WO2019015263A1 - 一种物料的干燥方法 - Google Patents

一种物料的干燥方法 Download PDF

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Publication number
WO2019015263A1
WO2019015263A1 PCT/CN2017/120078 CN2017120078W WO2019015263A1 WO 2019015263 A1 WO2019015263 A1 WO 2019015263A1 CN 2017120078 W CN2017120078 W CN 2017120078W WO 2019015263 A1 WO2019015263 A1 WO 2019015263A1
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Prior art keywords
drying
cavity
coal
hot air
chamber
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PCT/CN2017/120078
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English (en)
French (fr)
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王鹏云
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云南中翼鼎东能源科技开发有限公司
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Priority to AU2017424295A priority Critical patent/AU2017424295B2/en
Publication of WO2019015263A1 publication Critical patent/WO2019015263A1/zh

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B11/00—Machines or apparatus for drying solid materials or objects with movement which is non-progressive
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B21/00—Arrangements or duct systems, e.g. in combination with pallet boxes, for supplying and controlling air or gases for drying solid materials or objects
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
    • F26B25/06—Chambers, containers, or receptacles
    • F26B25/08—Parts thereof

Definitions

  • the invention relates to the field of drying methods for materials, in particular to the drying of high-water, high-viscosity materials.
  • the sludge formed after the treatment of urban domestic sewage generally has a moisture content of about 80%, is rich in nutrients such as organic matter, and contains a certain amount of heavy metals and viruses, pathogens, parasite eggs and other harmful substances. Improper disposal of sludge will result in Serious secondary environmental pollution. At present, there are three main methods for disposal of foreign sludge: 1. Land filling. In the past, many developed countries have adopted landfill methods to treat sludge, and they account for a large proportion (about 40%). Landfill is also the main method in China.
  • the treatment process of this method is very simple, especially suitable for the sludge of poor quality, but the site and a large amount of freight are required, and the foundation needs to be treated with anti-seepage to avoid polluting the groundwater and dissipating the odor.
  • the land suitable for filling is decreasing year by year. 2.
  • the water content is about 80%, and contains a large amount of organic matter.
  • the process of manufacturing organic compound fertilizer by using sludge is to dry the sludge at high temperature, kill the bacteria and eggs, preserve the organic components from damage, remove the harmful bacteria (for harmless treatment), access the beneficial bacteria culture, and eliminate the sludge.
  • the odor increase the nutrient elements in the sludge, add the active ingredients of nitrogen, phosphorus and potassium, increase the nutrient content in the sludge, and make the sludge biologically active and fully nutrient through granulation, low-temperature drying and other processes. , pollution-free organic compound fertilizer.
  • mineral resources are one of the important material foundations for human survival and development, and also the premise and guarantee for social development.
  • 95% of China's energy and 85% of raw materials come from mineral resources, and with the rapid development of China's economy, the demand for mineral resources is increasing.
  • the development of a large number of mineral resources not only brings a wealth of material raw materials, but also produces a large number of tailings. Therefore, tailings utilization is a major problem facing the sustainable development of mining enterprises.
  • China is a large country producing non-ferrous metals.
  • the tailings account for 70% to 95% of the ore.
  • the tailings are stored at more than 2.2 billion tons and grow at 140 million tons per year.
  • the tailings dam has few normal operations and tailings.
  • the average utilization rate is 8.2%. Therefore, from the actual situation of China's non-ferrous metal tailings resources, vigorously developing the comprehensive utilization of tailings resources is of great significance for improving the ecological environment and improving resource utilization. It is the most environmentally friendly use for drying non-ferrous metal tailings for use as building materials.
  • coal slime as a by-product of the raw coal washing process, has been regarded as a waste that is considered to be difficult to use because of its high water content, high viscosity and low calorific value.
  • the root cause of the difficulty in utilizing slime is that it has a high water content, and each time a water point is lowered, the calorific value will increase by 60 calories.
  • the calorific value of 30% moisture is generally 2000-4000 kcal. If it is dehydrated by 15%, the calorific value will increase by more than 900 kcal and reach 3000-5000 kcal.
  • China Coal mixed coal
  • the slime is mixed into the slime and sold together. This increases the ash and moisture of the commercial coal, lowers the quality of the commercial coal, transports the water, increases the transportation cost, and causes the slime.
  • the agglomeration causes problems such as blockage and difficulty in unloading the truck. When the temperature in winter is low, even the situation of the frozen car may seriously affect the transportation efficiency. In fact, this disposal method greatly reduces the effect of raw coal washing.
  • slime drying process In the coal industry, the main aspects of slime drying are: slime drum drying process, tunnel drying process (including flap dryer and mesh belt dryer) and airflow drying process.
  • Drum dryer is one of the earliest drying equipment. It is not only used for drying coal, but also widely used in metallurgy, building materials, chemical industry and other fields.
  • the disadvantage of the drum drying process machine is that the drying temperature of this kind of drying process is above 700 °C, which can not effectively control the oxygen content in the drying process.
  • the temperature is much higher than the ignition point of lignite and long flame coal at 278 °C, and the drying time is still relatively long. It is not suitable for the drying of lignite and long-flame coal slime, and physical reactions will occur, which will affect the performance of coal.
  • the drying equipment used for drying the slime can only increase the calorific value of 400-600 kcal/kg, the dehydration rate is less than 30%, and does not have a dust recovery function.
  • the tunnel drying process is suitable for the drying of block and strip materials.
  • There is a flap type device and a metal mesh belt type device and after the slime is extruded into a strip, it can be dried on a metal mesh belt dryer.
  • the disadvantage of this drying process is that it is not suitable for drying of loose coal slime and has low drying efficiency.
  • the airflow drying process utilizes a heating medium (hot air, flue gas, etc.) to directly contact the wet material particles, and suspends the solid particles in the heating medium fluid, thereby strengthening the mass transfer heat transfer process, belonging to "instant drying”, generally Applied to the drying of bulk materials.
  • a heating medium hot air, flue gas, etc.
  • the disadvantage of this drying process is that the drying equipment can only increase the calorific value of 200-400kcal/kg, the dehydration rate is less than 7%, and has no dust recovery function.
  • the industrial practice effect of drying the slime is not Preferably, the process is generally not used to dry the slime.
  • Non-coked coal is a low-medium metamorphic bituminous coal with high carbon content and high moisture content. It is of low value without drying and upgrading.
  • the existing lignite drying processes mainly include: cooking drying process and airflow reverse drum drying process, which are specifically described as follows:
  • CN102051246A discloses a lignite cooking and drying process, the specific steps are: a. using hot water with a temperature greater than 30 ° C for lignite
  • the granule raw material is subjected to washing and leaching treatment to remove dust and a part of ash and a part of sulphur contained in the lignite granule raw material, and at the same time, obtain the initially upgraded lignite granule; and then, b.
  • CN103013615A discloses a lignite efficient drying and upgrading device and method, the coal burning from the fuel tank and the pulverized coal separated from the cyclone and the electrostatic precipitator are burned in a hot air furnace to generate a high temperature of 700-900 ° C.
  • Flue gas which is used as a drying heat source, is sent to the drum dryer, and flows from bottom to top along the inclined drum dryer for drying the raw lignite, high temperature flue gas and raw materials in the drum dryer Convective heat exchange between lignite, high temperature flue gas drying the raw lignite, into low temperature flue gas carrying pulverized coal in the raw material lignite, the temperature of the low temperature flue gas is 90-120 ° C, the low temperature flue gas from the drum Dryer output.
  • this kind of drying process the oxygen content can not be controlled, easy to hang material, lignite and gas flow are retrograde, lignite residence time in the drying device is too long, easy to pyrolysis, and the drying rate is not high, it is not suitable for industrial promotion.
