CN110803876B - II type anhydrous gypsum thermal coupling production device and method - Google Patents
II type anhydrous gypsum thermal coupling production device and method Download PDFInfo
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- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 title claims abstract description 47
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 28
- 230000008878 coupling Effects 0.000 title claims abstract description 27
- 238000010168 coupling process Methods 0.000 title claims abstract description 27
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims description 54
- 238000001816 cooling Methods 0.000 claims abstract description 123
- 239000010440 gypsum Substances 0.000 claims abstract description 99
- 229910052602 gypsum Inorganic materials 0.000 claims abstract description 99
- 238000001035 drying Methods 0.000 claims abstract description 87
- 239000000463 material Substances 0.000 claims abstract description 72
- 238000006243 chemical reaction Methods 0.000 claims abstract description 68
- 239000006227 byproduct Substances 0.000 claims abstract description 22
- 238000010438 heat treatment Methods 0.000 claims description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 238000005243 fluidization Methods 0.000 claims description 18
- 230000008569 process Effects 0.000 claims description 17
- 238000000926 separation method Methods 0.000 claims description 14
- 239000000446 fuel Substances 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 11
- 238000002485 combustion reaction Methods 0.000 claims description 8
- 229910052925 anhydrite Inorganic materials 0.000 claims description 6
- 239000002002 slurry Substances 0.000 claims description 5
- 239000002826 coolant Substances 0.000 claims description 3
- 238000001354 calcination Methods 0.000 abstract description 18
- 239000000047 product Substances 0.000 abstract description 14
- 238000005516 engineering process Methods 0.000 abstract description 9
- 238000004134 energy conservation Methods 0.000 abstract description 8
- 230000009467 reduction Effects 0.000 abstract description 8
- 239000007789 gas Substances 0.000 description 61
- 238000005265 energy consumption Methods 0.000 description 7
- 239000000843 powder Substances 0.000 description 5
- PASHVRUKOFIRIK-UHFFFAOYSA-L calcium sulfate dihydrate Chemical compound O.O.[Ca+2].[O-]S([O-])(=O)=O PASHVRUKOFIRIK-UHFFFAOYSA-L 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
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- 230000035484 reaction time Effects 0.000 description 3
- WNEODWDFDXWOLU-QHCPKHFHSA-N 3-[3-(hydroxymethyl)-4-[1-methyl-5-[[5-[(2s)-2-methyl-4-(oxetan-3-yl)piperazin-1-yl]pyridin-2-yl]amino]-6-oxopyridin-3-yl]pyridin-2-yl]-7,7-dimethyl-1,2,6,8-tetrahydrocyclopenta[3,4]pyrrolo[3,5-b]pyrazin-4-one Chemical compound C([C@@H](N(CC1)C=2C=NC(NC=3C(N(C)C=C(C=3)C=3C(=C(N4C(C5=CC=6CC(C)(C)CC=6N5CC4)=O)N=CC=3)CO)=O)=CC=2)C)N1C1COC1 WNEODWDFDXWOLU-QHCPKHFHSA-N 0.000 description 2
- 239000004566 building material Substances 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000011343 solid material Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- DGLFSNZWRYADFC-UHFFFAOYSA-N chembl2334586 Chemical compound C1CCC2=CN=C(N)N=C2C2=C1NC1=CC=C(C#CC(C)(O)C)C=C12 DGLFSNZWRYADFC-UHFFFAOYSA-N 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000306 component Substances 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000005034 decoration Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- LPUQAYUQRXPFSQ-DFWYDOINSA-M monosodium L-glutamate Chemical compound [Na+].[O-]C(=O)[C@@H](N)CCC(O)=O LPUQAYUQRXPFSQ-DFWYDOINSA-M 0.000 description 1
- 235000013923 monosodium glutamate Nutrition 0.000 description 1
- 239000004223 monosodium glutamate Substances 0.000 description 1
- 239000004570 mortar (masonry) Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/46—Sulfates
- C01F11/466—Conversion of one form of calcium sulfate to another
-
- 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
- C04B11/26—Calcium sulfate cements strating from chemical gypsum; starting from phosphogypsum or from waste, e.g. purification products of smoke
-
- 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
- C04B11/26—Calcium sulfate cements strating from chemical gypsum; starting from phosphogypsum or from waste, e.g. purification products of smoke
- C04B11/262—Calcium sulfate cements strating from chemical gypsum; starting from phosphogypsum or from waste, e.g. purification products of smoke waste gypsum other than phosphogypsum
-
- 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
- C04B11/26—Calcium sulfate cements strating from chemical gypsum; starting from phosphogypsum or from waste, e.g. purification products of smoke
- C04B11/262—Calcium sulfate cements strating from chemical gypsum; starting from phosphogypsum or from waste, e.g. purification products of smoke waste gypsum other than phosphogypsum
- C04B11/264—Gypsum from the desulfurisation of flue gases
-
- 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
- C04B11/26—Calcium sulfate cements strating from chemical gypsum; starting from phosphogypsum or from waste, e.g. purification products of smoke
- C04B11/266—Chemical gypsum
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Ceramic Engineering (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Processing Of Solid Wastes (AREA)
- Drying Of Solid Materials (AREA)
Abstract
The invention provides a II-type anhydrous gypsum thermal coupling production device which comprises a drying device, a fluidized reactor, a cyclone reactor and a cooling unit, wherein the drying device, the fluidized reactor, the cyclone reactor and the cooling unit are sequentially connected, the cooling unit comprises at least one stage of cooling device, and a cold source outlet of the cooling unit is independently connected with gas inlets of the drying device, the fluidized reactor and the cyclone reactor. According to the invention, gypsum materials are subjected to graded calcination by utilizing different characteristics of the device, the reaction is controlled to be carried out, and then the II-type anhydrous gypsum product is obtained through multi-stage cooling, so that the resource utilization of industrial byproduct gypsum is realized; the device adopts a multistage thermal coupling technology, the heat in the product cooling stage is fully used in the drying and reaction stage, the heat in the system is fully utilized, and the energy conservation, consumption reduction and stable operation of the device are realized.
