阅读说明：本技术 一种ⅱ型无水石膏热耦合生产装置及方法 (II type anhydrous gypsum thermal coupling production device and method ) 是由 黄鹏 唐绍林 万建东 彭卓飞 唐永波 于 2019-11-25 设计创作，主要内容包括：本发明提供了一种Ⅱ型无水石膏热耦合生产装置,所述装置包括依次连接的干燥装置、流化反应器、旋流反应器和冷却单元,所述冷却单元包括至少一级冷却装置,所述冷却单元的冷源出口独立地与干燥装置、流化反应器和旋流反应器的气体入口相连。本发明利用装置的不同特性将石膏物料进行分级煅烧,控制反应进行,再经多级冷却,得到Ⅱ型无水石膏产品,实现了工业副产石膏的资源化利用；所述装置采用多级热耦合技术,将产品冷却阶段的热量充分用于干燥及反应阶段,系统内热量充分利用,实现节能降耗与装置的稳定运行。(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.)

1. The utility model provides a II type anhydrous gypsum thermal coupling apparatus for producing, its characterized in that, the device is including drying device, fluidization reactor, whirl reactor and the cooling unit who connects gradually, the cooling unit includes at least one grade of cooling device, the cold source export of cooling unit links to each other with drying device, fluidization reactor and whirl reactor's gas inlet independently.

2. The production apparatus according to claim 1, wherein the drying apparatus comprises a pneumatic drying tower;

preferably, the material inlet of the drying device is provided with a breaking assembly.

3. The production apparatus according to claim 1 or 2, wherein an inclined tray is provided on an inner wall of the fluidized reactor, and one end of the inclined tray is connected to the inner wall;

preferably, the inclination directions of two adjacent inclined trays are opposite;

preferably, the included angle between the inclined tower plate and the horizontal direction is 30-60 degrees;

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.

4. The production apparatus according to any one of claims 1 to 3, wherein a swirl plate is provided in the swirl reactor;

preferably, the number of the cyclone plates is 2-8;

preferably, the swirl plate is of a conical configuration.

5. The production device according to any one of claims 1 to 4, 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 a gas inlet of a 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;

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.

6. A method of thermally coupling the production of type ii anhydrite using the apparatus of any one of claims 1 to 5, 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).

7. The method of claim 6, wherein the source of the gypsum material of 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 free water content of the gypsum material in the step (1) is 20-25 wt%;

preferably, the gypsum material in the step (1) is broken up before being dried, and then is subjected to airflow drying;

preferably, after the drying in the step (1), the temperature of the gypsum material is 60-80 ℃;

preferably, after said drying of step (1), the gypsum material has a free water content of no more than 1 wt.%.

8. The process of claim 6 or 7, wherein the fluidized reaction of step (1) is carried out in a fluidized reactor;

preferably, the temperature of the fluidization reaction in the step (1) is 130-160 ℃;

preferably, the time of the fluidized reaction in the step (1) is 20-30 min.

9. The process according to any one of claims 6 to 8, wherein the swirling reaction of step (2) is carried out in a swirling reactor;

preferably, the temperature of the rotational flow reaction in the step (2) is 500-600 ℃;

preferably, the time of the cyclone reactor in the step (2) is 40-60 min;

preferably, the heat required by the cyclone reaction in the step (2) is provided by a hot blast stove;

preferably, the temperature of the outlet gas of the hot blast stove is 750-850 ℃.

10. The method according to any one of claims 6 to 9, wherein the cooling of step (3) comprises three stages of cooling, which are carried out in sequence in a first cooling tower, an auger cooler and a second cooling tower;

preferably, before the cooling in the step (3), the temperature of the type II anhydrous gypsum is more than 450 ℃, and the temperature of the material after the first-stage cooling is 240-300 ℃;

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 secondary cooling is 130-160 ℃;

preferably, the medium used for secondary cooling is water, and steam is formed after heating;

preferably, the temperature of the material after the third-stage cooling is 40-60 ℃;

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.

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, which comprises the steps of mixing phosphogypsum and lime, adding the mixture into a drying and calcining machine, arranging a flame jet furnace at the end part, 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 the qualified gypsum to obtain finished gypsum, wherein the drying and calcining machine cannot accurately control the calcining process in the method, needs to be provided with the grading outlet and then carries out mixing and aging to produce β type gypsum powder, and the drying and calcining machine is arranged with the flame jet 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 1 wt%, e.g., 1 wt%, 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: