CN215930577U

CN215930577U - Short-flow suspension calcining cooling device

Info

Publication number: CN215930577U
Application number: CN202122674510.5U
Authority: CN
Inventors: 席玉林; 席佳璐; 陈岚
Original assignee: Beijing Camberg Technology Co ltd
Current assignee: Beijing Camberg Technology Co ltd
Priority date: 2021-11-03
Filing date: 2021-11-03
Publication date: 2022-03-01
Anticipated expiration: 2031-11-03

Abstract

The utility model discloses a short-process suspension calcining cooling device, which comprises raw material processing equipment, a homogenizing warehouse, a fresh air fan, a suspension calcining furnace, multi-stage cooling equipment, heat exchange equipment, dust removal and purification equipment and an induced draft fan, wherein the raw materials are crushed, dried, ground, homogenized and enter the suspension calcining furnace for rapid reaction, gas and solid materials after the reaction are separated and cooled, high-temperature flue gas after the separation is cooled by a heat exchanger and then is partially circulated or purified and discharged, and the solid materials are cooled by the multi-stage cooling equipment and enter a finished product warehouse. Can meet the preparation and production requirements of large-scale materials.

Description

Short-flow suspension calcining cooling device

Technical Field

The present invention relates to the field of suspension calcination and cooling. More particularly, the utility model relates to a short-flow suspension calcination cooling device.

Background

Currently in the field of calcination and preparation of inorganic non-metallic materials, the most common solid calcination reactions are most widely used in the fields of bulk calcination (particle diameter is generally required to be larger than 10mm), particle calcination (particle diameter is smaller than 10mm), and powder calcination (particle diameter is smaller than 0.5 mm). The existing calcining and cooling equipment takes powder suspension calcining as a main development direction, related processes and equipment are developed in various material preparation industries, a suspension preheater and a decomposing furnace are used for producing cement clinker, the scale is the largest, the production is the most stable, the hour single machine production capacity of the current mainstream standardized production equipment reaches over 240 tons, but the suspension flow of the current cement clinker is only realized in the preheating and decomposing part, the clinker synthesis and cooling of main reaction are finished by blocky solids in a rotary kiln and a grate cooler, the long-flow preparation process is still realized, and the energy consumption is difficult to continue to be reduced by the current industrial level.

Along with the development of industrial capacity and the requirements of energy conservation and emission reduction, the capacity of long-flow reaction and the potential of energy conservation and emission reduction are close to the limit of the existing industry, along with the scale expansion of equipment, the input-output ratio is not changed greatly, a new preparation device and a new preparation method need to be found, the powder calcination is fast in heat transfer and large in surface area, the reaction time can be shortened to be within 1 minute in a suspension state, and the method has the basis of short-flow reaction.

The production process of powder suspension is developed in the industries of magnesia, ceramic sand, alpha-alumina, mullite, quick lime, light-burned magnesia, cement clinker, soda lime process calcined alumina, magnetizing roasting, reduced iron powder, metakaolin, calcined kaolin, rare earth smelting, nickel soil smelting, biochar, lignite semicoke, shale oil, IGCC and the like, the full-process suspension is the premise of preparing materials in a short process, but each industry is not really realized in the professional field.

The current technique generally adopts preheating, reaction, the whole process design and the production method of divided long flow of cooling, on the one hand because equipment is many, the production cycle is long, the heat dissipation link is many, must cause the calorific consumption many, on the other hand, the material is in preheating and reaction link separately, the material is the activity highest after preheating and the dehydration crystal water, preheat and react if fully fuse in a time quantum, the material takes place the reaction at the activity highest stage, can effectual reduction energy consumption, and along with the development of equipment and control technology, inorganic material's short flow preparation technique will obtain rapid development. The current main technology utilizes the preheating raw materials to reduce the temperature of the discharged flue gas, the technology does not need to recover a large amount of heat energy from the high-temperature flue gas, which is equivalent to the heat exchange of the raw materials, and the discharged flue gas can be directly discharged after being treated, so that the technology is simpler, but along with the increasing requirements of discharge regulations and environmental protection, the energy consumption of the long-flow technology can not be further reduced.

The matching of the above elements is difficult to be effectively completed in one set of equipment by the current technology, especially the temperature, pressure and atmosphere in the reaction and cooling processes are difficult to be balanced, adjusted and controlled, and a new technology and a new process route are needed to really realize the short-flow calcination and cooling.

SUMMERY OF THE UTILITY MODEL

An object of the present invention is to solve at least the above problems and to provide at least the advantages described later.

Still another object of the present invention is to provide a short-flow suspension calcination cooling device, which can achieve better temperature control and energy recovery of the finished product, is suitable for the calcination reaction of many inorganic non-metallic materials, and can meet the preparation and production requirements of large-scale materials.

To achieve these objects and other advantages in accordance with the purpose of the utility model, there is provided a short-flow suspension calcination cooling apparatus comprising:

the raw material processing equipment is used for crushing, drying and grinding the raw materials, the particle size is controlled to be less than 4.75mm, and the external moisture is controlled to be less than 8%;

the homogenizing chamber is internally provided with a mechanical or pneumatic homogenizing structure and is provided with a raw material inlet and a raw material outlet;

the fresh air machine is provided with an air inlet and an air outlet;

the device comprises a suspension calciner, a reaction zone and a transition zone, wherein a stable zone, the reaction zone and the transition zone are arranged in the suspension calciner from top to bottom, a raw material inlet, a fuel inlet and a fresh air inlet are formed in the side surface of the reaction zone or the transition zone of the suspension calciner, a material outlet is formed in the bottom of the suspension calciner, and a mixing outlet is formed in the top of the suspension calciner;

the multistage cooling equipment is formed by at least three stages of cyclone separators arranged in series from top to bottom, the top of the first-stage or second-stage cyclone separator is provided with a flue gas outlet, the side part of the first-stage or second-stage cyclone separator is provided with a mixing inlet, the top of the middle cyclone separator is provided with a hot air outlet, the side part of the last-stage cyclone separator is provided with a cold air inlet, and the bottom of the last-stage cyclone separator is provided with a material outlet;

the heat exchange equipment adopts a waste heat boiler, the top of the heat exchange equipment is provided with a flue gas inlet, and the bottom of the heat exchange equipment is provided with a flue gas outlet;

the dust removal and purification equipment is provided with a flue gas inlet and a flue gas outlet, and the bottom of the dust removal and purification equipment is provided with a discharge hole;

the induced draft fan is provided with an air inlet and an air outlet;

the raw material outlet of the raw material processing equipment is communicated with the raw material inlet of the homogenizing silo, the raw material inlet of the suspension calciner is communicated with the raw material outlet of the homogenizing silo, the fuel inlet of the suspension calciner is communicated with a fuel source through a pipeline, the mixing outlet of the suspension calciner is communicated with the mixing inlet of the multi-stage cooling equipment, the material outlet of the multi-stage cooling equipment is communicated with the material inlet of a finished product bin, and the material outlet of the suspension calciner is communicated with a waste bin;

the flue gas outlet of the multistage cooling equipment is communicated with the flue gas inlet of the heat exchange equipment, the flue gas outlet of the heat exchange equipment is communicated with the flue gas inlet of the dust removal and purification equipment, the flue gas outlet of the dust removal and purification equipment is communicated with the air inlet of an induced draft fan, the air outlet of the induced draft fan is communicated with a chimney, and the discharge hole of the dust removal and purification equipment is communicated with a byproduct bin;

and a cold air inlet of the multistage cooling equipment is communicated with an air outlet of the fresh air fan, and a hot air outlet of the multistage cooling equipment is communicated with a fresh air inlet of the suspension calciner.