Description
Technical Field
The invention belongs to the technical field of industrial solid waste utilization, and relates to a II-type anhydrous gypsum thermal coupling production device and method.
Background
With the rapid development of industry, a large amount of industrial by-product gypsum is discharged while natural gypsum resources are mined and consumed, wherein the industrial by-product gypsum refers to a by-product or waste residue which is generated in industrial production and takes calcium sulfate as a main component due to chemical reaction, is also called chemical gypsum or industrial waste gypsum and mainly comprises desulfurized gypsum, phosphogypsum, citric acid gypsum, fluorgypsum, salt gypsum, monosodium glutamate gypsum, copper gypsum, titanium gypsum and the like, and the production amount of the desulfurized gypsum and the phosphogypsum accounts for about 85% of the total amount of all the industrial by-product gypsum.
The industrial byproduct gypsum has various types, different process operation conditions and raw material sources cause different components and unstable quality of the industrial byproduct gypsum, and due to the problems of multiple and complex harmful impurity components, acid and fluorine containing and the like, the problem that the process can solve all the industrial byproduct gypsum is difficult to realize, so that the research and comprehensive application progress is slow, a large amount of industrial byproduct gypsum is accumulated, cultivated land is occupied, water and soil are polluted, the living environment of human is greatly damaged, and huge economic and environmental protection pressure is caused for industrial byproduct gypsum discharge enterprises.
At present, there are two main ways for the comprehensive utilization of industrial by-product gypsum: firstly, the cement retarder is used and accounts for about 70 percent of the comprehensive utilization amount of industrial byproduct gypsum; secondly, produce the gypsum building materials products, including paper-faced gypsum board, gypsum block, gypsum hollow slat, dry-mixed mortar, gypsum brick, etc., but in the above-mentioned utilization route, only to the application after simple of gypsum, harmful impurity in the gypsum is not fully removed, the comprehensive utilization rate is low, and when used as the building material, generally can only be used in the plane materiel or decoration, it is difficult to use as the main structure material, application amount and application range are limited. Therefore, gypsum needs to be converted to replace traditional cement, so that industrial byproduct gypsum can be digested in a large amount, and the problem of environmental protection is solved.
CN 105985036A discloses a method for processing phosphogypsum, mixing phosphogypsum and lime, adding the mixture into a drying and calcining machine, arranging a flame-jet furnace at the end, adopting a grading outlet at the outlet of the drying and calcining machine to obtain semi-hydrated gypsum and anhydrous gypsum II respectively, sending the outlet gypsum into a stirring, homogenizing, reducing and conveying device to fully contact the mixed gypsum with air, distributing the gypsum in different forms, and carrying out crystal conversion on qualified gypsum to obtain finished gypsum, wherein the drying and calcining machine cannot accurately control the calcining process in the method, the grading outlet is required to be arranged, and then mixing and aging are carried out to produce beta type gypsum powder; the drying and calcining machine is provided with a flame furnace, so that the calcining time is difficult to control, and the product fluctuation is large.
CN 204138536U discloses a device for drying and calcining desulfurized gypsum, which comprises a feeding structure, a scattering structure, an air flow drying tower, a pulse bag-type dust collector and a draught fan which are connected in sequence, wherein the pulse bag-type dust collector is connected with a calcining boiling furnace, the bottom of the pulse bag-type dust collector is provided with a spiral conveying structure, the spiral conveying structure is connected with a feeding hole of the calcining boiling furnace, and a waste heat outlet of the calcining boiling furnace is connected with the scattering structure through an air duct; the device has good sealing performance, can produce various gypsum products, but has unclear hierarchical distribution of drying and calcining, has lower temperature of the drying and calcining, can only obtain semi-hydrated gypsum, and has limited application range.
In conclusion, for the comprehensive utilization of the industrial byproduct gypsum, different devices are required to accurately control the drying and calcining processes, so that the anhydrous gypsum product with wider application range is prepared, the utilization rate of heat in the devices is improved, and the energy consumption is reduced.
Disclosure of Invention
Aiming at the problems in the prior art, the invention aims to provide a II-type anhydrous gypsum thermal coupling production device and a method, wherein gypsum materials are sequentially dried, fluidized reaction, cyclone reaction and multi-stage cooling, the characteristics of the device are utilized to carry out graded calcination, the residence time is controlled, the II-type anhydrous gypsum is obtained, and the resource utilization of industrial byproduct gypsum is realized; meanwhile, a multistage thermal coupling technology is adopted, so that the heat in the device is fully utilized, and energy conservation and consumption reduction are realized.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides a II-type anhydrous gypsum thermal coupling production device which comprises a drying device, a fluidized reactor, a cyclone reactor and a cooling unit, wherein the drying device, the fluidized reactor, the cyclone reactor and the cooling unit are sequentially connected, the cooling unit comprises at least one stage of cooling device, and a cold source outlet of the cooling unit is independently connected with gas inlets of the drying device, the fluidized reactor and the cyclone reactor.
