CN206156759U - Handle low aluminium coal series kaolinite's of high -speed railway fluidization sintering device - Google Patents

Abstract

A fluidized calcination device for processing high-iron and low-aluminum coal series kaolin, including a feed bin, a gas burner, a suspension preheater, a suspension calciner, a cyclone separator, an iron removal reducer, an electromagnetic iron remover, and a whiteness monitor feeder, material cooler and Rhodes fan; feeding bin, primary cyclone separator, suspension preheater, suspension calciner, iron removal reducer, electromagnetic iron remover, and material cooler are connected in sequence; primary cyclone separator and The secondary cyclone separator is connected, and the secondary cyclone separator is connected with the Roots blower; the bottom of the suspension preheater is assembled with the gas burner; the bottom of the iron removal reducer is provided with a nitrogen inlet and a reducing gas inlet. The device of the utility model can efficiently process high-iron coal series kaolin, has a sufficient calcining process, high product whiteness, can effectively remove iron impurity minerals in raw materials, and is easy to realize large-scale industrial production.

Description

A fluidized calcination device for processing high-iron and low-aluminum coal series kaolin

technical field

The utility model belongs to the technical field of mineral processing, in particular to a fluidized calcining device for processing high-iron and low-aluminum coal series kaolin.

Background technique

Coal-measure kaolin is a solid waste produced during coal mining and washing. It is mainly composed of kaolinite and carbonaceous. Coal-measure kaolin has become a unique kaolin resource in my country; coal-measure kaolin is mainly composed of kaolinite minerals Mainly, followed by a large amount of impurity components such as combustible carbon, organic matter and iron minerals. Coal series kaolin can obtain calcined kaolin with a certain whiteness after dehydration, decarburization, and iron removal. Calcined kaolin is characterized by its unique Its performance is widely used in papermaking, paint, coating, rubber, cable, ceramics and other industries. At the same time, calcined kaolin, as a raw material for some new resources, is gradually used in various high-end technology industries.

Iron is the main dyeing factor of kaolin. Iron mostly exists in kaolin in the form of hematite, limonite, siderite, pyrite, ilmenite and other minerals. The above iron minerals will become Fe when calcined at high temperature. ₂ O ₃ , causing the calcined kaolin to turn yellow or brick red, and cannot improve its whiteness and other properties; currently, high-iron coal-measure kaolin (TFe>2%) accounts for the majority of coal-measure kaolin in China, and is limited by the current technology that cannot efficiently remove calcined kaolin. The iron minerals in kaolin make it impossible to effectively utilize the high-iron coal series kaolin with abundant reserves in China.

At present, China's coal series kaolin calcination technology mainly adopts fixed bed tunnel kiln or downdraft kiln, moving bed shaft kiln, and rotary kiln for calcination. The above processes have small production scale, large investment, low output, high energy consumption, and product quality is not easy to control . In addition, there is a fluidized bed calcination technology in its infancy, such as the invention title of CN1915814A "The fluidized instant calcination process of coal series kaolin". The material is in contact with high-temperature and high-speed airflow to complete the transient calcination, but the process is transient calcination and does not circulate. The mineral material is a cold material. When it reacts with the high-temperature airflow transiently, the reaction time inside the particles cannot be completely reacted, and it is very easy to occur. Insufficient calcination of "blackening" phenomenon, in addition this process can only deal with high raw material whiteness, low-iron coal series kaolin, can't handle high-iron coal series kaolin materials; publication number is CN1600687 invention name "superfine kaolin rapid circulation Fluidized calcination process and its equipment", the process is a circulating fluidized calcination, repeated calcination, can achieve the purpose of whitening, the calcination process is sufficient; but the process has a long residence time of materials, insufficient heat utilization, and insufficient production of products Stability and small production capacity, and this process cannot handle high-iron coal series kaolin materials.

Therefore, the most urgent problem at present is to improve product quality and realize large-scale industrial production. Therefore, research on new calcination processes and development of large-scale fluidized calcination furnaces for high-efficiency treatment of high-iron coal series kaolin are the key to achieving technological breakthroughs in this process. .

Contents of the invention

Aiming at the above-mentioned problems existing in the existing calcination process of high-iron and low-aluminum coal-based kaolin, the utility model provides a fluidized calcination device for processing high-iron and low-aluminum coal-based kaolin, which is preheated and calcined by suspension, and then removed by reduction and magnetic separation. Iron, at the same time of rapid calcination, the product has high whiteness and effectively removes iron impurity minerals.

A fluidized calcination device for processing high-iron and low-aluminum coal series kaolin of the present utility model includes a feed bin, a gas burner, a suspension preheater, a suspension calciner, a cyclone separator, an iron removal reducer, an electromagnetic iron remover, Whiteness monitor, material cooler and Rhodes blower; the outlet of the feed bin is connected to the inlet of the first-stage cyclone separator, and the outlet of the first-stage cyclone separator is connected to the inlet at the bottom of the suspension preheater The top of the suspension preheater is connected to the top of the suspension calciner through the upper channel, the outlet at the bottom of the suspension calciner is connected to the feed port of the iron removal reducer, and the outlet at the side of the iron removal reducer is connected to the electromagnetic The feed port of the ironware is connected, the electromagnetic iron remover is assembled with the whiteness monitor, the concentrate outlet of the electromagnetic remover is connected with the feed port of the material cooler; the air outlet of the primary cyclone separator is connected with the secondary cyclone separator The air inlet of the secondary cyclone separator is connected with the air inlet of the Roots blower; the air inlet of the primary cyclone separator is connected with the air outlet of the suspension calciner, and the return inlet of the primary cyclone separator is connected with the electromagnetic The return outlet of the iron remover is connected; the bottom of the suspension preheater is assembled with the gas burner, and the inlet of the gas burner is connected with the gas channel; the bottom of the iron removal reducer is provided with a nitrogen inlet and a reducing gas inlet.

In the above device, the suspension preheater has a cylindrical structure; the upper part of the suspension calciner is a cylindrical structure, and the lower part is an inverted conical structure; the volume ratio of the suspension preheater to the suspension calciner is 1: (0.1-0.8).

In the above device, the iron removal reducer is composed of a large cylinder and a small cylinder connected to each other, the diameter-to-height ratio of the large cylinder is 1: (3-7), and the diameter-to-height ratio of the small cylinder is 1: (1-6) , the bottom plate of the large cylinder and the small cylinder are of the same height and the bottom is connected through the communication port; the bottom of the large cylinder is connected to the inverted large cone, and the nitrogen inlet is located at the bottom of the large cone; the bottom of the small cylinder is connected to the inverted small cone In the table body, the reducing gas inlet is located at the bottom of the small cone; the discharge port of the iron removal reducer is located at the upper side wall of the small cylinder; the feed port of the iron removal reducer is located at the top of the large cylinder.

In the above device, the ratio of the height of the communicating port to the height of the small cylinder itself is 1:(3-5).

In the above device, the volume ratio of the large cylinder to the small cylinder is 1:(0.2-0.8).

In the above device, the outlet of the secondary cyclone separator communicates with the ash tank.

In the above device, the volume ratio of the primary cyclone separator to the secondary cyclone separator is 1:(1-5).

The above-mentioned electromagnetic iron remover is a dry magnetic separator.

In the above device, the top of the material cooler communicates with the burner.

In the above device, the material cooler is a shell and tube heat exchanger.

In the above device, a heat exchanger is provided between the discharge port of the iron removal reducer and the feed port of the electromagnetic separator.

The fluidized calcining method of the utility model for processing high-iron and low-aluminum coal-series kaolin adopts the above-mentioned device, and proceeds according to the following steps:

1. Put the raw material of high-iron and low-aluminum coal series kaolin in the feed bin, after the raw material passes through the feed bin and the first-stage cyclone separator, the material after the first-stage separation enters the suspension preheater;

2. Turn on the Roots blower, the flue gas generated from the primary cyclone separator enters the secondary cyclone separator, and the flue gas generated by the secondary cyclone separator enters the Roots blower; at this time, the suspension preheater and the suspension calciner generate Negative pressure;

3. Feed gas into the burner, preheat the material entering the suspension preheater after being burned by the burner, and control the temperature of the material at 800-1300°C and in a suspended state;

4. Due to the effect of negative pressure, the preheated material enters the suspension calciner from the upper channel, and the carbon and organic matter in the preheated material are calcined under the action of heat storage to control the temperature of the material in the suspension calciner At 600～1000℃;

5. The calcined material enters the iron-removing reducer; nitrogen gas is introduced into the iron-removing reducer to make the calcined material part in a suspended state, and the reducing gas is introduced to react with the calcined material at a temperature of 450-800°C ;

6. After the reaction in the iron removal reducer, the material is discharged, cooled to room temperature after heat exchange by the heat exchanger, and then enters the electromagnetic iron remover, and the magnetic iron minerals generated by the reduction reaction are removed by magnetic separation under the condition of a magnetic field strength of 1000-9000Oe. The rest of the iron-removed material is inspected by the whiteness monitor and then enters the material cooler. After heat exchange, it is cooled to normal temperature to obtain calcined kaolin.

In the above method, the secondary cyclone separator separates the fine dust from the gas, and the fine dust enters the ash chute.

In the above method, the flue gas generated in the suspension calciner enters the primary cyclone separator.

In the above method, the nitrogen gas entering from the nitrogen inlet keeps part of the material in the large cylinder of the iron removal reducer in a suspended state, and the rest enters the small cylinder of the iron removal reducer, and the reducing gas entering from the reducing gas inlet makes the materials in the small cylinder The material is in a suspended state and undergoes a reduction reaction, and the reacted material is discharged from the outlet of the small cylinder.

In the above method, the magnetic iron minerals generated by the magnetic separation in step 6 are discharged through the tailings outlet, cooled to normal temperature after exchanging heat in a heat exchanger, and high-iron tailings are obtained.

In the above method, if the remaining iron-removed material in step 6 fails the inspection by the whiteness detector, it will be transported to the primary cyclone separator through the screw feeder.

In the above method, the top of the material cooler is connected to the channel of the gas burner, and after the gas-solid separation of the iron-removed material entering the material cooler, the unburned gas, reducing gas and air in the iron-removed material re-enter the gas burner for reaction , the solid material in the material after iron removal is cooled and discharged.

In the above method, the reaction formula that takes place in the suspension preheater and the suspension calciner is:

C+O ₂ ＝CO ₂

FeO(OH)+O ₂ ＝Fe ₂ O ₃ +H ₂ O (siderite, pyrite, etc.)

Al ₂ O ₃ .2SiO ₂ .2H ₂ O=Al ₂ O ₃ .2SiO ₂ +2H ₂ O.

In the above-mentioned method, the reaction formula of the reduction reaction that takes place in the deironing reducer is:

CO+Fe ₂ O ₃ =Fe ₃ O ₄ +CO ₂ .

In the above method, the amount of reducing gas entering the iron removal reducer is 1: ₁ according to the molar ratio of _CO in the reducing gas and Fe in the calcined material, and the reducing gas is _CO and N . Mixed gas, wherein the volume percentage of CO is 10-60%.

In the above method, the residence time of the first-stage separated material in the suspension preheater is 3-25 minutes, the residence time of the preheated material in the suspension calciner is 2-15 minutes, and the material calcined in the iron-removing reducer The residence time is 2-20min.

The principle of the method of the utility model is: the raw material first enters the suspension preheater through the feeding bin and the feeding system, the gas burner is heated to provide heat for the suspension preheater, and the material is processed in the suspension preheater and the suspension calciner. During the calcination process, the fully calcined material enters the iron-removing reducer, and the iron minerals in the coal-based kaolin are reduced to magnetic iron minerals through the action of reducing gas in the iron-removing reducer. The material enters the electromagnetic iron remover from the reducer. The magnetic field strength magnetically selects the iron mineral impurities. After the calcined kaolin after iron removal is detected by the online whiteness monitor, if the whiteness of the material reaches the set standard, it will enter the material cooler to cool and become a qualified product. If the whiteness of the material is not When the set standard is reached, the material re-enters the suspension preheater through the feeding system to carry out the process of cyclic calcination and iron removal to improve the whiteness and performance of calcined kaolin; the utility model can efficiently process high-iron coal series kaolin and overcome the fluidized calcination process The defects of "over-burning" and "under-burning" can quickly calcine coal-based kaolin, ensure the calcination process is sufficient, the calcined product has high whiteness, and the product is stable, and can effectively remove iron impurity minerals in high-iron coal-based kaolin, and the device It is easy to realize large-scale industrial production.

Description of drawings

Fig. 1 is the structural representation of the fluidized calcining device for processing high-iron and low-aluminum coal series kaolin in the embodiment of the utility model;

In the figure, 1. Feed bin, 2. Primary cyclone separator, 3. Gas burner, 4. Suspension preheater, 5. Suspension calciner, 6. Iron removal reducer, 7. Reduced material heat exchanger , 8. Electromagnetic iron remover (sensor equipped with whiteness monitor), 9. Material cooler, 10. Tailings heat exchanger, 11. Product receiving tank, 12. High-speed iron tailings receiving tank, 13. Secondary cyclone Separator, 14, ash tank, 15, Rhodes fan.

detailed description

Adopt CR14 (KonicaMinolta) whiteness monitor or XT-48BN whiteness tester in the utility model embodiment.

The composition of the high-iron and low-aluminum coal-based kaolin in the embodiment of the utility model contains 30-37% of Al ₂ O ₃ , 40-43% of SiO ₂ , 3-10% of TFe, 0.8-1.3% of TiO ₂ , and K ₂ O 0.8～1.3%, CaO 0.5～0.9%, MgO 0.3～0.7%, Na ₂ O 0.4～0.8%, S 1.3～2.2%, the balance is loss on ignition (LOI); the part with particle size ≤ 15μm accounts for the total weight 80-90% of that.

The composition of the calcined kaolin in the embodiment of the utility model contains 42-44% of Al ₂ O ₃ , 0.3-0.7% of TFe, 0.9-1.4% of TiO ₂ , 0.9-1.4% of K ₂ O , and 0.8-1.0% of CaO by weight percentage. %, MgO 0.4-0.9%, Na ₂ O 0.5-1.0%, S 0.2-0.5%, SiO ₂ balance; whiteness 86-92.

The electromagnetic separator used in the embodiment of the utility model is a dry magnetic separator.

The iron grade TFe of the high-iron tailings in the embodiment of the utility model is 10-40%.

The material cooler in the embodiment of the utility model is a tube-and-tube heat exchanger.

Example 1

The structure of the fluidized calcination device for processing high-iron and low-aluminum coal series kaolin is shown in Figure 1, including feed bin 1, gas burner 3, suspension preheater 4, suspension calciner 5, cyclone separator (first-stage cyclone separation device 2 and secondary cyclone separator 13), iron removal reducer 6, electromagnetic iron remover 8, whiteness monitor, material cooler 9 and Rhodes blower 15; the outlet of feed bin 1 and primary cyclone separator 2 The feed port of the primary cyclone separator 2 is connected to the feed port at the bottom of the suspension preheater 4, and the top of the suspension preheater 4 is connected to the top of the suspension calciner 5 through the upper channel, and the suspension calciner The discharge port at the bottom of the device 5 is connected with the feed port of the iron removal reducer 6, the discharge port at the side of the iron removal reducer 6 is connected with the feed port of the electromagnetic separator 8, and the electromagnetic remover 8 is connected with the whiteness monitor Assembled together, the concentrate outlet of the electromagnetic separator 8 communicates with the feed inlet of the material cooler 9; the air outlet of the primary cyclone separator 2 communicates with the air inlet of the secondary cyclone separator 13, and the secondary cyclone separator 13 The air outlet of the primary cyclone separator 2 is connected with the air inlet of the Roots blower 15; The outlet is connected (with a screw feeder); the bottom of the suspension preheater 4 is assembled with the gas burner 3, and the inlet of the gas burner 3 is connected with the gas channel; the bottom of the iron-removing reducer 6 is provided with a nitrogen inlet and reducing gas inlet;

The suspension preheater 4 is a cylindrical structure; the upper part of the suspension calciner 5 is a cylindrical structure, and the lower part is an inverted conical structure; the volume ratio of the suspension preheater 4 and the suspension calciner 5 is 1:0.4;

The iron removal reducer 6 is composed of a large cylinder and a small cylinder connected to each other. The diameter-to-height ratio of the large cylinder is 1:5, and the diameter-to-height ratio of the small cylinder is 1:4. The bottom plates of the large cylinder and the small cylinder are of equal height. And the bottom is connected through the connecting port; the bottom of the large cylinder is connected to the inverted large frustum, and the nitrogen inlet is located at the bottom of the large cone; the bottom of the small cylinder is connected to the inverted small frustum, and the reducing gas inlet is located at the small cone Bottom; the discharge port of the iron removal reducer 6 is located on the upper side wall of the small cylinder; the feed port of the iron removal reducer 6 is located at the top of the large cylinder;