Preferably, the device is of a calciner material circulation type, and further comprises:

the circulating cyclone separator is provided with a mixing inlet, a flue gas outlet and a material outlet;

the side surface of the reaction zone of the suspension calciner is also provided with a feed back port, the side surface of the reaction zone of the suspension calciner is provided with a fuel inlet, and the side surface of the transition zone of the suspension calciner is provided with a fresh air inlet;

the mixed inlet of the multistage cooling equipment is replaced by a flue gas inlet and a material inlet;

the mixing outlet of the suspension calciner is communicated with the mixing inlet of the circulating cyclone separator, the material outlet of the suspension calciner is communicated with the material inlet of the multistage cooling equipment, the material outlet of the circulating cyclone separator is communicated with the feed back port of the suspension calciner, and the smoke outlet of the circulating cyclone separator is communicated with the smoke inlet of the multistage cooling equipment.

Preferably, the device is of a calciner flue gas circulation type, and further comprises:

the mixed flow ejector is provided with an air inlet, an air outlet and a side air inlet;

the flue gas outlet of the multistage cooling equipment is also communicated with the side air inlet of the mixed flow ejector, the hot air outlet of the multistage cooling equipment is communicated with the air inlet of the mixed flow ejector, and the air outlet of the mixed flow ejector is also communicated with the fresh air inlet of the suspension calciner;

the flue gas circulation coefficient ratio is the volume ratio of the total flue gas generation amount, the flue gas amount of the calcination cycle and the flue gas amount of the cooling cycle, and the range of the flue gas circulation coefficient ratio is 1: 0.10-0.75: 0.

Preferably, the apparatus is of a cooling flue gas circulation type, further comprising:

the circulating fan is provided with an air inlet and an air outlet;

the heat exchange equipment adopts a plate type gas heat exchanger or a tube type gas heat exchanger, the top of the heat exchange equipment is provided with a flue gas inlet, the bottom of the heat exchange equipment is provided with a flue gas outlet, and the heat exchange equipment is also provided with a fresh air inlet and a hot air outlet;

the air outlet of the fresh air fan is only communicated with a fresh air inlet of the heat exchange equipment, a hot air outlet of the heat exchange equipment is communicated with a fresh air inlet of the suspension calciner, a flue gas outlet of the heat exchange equipment is also communicated with an air inlet of the circulating fan, and a cold air inlet of the multistage cooling equipment is communicated with an air outlet of the circulating fan;

the flue gas circulation coefficient ratio is the volume ratio of the total flue gas generation amount, the flue gas amount of the calcination cycle and the flue gas amount of the cooling cycle, and the range of the flue gas circulation coefficient ratio is 1:0: 0.30-1.50.

Preferably, the plant is of the calciner double-cycle type, further comprising:

the mixed inlet of the multistage cooling equipment is replaced by a flue gas inlet and a material inlet, and the multistage cooling equipment is also provided with a second cold air inlet;

the circulating fan is provided with an air inlet and an air outlet;

the mixing outlet of the suspension calciner is communicated with the mixing inlet of the circulating cyclone separator, the material outlet of the suspension calciner is communicated with the material inlet of the multistage cooling equipment, the material outlet of the circulating cyclone separator is communicated with the feed back port of the suspension calciner, and the flue gas outlet of the circulating cyclone separator is communicated with the flue gas inlet of the multistage cooling equipment;

the flue gas outlet of the multistage cooling equipment is also communicated with the flue gas inlet of the heat exchange equipment, the flue gas outlet of the heat exchange equipment is also communicated with the air inlet of the circulating fan, the cold air inlet of the multistage cooling equipment is communicated with the air outlet of the circulating fan, and the second cold air inlet of the multistage cooling equipment is communicated with the air outlet of the fresh air fan; the air outlet of the induced draft fan is communicated with the air storage tank;

the flue gas circulation coefficient ratio is the volume ratio of the total generated flue gas amount, the flue gas amount of the calcining cycle and the flue gas amount of the cooling cycle, and the range of the flue gas circulation coefficient ratio is 1:0: 0.10-0.75.

Preferably, the apparatus is of the calciner mixing cycle type, further comprising:

the circulating fan is provided with an air inlet and an air outlet;

the heat exchange equipment adopts plate type gas heat exchange equipment or tube type gas heat exchange equipment, the top of the heat exchange equipment is provided with a flue gas inlet, the bottom of the heat exchange equipment is provided with a flue gas outlet, and the heat exchange equipment is also provided with a fresh air inlet and a hot air outlet;

an air outlet of the fresh air fan is only communicated with a fresh air inlet of the heat exchange equipment, a hot air outlet of the heat exchange equipment is communicated with a fresh air inlet of the suspension calciner, a flue gas outlet of the heat exchange equipment is also communicated with an air inlet of the circulating fan, and a cold air inlet of the multistage cooling equipment is communicated with an air outlet of the circulating fan;

Preferably, the apparatus is of the flue gas double circulation type, further comprising:

the circulating fan is provided with an air inlet and an air outlet;

the heat exchange equipment is characterized in that a waste heat boiler and a plate type gas heat exchanger or a tube type gas heat exchanger are connected in series, the top of the waste heat boiler is provided with a flue gas inlet, the bottom of the plate type gas heat exchanger or the tube type gas heat exchanger is provided with a flue gas outlet, and the plate type gas heat exchanger or the tube type gas heat exchanger is also provided with a fresh air inlet and a hot air outlet;

the flue gas outlet of the multistage cooling equipment is also communicated with a side air inlet of the mixed flow ejector, the hot air outlet of the heat exchange equipment is communicated with an air inlet of the mixed flow ejector, and the air outlet of the mixed flow ejector is also communicated with a fresh air inlet of the suspension calciner;

the air outlet of the fresh air fan is only communicated with the fresh air inlet of the heat exchange equipment, the flue gas outlet of the heat exchange equipment is also communicated with the air inlet of the circulating fan, and the cold air inlet of the multistage cooling equipment is communicated with the air outlet of the circulating fan;

the flue gas circulation coefficient ratio is the volume ratio of the total generated flue gas amount, the flue gas amount of the calcining circulation and the flue gas amount of the cooling circulation, and the range of the flue gas circulation coefficient ratio is 1: 0.1-0.75: 0.30-1.50.

Preferably, the apparatus is of the three-cycle type, further comprising:

the circulating fan is provided with an air inlet and an air outlet;

the mixing outlet of the suspension calciner is communicated with the mixing inlet of the circulating cyclone separator, the material outlet of the suspension calciner is communicated with the material inlet of the multistage cooling equipment, the material outlet of the circulating cyclone separator is communicated with the material return port of the suspension calciner, the flue gas outlet of the circulating cyclone separator is communicated with the flue gas inlet of the multistage cooling equipment and the side air port of the mixed flow ejector, the hot air outlet of the heat exchange equipment is communicated with the air inlet of the mixed flow ejector, and the fresh air inlet of the suspension calciner is communicated with the air outlet of the mixed flow ejector;