According to the invention, the device utilizes the characteristics of different stages of gypsum materials to carry out drying, fluidized reaction, rotational flow reaction and multi-stage cooling in sequence, the fluidized reaction and the rotational flow reaction are two-stage calcining processes, different devices are selected to control the retention time, and in the multi-stage cooling stage of finished products, heat is transferred to a cooling medium and then used for heating of the drying and reaction, and the multi-stage thermal coupling technology is adopted to fully utilize the heat of the system, thereby realizing energy conservation and consumption reduction and stable operation of the device.
As a preferred technical scheme, the drying device comprises a pneumatic drying tower.
Preferably, the material inlet of the drying device is provided with a breaking assembly.
In the invention, the initial wet material has high water content, free water is on the surface of the material, the drying speed is high, and the method can be completed by using airflow drying in an airflow drying tower by applying a flash evaporation technology. Gypsum material enters the air flow dryer through the spiral conveyor, and the rotatable blade is installed at the material receiving part of the gypsum material, so that the gypsum material is ensured to fall into the air flow dryer and be scattered.
The air inlet of the airflow drying tower comes from air preheated by the cooling tower, the hot air blows and floats scattered wet materials, when the wet materials reach the upper part of the drying tower, the air pressure in the drying tower is reduced, free water on the surfaces of the materials is flashed into steam and taken away by the hot air, and the outlet of the airflow drying tower adopts an induced draft fan, so that negative pressure is kept in the tower, and the separation of moisture is facilitated. After being dried by airflow, the powder is subjected to gas-solid separation by a cyclone separator, the powder enters a fluidized reactor through a discharge valve after being collected, and dry exhausted gas is discharged into the atmosphere after being dedusted.
As a preferable technical scheme of the invention, an inclined tower plate is arranged on the inner wall of the fluidized reactor, and one end of the inclined tower plate is connected with the inner wall; wherein adjacent trays are disposed on opposite sides of the inner wall.
Preferably, the inclination directions of two adjacent inclined trays are opposite.
Preferably, the inclined plate has an angle of 30 to 60 degrees with the horizontal, such as 30 degrees, 35 degrees, 40 degrees, 45 degrees, 50 degrees, 55 degrees, or 60 degrees, but not limited to the recited values, and other values not recited in the range of values are also applicable.
Preferably, the inclined tower plate is provided with a bubble cap and a heating coil.
Preferably, the heating coils comprise an upper heating coil and a lower heating coil, respectively arranged on the upper side and the lower side of the inclined tray.
The fluidized reactor is a tower plate type heating reactor, the tower plate is obliquely arranged and is subjected to layered baffling, holes are formed in the plate, bubble caps are arranged on the holes, holes are formed in the bubble caps, airflow below the bubble caps is in direct contact heat exchange with materials through the bubble caps and has the functions of diversion and stirring of the materials, a heating coil is arranged above the tower plate, the gas in the heating coil is used for exhausting gas of the cyclone reactor to perform indirect heat exchange with the materials, the materials flow downwards along the oblique tower under the action of gravity and the airflow, the materials are heated and react in the flowing process, the reaction temperature is controlled by the temperature and the flow of hot air in the heating coil, and the flow speed of the materials in the reactor is controlled by the quantity of disturbed flow gas.
In the invention, the waste gas at the top of the fluidized reactor is subjected to gas-solid separation through the cyclone separator, a small amount of powder is conveyed into the cyclone reactor through the discharge valve after being collected, the gas is used for heating the inlet air of the airflow drying tower, and the hot air in the heating coil pipe also enters the air heater for heating the inlet air of the airflow drying tower.
As a preferable technical scheme of the invention, a cyclone plate is arranged in the cyclone reactor.
Preferably, the number of the swirl plates is 2-8, such as 2, 3, 4, 5, 6, 7 or 8.
Preferably, the swirl plate is of a conical configuration.
According to the invention, a plurality of layers of cyclone internals are arranged in the cyclone reactor, the air flow is controlled to spirally rise, hot flue gas generated by fuel combustion in a hot blast stove enters from the lower part of the cyclone reactor, entrained materials pass through the cyclone plates and then flow spirally, solid materials spirally rise along the inner wall of the reactor under the drive of centrifugal force and spiral air flow, when reaching the next cyclone plate, the air flow enters a spiral channel arranged in the center of the cyclone plate and spirally flows upwards from the center, and part of the materials fall without the air flow at the lower outer edge of the cyclone plate and are carried by the rising air flow in the falling process. The solid material falls and rises for many times and slowly passes through the cyclone reactor under the drive of the spiral airflow; the number of the rotational flow plates and the flow rate of the gas can control the retention time of the materials in the reactor.
As a preferable technical scheme of the present invention, the cooling unit comprises a first cooling tower, an auger cooler and a second cooling tower which are connected in sequence, a cold source outlet of the first cooling tower is connected to a gas inlet of the cyclone reactor through a hot blast stove, a gas outlet of the cyclone reactor is connected to a gas inlet of the fluidized reactor, and a cold source outlet of the second cooling tower is connected to a gas inlet of the drying device.
Preferably, the cold source outlet of the second cooling tower is connected with the gas inlet of the gas flow drying tower through a gas heater.
Preferably, the hot source inlet of the gas heater is connected with the gas outlet of the fluidized reactor and/or the cold source outlet of the auger cooler.
In the invention, the discharged material of the cyclone reactor is subjected to multi-stage cooling, one part of hot air discharged from a first cooling tower is conveyed to the lower part of the fluidized reactor for air inlet, the powder of the fluidized reactor is subjected to turbulent flow heating, and the other part of hot air enters a hot blast stove to be mixed and combusted with fuel, and then enters the cyclone reactor for providing heat;
the finished product material cooled by the first cooling tower enters an auger cooler, and the used medium water is heated or forms steam to provide heat for hot air of the airflow drying tower; and then the material is cooled by a second cooling tower, and the heated air medium enters an airflow drying tower for heat recovery.
