconds in reactor through reduction-oxidation two sections, go out reactor with gas entrainment, separated following in cyclonic separator 5, again through box solids constituent glassware 6 shuntings, 80% material returns main body reactor 4 through the returning charge mouth 27 of sub-material chamber 24, another small portion material (20%) is discharged by the discharge port 34 of the blowdown valve 30 of tripper 6, sends into rotary kiln 14 calcinings through pipeline 7 and makes cement clinker.The cement clinker kiln discharge is after cooler 15 discharges.
The SO that contains from reactor 4 discharges
2Gas remove light breeze preheater 2 through pipeline 11, in pipeline 11 with after the gypsum raw material that come out from one-level cyclone preheater 1 mix, enter in the secondary cyclone preheater 2 and feed separation, remove one-level cyclone preheater 1 through pipeline 12 again, in pipeline 12 ways, be mixed mutually with initiate gypsum raw material again and enter in the one-level cyclone preheater 1, separate after pipeline 13 is sent to relieving haperacidity with solid materials, contain SO
2Gas SO when reactor 4 is discharged
2Concentration is 15% (dry gas volume percent).
Because tripper 6 also is a fluidized bed type, therefore the fluidized wind (also being the primary air wind of sending into reactor) 8 that comes from rotary kiln has also been introduced tripper 6.According to the reaction and the operational circumstances that drop in the unit time in inventory and the reactor 4, regulate the height of the spool 32 of blowdown valve 30, can adjust the size of valve opening 31, thus the material amount of control Returning reactor 4 and the material amount ratio that is discharged into rotary kiln 14.The gypsum powder of the new input of control reactor is 1: 2.5～6.0 with the ratio of returns amount.Like this, just controlled the residence time of material in reactor, guaranteed that gypsum fully decomposes.For example: dropping into the virgin material amount is 11.0～11.6 tons/hour, is 35～38 tons/hour from the inventory of tripper 6 Returning reactors 4, and discharging material (return stove or go into kiln) quality index is CaS＜0.32, SO
3＜0.17.
The hot gas of rotary kiln waste gas and cement clinker cooler is used for for oven dry gypsum, burning (wind of reactor, secondary air) and preheating (fluidized wind of tripper 6 also has pre-heat effect), and heat is fully used.And from the SO that contains of decomposing furnace main reactor 4
2Gas then in two (or three) level cyclone preheater and pipeline to the direct preheating of new gypsum powder, contain SO
2Furnace gas is to separate running with rotary kiln waste gas, thereby can accurately control the operational condition that gypsum decomposes and grog is produced, and guarantees to produce normal operation.
Because device provided by the invention and technology make the kiln of gypsum be able to continuous operation in actual production outer the decomposition, carry out smoothly.In the cover production equipment by the present invention design, per hour drop into 11.4 tons of new gypsum materials, but 6.3 tons of the materials that decompose of output per hour, the SO after the decomposition
2Gas concentration is that rate of decomposition reaches 100% more than 15%, has guaranteed the quality of sulfuric acid and cement clinker.And because this device has overcome the defective that exists in the prior art, the heat energy utilization rate is higher, such as utilizing the reactor furnace gas, contains SO
2The directly pre-thermal material of gas, utilize rotary kiln waste gas for oven dry, burning etc. form each stage heat closed circulation, thereby guarantee that the heat energy that produces in the flow process obtains optimum utilization, both make full use of heat energy, saved the energy, simplified technical process again, reduced primary heater unit and reached good effect than prior art, saved a large amount of construction investments, reduced production cost, helped decomposing the maximization production of system sulfuric acid, cement clinker with gypsum.
Claims (8)
1, kiln decomposes gypsum outward becomes solid CaO and gas SO
2Production technique, be in the recycle system that forms by fluidized-bed reactor, cyclonic separator, tripper and return line, gypsum powder, fuel are dropped into the cylindrical bodies reactor, and lead people's primary air as fluidized wind, make its burning produce CO or H from reactor bottom
2, import secondary air on reactor top, in the main body reactor, form a reduction zone and an oxidation zone, the gypsum particulate constantly circulates decomposition between reduction zone and oxidation zone, gypsum degradation production CaO, SO
2Other reactant gasess, discharge from cylindrical bodies reactor top simultaneously, through cyclonic separator and solids constituent glassware, the solid materials part that gypsum is decomposed turns back to the main body reactor, mix with the gypsum powder of new input, realize the circulation decomposition reaction, another part discharges into calcined by rotary kiln and becomes cement clinker, it is characterized in that entering first step cyclone preheater after expellant gas directly mixes in the new material that drops into and the second stage cyclone preheater, separated solid materials mixes with expellant gas in the main body reactor cyclone again, after second stage cyclone preheater separates in the investment subject reactor; The residence time of gypsum powder in the main body reactor is 20-60 second, and the solid decomposer material returns the main body reactor from the solids constituent glassware the amount of returning is 70-90%.