Preferably, the device is of a spray recovery type, and does not include the dust removal purification equipment and the induced draft fan, and further includes:

the high-temperature dust removal equipment is provided with an air inlet, an air outlet and a material outlet;

the circulating water spraying equipment is provided with an air inlet, an air outlet, a water inlet, a water outlet and a tar outlet;

the first-stage or second-stage cyclone separator of the multistage cooling equipment is also provided with a material inlet and a second flue gas outlet;

the circulating fan is provided with an air inlet and an air outlet;

the gas fan is provided with an air inlet and an air outlet;

the second induced draft fan is provided with an air inlet and an air outlet;

the side surface of the transition zone of the suspension calciner is provided with a coal gas inlet, the side surface of the reaction zone of the suspension calciner is provided with a fuel inlet, and the side surface of the transition zone of the suspension calciner is provided with a fresh air inlet;

the second flue gas outlet of the multistage cooling equipment is communicated with the flue gas inlet of the heat exchange equipment, the flue gas outlet of the multistage cooling equipment is communicated with the air inlet of the high-temperature dust removal equipment, the air outlet of the high-temperature dust removal equipment is communicated with the air inlet of the circulating water spraying equipment, the material outlet of the high-temperature dust removal equipment is communicated with the material inlet of the multistage cooling equipment, the air outlet of the circulating water spraying equipment is communicated with the air inlet of the second induced draft fan, the air inlet of the circulating fan and the air inlet of the coal gas fan, the air outlet of the second induced draft fan is communicated with the gas storage tank, and the air outlet of the coal gas fan is communicated with the coal gas inlet of the suspension calciner;

the water inlet and the water outlet of the circulating water spraying equipment are respectively communicated with the water outlet and the water inlet of the cooling tower, and the tar outlet of the circulating water spraying equipment is communicated with the inlet of the oil outlet equipment;

Preferably, the apparatus is of a secondary reaction type, further comprising:

the circulating fan is provided with an air inlet and an air outlet;

the gas fan is provided with an air inlet and an air outlet;

the second induced draft fan is provided with an air inlet and an air outlet;

the secondary fan is provided with an air inlet and an air outlet;

the mixing inlet of the multistage cooling equipment is replaced by a material inlet, and the side part of the last stage of cyclone separator of the multistage cooling equipment is provided with a secondary air inlet;

the mixing outlet of the suspension calciner is communicated with the mixing inlet of the circulation cyclone separator, the material outlet of the suspension calciner is communicated with the material inlet of the multistage cooling equipment, the material outlet of the circulation cyclone separator is communicated with the material return port of the suspension calciner, the flue gas outlet of the circulation cyclone separator is communicated with the air inlet of the high-temperature dust removal equipment and the side air port of the mixed flow ejector, and the discharge port of the high-temperature dust removal equipment is also communicated with the material inlet of the multistage cooling equipment;

the air outlet of the high-temperature dust removal equipment is communicated with the air inlet of the circulating water spraying equipment, the air outlet of the circulating water spraying equipment is communicated with the air inlet of the second induced draft fan and the air inlet of the gas fan, the air outlet of the second induced draft fan is communicated with the gas storage tank, and the air outlet of the gas fan is communicated with the air inlet of the mixed flow ejector;

the hot air outlet of the heat exchange equipment is communicated with the side air inlet of the mixed flow ejector, and the fresh air inlet of the suspension calciner is communicated with the air outlet of the mixed flow ejector;

the air outlet of the fresh air fan is only communicated with the fresh air inlet of the heat exchange equipment, the flue gas outlet of the heat exchange equipment is also communicated with the air inlet of the circulating fan, the cold air inlet of the multistage cooling equipment is communicated with the air outlet of the circulating fan, and the secondary air inlet of the multistage cooling equipment is communicated with the air outlet of the secondary fan;

The utility model at least comprises the following beneficial effects:

according to the short-flow suspension calcination cooling device provided by the utility model, preheating, decomposition and synthesis reaction of raw materials are carried out in a calcination furnace, the suspension rapid calcination and reaction of the raw material powder are realized by accurately controlling oxygen, material concentration, temperature and pressure in the calcination furnace, a multi-stage preheating link is omitted, the main reaction flow is compressed to the maximum extent, the flow is greatly shortened, the raw materials are decomposed while related synthesis reaction is carried out, related process flows are highly overlapped, and finally, the energy is recovered as much as possible by multi-stage cooling in a cooling stage, so that the energy consumption is reduced.

According to the short-flow suspension calcination cooling device provided by the utility model, raw materials are prepared into small particles and powder, biological materials and light raw materials are granular, the granularity is less than 4.75mm, other raw materials are generally less than 1mm, the granularity range of 100-400 meshes can be adopted according to reaction requirements, the reaction speed is fully increased to within 1 minute or even within several seconds, and the same cooling efficiency can be greatly improved.

The utility model provides a short-flow suspension calcining cooling device, which introduces new devices and new technologies such as material circulation, flue gas calcining circulation, flue gas cooling circulation and the like in the links of process and equipment, introduces the concept of flue gas circulation coefficient for facilitating design and process calculation, adopts the flue gas reflux to participate in calcining and cooling in the calcining and cooling device (for being different from the current calcining system without flue gas circulation, the utility model adopts the flue gas reflux to participate in calcining and cooling in the calcining and cooling device, calculates the flue gas circulation amount for facilitating design and calculation aiming at specific materials, takes the standard condition flue gas volume generated by the reaction of a calcining furnace as the calculation reference, and the ratio of the standard condition flue gas volume returned to the calcining furnace and the standard condition flue gas volume returned to multi-stage cooling equipment as the flue gas circulation coefficient) as the volume ratio of the flue gas generation total amount, the flue gas amount of calcining circulation and the flue gas amount of cooling circulation (calculated according to the standard condition, in the calculation, the coefficient without circulation is calculated according to 0, and is converted into a specific working condition in a design link for comparison, and the method can be applied to reaction and preparation systems of various inorganic materials by adjusting and controlling the flue gas circulation coefficient.

The utility model provides a short-flow suspension calcining cooling device, which can effectively balance the relation between material suspension, energy transfer and gas speed by combining and designing different devices, can fully meet the requirements of material suspension and energy transfer in the heat exchange process by adjusting the circulation of flue gas and materials, and further solves the contradictions of material suspension, energy transfer and gas speed in a plurality of inorganic material industries, thereby being capable of designing stably-operating suspension calcining and cooling devices suitable for the requirements of the plurality of inorganic material industries.

The utility model provides a short-flow suspension calcination cooling device, wherein the control range of the air supply pressure of a fresh air fan is 0.75-9.5 atm, the oxygen content of fresh air is more than 20%, the device has the functions of pressure adjustment and pulse air supply, high-density fresh air can provide more oxygen, more energy can be provided in a limited space, the distance between particles of materials is greatly shortened, the probability and the speed of reaction are rapidly increased, the process design can reduce the weight of equipment, increase the reaction speed and the productivity, and simultaneously improve the active adaptability of the reaction materials when the particle size, the temperature and the working condition are changed by periodic pressure pulse change, thereby keeping the stable operation of the whole process.

The utility model provides a short-flow suspension calcining cooling device, which adopts supercharging and oxygenation equipment in a fresh air device, so that the adjustment and control of temperature, pressure and atmosphere can be better carried out in the reaction process, the reaction can be completed when the activity of the material is highest, the energy recovery efficiency is higher, one, two or three of the material and flue gas circulation technologies can be independently or combinatively applied, the calcining and cooling processes of different inorganic nonmetallic materials can be met, and meanwhile, the adopted fresh air machine pressure adjustment and pulse air supply technology can adjust the fresh air quantity and control the periodic change of the air pressure, so that the flow of the produced material and the gas can be periodically changed, the material blocking condition can be effectively improved, the heat exchange efficiency can be improved, and the working condition and the adaptability of the whole short-flow suspension calcining cooling device can be improved.