Preferably, the device further comprises a solid-liquid separation device which is arranged in front of the drying device.
Preferably, the solid-liquid separation device comprises a centrifuge.
In the present invention, since the gypsum raw material to be treated contains impurities, it is necessary to perform pretreatment and sometimes to obtain a gypsum slurry, and therefore, it is necessary to perform preliminary solid-liquid separation.
In another aspect, the present invention provides a method for thermally coupling production of type ii anhydrite using the above apparatus, the method comprising the steps of:
(1) drying the gypsum material and then carrying out a fluidization reaction to generate semi-hydrated gypsum;
(2) carrying out rotational flow reaction on the semi-hydrated gypsum obtained in the step (1) to obtain II type anhydrous gypsum;
(3) and (3) cooling the type II anhydrous gypsum obtained in the step (2), and supplying heat for the reaction in the step (1) and the step (2) after the medium serving as a cold source is heated in the cooling process.
As a preferable technical scheme of the invention, the source of the gypsum material in the step (1) is industrial by-product gypsum.
Preferably, the gypsum material in the step (1) is obtained by solid-liquid separation of gypsum slurry.
Preferably, the gypsum material of step (1) has a free water content of 20 to 25 wt.%, such as 20 wt.%, 21 wt.%, 22 wt.%, 23 wt.%, 24 wt.% or 25 wt.%, and the like, but is not limited to the recited values, and other values not recited within this range are equally applicable.
Preferably, the gypsum material in step (1) is broken up before being dried, and then dried by gas flow.
Preferably, after drying in step (1), the temperature of the gypsum material is 60 to 80 ℃, for example 60 ℃, 65 ℃, 70 ℃, 75 ℃ or 80 ℃, but not limited to the recited values, and other values not recited in the range of values are also applicable.
Preferably, after drying in step (1), the gypsum material has a free water content of no greater than 1wt%, e.g., 1wt%, 0.9 wt%, 0.8 wt%, 0.7 wt%, 0.6 wt%, 0.5 wt%, or 0.4 wt%, etc., but is not limited to the recited values, and other values not recited within the range are equally applicable.
As a preferred technical scheme of the invention, the fluidization reaction in the step (1) is carried out in a fluidization reactor.
Preferably, the temperature of the fluidization reaction in step (1) is 130 to 160 ℃, for example 130 ℃, 135 ℃, 140 ℃, 145 ℃, 150 ℃, 155 ℃ or 160 ℃, but is not limited to the recited values, and other values not recited in the range of the values are also applicable.
Preferably, the fluidized reaction time in step (1) is 20-30 min, such as 20min, 22min, 24min, 25min, 26min, 28min or 30min, but not limited to the recited values, and other values not recited in the range of the values are also applicable.
In the present invention, under the above-mentioned fluidization reaction conditions, the dried gypsum material CaSO4·2H2Removing part of bound water from O, and converting into CaSO4·0.5H2O。
As a preferred technical scheme of the invention, the cyclone reaction in the step (2) is carried out in a cyclone reactor.
Preferably, the temperature of the swirling reaction in step (2) is 500 to 600 ℃, for example, 500 ℃, 520 ℃, 540 ℃, 560 ℃, 580 ℃, or 600 ℃, but not limited to the recited values, and other values not recited in the range of the values are also applicable.
Preferably, the time of the cyclone reactor in step (2) is 40-60 min, such as 40min, 45min, 50min, 55min or 60min, but not limited to the recited values, and other values not recited in the range of the recited values are also applicable.
Preferably, the heat required by the cyclone reaction in the step (2) is provided by a hot blast stove.
Preferably, the outlet gas temperature of the hot blast stove is 750 to 850 ℃, such as 750 ℃, 760 ℃, 780 ℃, 800 ℃, 820 ℃, 840 ℃ or 850 ℃, but is not limited to the recited values, and other values not recited in the range of values are equally applicable.
In the invention, the hot blast stove is independently arranged, oil, gas or coal can be used as fuel, the temperature of the gas outlet of the hot blast stove is controlled, the hot blast stove enters the cyclone reactor, and the semi-hydrated gypsum CaSO is added4·0.5H2The O is further converted into anhydrous gypsum.
As a preferable technical scheme of the invention, the cooling in the step (3) comprises three-stage cooling, and the three-stage cooling is sequentially carried out in the first cooling tower, the auger cooler and the second cooling tower.
Preferably, the temperature of the type ii anhydrite before the cooling in step (3) is 450 ℃ or higher, for example 450 ℃, 480 ℃, 500 ℃, 520 ℃, 540 ℃, 550 ℃ or the like, but not limited to the recited values, and other values not recited in the range of the values are also applicable, and the material temperature after the primary cooling is 240 to 300 ℃, for example 240 ℃, 250 ℃, 260 ℃, 270 ℃, 280 ℃, 290 ℃, 300 ℃ or the like, but not limited to the recited values, and other values not recited in the range of the values are also applicable.
Preferably, the medium used for the primary cooling is air, and the heated air enters the hot blast stove and supplies heat for rotational flow reaction and fluidization reaction in sequence after being combusted with fuel.
Preferably, the temperature of the material after the secondary cooling is 130 to 160 ℃, for example 130 ℃, 135 ℃, 140 ℃, 145 ℃, 150 ℃, 155 ℃ or 160 ℃, but not limited to the recited values, and other values not recited in the range of the values are also applicable.