The height ratio of the connecting port to the height of the small cylinder itself is 1:4; the volume ratio of the large cylinder to the small cylinder is 1:0.6; the discharge port of the secondary cyclone separator 13 is connected to the ash tank 14; the primary cyclone The volume ratio of the separator 2 and the secondary cyclone separator 13 is 1:2; the top of the material cooler 9 communicates with the gas burner 3; There is a reducing material heat exchanger 7 (a heat exchanger group composed of multi-stage heat exchangers);

The outlet of the material cooler 9 is connected to the product receiving tank 11; the tailings outlet of the electromagnetic separator 8 is connected to the high-speed iron tailings receiving tank 12, and a tailings heat exchanger is set between the tailings outlet and the high-speed iron tailings receiving tank 12 10 (heat exchanger group consisting of multi-stage heat exchangers);

The fluidized calcination method for processing high-iron and low-aluminum coal series kaolin is to use the above-mentioned device, and proceed according to the following steps:

1. Put the raw material of high-iron and low-aluminum coal series kaolin in the feed bin, after the raw material passes through the feed bin and the first-stage cyclone separator, the material after the first-stage separation enters the suspension preheater;

2. Turn on the Roots blower, the flue gas generated from the primary cyclone separator enters the secondary cyclone separator, and the flue gas generated by the secondary cyclone separator enters the Roots blower; at this time, the suspension preheater and the suspension calciner generate Negative pressure;

3. Feed gas into the burner, preheat the material entering the suspension preheater after being burned by the burner, and control the temperature of the material at 1100°C and in a suspended state;

4. Due to the effect of negative pressure, the preheated material enters the suspension calciner from the upper channel, and the carbon and organic matter in the preheated material are calcined under the action of heat storage to control the temperature of the material in the suspension calciner at 800°C;

5. The calcined material enters the iron-removing reducer; nitrogen gas is introduced into the iron-removing reducer to make the calcined material part in a suspended state, and the reducing gas is introduced to reduce the calcined material at a temperature of 600 °C;

6. After the reaction in the iron removal reducer, the material is discharged, cooled to room temperature after heat exchange by the heat exchanger, and then enters the electromagnetic iron remover, and the magnetic iron minerals generated by the reduction reaction are removed by magnetic separation under the condition of a magnetic field strength of 3000Oe, and the remaining After iron removal, the material passes the inspection of the whiteness monitor, enters the material cooler, and cools to room temperature after heat exchange to obtain calcined kaolin; the magnetic iron minerals generated by magnetic separation are discharged through the tailings outlet, and after heat exchange by the heat exchanger Cool to normal temperature to obtain high-iron tailings; if the remaining iron-removed material fails the whiteness detector inspection, it will be transported to the first-stage cyclone separator through the screw feeder;

Raw material composition and particle size are as shown in Table 1;

Table 1

Al ₂ O ₃ SiO ₂ TF TiO ₂ K ₂ O CaO MgO Na ₂ O S LOI -38um 36.10 42.10 3.14 0.81 1.02 0.86 0.39 0.46 2.10 margin 90

The composition of calcined kaolin is as shown in table 2;

Table 2

Al ₂ O ₃ SiO ₂ TF TiO ₂ K ₂ O CaO MgO Na ₂ O S BaiDu 42.47 margin 0.48 0.89 0.90 0.91 0.46 0.54 0.20 86

The secondary cyclone separator separates the fine dust from the gas, and the fine dust enters the ash tank;

The flue gas produced in the suspension calciner enters the primary cyclone separator;

The nitrogen gas entering from the nitrogen inlet makes part of the material in the large cylinder of the iron removal reducer in a suspended state, and the rest enters the small cylinder of the iron removal reducer, and the reducing gas entering from the reducing gas inlet makes the material in the small cylinder in a suspended state And a reduction reaction occurs, and the reacted material is discharged from the discharge port of the small cylinder;

The top of the material cooler is connected to the channel of the gas burner. After the material gas and solid are separated after iron removal, the unburned gas, reducing gas and air in the material after iron removal enter the gas burner again for reaction. The solid material in the material is discharged after cooling;

The consumption of the reduction gas that enters the deironing reducer is 1:1 according to the molar ratio of _CO in the reduction gas and Fe in the calcined material O _The described reduction gas is the mixed gas of _CO and N , wherein The volume percentage of CO is 10%;

The residence time of the primary separated material in the suspension preheater is 10 minutes, the residence time of the preheated material in the suspension calciner is 5 minutes, and the residence time of the calcined material in the iron removal reducer is 8 minutes.