Additional advantages, objects, and features of the utility model will be set forth in part in the description which follows and in part will become apparent to those having ordinary skill in the art upon examination of the following or may be learned from practice of the utility model.

Drawings

FIG. 1 is a schematic structural diagram of one embodiment of the present invention;

FIG. 2 is a schematic structural diagram of a material circulation type of a calcining furnace according to another technical scheme of the utility model;

FIG. 3 is a schematic structural diagram of a smoke circulating type of a calcining furnace according to another technical scheme of the utility model;

FIG. 4 is a schematic view of a cooling flue gas circulation type according to another embodiment of the present invention;

FIG. 5 is a schematic structural view of a double circulation type calciner according to another embodiment of the utility model;

FIG. 6 is a schematic structural view of a mixing circulation type calciner according to another technical scheme of the utility model;

FIG. 7 is a schematic structural view of a flue gas double circulation type according to another embodiment of the present invention;

FIG. 8 is a schematic view showing a three-cycle type structure according to another embodiment of the present invention;

FIG. 9 is a schematic structural view of a spray recycling type according to another embodiment of the present invention;

FIG. 10 is a schematic structural view of a secondary reaction type according to another embodiment of the present invention.

Detailed Description

The present invention is further described in detail below with reference to the attached drawings so that those skilled in the art can implement the utility model by referring to the description text.

It will be understood that terms such as "having," "including," and "comprising," as used herein, do not preclude the presence or addition of one or more other elements or groups thereof.

It is to be noted that the experimental methods described in the following embodiments are all conventional methods unless otherwise specified, and the reagents and materials, if not otherwise specified, are commercially available; in the description of the present invention, it should be noted that the terms "mounted," "connected," and "disposed" are to be construed broadly and may include, for example, a fixed connection, a removable connection, or an integral connection or arrangement unless expressly stated or limited otherwise. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art. The terms "lateral," "longitudinal," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in the orientation or positional relationship indicated in the drawings for convenience in describing the utility model and to simplify the description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus should not be construed as limiting the utility model.

As shown in fig. 1, the present invention provides a short-flow suspension calcination cooling device, comprising:

raw material treatment equipment (not shown in the figure) is used for crushing, drying and grinding raw materials, controlling the particle size to be smaller than 4.75mm and the external moisture to be smaller than 8%, controlling the particle size of the raw materials to be larger than 4.75mm when aiming at organic materials such as straws and the like and smaller than 1mm when aiming at inorganic non-metallic materials such as minerals or wastes and the like, and adopting thinner 100-400 meshes for some raw materials in order to increase the reaction speed, wherein the raw material treatment equipment is provided with a raw material inlet and a raw material outlet;

the homogenizing chamber 2 is internally provided with a mechanical or pneumatic homogenizing structure, and the homogenizing chamber 2 is provided with a raw material inlet and a raw material outlet;

the new blower 1 is provided with an air inlet and an air outlet, adopts a high-pressure blower, is mainly used for supplying oxygen for the suspension calcination reactor, comprises air, oxygen-enriched air and pure oxygen, the air supply pressure can be operated within 1MPa, the pressure and the oxygen content of the new air are controlled by adopting supercharging equipment or supercharging oxygenation equipment, the air supply pressure control range of the new blower 1 is 0.65-9.8 atm, the oxygen content of the new air is more than 20 percent, and the new blower has the functions of pressure adjustment and pulsation air supply. The pressure adjustment and the pulse air supply of the fresh air fan 1 enable the pressure inside the suspension calcining and cooling device to be changed periodically, and can be carried out for a period within the range of 3-1000 seconds, so that the material moving speed in the suspension calcining furnace is changed periodically, and the distance between the materials can be changed obviously and periodically, therefore, the periodic change can obviously prevent the materials from being blocked and accumulated at a uniform speed, the granularity of the materials after reaction can be controlled, and the yield is improved. The method comprises the following steps: when the rotating speed of the new fan 1 is variable, the fresh air volume is adjusted and the periodic change of the air pressure is controlled through the change of the rotating speed of a main shaft of the new fan 1, and when the rotating speed of the new fan 1 is not variable, the fresh air volume is adjusted and the periodic change of the air pressure is controlled through the increase of a pulsating fan and the change of the rotating speed;

the suspension calciner 3 is internally provided with a stable area, a reaction area and a transition area from top to bottom, the suspension calciner 3 can select dilute-phase negative pressure calcination and positive pressure dense phase calcination, the absolute pressure range is 0.65-9.8 atm, the side surface of the reaction area or the transition area of the suspension calciner 3 is provided with a raw material inlet, a fuel inlet and a fresh air inlet, the bottom of the suspension calciner 3 is provided with a material outlet, and the top of the suspension calciner 3 is provided with a mixing outlet;

the multistage cooling equipment 4 is formed by arranging at least three stages of cyclone separators from top to bottom in series, the top of the first-stage or second-stage cyclone separator is provided with a flue gas outlet, the side part of the first-stage or second-stage cyclone separator is provided with a mixing inlet, the top of the middle cyclone separator is provided with a hot air outlet, the side part of the last-stage cyclone separator is provided with a cold air inlet, and the bottom of the last-stage cyclone separator is provided with a material outlet;

the heat exchange equipment adopts a waste heat boiler 51, when the heat is sufficient, the waste heat boiler 51 is adopted for generating electricity, so that the electricity consumption cost is reduced, the top of the heat exchange equipment is provided with a flue gas inlet, and the bottom of the heat exchange equipment is provided with a flue gas outlet;

the dust removal and purification equipment 6 is provided with a flue gas inlet and a flue gas outlet, a bag type dust collector, a wet type electric dust collector or spray water oil removal equipment is adopted, and a discharge hole is formed in the bottom of the dust removal and purification equipment 6;

the induced draft fan 7 is provided with an air inlet and an air outlet, adopts a centrifugal fan, controls the pressure in the suspension calciner 3 and discharges flue gas;

the raw material outlet of the raw material processing equipment is communicated with the raw material inlet of the homogenizing silo 2, the raw material inlet of the suspension calciner 3 is communicated with the raw material outlet of the homogenizing silo 2, the fuel inlet of the suspension calciner 3 is communicated with a fuel source through a pipeline, the mixing outlet of the suspension calciner 3 is communicated with the mixing inlet of the multi-stage cooling equipment 4, the material outlet of the multi-stage cooling equipment 4 is communicated with the material inlet of a finished product bin, and the material outlet of the suspension calciner 3 is communicated with a waste bin;

the flue gas outlet of the multistage cooling equipment 4 is communicated with the flue gas inlet of the heat exchange equipment, the flue gas outlet of the heat exchange equipment is communicated with the flue gas inlet of the dust removal and purification equipment 6, the flue gas outlet of the dust removal and purification equipment 6 is communicated with the air inlet of the draught fan 7, the air outlet of the draught fan 7 is communicated with a chimney, and the discharge hole of the dust removal and purification equipment 6 is communicated with the byproduct bin;

and a cold air inlet of the multistage cooling equipment 4 is communicated with an air outlet of the fresh air fan 1, and a hot air outlet of the multistage cooling equipment 4 is communicated with a fresh air inlet of the suspension calciner 3.