Preferably, the medium used for secondary cooling is water, which forms steam upon heating.
Preferably, the temperature of the material after the tertiary cooling is 40 to 60 ℃, for example, 40 ℃, 45 ℃, 50 ℃, 55 ℃, or 60 ℃, but not limited to the recited values, and other values not recited in the range of the values are also applicable.
Preferably, the medium used for the tertiary cooling is air, and heat is supplied for the drying in the step (1) after the medium is heated by the effluent gas of the fluidized reactor and/or steam after the secondary cooling.
In the invention, gypsum materials pass through a fluidized reactor from an airflow drying tower and then enter a cyclone reactor, the temperature is gradually increased, core equipment for three-stage temperature rise dehydration has different structural forms, the temperature of the completely dehydrated II anhydrous gypsum reaches more than 450 ℃ by the characteristics of being suitable for a logistics dehydration process, and the temperature is reduced to the suitable temperature by three-stage cooling and then is sent to a finished product bin. Wherein, the air passes through a first cooling tower and a hot blast stove to be a temperature rising process, and then passes through a fluidized reactor and an air heater to be a temperature lowering process, which is the multi-stage coupling of the air in the inner layer of the system; the steam generated by the screw cooler heats the hot air further and enters a drying tower, which is the thermal coupling of the water vapor of the system on the outer layer; the heat generated by the hot blast stove is basically used for dehydrating materials through the thermal coupling of the inner layer and the outer layer, and the coupled heat exchange is adopted between the heating and cooling processes before and after the production process so as to fully utilize the heat energy.
Compared with the prior art, the invention has the following beneficial effects:
(1) according to the invention, gypsum materials are subjected to classified calcination by utilizing different characteristics of the device, the reaction is controlled to be carried out, and then the obtained II-type anhydrous gypsum is subjected to multi-stage cooling, so that the purity of the obtained II-type anhydrous gypsum meets the quality requirement, and the resource utilization of industrial byproduct gypsum is realized;
(2) the device adopts a multistage thermal coupling technology, fully utilizes the heat in the product cooling stage in the drying and reaction stages, fully utilizes the heat in the system, realizes energy conservation and consumption reduction and stable operation of the device, and reduces the heat consumption by more than 50%.
Drawings
FIG. 1 is a schematic view of the structural connection of a type II anhydrous gypsum thermal coupling production device provided in example 1 of the present invention;
FIG. 2 is a schematic view showing a partial structure of the interior of a fluidized reactor provided in example 1 of the present invention;
FIG. 3 is a schematic view of the internal cross-sectional structure of a cyclone reactor provided in example 1 of the present invention;
the method comprises the following steps of 1-solid-liquid separation device, 2-drying device, 3-fluidized reactor, 31-inclined tower plate, 32-bubble cap, 33-upper heating coil, 34-lower heating coil, 4-cyclone reactor, 41-cyclone plate, 42-central windshield, 5-first cooling tower, 6-auger cooler, 7-second cooling tower, 8-hot blast stove, 9-first gas heater, 10-second gas heater and 11-third gas heater.
Detailed Description
In order to better illustrate the present invention and facilitate the understanding of the technical solutions of the present invention, the following embodiments are only simple examples of the present invention and do not represent or limit the scope of the present invention, which is defined by the claims.
The invention provides a II-type anhydrous gypsum thermal coupling production device and a method, the device comprises a drying device 2, a fluidized reactor 3, a cyclone reactor 4 and a cooling unit which are sequentially connected, the cooling unit comprises at least one stage of cooling device, and a cold source outlet of the cooling unit is independently connected with gas inlets of the drying device 2, the fluidized reactor 3 and the cyclone reactor 4.
The method comprises the following steps:
(1) drying the gypsum material and then carrying out a fluidization reaction to generate semi-hydrated gypsum;
(2) carrying out rotational flow reaction on the semi-hydrated gypsum obtained in the step (1) to obtain II type anhydrous gypsum;
(3) and (3) cooling the type II anhydrous gypsum obtained in the step (2), and supplying heat for the reaction in the step (1) and the step (2) after the medium serving as a cold source is heated in the cooling process.
The following are typical but non-limiting examples of the invention:
example 1:
the embodiment provides a type II anhydrous gypsum thermal coupling production device, the structural connection schematic diagram of the device is shown in fig. 1, the device comprises a drying device 2, a fluidized reactor 3, a cyclone reactor 4 and a cooling unit which are connected in sequence, the cooling unit comprises at least one stage of cooling device, and a cold source outlet of the cooling unit is independently connected with gas inlets of the drying device 2, the fluidized reactor 3 and the cyclone reactor 4.
The drying device 2 comprises an airflow drying tower, and a breaking component is arranged at a material inlet of the drying device 2.
The schematic diagram of the internal partial structure of the fluidized reactor 3 is shown in fig. 2, inclined trays 31 are alternately arranged on the inner walls of two sides of the fluidized reactor from top to bottom, the inclination directions of two adjacent inclined trays 31 are opposite, and the included angle between each inclined tray 31 and the horizontal direction is 50 degrees;
the inclined tower plate 31 is provided with a bubble cap 32 and a heating coil; the heating coils include an upper heating coil 33 and a lower heating coil 34, which are disposed at the upper and lower sides of the inclined deck 31, respectively.
The schematic diagram of the internal cross-sectional structure of the cyclone reactor 4 is shown in fig. 3, a cyclone plate 41 and a central windshield 42 are arranged in the cyclone reactor 4, and the number of the cyclone plates 41 is 6, and the cyclone plates are in a conical structure; the center damper 42 is of a hemispherical configuration.