Example 2

The structure of the fluidized calcination device for processing high-iron and low-aluminum coal series kaolin is the same as that in Example 1, except that:

(1) The volume ratio of the suspension preheater to the suspension calciner is 1:0.6;

(2) The diameter-to-height ratio of the large cylinder is 1:4, and the diameter-to-height ratio of the small cylinder is 1:2;

(3) The ratio of the height of the connecting port to the height of the small cylinder itself is 1:3; the volume ratio of the large cylinder to the small cylinder is 1:0.4; the volume ratio of the primary cyclone separator to the secondary cyclone separator is 1 :3;

Method is with embodiment 1, and difference is:

(1) Control the temperature of the material at 1000°C and in a suspended state;

(2) Control the material temperature in the suspension calciner at 700°C;

(3) A reduction reaction occurs between the reducing gas and the calcined material at a temperature of 500°C;

(4) Magnetic separation under the condition of magnetic field strength 6000Oe;

Raw material composition and particle size are as shown in table 3;

table 3

Al ₂ O ₃ SiO ₂ TF TiO ₂ K ₂ O CaO MgO Na ₂ O S LOI -15um 36.10 42.10 3.14 0.81 1.02 0.86 0.39 0.46 2.10 margin 80

The composition of calcined kaolin is as shown in table 4;

Table 4

Al ₂ O ₃ SiO ₂ TF TiO ₂ K ₂ O CaO MgO Na ₂ O S BaiDu 43.12 margin 0.38 0.90 1.18 0.86 0.75 0.67 0.32 92

(5) The volume percentage of CO in the reducing gas is 30%;

(6) The residence time of the material in the suspension preheater is 15 minutes, the residence time in the suspension calciner is 10 minutes, and the residence time of the calcined material in the iron removal reducer is 12 minutes.

Example 3

The structure of the fluidized calcination device for processing high-iron and low-aluminum coal series kaolin is the same as that in Example 1, except that:

(1) The volume ratio of the suspension preheater to the suspension calciner is 1:0.1;

(2) The diameter-to-height ratio of the large cylinder is 1:3, and the diameter-to-height ratio of the small cylinder is 1:1;

(3) The ratio of the height of the connecting port to the height of the small cylinder itself is 1:5; the volume ratio of the large cylinder to the small cylinder is 1:0.2; the volume ratio of the primary cyclone separator to the secondary cyclone separator is 1 :5;

Method is with embodiment 1, and difference is:

(1) Control the temperature of the material at 1300°C and in a suspended state;

(2) Control the material temperature in the suspension calciner at 1000°C;

(3) A reduction reaction occurs between the reducing gas and the calcined material at a temperature of 800°C;

(4) Magnetic separation under the condition of magnetic field strength 1000Oe;

Raw material composition and particle size are as shown in table 5;

table 5

Al ₂ O ₃ SiO ₂ TF TiO ₂ K ₂ O CaO MgO Na ₂ O S LOI -25um 32.6 41.3 6.7 0.87 1.32 0.71 0.51 0.62 1.3 margin 80

The composition of calcined kaolin is as shown in table 6;

Table 6

Al ₂ O ₃ SiO ₂ TF TiO ₂ K ₂ O CaO MgO Na ₂ O S BaiDu 42.34 margin 0.41 0.91 1.21 0.92 0.66 0.81 0.46 90

(5) The volume percentage of CO in the reducing gas is 50%;

(6) The residence time of the material in the suspension preheater is 3 minutes, the residence time in the suspension calciner is 2 minutes, and the residence time of the calcined material in the iron removal reducer is 2 minutes.

Example 4

The structure of the fluidized calcination device for processing high-iron and low-aluminum coal series kaolin is the same as that in Example 1, except that:

(1) The volume ratio of the suspension preheater to the suspension calciner is 1:0.8;

(2) The diameter-to-height ratio of the large cylinder is 1:7, and the diameter-to-height ratio of the small cylinder is 1:6;

(3) The ratio of the height of the connecting port to the height of the small cylinder itself is 1:4; the volume ratio of the large cylinder to the small cylinder is 1:0.8; the volume ratio of the primary cyclone separator to the secondary cyclone separator is 1 :1;

Method is with embodiment 1, and difference is:

(1) Control the temperature of the material at 800°C and in a suspended state;