In the technical scheme, the basic type is the most basic oxidation calcining and oxidation cooling process, the arrangement is easy, the connection is simple and convenient, the preheating, the decomposition, the synthesis and the cooling are all performed by adopting a powder suspension process, the three processes of preheating, decomposition and synthesis of raw materials are completed in the suspension calcining furnace 3, wherein oxygen, pressure, temperature and concentration in the suspension calcining furnace 3 are accurately controlled and stably operated, the suspension calcining furnace 3 can be calcined from a negative pressure dilute phase to a positive pressure dense phase, the absolute pressure can be designed and adjusted within the range of 0.65-9.8 atm, the cooling process is independently completed through the multi-stage cooling equipment 4, the better temperature control and energy recovery of finished products can be realized, the method is suitable for the calcining reaction of various inorganic non-metallic materials, and the preparation and production requirements of large-scale inorganic materials can be met.

In the technical scheme, the device comprises raw material processing equipment, a homogenizing warehouse, a fresh air fan, a suspension calciner, multi-stage cooling equipment, heat exchange equipment, dust removal and purification equipment and a draught fan, wherein the raw materials are crushed, dried and ground, then enter the homogenizing warehouse, directly enter the suspension calciner to quickly complete reaction after being homogenized, gas and solid materials after reaction enter the multi-stage cooling equipment to be separated and cooled, separated high-temperature flue gas is cooled by a heat exchanger and then circulated or purified and then discharged, and the solid materials enter a finished product warehouse after being cooled by the multi-stage cooling equipment, the reaction pressure range of the suspension calciner and the multi-stage cooling device is 0.65-9.8 atm, the calcination and cooling can be realized independently, the reaction speed can be effectively improved, the process flow is shortened, more accurate temperature and pressure control can be realized, the energy recovery efficiency is improved, and the device is suitable for the calcination reaction of various inorganic non-metallic materials, can meet the requirements of large-scale preparation and production of materials.

In another technical solution, as shown in fig. 2, the apparatus is of a calciner material circulation type, and a part of the material leaving the suspension calciner 3 is separated from the flue gas and then returned to the suspension calciner 3, and the apparatus further includes:

a circulation cyclone separator 31 having a mixing inlet, a flue gas outlet, a material outlet;

the side surface of the reaction zone of the suspension calciner 3 is also provided with a feed back port, the side surface of the reaction zone of the suspension calciner 3 is provided with a fuel inlet, and the side surface of the transition zone of the suspension calciner 3 is provided with a fresh air inlet;

the mixed inlet of the multistage cooling equipment 4 is replaced by a flue gas inlet and a material inlet;

the raw material outlet of the raw material processing equipment is communicated with the raw material inlet of the homogenizing silo 2, the raw material inlet of the suspension calcining furnace 3 is communicated with the raw material outlet of the homogenizing silo 2, the fuel inlet of the suspension calcining furnace 3 is communicated with a fuel source through a pipeline, the mixing outlet of the suspension calcining furnace 3 is communicated with the mixing inlet of the circulating cyclone separator 31, the flue gas outlet of the circulating cyclone separator 31 is communicated with the flue gas inlet of the multistage cooling equipment 4, the material outlet of the circulating cyclone separator 31 is communicated with the feed back port of the suspension calcining furnace 3, the material outlet of the suspension calcining furnace 3 is communicated with the material inlet of the multistage cooling equipment 4, and the material outlet of the multistage cooling equipment 4 is communicated with the material inlet of a finished product bin;

On the basis of a basic type process, a developed suspension calciner 3 material circulation type is provided, a cyclone separator is arranged at the top of the suspension calciner 3, a part of materials leaving the suspension calciner 3 are separated and then returned to the suspension calciner 3, the increased material circulation is realized, lighter fine particle materials which are not completely reacted are returned to the suspension calciner 3 for continuous reaction, the method is suitable for raw materials with high density and ceramsite sand and magnesia which are increased in volume and weight after reaction, in the design of preparing ceramsite sand from shale and fly ash in a certain place in Shaanxi, a material circulation method is adopted, the particle size of the ceramsite sand can be effectively controlled, the quality of a finished product is easy to control, the air flow velocity is adjusted and controlled, the finished product after reaction is directly cooled after entering a transition zone, the materials after reaction are prevented from being bonded into large blocks and finally fall into a material outlet and then enter a multi-stage cooling device 4 for cooling, is suitable for large-scale production, and has high capacity and good quality.

In another technical solution, as shown in fig. 3, the device is of a suspension calciner 3 flue gas circulation type, and a part of high temperature flue gas returns to the suspension calciner 3 for reaction, and further includes:

the mixed flow ejector 9 is provided with an air inlet, an air outlet and a side air inlet;

the raw material outlet of the raw material processing equipment is communicated with the raw material inlet of the homogenizing silo 2, the raw material inlet of the suspension calcining furnace 3 is communicated with the raw material outlet of the homogenizing silo 2, the fuel inlet of the suspension calcining furnace 3 is communicated with a fuel source through a pipeline, the mixing outlet of the suspension calcining furnace 3 is communicated with the mixing inlet of the multi-stage cooling equipment 4, the material outlet of the multi-stage cooling equipment 4 is communicated with the material inlet of a finished product bin, and the material outlet of the suspension calcining furnace 3 is communicated with a waste bin;

the flue gas outlet of the multistage cooling equipment 4 is communicated with the flue gas inlet of the heat exchange equipment and the side air inlet of the mixed flow ejector 9, the flue gas outlet of the heat exchange equipment is communicated with the flue gas inlet of the dust removal and purification equipment 6, the flue gas outlet of the dust removal and purification equipment 6 is communicated with the air inlet of an induced draft fan 7, the air outlet of the induced draft fan 7 is communicated with a chimney, and the discharge hole of the dust removal and purification equipment 6 is communicated with a byproduct bin;

a cold air inlet of the multistage cooling equipment 4 is communicated with an air outlet of the fresh air fan 1, a hot air outlet of the multistage cooling equipment 4 is communicated with an air inlet of the mixed flow ejector 9, and an air outlet of the mixed flow ejector 9 is communicated with a fresh air inlet of the suspension calciner 3;

in order to be obviously different from the characteristics of the current calcining and cooling system, the flue gas circulation coefficient is used as an important parameter for designing and operating the device, the flue gas circulation coefficient ratio is the volume ratio of the total flue gas generation amount, the flue gas amount of calcining circulation and the flue gas amount of cooling circulation, only the calcining part adopts flue gas circulation, and the controllable flue gas circulation coefficient ratio range is 1: 0.10-0.75: 0.

On the basis of a basic type process, a mixed flow ejector 9 is added, a flue gas inlet is added at the side part of a suspension calcining furnace 3, flue gas entering a multistage cooling device 4 from the suspension calcining furnace 3 is separated, and a part of high-temperature flue gas returns to the suspension calcining furnace 3. In the alumina generation processing production line in the inner Mongolian quasi-Geer area, the technical scheme of the device is adopted for technical transformation, the production capacity is improved by 50 percent, and the product quality is correspondingly improved.