The cooling unit comprises a first cooling tower 5, an auger cooler 6 and a second cooling tower 7 which are sequentially connected, a gas outlet of the first cooling tower 5 is connected to a gas inlet of the cyclone reactor 4 through a hot blast stove 8, a gas outlet of the cyclone reactor 4 is connected with a gas inlet of the fluidized reactor 3, and a gas outlet of the second cooling tower 7 is connected with a gas inlet of the drying device 2.
And a gas outlet of the second cooling tower 7 is connected with a gas inlet of the airflow drying tower sequentially through a first gas heater 9, a second gas heater 10 and a third gas heater 11.
The heat source inlet of the second gas heater 10 is connected with the gas outlet of the fluidized reactor 3, and the heat source inlet of the third gas heater 11 is connected with the cold source outlet of the auger cooler 6.
The device also comprises a solid-liquid separation device 1, wherein the solid-liquid separation device 1 is arranged in front of the drying device 2, and the solid-liquid separation device 1 comprises a centrifugal machine.
Example 2:
the embodiment provides a II type anhydrous gypsum thermal coupling apparatus for producing, the apparatus includes drying device 2, fluidized reactor 3, whirl reactor 4 and the cooling unit that connects gradually, the cooling unit includes at least one stage of cooling device, the cold source export of cooling unit links to each other with drying device 2, fluidized reactor 3 and the gas inlet of whirl reactor 4 independently.
The drying device 2 comprises an airflow drying tower, and a breaking component is arranged at a material inlet of the drying device 2.
the inclined tower plate 31 is provided with a bubble cap 32 and a heating coil; the heating coils include an upper heating coil 33 and a lower heating coil 34, which are disposed at the upper and lower sides of the inclined deck 31, respectively.
A cyclone plate 41 and a central wind shield 42 are arranged in the cyclone reactor 4, and the number of the cyclone plates 41 is 3, and the cyclone plates are of a conical structure; the center damper 42 is of a hemispherical configuration.
The cooling unit comprises a first cooling tower 5, an auger cooler 6 and a second cooling tower 7 which are sequentially connected, wherein a gas outlet of the first cooling tower 5 is divided into two branches, one branch is connected to a gas inlet of the cyclone reactor 4 through a hot blast stove 8, the other branch is connected to a lower part gas inlet of the fluidized reactor 3, a gas outlet of the cyclone reactor 4 is connected with a gas inlet of a heating coil in the fluidized reactor 3, and a gas outlet of the second cooling tower 7 is connected with a gas inlet of the drying device 2.
And the gas outlet of the second cooling tower 7 is connected with the gas inlet of the airflow drying tower through a second gas heater 10 and a third gas heater 11 in sequence.
The heat source inlet of the second gas heater 10 is connected with the gas outlet of the fluidized reactor 3, and the heat source inlet of the third gas heater 11 is connected with the cold source outlet of the auger cooler 6.
Example 3:
the embodiment provides a type II anhydrous gypsum thermal coupling production method, which is carried out by adopting the device in the embodiment 1 and comprises the following steps:
(1) firstly, centrifugally separating the industrial byproduct gypsum slurry to obtain a gypsum material with the free water content of 20 wt%, scattering and drying by using an airflow drying tower, wherein the temperature of the dried gypsum material is 65 ℃, the free water content is 0.8 wt%, and carrying out a fluidization reaction in a fluidization reactor 3, the reaction temperature is 150 ℃, and the reaction time is 30min to generate the semi-hydrated gypsum;
(2) carrying out cyclone reaction on the semi-hydrated gypsum obtained in the step (1) in a cyclone reactor 4, wherein the cyclone reaction temperature is 500 ℃ and the time is 60min to obtain II type anhydrous gypsum, the heat required by the cyclone reaction is provided by fuel combustion, and the temperature of gas generated by the combustion is 800 ℃;
(3) and (3) carrying out tertiary cooling on the type II anhydrous gypsum obtained in the step (2), wherein the primary cooling is carried out in a first cooling tower 5, the temperature of the material is reduced to 250 ℃ from 500 ℃, the used medium air is heated and then enters a hot blast stove 8, the swirling flow reaction and the fluidization reaction heat supply are carried out in sequence after the material is combusted with fuel, the secondary cooling is carried out in an auger type cooler 6, the temperature of the cooled material is 150 ℃, the used medium water is heated to form steam, the tertiary cooling is carried out in a second cooling tower 7, the temperature of the cooled material is 50 ℃, the used medium air is heated and then heated by the fluidization reaction exhaust gas and the steam after the secondary cooling, and the drying heat supply in the step (1) is carried out.
In the embodiment, the gypsum material is dried, calcined in stages and cooled in multiple stages, the purity of the obtained II-type anhydrous gypsum meets the quality requirement, the multistage thermal coupling technology is adopted in the process, the heat in the product cooling stage is fully used in the drying and reaction stages, the heat in the system is fully utilized, energy conservation and consumption reduction are realized, and the heat consumption can be reduced by more than 50%.