2, according to the described gypsum decomposition and production process of claim 1, the temperature of reaction that it is characterized in that reduction zone in the main body reactor is 850-1080 ℃, and is 1000-1150 ℃ in the temperature of reaction of oxidation zone.
3,, it is characterized in that the cross section wind speed of reduction zone in the main body reactor is controlled at the 1.6-5 meter per second, and the cross section wind speed of oxidation zone is controlled at the 3.4-6 meter per second according to the described gypsum decomposition and production process of claim 1.
4, according to the described gypsum decomposition and production process of claim 1, the ratio that it is characterized in that newly dropping into gypsum inventory and the returns amount of returning the main body reactor from tripper is 1: 2.5-6.0.
5, according to the described gypsum decomposition and production process of claim 1, the atmosphere CO that it is characterized in that controlling reduction zone in the main body reactor is 1.5～4%, the atmosphere O of oxidation zone
2Be 0.5～2%.
6, a kind of fluidized bed type decomposer that is used for the outer decomposition technique of the described plaster kiln of claim 1, comprise a decomposing furnace main part and a whirlwind preheating system, it is characterized in that said decomposing furnace main part has one to become the inclined to one side bevel-type of integral body not have the inner core cyclonic separator with it above a cylindrical bodies reactor, below cyclonic separator, connect a box solids constituent glassware; Said box solids constituent glassware becomes the fluidized bed type blowdown valve of integral body to be made up of the sub-material chamber with one with it, make solid powder when the solids constituent glassware is distributed, and solid powder is shunted between the returning charge mouth of blowdown valve and sub-material chamber in proportion; Above cyclonic separator, link to each other with the two stage cyclone preheater.
7, according to the described fluidized bed type decomposer of claim 6, it is characterized in that said inclined to one side bevel-type cyclonic separator, the minimum angle of its cylindrical shell bus and cone generatrices is 0-30 °.
8,, it is characterized in that having in the said fluidized bed type blowdown valve spool of an adjustable valve hole size according to the described fluidized bed type decomposer of claim 6.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 93111274 CN1031499C (en) | 1993-06-05 | 1993-06-05 | Outer decomposition technology and device for plaster kiln |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 93111274 CN1031499C (en) | 1993-06-05 | 1993-06-05 | Outer decomposition technology and device for plaster kiln |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1079724A CN1079724A (en) | 1993-12-22 |
| CN1031499C true CN1031499C (en) | 1996-04-10 |
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ID=4989073
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 93111274 Expired - Fee Related CN1031499C (en) | 1993-06-05 | 1993-06-05 | Outer decomposition technology and device for plaster kiln |
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| CN (1) | CN1031499C (en) |
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| DE10333361A1 (en) * | 2003-07-23 | 2005-02-10 | Gebr. Pfeiffer Ag | Process for preparation of cement e.g. Portland cement involves milling cement clinker with sulfate containing carrier material and other components in a roller mill |
| CN102219410B (en) * | 2011-03-24 | 2012-10-24 | 西安建筑科技大学 | Suspended-stated external circulating type high-solid-gas-ratio decomposition reactor |
| CN104474887B (en) * | 2014-11-24 | 2016-10-19 | 黄晓研 | Preparation and application method of desulfurization and denitrification compound agent for dry process cement kiln |
| CN105858620B (en) * | 2016-05-20 | 2018-01-02 | 四川大学 | A kind of method for cooperateing with fluidisation decomposing gypsum |
| CN108503247B (en) * | 2018-06-21 | 2023-11-28 | 四川方大新型建材科技开发有限责任公司 | Method and equipment for producing high-temperature gypsum from industrial byproduct gypsum |
| CN114646220B (en) * | 2020-12-17 | 2024-11-05 | 中国科学院工程热物理研究所 | Cement material processing device and cement material processing method |
| CN112984784A (en) * | 2021-02-05 | 2021-06-18 | 陕西翼飞航智能科技有限公司 | CaSO4 decomposition and decomposition gas recovery system and method based on SO2 and O2 plasma hot blast stove |
| CN119706753B (en) * | 2025-03-04 | 2025-05-16 | 杭州亚太化工设备有限公司 | Industrial by-product phosphogypsum reprocessing sulfuric acid system and acid production process |
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1993
- 1993-06-05 CN CN 93111274 patent/CN1031499C/en not_active Expired - Fee Related
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