In another technical solution, as shown in fig. 4, the apparatus is of a cooling flue gas circulation type, and a part of the low-temperature flue gas returns to the multi-stage cooling device 4 to cool the material, and further includes:

a circulating fan 10 having an air inlet and an air outlet;

the flue gas outlet of the multistage cooling equipment 4 is communicated with the flue gas inlet of the heat exchange equipment, the flue gas outlet of the heat exchange equipment is communicated with the flue gas inlet of the dust removal and purification equipment 6 and the air inlet of the circulating fan 10, the cold air inlet of the multistage cooling equipment 4 is communicated with the air outlet of the circulating fan 10, the flue gas outlet of the dust removal and purification equipment 6 is communicated with the air inlet of an induced draft fan 7, the air outlet of the induced draft fan 7 is communicated with a chimney, and the discharge hole of the dust removal and purification equipment 6 is communicated with a byproduct bin;

a fresh air inlet of the heat exchange equipment is communicated with an air outlet of the fresh air fan 1, and a hot air outlet of the heat exchange equipment is communicated with a fresh air inlet of the suspension calciner 3;

On the basis of the basic process, a cooling flue gas circulation type is developed, heat exchange equipment of the cooling flue gas circulation type is of a plate type or tube array structure, a circulating fan 10 is additionally arranged behind the heat exchange equipment, and a part of low-temperature flue gas returns to the multistage cooling equipment 4; the device is characterized in that an inlet of a circulating fan 10 is communicated with a flue gas outlet of heat exchange equipment, an outlet of the circulating fan 10 is communicated with a fresh air inlet of the multi-stage cooling equipment 4, a fresh air fan 1 is connected with the fresh air inlet of the heat exchange equipment, a hot air outlet of the heat exchange equipment is connected with a fresh air inlet of a suspension calcining furnace 3, the flue gas inlet of the heat exchange equipment is communicated with the flue gas outlet of the multi-stage cooling equipment 4, the ratio range of the flue gas circulation coefficient of the device is 1:0: 0.30-1.50, the circulation mode and the furnace type are suitable for preparation and production of active quicklime and light-burned magnesium oxide, the energy utilization efficiency is high, and the capacity is large. The device is used for the powder calcination modification design of light-burned magnesium oxide of a certain company in Yingkou Liaoning area, so that the product quality is stable, the yield is improved by 1 time, the energy is saved by 20 percent, the device is also suitable for lime production, and the activity of quicklime is more than 350 percent.

In another technical solution, as shown in fig. 5, the apparatus is a suspension calciner 3 dual-circulation type, after the flue gas exiting from the suspension calciner 3 is separated, a part of the flue gas returns to a transition zone in the suspension calciner 3, and a part of the flue gas also returns to a reaction zone in the calciner, which further includes:

the mixed inlet of the multistage cooling equipment 4 is replaced by a flue gas inlet and a material inlet, and the multistage cooling equipment 4 is also provided with a second cold air inlet;

a circulating fan 10 having an air inlet and an air outlet;

the flue gas outlet of the multistage cooling equipment 4 is communicated with the flue gas inlet of the heat exchange equipment, the flue gas outlet of the heat exchange equipment is communicated with the flue gas inlet of the dust removal and purification equipment 6 and the air inlet of the circulating fan 10, the air outlet of the circulating fan 10 is communicated with the cold air inlet of the multistage cooler, the flue gas outlet of the dust removal and purification equipment 6 is communicated with the air inlet of an induced draft fan 7, the air outlet of the induced draft fan 7 is communicated with an air storage tank, and the discharge port of the dust removal and purification equipment 6 is communicated with a byproduct bin;

a second cold air inlet of the multistage cooling equipment 4 is communicated with an air outlet of the fresh air fan 1, and a hot air outlet of the multistage cooling equipment 4 is communicated with a fresh air inlet of the suspension calciner 3;

the flue gas circulation coefficient ratio is the volume ratio of the total generated flue gas, the flue gas amount of the calcination cycle and the flue gas amount of the cooling cycle, and the range of the flue gas circulation coefficient ratio is 1:0: 0.10-0.75.

On the basis of the basic type process, a suspension calciner 3 double-circulation type is developed, the suspension calciner 3 adopts double circulation, material circulation is adopted in the suspension calciner 3, a part of materials return to a reaction zone in the suspension calciner 3, wherein the transition area of the suspension calciner 3 is connected with two mixed flow ejectors 9, the ratio range of the flue gas circulation coefficient of the device is 1:0: 0.10-0.75, the circulating calcining furnace is suitable for the particle enlargement and density increase in the reaction process, the reaction process is limited by time and granularity, the circulating calcining furnace is suitable for the preparation and production of cement clinker and calcined alumina by a soda lime method, in a design scheme of a certain cement suspension calcination test in Beijing, an air compressor is adopted for air supply, the pressure is controlled to be 0.3-0.4 MPa, cement clinker particles are successfully prepared, a feasible scheme is provided for large-scale cement production, and the energy consumption can be reduced by more than 10%.

In another technical solution, as shown in fig. 6, the device is a suspension calciner 3 mixed circulation type, after the materials and the flue gas discharged from the suspension calciner 3 are separated, a part of the flue gas returns to a transition zone in the suspension calciner 3, a part of the materials also returns to a reaction zone in the suspension calciner, and the low-temperature flue gas discharged from the heat exchange equipment returns to the multistage cooling equipment 4 to participate in cooling circulation, and the device further includes:

a circulating fan 10 having an air inlet and an air outlet;

the heat exchange equipment adopts plate type gas heat exchange equipment or tube type gas heat exchange equipment 52, the top of the heat exchange equipment is provided with a flue gas inlet, the bottom of the heat exchange equipment is provided with a flue gas outlet, and the heat exchange equipment is also provided with a fresh air inlet and a hot air outlet;

On the basis of a basic type process, a calciner mixed circulation type is developed, meanwhile, material circulation of a suspension calciner 3 and cooler flue gas circulation are adopted, after flue gas out of the suspension calciner 3 is separated, part of material also returns to a reaction zone in the suspension calciner 3, low-temperature flue gas out of heat exchange equipment returns to a multistage cooling device 4 to participate in cooling circulation, and the ratio of the flue gas circulation coefficients of the device is 1:0: 0.30-1.50. Because the materials participating in the reaction are heavy, the cooling circulation needs a reducing atmosphere, the calcining furnace type and the process adopt oxidation calcining and reduction cooling, are suitable for large-scale preparation and production of magnetized roasting and reduced iron powder, have high productivity and stable quality, replace a rotary kiln calcining scheme in a limonite magnetized roasting test of Mengmingzhuyi, and adopt the design of a calcining furnace mixed circulation type through test comparison, so that the reaction speed is improved by 5 times, and the yield is improved by 30%.

In another technical solution, as shown in fig. 7, the device is of a flue gas double circulation type, a part of high-temperature flue gas discharged from the suspension calciner 3 directly returns to a transition zone in the suspension calciner 3, and another part of low-temperature flue gas entering the heat exchange equipment returns to the multistage cooling equipment 4 to participate in cooling circulation, and the device further includes:

a circulating fan 10 having an air inlet and an air outlet;

the heat exchange equipment adopts a waste heat boiler 51 and a plate type gas heat exchanger or a tube type gas heat exchanger which are connected in series, the top of the waste heat boiler 51 is provided with a flue gas inlet, the bottom of the plate type gas heat exchanger or the tube type gas heat exchanger is provided with a flue gas outlet, and the plate type gas heat exchanger or the tube type gas heat exchanger is also provided with a fresh air inlet and a hot air outlet;

a flue gas outlet of the multistage cooling equipment 4 is communicated with a flue gas inlet of the heat exchange equipment and a side air port of the mixed flow ejector 9, a hot air outlet of the heat exchange equipment is communicated with an air inlet of the mixed flow ejector 9, an air outlet of the mixed flow ejector 9 is communicated with a fresh air inlet of the suspension calcining furnace 3, the fresh air inlet of the heat exchange equipment is communicated with an air outlet of a fresh air fan 1, a flue gas outlet of the heat exchange equipment is communicated with a flue gas inlet of the dust removal and purification equipment 6 and an air inlet of the circulating fan 10, a cold air inlet of the multistage cooling equipment 4 is communicated with an air outlet of the circulating fan 10, an air outlet of the induced draft fan 7 is communicated with a chimney, and a discharge port of the dust removal and purification equipment 6 is communicated with a byproduct bin;

On the basis of a basic type process, a flue gas double circulation type is developed, flue gas circulation is adopted in a calcining furnace, flue gas circulation is also adopted in a cooler, after the flue gas out of a suspension calcining furnace 3 is separated, a part of the flue gas returns to a transition region in the suspension calcining furnace 3, the low-temperature flue gas out of heat exchange equipment returns to a multistage cooling device 4 to participate in cooling circulation, and the suspension calcining furnace 3 is connected with a mixed flow ejector 9; the ratio range of the flue gas circulation coefficient of the device is 1: 0.1-0.75: 0.30-1.50; the atmosphere of the suspension calcining furnace 3 and the cooler is adjusted to be of a reduction type, the furnace type and the process adopt oxidation calcining and reduction cooling, the method is suitable for large-scale production and preparation of metakaolin and calcined kaolin and production of calcined kaolin, and in Oriental Eldos kaolin company, the design of the scheme is adopted for experimental comparison, the volume yield of the kiln is improved by 3 times, and the control of the reduction product is more uniform, the quality is good, and the energy consumption is low.

In another technical solution, as shown in fig. 8, the apparatus is of a three-cycle type, after the materials and the flue gas exiting from the suspension calciner 3 are separated, a part of high-temperature flue gas returns to a transition zone in the suspension calciner 3, a part of materials also returns to a reaction zone in the suspension calciner 3, and a part of low-temperature flue gas after being cooled by the heat exchange equipment returns to the multistage cooling equipment 4 to participate in the cooling cycle, and the apparatus further includes:

a circulating fan 10 having an air inlet and an air outlet;

the raw material outlet of the raw material processing equipment is communicated with the raw material inlet of the homogenizing silo 2, the raw material inlet of the suspension calcining furnace 3 is communicated with the raw material outlet of the homogenizing silo 2, the fuel inlet of the suspension calciner 3 is communicated with a fuel source through a pipeline, the mixing outlet of the suspension calciner 3 is communicated with the mixing inlet of the circulating cyclone separator 31, the flue gas outlet of the circulating cyclone separator 31 is communicated with the flue gas inlet of the multi-stage cooling equipment 4 and the side air inlet of the mixed flow ejector 9, the air outlet of the mixed flow ejector 9 is communicated with the fresh air inlet of the suspension calciner 3, the material outlet of the circulating cyclone separator 31 is communicated with the feed back port of the suspension calciner 3, the material outlet of the suspension calciner 3 is communicated with the material inlet of the multistage cooling equipment 4, and the material outlet of the multistage cooling equipment 4 is communicated with the material inlet of a finished product bin;

a fresh air inlet of the heat exchange equipment is communicated with an air outlet of the fresh air fan 1, and a hot air outlet of the heat exchange equipment is communicated with an air inlet of the mixed flow ejector 9;

On the basis of a basic process, a three-cycle type is developed, material circulation and flue gas circulation are adopted in a suspension calciner 3 at the same time, flue gas circulation is adopted in a cooler, after flue gas out of the suspension calciner 3 is separated, a part of flue gas returns to a transition region in the suspension calciner 3, a part of flue gas also returns to a reaction region in the suspension calciner 3, low-temperature flue gas out of heat exchange equipment returns to a multistage cooling device 4 to participate in cooling circulation, wherein a fresh air inlet and a flue gas inlet of the suspension calciner 3 are separately arranged and can be combined, the ratio range of the flue gas circulation coefficient of the device is 1: 0.1-0.75: 0.30-1.50, as the ratio of the calcined material, the calcining atmosphere and the cooling atmosphere is easy to adjust and control, the furnace type and the process adopt oxidation calcining and reduction cooling, are suitable for rare earth smelting and nickel earth smelting processes, and are tested by a certain rare earth company in Baotou, the equipment capacity is improved by 50 percent, and the energy consumption is reduced by 30 percent.

In another technical solution, as shown in fig. 9, the apparatus is of a spray recovery type, which does not include the dust removal purification device 6 and the induced draft fan 7, a high temperature dust removal device 54 and a circulating water spray device 53 are added to recover tar and liquid in the flue gas, the high temperature dust removal device 54 is used to purify solid-containing particles in the flue gas, the circulating water spray system is used to recover oil and liquid in the flue gas, a part of the gas after oil removal returns to the suspension calciner 3 to participate in the reaction, and a part of the gas participates in the flue gas circulation cooling of the cooling device, and further includes:

the high-temperature dust removal equipment 54 is provided with an air inlet, an air outlet and a material outlet;

a circulating water spraying device 53 having an air inlet, an air outlet, a water inlet, a water outlet, and a tar outlet;

the first-stage or second-stage cyclone separator of the multistage cooling equipment 4 is also provided with a material inlet and a second flue gas outlet;

a circulating fan 10 having an air inlet and an air outlet;

the gas fan 11 is provided with an air inlet and an air outlet;

a second induced draft fan 12, which is provided with an air inlet and an air outlet;

the side surface of the transition zone of the suspension calciner 3 is provided with a coal gas inlet, the side surface of the reaction zone of the suspension calciner 3 is provided with a fuel inlet, and the side surface of the transition zone of the suspension calciner 3 is provided with a fresh air inlet;

the air inlet of the high-temperature dust removing device 54 is communicated with the flue gas outlet of the multi-stage cooling device 4, the material outlet of the high-temperature dust removing device 54 is communicated with the material inlet of the multi-stage cooling device 4, the second flue gas outlet of the multi-stage cooling device 4 is communicated with the flue gas inlet of the heat exchange device, the flue gas outlet of the heat exchange equipment is communicated with the air inlet of the circulating fan 10, the cold air inlet of the multistage cooling equipment 4 is communicated with the air outlet of the circulating fan 10, the air outlet of the high-temperature dust removing equipment 54 is communicated with the air inlet of the circulating water spraying equipment 53, the air outlet of the circulating water spraying equipment 53 is communicated with the air inlet of the second induced draft fan 12, the air inlet of the circulating fan 10 and the air inlet of the gas fan 11, the air outlet of the second induced draft fan 12 is communicated with an air storage tank, and the air outlet of the coal gas fan 11 is communicated with the coal gas inlet of the suspension calciner 3;

On the basis of basic type process, developing a spray recovery type, adding a high-temperature dust removal device 54 and a circulating water spray device 53, recovering tar and liquid in the flue gas, purifying solid-containing particles in the flue gas by using the high-temperature dust removal device 54 on the basis of flue gas circulation of a cooler, and recovering oil and liquid in the flue gas by using a circulating water spray system, wherein an air inlet of the high-temperature dust removal device 54 is connected with a flue gas outlet of the multistage cooling device 4, an air outlet of the high-temperature dust removal device 54 is connected with an air inlet of the circulating water spray device 53, and an air outlet of the circulating water spray device 53 is connected with an air inlet of the flue gas purification device and an air inlet of the multistage cooling device 4; the furnace type and process adopt oxidation calcination and reduction cooling, and are suitable for the production process of biochar and lignite semi-coke, in the course of internal opal brown coal test, a spray recovery type design scheme is adopted, and the fresh air adopts oxygen-enriched air with oxygen content of 70%, so that the coal gas and semi-coke product capable of replacing coke can be successfully made.

In another technical scheme, as shown in fig. 10, the apparatus is of a secondary reaction type, a secondary fan 8 is added to promote the continuous reaction of the semicoke product, after the material and the flue gas discharged from the suspension calciner 3 are separated, a part of high-temperature flue gas returns to a transition zone in the suspension calciner 3, a part of material also returns to a reaction zone in the suspension calciner 3, a part of low-temperature flue gas after being cooled by the heat exchange equipment returns to the multistage cooling equipment 4 to participate in cooling circulation, solid particles in the flue gas are purified by the high-temperature dust removal equipment 54, and oil and liquid in the flue gas are recovered by the circulating water spray system, and the apparatus further includes:

a circulating fan 10 having an air inlet and an air outlet;

the gas fan 11 is provided with an air inlet and an air outlet;

the secondary fan 8 is provided with an air inlet and an air outlet;

the mixing inlet of the multistage cooling equipment 4 is replaced by a material inlet, and the side part of the last stage of cyclone separator of the multistage cooling equipment 4 is provided with a secondary air inlet;

the raw material outlet of the raw material processing equipment is communicated with the raw material inlet of the homogenizing silo 2, the raw material inlet of the suspension calciner 3 is communicated with the raw material outlet of the homogenizing silo 2, the fuel inlet of the suspension calciner 3 is communicated with a fuel source through a pipeline, the mixing outlet of the suspension calciner 3 is communicated with the mixing inlet of the circulating cyclone separator 31, the flue gas outlet of the circulating cyclone separator 31 is communicated with the air inlet of the high-temperature dust removal equipment 54 and the side air inlet of the mixed flow ejector 9, the air outlet of the mixed flow ejector 9 is communicated with the fresh air inlet of the suspension calciner 3, the material outlet of the circulating cyclone separator 31 is communicated with the feed back port of the suspension calciner 3, the material outlet of the suspension calciner 3 and the material outlet of the high-temperature dust removal equipment 54 are communicated with the material inlet of the multistage cooling equipment 4, a secondary air inlet of the multistage cooling equipment 4 is communicated with an air outlet of a secondary air fan 8, and a material outlet of the multistage cooling equipment 4 is communicated with a material inlet of a finished product bin;

a fresh air inlet of the heat exchange device is communicated with an air outlet of a fresh air fan 1, a hot air outlet of the heat exchange device is communicated with a side air port of the mixed flow ejector 9, a flue gas outlet of the multistage cooling device 4 is communicated with a flue gas inlet of the heat exchange device, a flue gas outlet of the heat exchange device is communicated with an air inlet of the circulating fan 10 and a flue gas inlet of the dust removal purification device 6, a cold air inlet of the multistage cooling device 4 is communicated with an air outlet of the circulating fan 10, a flue gas outlet of the dust removal purification device 6 is communicated with an air inlet of an induced draft fan 7, an air outlet of the induced draft fan 7 is communicated with an air storage tank, and a discharge port of the dust removal purification device 6 is communicated with a byproduct bin;

the air outlet of the high-temperature dust removing equipment 54 is communicated with the air inlet of the circulating water spraying equipment 53, the air outlet of the circulating water spraying equipment 53 is communicated with the air inlet of a second induced draft fan 12 and the air inlet of the coal gas fan 11, the air outlet of the second induced draft fan 12 is communicated with an air storage tank, and the air outlet of the coal gas fan 11 is communicated with the fuel inlet of the suspension calciner 3;

On the basis of a basic process, a secondary reaction type is developed, a high-temperature dust removal device 54 and a circulating water spraying device 53 are added to recover tar and liquid in the flue gas, a secondary fan 8 promotes the continuous oxidation reaction of a semi-coke product, the carbon content of slag discharge is reduced, so that the energy is recovered, the high-temperature dust removal device 54 is used for purifying solid-containing particles in the flue gas, and a circulating water spraying system is used for recovering oil and liquid in the flue gas; wherein the air inlet of the high-temperature dust removing equipment 54 is connected with the flue gas outlet of the multi-stage cooling equipment 4, the air outlet is connected with the air inlet of the circulating water spraying equipment 53, the air outlet of the circulating water spraying equipment 53 is connected with the air inlet of the flue gas purifying equipment and the air inlet of the multi-stage cooling equipment 4, and the secondary fan 8 is connected with the secondary air inlet in the middle of the multi-stage cooling equipment 4. Because the secondary air can continuously carry out secondary oxidation reaction on the semicoke, the heat is extracted to the maximum extent, and the furnace type and the process adopt oxidation calcination and oxidation cooling, the secondary reaction type is suitable for shale oil and IGCC, the productivity is high, and the quality of oil products and coal gas is stable.

Taking Liaoning shun shale oil production as an example, the discharged semicoke of the original equipment is black, the carbon content is more than 4 percent, the semicoke cannot be directly used due to high carbon content, the discharged slag is piled up into a mountain, and the mountain slag is natural and seriously pollutes air due to high carbon content. In the test of the coal-to-gas combined steam power generation system in a certain place in Beijing, the design device of the scheme is adopted, and air with the oxidation content of 85 percent is adopted, so that the problem of coal gas purity is effectively solved, and the improvement of the power generation efficiency becomes possible.

The number of apparatuses and the scale of the process described herein are intended to simplify the description of the present invention. Applications, modifications and variations of the present invention will be apparent to those skilled in the art.

While embodiments of the utility model have been described above, it is not limited to the applications set forth in the description and the embodiments, which are fully applicable in various fields of endeavor to which the utility model pertains, and further modifications may readily be made by those skilled in the art, it being understood that the utility model is not limited to the details shown and described herein without departing from the general concept defined by the appended claims and their equivalents.

Claims

1. Short flow suspension calcines cooling device, its characterized in that includes:

the fresh air machine is provided with an air inlet and an air outlet;

the induced draft fan is provided with an air inlet and an air outlet;

2. The short-circuit suspension calcination cooling apparatus of claim 1, wherein the apparatus is of the calciner material circulation type, further comprising:

3. The short-flow suspension calcination cooling device according to claim 1, wherein the device is of a calciner flue gas circulation type, and further comprises:

4. The short-flow suspension calcination cooling device according to claim 1, wherein the device is of a cooling flue gas circulation type, and further comprises:

the circulating fan is provided with an air inlet and an air outlet;

5. The short-circuit suspension calcination cooling apparatus of claim 1, wherein the apparatus is of the calciner double-cycle type, further comprising:

the circulating fan is provided with an air inlet and an air outlet;

6. The short-circuit suspension calcination cooling apparatus of claim 1, wherein the apparatus is of the calciner hybrid cycle type, further comprising:

the circulating fan is provided with an air inlet and an air outlet;

7. The short-flow suspension calcination cooling device according to claim 1, wherein the device is of a flue gas double circulation type, further comprising:

the circulating fan is provided with an air inlet and an air outlet;

8. The short-circuit suspension calcination cooling device according to claim 1, wherein the device is of a three-cycle type, further comprising:

the circulating fan is provided with an air inlet and an air outlet;

9. The short-flow suspension calcination cooling device according to claim 1, wherein the device is of a spray recovery type, does not include the dust removal purification equipment and the induced draft fan, and further comprises:

the circulating fan is provided with an air inlet and an air outlet;

the gas fan is provided with an air inlet and an air outlet;

the second induced draft fan is provided with an air inlet and an air outlet;

10. The short-flow suspension calcination cooling device according to claim 1, wherein the device is of a secondary reaction type, and further comprises:

the circulating fan is provided with an air inlet and an air outlet;

the gas fan is provided with an air inlet and an air outlet;

the second induced draft fan is provided with an air inlet and an air outlet;

the secondary fan is provided with an air inlet and an air outlet;