Example 4:
the embodiment provides a type II anhydrous gypsum thermal coupling production method, which is carried out by adopting the device in the embodiment 1 and comprises the following steps:
(1) firstly, centrifugally separating the industrial byproduct gypsum slurry to obtain a gypsum material with the free water content of 25wt%, scattering and drying by using an airflow drying tower, carrying out fluidization reaction in a fluidization reactor 3 at the reaction temperature of 135 ℃ for 25min after the dried gypsum material is dried at the temperature of 75 ℃ and the free water content of 1wt%, and generating the semi-hydrated gypsum;
(2) carrying out rotational flow reaction on the semi-hydrated gypsum obtained in the step (1) in a rotational flow reactor 4, wherein the rotational flow reaction temperature is 600 ℃, the time is 40min, and II-type anhydrous gypsum is obtained, the heat required by the rotational flow reaction is provided by fuel combustion, and the temperature of gas generated by the combustion is 850 ℃;
(3) and (3) performing tertiary cooling on the type II anhydrous gypsum obtained in the step (2), performing primary cooling in a first cooling tower 5, cooling the material from 550 ℃ to 280 ℃, heating the used medium air, then feeding the heated medium air into a hot blast stove 8, combusting the heated medium air with fuel, sequentially supplying heat for a rotational flow reaction and a fluidization reaction, performing secondary cooling in an auger type cooler 6, performing tertiary cooling in a second cooling tower 7, heating the cooled medium air, and then heating the heated medium air by the fluidization reaction exhaust gas and the steam after the secondary cooling to perform drying heat supply in the step (1).
In the embodiment, the gypsum material is dried, calcined in stages and cooled in multiple stages, the purity of the obtained II-type anhydrous gypsum meets the quality requirement, the multistage thermal coupling technology is adopted in the process, the heat in the product cooling stage is fully used in the drying and reaction stages, the heat in the system is fully utilized, energy conservation and consumption reduction are realized, and the heat consumption can be reduced by more than 50%.
Example 5:
this example provides a type ii anhydrite thermal coupling production method, which is performed using the apparatus of example 2, and includes the following steps:
(1) scattering and drying an industrial byproduct gypsum material with the free water content of 22 wt% by using an airflow drying tower, wherein the temperature of the dried gypsum material is 60 ℃, the free water content is 0.6 wt%, and carrying out a fluidization reaction in a fluidization reactor 3, wherein the reaction temperature is 160 ℃, and the reaction time is 20min, so as to generate semi-hydrated gypsum;
(2) carrying out cyclone reaction on the semi-hydrated gypsum obtained in the step (1) in a cyclone reactor 4, wherein the cyclone reaction temperature is 550 ℃, the time is 50min, and II-type anhydrous gypsum is obtained, the heat required by the cyclone reaction is provided by fuel combustion, and the temperature of gas generated by the combustion is 750 ℃;
(3) and (3) carrying out three-stage cooling on the type II anhydrous gypsum obtained in the step (2), wherein the first-stage cooling is carried out in a first cooling tower 5, the temperature of the material is reduced to 240 ℃ from 520 ℃, part of heated medium air enters a fluidized reactor 3, the other part of heated medium air enters a hot blast stove 8, the heated medium air and fuel sequentially carry out rotational flow reaction and fluidized reaction heat supply, the second-stage cooling is carried out in an auger type cooler 6, the temperature of the cooled material is 130 ℃, the heated medium water forms steam, the third-stage cooling is carried out in a second cooling tower 7, the temperature of the cooled material is 40 ℃, the heated medium air is heated by fluidized reaction exhaust gas and the steam after the second-stage cooling, and the drying heat supply in the step (1) is carried out.
In the embodiment, the gypsum material is dried, calcined in stages and cooled in multiple stages, the purity of the obtained II-type anhydrous gypsum meets the quality requirement, the multistage thermal coupling technology is adopted in the process, the heat in the product cooling stage is fully used in the drying and reaction stages, the heat in the system is fully utilized, energy conservation and consumption reduction are realized, and the heat consumption can be reduced by more than 50%.
The embodiment is integrated, so that the gypsum material is subjected to classified calcination by utilizing different characteristics of the device, the reaction is controlled to be carried out, and then the type II anhydrous gypsum is obtained by multi-stage cooling, so that the purity of the type II anhydrous gypsum meets the quality requirement, and the resource utilization of industrial byproduct gypsum is realized; the device adopts a multistage thermal coupling technology, the heat in the product cooling stage is fully used in the drying and reaction stage, the heat in the system is fully utilized, and the energy conservation, consumption reduction and stable operation of the device are realized.
The applicant states that the present invention is illustrated by the detailed apparatus and method of the present invention through the above embodiments, but the present invention is not limited to the above detailed apparatus and method, i.e. it is not meant to imply that the present invention must be implemented by the above detailed apparatus and method. It will be apparent to those skilled in the art that any modifications to the present invention, equivalents of the means for substitution and addition of means for carrying out the invention, selection of specific means, etc., are within the scope and disclosure of the invention.
Claims (34)
1. The II-type anhydrous gypsum thermal coupling production device is characterized by comprising a drying device, a fluidized reactor, a cyclone reactor and a cooling unit which are sequentially connected, wherein the cooling unit comprises at least one stage of cooling device, and a cold source outlet of the cooling unit is independently connected with gas inlets of the drying device, the fluidized reactor and the cyclone reactor;
the inner wall of the fluidized reactor is provided with inclined tower plates, one end of each inclined tower plate is connected with the inner wall, and the inclination directions of two adjacent inclined tower plates are opposite;
be equipped with the whirl board in the whirl reactor, the whirl board is the toper structure.
2. The production device of claim 1, wherein the drying device comprises a pneumatic drying tower.
3. The production device as claimed in claim 1, wherein the drying device is provided with a breaking-up assembly at the material inlet.
4. The production device as claimed in claim 1, wherein the inclined tower plate has an angle of 30-60 degrees with the horizontal direction.
5. The production device of claim 1, wherein the sloped tray is provided with bubble caps and heating coils.
6. The production device according to claim 5, wherein the heating coils comprise an upper heating coil and a lower heating coil, respectively arranged on the upper and lower sides of the inclined tray.
7. The production device according to claim 1, wherein the number of the swirl plates is 2 to 8.
8. The production device of claim 1, wherein the cooling unit comprises a first cooling tower, an auger cooler and a second cooling tower which are connected in sequence, a cold source outlet of the first cooling tower is connected to a gas inlet of a cyclone reactor through a hot blast stove, the gas outlet of the cyclone reactor is connected with the gas inlet of a fluidized reactor, and a cold source outlet of the second cooling tower is connected with the gas inlet of a drying device.
9. The production device as claimed in claim 8, wherein the cold source outlet of the second cooling tower is connected to the gas inlet of the gas flow drying tower through a gas heater.
10. The production plant as claimed in claim 9, characterized in that the hot source inlet of the gas heater is connected to the gas outlet of the fluidized reactor and/or to the cold source outlet of the auger cooler.
11. The production apparatus according to claim 1, wherein the apparatus further comprises a solid-liquid separation device disposed before the drying device.
12. The production apparatus as claimed in claim 11, wherein the solid-liquid separation apparatus comprises a centrifuge.
13. A method of thermally coupling the production of type ii anhydrite using the apparatus of any one of claims 1 to 12, wherein the method comprises the steps of:
(1) drying the gypsum material and then carrying out a fluidization reaction to generate semi-hydrated gypsum;
(2) carrying out rotational flow reaction on the semi-hydrated gypsum obtained in the step (1) to obtain II type anhydrous gypsum;
(3) and (3) cooling the type II anhydrous gypsum obtained in the step (2), and heating the medium serving as a cold source in the cooling process to supply heat for the reaction in the step (1) and the step (2).
14. The method of claim 13, wherein the source of gypsum material in step (1) is industrial by-product gypsum.
15. The method of claim 13, wherein the gypsum material of step (1) is obtained by solid-liquid separation of a gypsum slurry.
16. The method of claim 13, wherein the free water content of the gypsum material of step (1) is 20 to 25 wt.%.
17. The method of claim 13, wherein the gypsum material of step (1) is broken up prior to drying and then dried by gas flow.
18. The method of claim 13, wherein the temperature of the gypsum material after drying in step (1) is 60-80 ℃.
19. The method of claim 13, wherein the free water content of the gypsum material after said drying of step (1) is no greater than 1 wt.%.
20. The process of claim 13, wherein the fluidized reaction of step (1) is carried out in a fluidized reactor.
21. The method according to claim 13, wherein the temperature of the fluidized reaction in the step (1) is 130 to 160 ℃.
22. The method according to claim 13, wherein the time of the fluidized reaction in the step (1) is 20-30 min.
23. The method of claim 13, wherein the cyclone reaction of step (2) is carried out in a cyclone reactor.
24. The method according to claim 13, wherein the temperature of the swirling reaction in the step (2) is 500-600 ℃.
25. The method according to claim 13, wherein the time of the cyclone reactor in the step (2) is 40-60 min.
26. The method of claim 13, wherein the heat required for the cyclone reaction of step (2) is provided by a hot blast stove.
27. The method according to claim 26, wherein the outlet gas temperature of the hot blast stove is 750-850 ℃.
28. The method of claim 13, wherein said cooling of step (3) comprises three stages of cooling, carried out in sequence in a first cooling tower, an auger cooler, and a second cooling tower.
29. The method as claimed in claim 28, wherein the temperature of the type ii anhydrite is 450 ℃ or higher before the cooling in the step (3), and the temperature of the material after the primary cooling is 240 to 300 ℃.
30. The method of claim 28, wherein the primary cooling medium is air, and the heated air is introduced into the stove to provide heat for the rotational flow reaction and the fluidized reaction in sequence after combustion with the fuel.
31. The method of claim 28, wherein the temperature of the material after the secondary cooling is 130 to 160 ℃.
32. The method of claim 28, wherein the secondary cooling medium is water and forms steam upon heating.
33. The method of claim 28, wherein the temperature of the material after the tertiary cooling is 40-60 ℃.
34. The method of claim 28, wherein the medium used for the tertiary cooling is air, and the heat for the drying in step (1) is supplied after heating by the fluidized reactor exhaust gas and/or the steam after the secondary cooling.
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| CN201911165525.XA CN110803876B (en) | 2019-11-25 | 2019-11-25 | II type anhydrous gypsum thermal coupling production device and method |
| PCT/CN2020/113702 WO2021103736A1 (en) | 2019-11-25 | 2020-09-07 | Device and method for producing type-ii anhydrite by means of thermal coupling |
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| CN110803876B (en) * | 2019-11-25 | 2020-09-18 | 江苏一夫科技股份有限公司 | II type anhydrous gypsum thermal coupling production device and method |
| CN112266190B (en) * | 2020-10-30 | 2022-06-28 | 辽宁东大粉体工程技术有限公司 | Device and method for producing self-excited II type anhydrous gypsum by using industrial byproduct gypsum |
| CN114804682B (en) * | 2021-01-21 | 2024-04-12 | 中山嘉珂环保科技有限公司 | A gypsum energy-saving and environmentally friendly calcining system |
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| CN108569853A (en) * | 2018-07-19 | 2018-09-25 | 西安建筑科技大学 | A kind of industry by-product gypsum dewatering system and technique |
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| Publication number | Publication date |
|---|---|
| WO2021103736A1 (en) | 2021-06-03 |
| CN110803876A (en) | 2020-02-18 |
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