(2) Control the material temperature in the suspension calciner at 600°C;

(3) A reduction reaction occurs between the reducing gas and the calcined material at a temperature of 450°C;

(4) Magnetic separation under the condition of magnetic field strength 9000Oe;

Raw material composition and particle size are as shown in Table 7;

Table 7

Al ₂ O ₃ SiO ₂ TF TiO ₂ K ₂ O CaO MgO Na ₂ O S LOI -25um 33.1 38.6 8.2 1.05 0.82 0.56 0.64 0.79 1.62 margin 90

The composition of calcined kaolin is as shown in Table 8;

Table 8

Al ₂ O ₃ SiO ₂ TF TiO ₂ K ₂ O CaO MgO Na ₂ O S BaiDu 43.55 margin 0.62 1.13 1.08 0.75 0.84 0.97 0.38 87

(5) The volume percentage of CO in the reducing gas is 60%;

(6) The residence time of the material in the suspension preheater is 25 minutes, the residence time in the suspension calciner is 15 minutes, and the residence time of the calcined material in the iron removal reducer is 20 minutes.

Claims (6)

1. A fluidized calcination device for processing high-iron and low-aluminum coal series kaolin, characterized in that it includes a feed bin, a gas burner, a suspension preheater, a suspension calciner, a cyclone separator, an iron removal reducer, an electromagnetic Ironware, whiteness monitor, material cooler and Rhodes blower; the outlet of the feeding bin is connected with the inlet of the first-stage cyclone separator, and the outlet of the first-stage cyclone separator is connected with the inlet of the bottom of the suspension preheater. The feed port is connected, the top of the suspension preheater is connected with the top of the suspension calciner through the upper channel, the discharge port at the bottom of the suspension calciner is connected with the feed port of the iron removal reducer, and the discharge port at the side of the iron removal reducer is connected with the The feed port of the electromagnetic separator is connected, the electromagnetic separator is assembled with the whiteness monitor, the concentrate outlet of the electromagnetic separator is connected with the feed port of the material cooler; the air outlet of the primary cyclone separator is connected with the secondary cyclone The air inlet of the separator is connected, the air outlet of the second-stage cyclone separator is connected with the air inlet of the Roots blower; the air inlet of the first-stage cyclone separator is connected with the air outlet of the suspension calciner, and the return inlet of the first-stage cyclone separator It is connected with the return outlet of the electromagnetic separator; the bottom of the suspension preheater is assembled with the gas burner, and the inlet of the gas burner is connected with the gas channel; the bottom of the iron removal reducer is equipped with a nitrogen inlet and a reduction gas inlet. 2. The fluidized calcination device for processing high-iron and low-aluminum coal series kaolin according to claim 1, characterized in that the suspension preheater is a cylindrical structure; the upper part of the suspension calciner is a cylindrical structure, and the lower part is an inverted The conical structure; the volume ratio of the suspension preheater to the suspension calciner is 1:(0.1～0.8). 3. The fluidized calcination device for processing high-iron and low-aluminum coal series kaolin according to claim 1, wherein the iron removal reducer is composed of a large cylinder and a small cylinder connected to each other, and the diameter and height of the large cylinder are The ratio is 1:(3~7), the diameter-to-height ratio of the small cylinder is 1:(1-6), the bottom plates of the large cylinder and the small cylinder are of the same height and the bottoms are connected through the communication port; the bottom of the large cylinder is connected to the inverted Large frustum, the nitrogen inlet is located at the bottom of the large frustum; the bottom of the small cylinder is connected to the inverted small frustum, and the reducing gas inlet is located at the bottom of the small cone; the outlet of the iron removal reducer is located in the small cylinder The upper side wall of the body; the feed port of the iron removal reducer is located at the top of the large cylinder. 4. The fluidized calcination device for processing high-iron and low-aluminum coal series kaolin according to claim 1, characterized in that the ratio of the height of the communication port to the height of the small cylinder itself is 1: (3-5). 5. The fluidized calcination device for processing high-iron and low-aluminum coal series kaolin according to claim 3, characterized in that the volume ratio of the large cylinder to the small cylinder is 1:(0.2-0.8). 6. The fluidized calcination device for processing high-iron and low-aluminum coal series kaolin according to claim 1, characterized in that the volume ratio of the first-stage cyclone separator and the second-stage cyclone separator is 1:(1～5 ).