  • the object of the present invention is to overcome the deficiencies of the prior art and provide a material drying method with high dehydration rate, simple equipment, safe operation, high drying efficiency, good versatility and environmental protection.
  • the drying method of the invention has good versatility and is suitable for drying various materials such as low-rank coal, coal slime, municipal sludge or non-ferrous metal tailings.
  • the invention provides a method for drying a material, and the technical solution thereof is:
  • a method for drying a material comprises the steps of: introducing a hot gas stream having a temperature of 200-1500 degrees Celsius and an oxygen content of less than 12% into the cavity of the drying device from the air inlet, and providing an air blower at the end of the air outlet for drying
  • the cavity of the device generates a negative pressure of 100-6000 Pa, and the flow rate of the hot air flow in the cavity is 2-24 m/s; the bottom of the cavity is provided with a rotating device, and the setting position of the inlet of the drying device is higher than that of the rotating device At the top, the rotating device rotates at a speed of 50-500 rpm.
  • the material and the hot air flow enter the cavity concurrently.
  • the lifting teeth are broken and the material is thrown in the hot air flow.
  • the drying time of the material in the whole cavity is 1 -20s; the material is dried by the hot air stream and discharged from the drying device.
  • the cavity of the drying device is divided into a plurality of chambers divided by the baffle plate, and the material is dissipated in the chamber through the lifting teeth of the lifting teeth, and the depolymerized material is dried in the chamber with the hot air flow. , gradually flow to the next chamber, and finally discharged through the discharge port.
  • the cavity of the drying device is divided into a plurality of chambers which are divided by the staggered baffles and the wind deflectors so that the flow of hot air and the material in the chamber are S-shaped.
  • the width of the last chamber is greater than the width of the other chambers such that the material flow rate is reduced.
  • the material is collected through the discharge end, the flue gas stream to the separator and the precipitator.
  • the temperature at the outlet of the hot gas stream is between 60 and 200 degrees Celsius.
  • the material has a particle size of from 0.01 to 15 mm after drying.
  • the temperature of the hot air flow at the air inlet is 800-1100 degrees Celsius, the oxygen content is less than 8%, the negative pressure of the drying device is 900-6000 Pa, and the flow rate of the hot air flow in the cavity is 8-18 m/s; the rotation speed of the rotating device For 100-400 rpm, the drying time of the material in the entire chamber is 1-5 s.
  • the temperature of the hot air flow at the air inlet is 600-900 degrees Celsius, the oxygen content is less than 11%, the negative pressure of the drying device is 900-6000 Pa, and the flow rate of the hot air flow in the cavity is 8-14 m/s; the rotation speed of the rotating device For 100-400 rpm, the drying time of the material in the entire chamber is 1-5 s.
  • the drying method is used for drying brown coal, long flame coal, non-stick coal, weakly cohesive coal, blast furnace injection coal, gas coal, gas fat coal, lean coal, lean coal, fat coal, anthracite, slime , municipal sludge or non-ferrous metal tailings.
  • the above drying method is used for drying low rank coal
  • the low rank coal is lignite, long flame coal, non-stick coal, weakly cohesive coal, blast furnace injection coal, gas coal, gas fat coal, lean coal, lean coal, Any of fat coal and anthracite.
  • the invention discloses a method for drying low-rank coal, wherein the temperature of the hot air flow at the air inlet is 901-1100 degrees Celsius, the oxygen content is less than 8%, the negative pressure of the drying device is 900-6000 Pa, and the flow rate of the hot air flow in the cavity is 8- 18m/s; the rotation speed of the rotating device is 100-400 rpm, and the drying time of the material in the whole cavity is 1-5 s.
  • the above drying method is used to dry the slime.
  • a method for drying coal slime wherein the temperature of the hot air flow at the air inlet is 800-1100 degrees Celsius, the oxygen content is less than 8%, the negative pressure of the drying device is 900-6000 Pa, and the flow rate of the hot air flow in the cavity is 8-18 m. /s;
  • the rotation speed of the rotating device is 100-400 rpm, and the drying time of the material in the entire cavity is 1-5 s.
  • the above drying method is used to dry municipal sludge.
  • the invention relates to a method for drying urban sludge, wherein the temperature of the hot air flow of the air inlet is 900-1500 degrees Celsius, the oxygen content is less than 10%, the negative pressure of the drying device is 900-6000 Pa, and the flow rate of the hot air flow in the cavity is 8- 18m/s; the rotation speed of the rotating device is 100-400 rpm, and the drying time of the material in the whole cavity is 1-5 s.
  • the above drying method is used to dry non-ferrous metal tailings.
  • a method for drying non-ferrous metal tailings wherein the temperature of the hot air flow at the air inlet is 700-1500 degrees Celsius, the oxygen content is less than 10%, the negative pressure of the drying device is 900-6000 Pa, and the flow rate of the hot air flow in the cavity is 8 -14 m/s; the rotation speed of the rotating device is 100-400 rpm, and the drying time of the material in the entire cavity is 1-5 s.
  • Depolymerization The process by which a material is broken up into small particles.
  • Heat exchange the process of heat transfer between the two, the process of mass change, specifically to the process in which the hot gas flow conducts heat to the material, causes the material to heat up, and is accompanied by evaporation of water, and the material is dried.
  • Implementations of the present invention include the following benefits:
  • the invention defines the dehydration rate of the drying method defined by the invention by more than 60% by limiting the parameters such as the negative pressure value, the temperature, the oxygen content and the like in the cavity of the drying device; the explosion does not occur, the operation of the workshop is safe; and the drying rate is high. It can reach 600-750kg ⁇ H 2 0/m 3 ⁇ h (600-750 kg of water can be extracted per cubic meter of dry space per hour), and the drying method can dry 30-80 cubic meters of material per hour. The moisture content of the dried coal is better controlled, the particle size of the material is uniform, and the quality of the product after drying is effectively ensured.
  • the invention is limited in that the drying time of the material in the entire cavity is short, which can ensure a high dehydration rate without causing pyrolysis (combustion reaction) of the material.
  • the invention sets the drying time, the hot air temperature and the chamber negative pressure parameter so that the material is quickly dried and does not stick to the chamber casing.
  • the drying method of the present invention When the drying method of the present invention is used for drying coal, due to the reasonable setting of the drying temperature, the negative pressure, the flow rate, and the oxygen content parameter, the combustible component of the coal does not volatilize or burn, and the explosion critical value cannot be reached, affecting the coal. Calorific value.
  • FIG. 1 is a flow chart of a method for drying a material according to an embodiment of the present invention.
  • FIG. 2 is a schematic structural view of a drying apparatus according to an embodiment of the present invention.
  • FIG. 3 is a schematic cross-sectional view of the A-A of FIG. 2.
  • FIG. 4 is a schematic structural view of a drying device including a baffle plate according to an embodiment of the present invention.
  • FIG. 5 is a schematic structural view of a drying device including a baffle plate and a windshield according to an embodiment of the present invention.
  • Fig. 6 is another flow chart of the method for drying materials according to an embodiment of the present invention.
  • FIG. 7 is a schematic structural view of a drying device for discharging a hot air flow according to an embodiment of the present invention.
  • a method for drying a slime provided in this embodiment includes the following steps: generating a hot gas flow (flue gas) by using a gas heating device (commonly, such as a hot air furnace), and setting the temperature to 200-1500 degrees Celsius (901 degrees Celsius in this embodiment), a hot air flow with an oxygen content of less than 10% is introduced into the cavity of the drying device from the air inlet 6, and an induced draft fan is provided at the end of the air outlet 8 (not shown)
  • the cavity of the drying device is caused to generate a negative pressure of 100-6000 Pa (4000 Pa in this embodiment), and the flow rate of the hot gas flow in the cavity is 8-14 m/s (10 m/s in this embodiment); the inlet of the drying device
  • the set position of 7 needs to be higher than the top of the lifter tooth 4, and this embodiment is disposed at the top of the housing.
  • the inlet port 7 and the air inlet port 6 may be disposed as shown in FIG. 2, and the air inlet port 6 and the inlet port 7 may be simultaneously disposed in the shell.
  • the bottom of the cavity is provided with a rotating device, the rotating device is provided with a lifting tooth 4, the rotating device is driven by the driving shaft 5 of the driving device 1, the rotating device and the driving device are arranged on the frame 2, and the casing 3 is provided with the casing 3
  • the rotation speed of the rotating device is 50-500 rpm (200 rpm in this embodiment), and the lifting teeth 4 on the rotating device throw the material so that the material is diffused in the hot air flow, and the drying time of the material in the entire cavity It is 1-5s (5s in this embodiment); the material is dried by hot air flow (mass heat exchange) and then discharged with the drying device.
  • the temperature at the hot air outlet 8 is 120-200 degrees Celsius.
  • the hot gas flow direction curve 10 is as shown in FIG. 2.
  • the dehydration rate of the drying method defined by the present invention is greatly improved by limiting the parameters such as the negative pressure value, the temperature, the oxygen content, and the like; , no explosion, safe operation in the workshop; high drying rate.
  • the moisture content of the dried coal is better controlled, the particle size of the material is uniform, and the quality of the product after drying is effectively ensured.
  • the invention is limited in that the drying time of the material in the entire cavity is short, which can ensure high dehydration rate without pyrolysis (combustion reaction) of the material, and the material is quickly dried and does not stick to the chamber casing.
  • the material is collected through the discharge end 9, the flue gas stream to the separator and the precipitator, and the width of the last chamber is greater than the width of the other chambers, so that the material flow rate is reduced, and most of the slime is discharged from the discharge end 9.
  • the rotational speed of the drive shaft can be adjusted by the frequency converter to adjust the speed of the spreading of the coal slurry material in the casing, thereby adjusting the temperature of the hot air flow during the heat exchange process and the internal oxygen content.
  • the wind pressure of the induced draft fan is also matched, which can improve the heat exchange efficiency of the material in the chamber space and reduce the resistance of the material during the depolymerization along the motion curve.
  • the method of the present embodiment is used for drying the coal slurry produced by the coal washing, and the washing process of the coal preparation plant can be improved, and the second leap from the closed circuit of washing water to the recycling and utilization of the slime is realized, and the coal is completely solved.
  • the mud products are stacked in the open air, causing secondary pollution problems in the mining environment, such as water loss and wind flying, reducing the waste floor area, reducing the sewage charges of enterprises, thereby increasing the economic benefits of enterprises; and solving the slime due to seasonal changes. Poor sales, or handling the passive situation that affects production.
  • the water is reduced, the cost of transporting moisture can be reduced, and problems such as racing and freezing are avoided. To the end user, it can also improve boiler thermal efficiency, reduce emissions, and reduce environmental protection investment.
  • the embodiment provides a method for drying coal slime.
  • the difference from the embodiment 1 is that the temperature of the hot air flow at the air inlet is 1000 degrees Celsius, the oxygen content is less than 8%, the negative pressure of the drying device is 4500 Pa, and the hot air flow in the cavity.
  • the flow rate was 10 m/s; the rotation speed of the rotating device was 200 rpm, and the drying time of the material in the entire cavity was 3 s.
  • the cavity of the drying device of the present embodiment is divided into a plurality of chambers divided by the baffle plate 11, and the material is disintegrated in the chamber through the disintegration and spreading of the material. After the hot gas is dried in the chamber (mass heat exchange), it gradually flows to the next chamber and is finally discharged through the discharge port.
  • the baffle 11 is disposed at the bottom of the casing 3.
  • the hot gas flow direction curve 10 is as shown in FIG.
  • the method of this embodiment is equally applicable to drying low rank coal, municipal sludge or non-ferrous metal tailings. The same components as those in Embodiment 1 will not be described in detail in this embodiment.
  • the embodiment provides a method for drying coal slime.
  • the difference from the embodiment 1 is that the temperature of the hot air flow at the air inlet is 1200 degrees Celsius, the oxygen content is less than 8%, the negative pressure of the drying device is 4000 Pa, and the hot air flow in the cavity.
  • the flow rate was 10 m/s; the rotation speed of the rotating device was 200 rpm, and the drying time of the material in the entire cavity was 3 s.
  • the cavity of the drying device is divided into a plurality of chambers which are divided by the staggered baffle 11 and the wind deflector 12, so that the flow of the hot air and the material in the chamber is S-shaped. The heat exchange is sufficient and the thermal efficiency is improved.
  • the hot air flow direction curve 10 is as shown in Fig.
  • the baffle 11 is disposed at the bottom of the casing 3, and the windshield 12 is disposed at the top of the casing.
  • the method of this embodiment is equally applicable to drying low rank coal, municipal sludge or non-ferrous metal tailings. The same components as those in Embodiment 1 will not be described in detail in this embodiment.
  • the lower baffle divides the casing into a plurality of chambers, and the granularity and the dry humidity reach a certain level before entering the latter chamber.
  • the material with large granularity and high humidity has a large self-weight and cannot move along with the hot air.
  • a chamber continues to fall into the current chamber and is lifted by the lifting teeth, and the continuous crushing of the large particles of the slime is realized.
  • the crushing is realized by the impact of the lifting teeth, the lower baffle and the particles, and is divided into a plurality of chambers. After the transition of the chamber, the discharge air damper is finally reached to ensure uniformity of the finished product and the humidity meets the requirements.
  • the upper air and the lower baffle form the S-shaped hot air and the flow, and the exchange efficiency is high and the energy consumption is small.
  • the present embodiment provides a method for drying brown coal, as shown in FIG. 6 and FIG. 7, comprising the steps of: generating a hot gas flow (flue gas) with a gas heating device (commonly such as a hot air furnace), and setting the temperature to 200- 1500 degrees Celsius (900 degrees Celsius in this embodiment), a hot gas flow having an oxygen content of less than 8% is introduced into the cavity of the drying device from the air inlet 6, and an air blower (not shown) is provided at the end of the air outlet 8 so that
  • the cavity of the drying device generates a negative pressure of 100-6000 Pa (4000 Pa in this embodiment), the flow rate of the hot gas flow in the cavity is 8-14 m/s (10 m/s in this embodiment); the inlet of the drying device 7
  • the setting position needs to be higher than the top of the lifting teeth 4, and this embodiment is provided at the top of the housing.
  • the arrangement is such that the material and the hot air flow co-currently enter the cavity.
  • the inlet port 7 and the air inlet port 6 may be disposed as shown in FIG. 7, and the air inlet port 6 and the inlet port 7 may be simultaneously disposed in the shell.
  • the bottom of the cavity is provided with a rotating device, the rotating device is provided with a lifting tooth 4, the rotating device is driven by the driving shaft 5 of the driving device 1, the rotating device and the driving device are arranged on the frame 2, and the casing 3 is provided with the casing 3
  • the rotation speed of the rotating device is 50-500 rpm (200 rpm in this embodiment), and the lifting teeth 4 on the rotating device throw the material so that the material is diffused in the hot air flow, and the drying time of the material in the entire cavity It is 1-5s (3s in this embodiment); the material is dried by hot air flow (mass heat exchange) and then discharged with the drying device.
  • the temperature at the hot air outlet 8 is 120-200 degrees Celsius.
  • the hot gas flow direction curve 10 is as shown in FIG. 7.
  • the dehydration rate of the drying method defined by the present invention is greatly improved by limiting the parameters such as the negative pressure value, the temperature, the oxygen content, and the like; , no explosion, safe operation in the workshop; high drying rate.
  • the moisture content of the dried coal is better controlled, the particle size of the material is uniform, and the quality of the product after drying is effectively ensured.
  • the invention is limited in that the drying time of the material in the entire cavity is short, which can ensure high dehydration rate without pyrolysis (combustion reaction) of the material, and the material is quickly dried and does not stick to the chamber casing.
  • the cavity of the drying device is divided into a plurality of chambers which are divided by the staggered baffles and the wind deflector, so that the flow of the hot gas and the material in the chamber is S-shaped, the mass heat exchange is sufficient, and the thermal efficiency is improve.
  • the baffle plate is disposed at the bottom of the casing 3, and the windshield is disposed at the top of the casing. The materials are all carried away with the hot gas stream and then collected by the flue gas stream to the separator and the dust collector.
  • the width of the last chamber is greater than the width of the other chambers, so that the material flow rate is reduced, and most of the slime is discharged from the discharge end 9.
  • the present embodiment provides a method for drying long flame coal, as shown in FIG. 1 to FIG. 3, comprising the steps of: generating a hot gas flow (flue gas) by using a gas heating device (commonly, such as a hot air furnace), and setting the temperature to 200-1500 degrees Celsius (900 degrees Celsius in this embodiment), a hot gas flow of less than 10% oxygen is introduced into the cavity of the drying device from the air inlet 6, and an air blower is provided at the end of the air outlet 8 (not shown)
  • the cavity of the drying device is caused to generate a negative pressure of 100-6000 Pa (4000 Pa in this embodiment), and the flow rate of the hot gas flow in the cavity is 8-14 m/s (10 m/s in this embodiment); the inlet of the drying device
  • the set position of 7 needs to be higher than the top of the lifter tooth 4, and this embodiment is disposed at the top of the housing.
  • the inlet port 7 and the air inlet port 6 may be disposed as shown in FIG. 2, and the air inlet port 6 and the inlet port 7 may be simultaneously disposed in the shell.
  • the bottom of the cavity is provided with a rotating device, the rotating device is provided with a lifting tooth 4, the rotating device is driven by the driving shaft 5 of the driving device 1, the rotating device and the driving device are arranged on the frame 2, and the casing 3 is provided with the casing 3
  • the rotation speed of the rotating device is 50-500 rpm (200 rpm in this embodiment), and the lifting teeth 4 on the rotating device throw the material so that the material is diffused in the hot air flow, and the drying time of the material in the entire cavity It is 1-5s (3s in this embodiment); the material is dried by hot air flow (mass heat exchange) and then discharged with the drying device.
  • the temperature at the hot air outlet 8 is 120-200 degrees Celsius.
  • the hot gas flow direction curve 10 is as shown in FIG. 2.
  • the dehydration rate of the drying method defined by the present invention is greatly improved by limiting the parameters such as the negative pressure value, the temperature, the oxygen content, and the like; , no explosion, safe operation in the workshop; high drying rate.
  • the moisture content of the dried coal is better controlled, the particle size of the material is uniform, and the quality of the product after drying is effectively ensured.
  • the invention is limited in that the drying time of the material in the entire cavity is short, which can ensure high dehydration rate without pyrolysis (combustion reaction) of the material, and the material is quickly dried and does not stick to the chamber casing.
  • the material is collected at the discharge end 9, the flue gas stream is collected to the separator and the dust collector, and the width of the last chamber is greater than the width of the other chambers, so that the material flow rate is reduced, and most of the slime is discharged from the discharge end 9. .
  • the drying device of this embodiment can also be as shown in FIG. 4, the cavity of the drying device is divided into a plurality of chambers divided by the baffle plate, and the material is dispersed in the chamber through the disintegration of the lifting teeth, and after depolymerization After the material is dried in the chamber with the hot gas flow (mass heat exchange), it gradually flows to the next chamber and is finally discharged through the discharge port.
  • the cavity of the drying device is divided into a plurality of chambers which are divided by the staggered baffles and the wind deflector, so that the flow of the hot air and the material in the chamber is S-shaped. The heat exchange is sufficient and the thermal efficiency is improved.
  • the present embodiment provides a method for drying non-stick coal, as shown in FIG. 1 to FIG. 3, comprising the steps of: generating a hot gas flow (flue gas) by using a gas heating device (commonly such as a hot air furnace), and setting the temperature to 200-1500 degrees Celsius (1000 degrees Celsius in this embodiment), a hot gas flow of less than 10% oxygen is introduced into the cavity of the drying device from the air inlet 6, and an air blower is provided at the end of the air outlet 8 (not shown)
  • the cavity of the drying device is caused to generate a negative pressure of 100-6000 Pa (4000 Pa in this embodiment), and the flow rate of the hot gas flow in the cavity is 8-14 m/s (10 m/s in this embodiment); the inlet of the drying device
  • the set position of 7 needs to be higher than the top of the lifter tooth 4, and this embodiment is disposed at the top of the housing.
  • the inlet port 7 and the air inlet port 6 may be disposed as shown in FIG. 2, and the air inlet port 6 and the inlet port 7 may be simultaneously disposed in the shell.
  • the bottom of the cavity is provided with a rotating device, the rotating device is provided with a lifting tooth 4, the rotating device is driven by the driving shaft 5 of the driving device 1, the rotating device and the driving device are arranged on the frame 2, and the casing 3 is provided with the casing 3
  • the rotation speed of the rotating device is 50-500 rpm (50 rpm in this embodiment), and the lifting teeth 4 on the rotating device throw the material so that the material is diffused in the hot air flow, and the drying time of the material in the entire cavity It is 1-20 s (12 s in this embodiment); the material is dried by hot air flow (mass heat exchange) and then discharged with the drying device.
  • the temperature at the hot air outlet 8 is 120-200 degrees Celsius.
  • the hot gas flow direction curve 10 is as shown in FIG. 2.
  • the dehydration rate of the drying method defined by the present invention is greatly improved by limiting the parameters such as the negative pressure value, the temperature, the oxygen content, and the like; , no explosion, safe operation in the workshop; high drying rate.
  • the moisture content of the dried coal is better controlled, the particle size of the material is uniform, and the quality of the product after drying is effectively ensured.
  • the invention is limited in that the drying time of the material in the entire cavity is short, which can ensure high dehydration rate without pyrolysis (combustion reaction) of the material, and the material is quickly dried and does not stick to the chamber casing.
  • the material is collected at the discharge end 9, the flue gas stream is collected to the separator and the dust collector, and the width of the last chamber is greater than the width of the other chambers, so that the material flow rate is reduced, and most of the slime is discharged from the discharge end 9. .
  • the drying device of this embodiment can also be as shown in FIG. 4, the cavity of the drying device is divided into a plurality of chambers divided by the baffle plate, and the material is dispersed in the chamber through the disintegration of the lifting teeth, and after depolymerization After the material is dried in the chamber with the hot gas flow (mass heat exchange), it gradually flows to the next chamber and is finally discharged through the discharge port.
  • the cavity of the drying device is divided into a plurality of chambers which are divided by the staggered baffles and the wind deflector, so that the flow of the hot air and the material in the chamber is S-shaped. The heat exchange is sufficient and the thermal efficiency is improved.
  • the present embodiment provides a method for drying weakly viscous coal, as shown in FIG. 1 to FIG. 3, comprising the steps of: generating a hot gas flow (flue gas) by using a gas heating device (commonly such as a hot air furnace), and setting the temperature to 200-1500 degrees Celsius (1000 degrees Celsius in this embodiment), a hot gas flow of less than 10% oxygen is introduced into the cavity of the drying device from the air inlet 6, and an air blower is provided at the end of the air outlet 8 (not shown)
  • the cavity of the drying device is caused to generate a negative pressure of 100-6000 Pa (4000 Pa in this embodiment), and the flow rate of the hot gas flow in the cavity is 8-14 m/s (8 m/s in this embodiment); the inlet of the drying device
  • the set position of 7 needs to be higher than the top of the lifter tooth 4, and this embodiment is disposed at the top of the housing.
  • the inlet port 7 and the air inlet port 6 may be disposed as shown in FIG. 2, and the air inlet port 6 and the inlet port 7 may be simultaneously disposed in the shell.
  • the bottom of the cavity is provided with a rotating device, the rotating device is provided with a lifting tooth 4, the rotating device is driven by the driving shaft 5 of the driving device 1, the rotating device and the driving device are arranged on the frame 2, and the casing 3 is provided with the casing 3
  • the rotation speed of the rotating device is 50-500 rpm (200 rpm in this embodiment), and the lifting teeth 4 on the rotating device throw the material so that the material is diffused in the hot air flow, and the drying time of the material in the entire cavity It is 1-5s (3s in this embodiment); the material is dried by hot air flow (mass heat exchange) and then discharged with the drying device.
  • the temperature at the hot air outlet 8 is 120-200 degrees Celsius.
  • the hot gas flow direction curve 10 is as shown in FIG. 2.
  • the dehydration rate of the drying method defined by the present invention is greatly improved by limiting the parameters such as the negative pressure value, the temperature, the oxygen content, and the like; , no explosion, safe operation in the workshop; high drying rate.
  • the moisture content of the dried coal is better controlled, the particle size of the material is uniform, and the quality of the product after drying is effectively ensured.
  • the invention is limited in that the drying time of the material in the entire cavity is short, which can ensure high dehydration rate without pyrolysis (combustion reaction) of the material, and the material is quickly dried and does not stick to the chamber casing.
  • the material is collected at the discharge end 9, the flue gas stream is collected to the separator and the dust collector, and the width of the last chamber is greater than the width of the other chambers, so that the material flow rate is reduced, and most of the slime is discharged from the discharge end 9. .
  • the drying device of this embodiment can also be as shown in FIG. 4, the cavity of the drying device is divided into a plurality of chambers divided by the baffle plate, and the material is dispersed in the chamber through the disintegration of the lifting teeth, and after depolymerization After the material is dried in the chamber with the hot gas flow (mass heat exchange), it gradually flows to the next chamber and is finally discharged through the discharge port.
  • the cavity of the drying device is divided into a plurality of chambers which are divided by the staggered baffles and the wind deflector, so that the flow of the hot air and the material in the chamber is S-shaped. The heat exchange is sufficient and the thermal efficiency is improved.
  • the present embodiment provides a method for drying gas coal, as shown in FIG. 1 to FIG. 3, comprising the steps of: generating a hot gas flow (flue gas) with a gas heating device (commonly, such as a hot air furnace), and setting the temperature to 200. - 1500 degrees Celsius (900 degrees Celsius in this embodiment), a hot gas stream having an oxygen content of less than 10% is introduced into the cavity of the drying device from the air inlet 6, and an air blower is provided at the end of the air outlet 8 (not shown).
  • a hot gas flow flue gas
  • a gas heating device commonly, such as a hot air furnace
  • the cavity of the drying device is caused to generate a negative pressure of 100-6000 Pa (4000 Pa in this embodiment), and the flow rate of the hot gas flow in the cavity is 8-14 m/s (8 m/s in this embodiment); the feeding device inlet port 7
  • the set position needs to be higher than the top of the lifter tooth 4, and this embodiment is disposed at the top of the housing. In this way, the material and the hot air flow are concurrently flowed into the cavity.
  • the inlet port 7 and the air inlet port 6 may be disposed as shown in FIG. 2, and the air inlet port 6 and the inlet port 7 may be simultaneously disposed in the shell.
  • the bottom of the cavity is provided with a rotating device, the rotating device is provided with a lifting tooth 4, the rotating device is driven by the driving shaft 5 of the driving device 1, the rotating device and the driving device are arranged on the frame 2, and the casing 3 is provided with the casing 3
  • the rotation speed of the rotating device is 50-500 rpm (250 rpm in this embodiment), and the lifting teeth 4 on the rotating device throw the material so that the material is diffused in the hot air flow, and the drying time of the material in the entire cavity It is 1-5s (3s in this embodiment); the material is dried by hot air flow (mass heat exchange) and then discharged with the drying device.
  • the temperature at the hot air outlet 8 is 120-200 degrees Celsius.
  • the hot gas flow direction curve 10 is as shown in FIG. 2.
  • the dehydration rate of the drying method defined by the present invention is greatly improved by limiting the parameters such as the negative pressure value, the temperature, the oxygen content, and the like; , no explosion, safe operation in the workshop; high drying rate.
  • the moisture content of the dried coal is better controlled, the particle size of the material is uniform, and the quality of the product after drying is effectively ensured.
  • the invention is limited in that the drying time of the material in the entire cavity is short, which can ensure high dehydration rate without pyrolysis (combustion reaction) of the material, and the material is quickly dried and does not stick to the chamber casing.
  • the material is collected at the discharge end 9, the flue gas stream is collected to the separator and the dust collector, and the width of the last chamber is greater than the width of the other chambers, so that the material flow rate is reduced, and most of the slime is discharged from the discharge end 9. .
  • the drying device of this embodiment can also be as shown in FIG. 4, the cavity of the drying device is divided into a plurality of chambers divided by the baffle plate, and the material is dispersed in the chamber through the disintegration of the lifting teeth, and after depolymerization After the material is dried in the chamber with the hot gas flow (mass heat exchange), it gradually flows to the next chamber and is finally discharged through the discharge port.
  • the cavity of the drying device is divided into a plurality of chambers which are divided by the staggered baffles and the wind deflector, so that the flow of the hot air and the material in the chamber is S-shaped. The heat exchange is sufficient and the thermal efficiency is improved.
  • the present embodiment provides a method for drying lean coal, as shown in FIG. 1 to FIG. 3, comprising the steps of: generating a hot gas flow (flue gas) with a gas heating device (commonly, such as a hot air furnace), and setting the temperature to 200. -1500 degrees Celsius (1000 degrees Celsius in this embodiment), a hot gas stream having an oxygen content of less than 10% is introduced into the cavity of the drying device from the air inlet 6, and an air blower is provided at the end of the air outlet 8 (not shown).
  • a hot gas flow flue gas
  • a gas heating device commonly, such as a hot air furnace
  • a hot gas stream having an oxygen content of less than 10% is introduced into the cavity of the drying device from the air inlet 6, and an air blower is provided at the end of the air outlet 8 (not shown).
  • the cavity of the drying device is caused to generate a negative pressure of 100-6000 Pa (4000 Pa in this embodiment), and the flow rate of the hot gas flow in the cavity is 8-14 m/s (8 m/s in this embodiment); the feeding device inlet port 7
  • the set position needs to be higher than the top of the lifter tooth 4, and this embodiment is disposed at the top of the housing. In this way, the material and the hot air flow are concurrently flowed into the cavity.
  • the inlet port 7 and the air inlet port 6 may be disposed as shown in FIG. 2, and the air inlet port 6 and the inlet port 7 may be simultaneously disposed in the shell.
  • the bottom of the cavity is provided with a rotating device, the rotating device is provided with a lifting tooth 4, the rotating device is driven by the driving shaft 5 of the driving device 1, the rotating device and the driving device are arranged on the frame 2, and the casing 3 is provided with the casing 3
  • the rotation speed of the rotating device is 50-500 rpm (180 rpm in this embodiment), and the lifting teeth 4 on the rotating device throw the material so that the material is diffused in the hot air flow, and the drying time of the material in the entire cavity It is 1-5s (3s in this embodiment); the material is dried by hot air flow (mass heat exchange) and then discharged with the drying device.
  • the temperature at the hot air outlet 8 is 120-200 degrees Celsius.
  • the hot gas flow direction curve 10 is as shown in FIG. 2.
  • the dehydration rate of the drying method defined by the present invention is greatly improved by limiting the parameters such as the negative pressure value, the temperature, the oxygen content, and the like; , no explosion, safe operation in the workshop; high drying rate.
  • the moisture content of the dried coal is better controlled, the particle size of the material is uniform, and the quality of the product after drying is effectively ensured.
  • the invention is limited in that the drying time of the material in the entire cavity is short, which can ensure a high dehydration rate without causing pyrolysis (combustion reaction) of the material, and the material is quickly dried and does not stick to the chamber casing.
  • the material is collected at the discharge end 9, the flue gas stream is collected to the separator and the dust collector, and the width of the last chamber is greater than the width of the other chambers, so that the material flow rate is reduced, and most of the slime is discharged from the discharge end 9. .
  • the drying device of this embodiment can also be as shown in FIG. 4, the cavity of the drying device is divided into a plurality of chambers divided by the baffle plate, and the material is dispersed in the chamber through the disintegration of the lifting teeth, and after depolymerization After the material is dried in the chamber with the hot gas flow (mass heat exchange), it gradually flows to the next chamber and is finally discharged through the discharge port.
  • the cavity of the drying device is divided into a plurality of chambers which are divided by the staggered baffles and the wind deflector, so that the flow of the hot air and the material in the chamber is S-shaped. The heat exchange is sufficient and the thermal efficiency is improved.
  • the present embodiment provides a method for drying anthracite coal, as shown in FIG. 1 to FIG. 3, comprising the steps of: generating a hot gas flow (flue gas) with a gas heating device (commonly, such as a hot air furnace), and setting the temperature to 200- 1500 degrees Celsius (800 degrees Celsius in this embodiment), a hot gas flow having an oxygen content of less than 10% is introduced into the cavity of the drying device from the air inlet 6, and an induced draft fan (not shown) is provided at the end of the air outlet 8 so that
  • the cavity of the drying device generates a negative pressure of 100-6000 Pa (4000 Pa in this embodiment), the flow rate of the hot gas flow in the cavity is 8-14 m/s (8 m/s in this embodiment); the inlet of the drying device 7
  • the setting position needs to be higher than the top of the lifting teeth 4, and this embodiment is provided at the top of the housing.
  • the inlet port 7 and the air inlet port 6 may be disposed as shown in FIG. 2, and the air inlet port 6 and the inlet port 7 may be simultaneously disposed in the shell.
  • the bottom of the cavity is provided with a rotating device, the rotating device is provided with a lifting tooth 4, the rotating device is driven by the driving shaft 5 of the driving device 1, the rotating device and the driving device are arranged on the frame 2, and the casing 3 is provided with the casing 3
  • the rotation speed of the rotating device is 50-500 rpm (200 rpm in this embodiment), and the lifting teeth 4 on the rotating device throw the material so that the material is diffused in the hot air flow, and the drying time of the material in the entire cavity It is 1-5s (2s in this embodiment); the material is dried by hot air flow (mass heat exchange) and then discharged with the drying device.
  • the temperature at the hot air outlet 8 is 120-200 degrees Celsius.
  • the hot gas flow direction curve 10 is as shown in FIG. 2.
  • the dehydration rate of the drying method defined by the present invention is greatly improved by limiting the parameters such as the negative pressure value, the temperature, the oxygen content, and the like; , no explosion, safe operation in the workshop; high drying rate.
  • the moisture content of the dried coal is better controlled, the particle size of the material is uniform, and the quality of the product after drying is effectively ensured.
  • the invention is limited in that the drying time of the material in the entire cavity is short, which can ensure high dehydration rate without pyrolysis (combustion reaction) of the material, and the material is quickly dried and does not stick to the chamber casing.
  • the material is collected at the discharge end 9, the flue gas stream is collected to the separator and the dust collector, and the width of the last chamber is greater than the width of the other chambers, so that the material flow rate is reduced, and most of the slime is discharged from the discharge end 9. .
  • the drying device of this embodiment can also be as shown in FIG. 4, the cavity of the drying device is divided into a plurality of chambers divided by the baffle plate, and the material is dispersed in the chamber through the disintegration of the lifting teeth, and after depolymerization After the material is dried in the chamber with the hot gas flow (mass heat exchange), it gradually flows to the next chamber and is finally discharged through the discharge port.
  • the cavity of the drying device is divided into a plurality of chambers which are divided by the staggered baffles and the wind deflector, so that the flow of the hot air and the material in the chamber is S-shaped. The heat exchange is sufficient and the thermal efficiency is improved.
  • the present embodiment provides a method for drying urban sludge, as shown in FIG. 1 to FIG. 3, comprising the steps of: generating a hot gas flow (flue gas) by using a gas heating device (commonly such as a hot air furnace), and setting the temperature to 900-1500 degrees Celsius (1000 degrees Celsius in this embodiment), a hot gas flow of less than 10% oxygen is introduced into the cavity of the drying device from the air inlet 6, and an induced draft fan is provided at the end of the air outlet 8 (not shown)
  • the cavity of the drying device is caused to generate a negative pressure of 100-6000 Pa (4000 Pa in this embodiment), and the flow rate of the hot gas flow in the cavity is 8-14 m/s (8 m/s in this embodiment); the inlet of the drying device
  • the set position of 7 needs to be higher than the top of the lifter tooth 4, and this embodiment is disposed at the top of the housing.
  • the inlet port 7 and the air inlet port 6 may be disposed as shown in FIG. 2, and the air inlet port 6 and the inlet port 7 may be simultaneously disposed in the shell.
  • the bottom of the cavity is provided with a rotating device, the rotating device is provided with a lifting tooth 4, the rotating device is driven by the driving shaft 5 of the driving device 1, the rotating device and the driving device are arranged on the frame 2, and the casing 3 is provided with the casing 3
  • the rotation speed of the rotating device is 50-500 rpm (200 rpm in this embodiment), and the lifting teeth 4 on the rotating device throw the material so that the material is diffused in the hot air flow, and the drying time of the material in the entire cavity It is 1-5s (3s in this embodiment); the material is dried by hot air flow (mass heat exchange) and then discharged with the drying device.
  • the temperature at the hot air outlet 8 is 120-200 degrees Celsius.
  • the hot gas flow direction curve 10 is as shown in FIG. 2.
  • the dehydration rate of the drying method defined by the present invention is greatly improved by limiting the parameters such as the negative pressure value, the temperature, the oxygen content, and the like; , no explosion, safe operation in the workshop; high drying rate.
  • the moisture content of the dried coal is better controlled, the particle size of the material is uniform, and the quality of the product after drying is effectively ensured.
  • the invention is limited in that the drying time of the material in the entire cavity is short, which can ensure high dehydration rate without pyrolysis (combustion reaction) of the material, and the material is quickly dried and does not stick to the chamber casing.
  • the material is collected at the discharge end 9, the flue gas stream is collected to the separator and the dust collector, and the width of the last chamber is greater than the width of the other chambers, so that the material flow rate is reduced, and most of the slime is discharged from the discharge end 9. .
  • the drying device of this embodiment can also be as shown in FIG. 4, the cavity of the drying device is divided into a plurality of chambers divided by the baffle plate, and the material is dispersed in the chamber through the disintegration of the lifting teeth, and after depolymerization After the material is dried in the chamber with the hot gas flow (mass heat exchange), it gradually flows to the next chamber and is finally discharged through the discharge port.
  • the cavity of the drying device is divided into a plurality of chambers which are divided by the staggered baffles and the wind deflector, so that the flow of the hot air and the material in the chamber is S-shaped. The heat exchange is sufficient and the thermal efficiency is improved.
  • the present embodiment provides a method for drying a non-ferrous metal tailings, as shown in FIG. 1 to FIG. 3, comprising the steps of: generating a hot gas flow (flue gas) by using a gas heating device (commonly such as a hot air furnace)
  • a gas heating device commonly such as a hot air furnace
  • a hot gas stream of 200-1500 degrees Celsius, preferably 700-1500 degrees Celsius (1100 degrees Celsius in the present embodiment) and an oxygen content of less than 10% is introduced into the cavity of the drying device from the air inlet 6 and an induced draft fan is provided at the end of the air outlet 8 (not shown in the figure)
  • the cavity of the drying device is made to generate a negative pressure of 100-6000 Pa (4000 Pa in this embodiment)
  • the flow rate of the hot gas flow in the cavity is 8-14 m/s (8 m/s in this embodiment).
  • the setting position of the drying device inlet port 7 needs to be higher than the top of the lifting tooth 4, and this embodiment is disposed at the top of the housing. In this way, the material and the hot air flow are concurrently flowed into the cavity.
  • the inlet port 7 and the air inlet port 6 may be disposed as shown in FIG. 2, and the air inlet port 6 and the inlet port 7 may be simultaneously disposed in the shell.
  • the bottom of the cavity is provided with a rotating device, the rotating device is provided with a lifting tooth 4, the rotating device is driven by the driving shaft 5 of the driving device 1, the rotating device and the driving device are arranged on the frame 2, and the casing 3 is provided with the casing 3
  • the rotation speed of the rotating device is 50-500 rpm (200 rpm in this embodiment), and the lifting teeth 4 on the rotating device throw the material so that the material is diffused in the hot air flow, and the drying time of the material in the entire cavity It is 1-5s (3s in this embodiment); the material is dried by hot air flow (mass heat exchange) and then discharged with the drying device.
  • the temperature at the hot air outlet 8 is 120-200 degrees Celsius.
  • the hot gas flow direction curve 10 is as shown in FIG. 2.
  • the dehydration rate of the drying method defined by the present invention is greatly improved by limiting the parameters such as the negative pressure value, the temperature, the oxygen content, and the like; , no explosion, safe operation in the workshop; high drying rate.
  • the moisture content of the dried coal is better controlled, the particle size of the material is uniform, and the quality of the product after drying is effectively ensured.
  • the invention is limited in that the drying time of the material in the entire cavity is short, which can ensure high dehydration rate without pyrolysis (combustion reaction) of the material, and the material is quickly dried and does not stick to the chamber casing.
  • the material is collected at the discharge end 9, the flue gas stream is collected to the separator and the dust collector, and the width of the last chamber is greater than the width of the other chambers, so that the material flow rate is reduced, and most of the slime is discharged from the discharge end 9. .
  • the drying device of this embodiment can also be as shown in FIG. 4, the cavity of the drying device is divided into a plurality of chambers divided by the baffle plate, and the material is dispersed in the chamber through the disintegration of the lifting teeth, and after depolymerization After the material is dried in the chamber with the hot gas flow (mass heat exchange), it gradually flows to the next chamber and is finally discharged through the discharge port.
  • the cavity of the drying device is divided into a plurality of chambers which are divided by the staggered baffles and the wind deflector, so that the flow of the hot air and the material in the chamber is S-shaped. The heat exchange is sufficient and the thermal efficiency is improved.
  • the low rank coal is any one of lignite, long flame coal, non-stick coal, weakly cohesive coal, blast furnace coal, gas coal, gas fat coal, lean coal, lean coal, fat coal, anthracite. After the test, the drying effect of the above examples is also excellent, and will not be described herein.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
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  • Treatment Of Sludge (AREA)

Abstract

一种物料的干燥方法，将温度为200-1500摄氏度、含氧量小于12％的热气流从进风口(6)引入干燥装置的腔体中，出风口(8)尾端设有引风机，使干燥装置的腔体产生100-6000Pa的负压，腔体中热气流的流速为2-24m/s；旋转装置上的扬料齿(4)抛洒物料使得物料弥漫在热气流中，物料和热气流并流进入腔体，干燥装置入料口(7)的设置位置高于扬料齿(4)顶部，物料在整个腔体中的干燥时间是1-20s；物料被热气流干燥后从干燥装置排出。通过对干燥装置的腔体内的负压值、温度、含氧量等参数的限定，使得脱水率大于60％，不会发生爆炸，干燥速率高。

Description

一种物料的干燥方法 技术领域
本发明涉及物料的干燥方法领域，特别涉及高含水、高粘稠的物料干燥。
背景技术
随着我国工业化水平的发展，我国的环境污染也越来越严重，环境的承载力受到越来越大的挑战。
首先，城市生活污水处理后形成的污泥，一般含水率约80％，富含有机质等营养成分，又含有一定量的重金属和病毒、病原体、寄生虫卵等有害物质，污泥处置不当会造成严重的二次环境污染。目前国外污泥主要的处置方法有一下三种：1.土地填理。在过去，许多发达国家都采用土地填埋的方法来处理污泥，且占有很大的比例(约40％左右)。在我国，土地填埋也是主要的方法。该法的处理过程非常简单，特别适于质量较差的污泥，但需要场地和大量的运费，地基需作防渗处理以免污染地下水和散逸臭味。另外，适合充填的土地逐年减少。2.投弃海洋。在一些靠海的国家和地区，大型的污水处理厂常直接将液态污泥排海或将脱水污泥直接投海。这是一种方便而经济的处理方法，但此法会危害海洋生态系统及人类食物链，造成全球范围内的危害。1988年美国已禁止向海洋倾倒污泥，并于1991年全面加以禁止。欧共体在1991年5月颁布《Directive Concerning Urban Wastewater Treatment》中指出：在1998年12月31日起，不得在水体中处置污泥。3.焚烧法。在欧美，当污泥中重金属或其它有毒物质含量高而不适用于农业利用的情况下，常采取焚烧法。污泥经焚烧后产生无菌、无臭的无机残渣，并大大减少了体积，是一种可靠而有效的污泥处置方法。污泥焚烧灰能有效地用在沥青填料和轻质基材等建筑材料，如做砖的主要原料。燃烧产生的热可以用来供电。但焚烧法设备及运行费用昂贵，易造成大气污染，仍存在有1/3左右固体重量的废 弃物，以灰分的形式存留下来。
以上这些对城市污泥的处置方法均不能实现对污泥的综合利用，存在一定的社会及环境问题，不是污泥处置的最佳出路。对我国这样一个发展中国家而言，综合利用尤其是农业利用无疑是较好的选择，实现污泥的有效利用、变废为宝，使之资源化并产生经济效益，将成为污泥处置的发展方向。
在城市生活污水水处理的污泥中，含水率约80％，并含有大量有机质成份。利用污泥制造有机复合肥过程是将污泥高温干燥，杀灭病菌、虫卵，保存有机成份不受破坏且除去有害菌(进行无害化处理)，接入有益菌培养，消除污泥的臭味，增加污泥中的营养元素，再添加氮、磷、钾有效成分，增加污泥中的养分含量，经造粒、低温烘干等工艺，将污泥制成具有生物活性、全营养、无公害的有机复合肥。从而为水处理后的污泥找到了很好的出路，并增加了污水处理厂和设备生产厂家的经济效益、社会效益，使污泥变废为宝，减少了环境污泥，保护了人类赖以生存的自然环境，同时又有利于生态农业的发展。
但是能把污泥变废为宝的关键在于干燥设备和干燥方法，目前的干燥方法无法做到高效率、高脱水率，并且安全无法保障。
其次，矿产资源是人类生存和发展的重要物质基础之一，也是社会发展的前提和保证。目前我国95％的能源和85％的原材料来自矿产资源，且随着我国经济的快速发展，对矿产资源的需求不断增加。大量矿产资源的开发不仅带来了丰富的物质原料，同时也产生了大量的尾矿。因此尾矿利用是矿山企业可持续发展所面临的重大问题。
我国是有色金属生产大国，尾矿量占入选矿石的70％～95％，尾矿量堆存为22亿吨以上，并以每年1.4亿吨增长，而尾矿坝正常运行很少，尾矿平均利用率为8.2％。因此，从我国有色金属尾矿资源的实际出发，大力发展尾矿资源综合利 用，对改善生态环境、提高资源利用率，都有十分重要的意义。将有色金属尾矿干燥后用作建筑材料等用途是最环保的用途。
但是能把有色金属尾矿关键还是干燥设备和干燥方法，目前的干燥方法无法做到高效率、高脱水率，并且安全无法保障。
再者，我国以煤为基础能源，随着环境污染问题和资源短缺问题的日益凸显，煤炭高效利用已刻不容缓。我国仍处于工业化，城镇化加快发展的历史阶段。能源需求总量仍有增长空间，煤炭占我国化石能源资源的90％以上，在相当长时期内，煤炭的主体能源地位不会变化，煤炭发展的生态环境约束日益强化。煤炭清洁高效开发利用成为能源转型发展的首要任务。煤炭分级分质梯级利用技术开发及产业化、低价煤绿色高效利用技术开发被列为国家能源发展战略行动计划。
目前，我国对高含水、高粘稠煤(煤泥、低阶煤等)的利用率较低，但是高含水、高粘稠煤(煤泥、低阶煤等)的提质利用已经被列入国家的能源十三五规划中，该产业将长期得到国家政策的支持。煤的提质的关键工艺是干燥，因为煤的发热量与含水量息息相关，只要将水分降低，发热量就会相应提高。
以煤泥为例，煤泥作为原煤洗选过程产生的副产品，因其含水高、粘性大、热值低，一直是被视为难以利用的废弃物。实际上，煤泥难以利用的根源在于其水分高，每降低一个水分点，发热量将增加60大卡。水分30％的煤泥的发热量一般为2000-4000大卡，如果再脱水15％，发热量将提高900大卡以上，达到3000-5000大卡。达到商品动力煤的质量要求，可单独销售，也可与中煤(混煤)掺配销售，使煤泥由选煤废弃物或副产品价格增值为商品动力煤价格。
目前煤泥的处置方式有三种：
(1)大部分地区因煤泥没有销路，直接将煤泥堆放在自然天坑或山沟。煤泥经压滤后仍含水30％左右，很容易再液化流动污染周边环境。干化后，遇风漫 天飞扬，遇水四处流淌，污染道路、土地、河流，还可能直接渗入地下污染地下水。这种简单的处置方式，不但企业承担的土地费、运输费、排污费等经济成本相对较高，而且还会污染环境，污染水体造成的社会成本是巨大的。
(2)一些地区煤泥被掺入到煤泥中一起出售，这样做就增加了商品煤的灰分和水分，拉低了商品煤的质量，运输水分也增加了运输成本，还会造成煤泥结团引起堵塞和卸车困难等问题，遇到冬季气温较低时，甚至出现冻车情况，严重影响运输效率。实际上这种处置方式让原煤洗选效果大打折扣。
(3)这些年发展了一批煤矸石和煤泥综合利用的电厂，燃烧处理一部分煤泥。但含水30％的煤泥对于电厂煤粉锅炉来说水分太高，气化潜热消耗大量热量，严重降低锅炉的热效率，增大运营成本的同时也增大排放量，增大环保的投入。
上述三种处置方式，或就地堆存、或带水销售、或带水燃烧均是为了消耗煤泥本身而处置，既没有经济效益又造成资源浪费。
基于以上，高含水、高粘稠煤(煤泥、低阶煤等)一直难以被利用，关键在于其含水量过高影响了发热效率，对其提质的关键在于干燥。众所周知，物料的干燥尤其是煤的干燥存在着以下几大难题：1、如果温度和含氧量均过高，那么在干燥过程中煤会发生热解(燃烧反应)，影响煤的发热值；2、“粉尘浓度、含氧量、温度”三个参数控制不好，会发生着火爆炸。3、现有干燥方法或装置一般只能用于干燥单一物料，通用性差；而且干燥速率低。
目前国内干燥工艺及设备很多。在煤炭行业煤泥干燥领域主要有：煤泥滚筒干燥工艺、隧道式干燥工艺(包括翻板干燥机和网带干燥机)和气流干燥工艺三大类。
滚筒干燥机是最早的干燥设备之一，它不仅用于煤炭的干燥，而且早已广泛应用于冶金、建材、化工等领域。滚筒干燥工艺机的缺点是：这类干燥工艺的干 燥温度在700℃以上，不能有效控制干燥过程中的氧含量，温度远远高于褐煤及长焰煤的着火点278℃，干燥时间还比较长，不适合褐煤及长焰煤煤泥干燥，会发生物理反应，影响煤的使用性能。而且，该种干燥设备用于干燥煤泥仅能够提升热值400-600kcal/kg，脱水率小于30％，不具有粉尘回收功能。
隧道式干燥工艺适用于块状、条状物料的干燥。有翻板式装置和金属网带式装置，煤泥挤压成条后，可以在金属网带烘干机上进行干燥。这种干燥工艺的缺点是：不适应于散状煤泥的干燥，干燥效率较低。
气流式干燥工艺是利用加热介质(热空气、烟道气等)和湿物料颗粒直接接触，并使固体颗粒悬浮于加热介质流体中，强化了传质传热过程，属于“瞬间干燥”，一般应用于散状物料的干燥。对煤炭行业的煤泥干燥，也先要“造粒”或“成型”。这种干燥工艺的缺点是：该种干燥设备用于干燥煤泥仅能够提升热值200-400kcal/kg，脱水率小于7％，不具有粉尘回收功能，用于干燥煤泥的工业实践效果不佳，一般不采用该工艺干燥煤泥。
不黏煤、褐煤等低阶煤的利用同样存在着技术壁垒。不黏煤是一种低-中变质程度的烟煤，它的丝炭化组分普遍含量高，水分大。不经过干燥提质处理，其利用价值很低。
现有的褐煤干燥工艺主要有：蒸煮干燥工艺、气流逆行滚筒干燥工艺，具体介绍如下：CN102051246A公开了一种褐煤的蒸煮干燥工艺，具体步骤为：a.用温度大于30℃的热水对褐煤颗粒原料进行洗涤和浸出处理，以除去所述褐煤颗粒原料中所含的粉尘和一部分灰份以及一部分硫，同时得到经初步提质的褐煤颗粒；然后，b.使所述经初步提质的褐煤颗粒进入蒸煮器，然后在加压条件下用蒸汽蒸煮该褐煤颗粒一定时间，以得到经进一步提质的褐煤颗粒，并排出在蒸煮过程中所得到的液体水；然后，c.使所述蒸煮器卸压，然后从中排出所述经进一步 提质的褐煤颗粒。但是该种方法的脱水率很低，干燥速率也很低，没有工业运用价值。CN103013615A公开了一种褐煤高效干燥提质装置和方法，来自燃料仓的燃煤以及从旋风除尘器和电除尘器中分离出来的粉煤在热风炉中燃烧，产生温度为700-900℃的高温烟气，该高温烟气作为干燥热源，输送到滚筒式干燥器中，并沿倾斜的滚筒式干燥器从下往上流动，用于干燥滚筒式干燥器中的原料褐煤，高温烟气和原料褐煤之间进行对流换热，高温烟气对原料褐煤进行干燥后，变成携带有原料褐煤中的粉煤的低温烟气，低温烟气的温度为90-120℃，该低温烟气从滚筒式干燥器输出。但是该种干燥工艺，含氧量无法控制，容易挂料，褐煤与气流是逆行的，褐煤在干燥装置中的停留时间过长，容易热解，且干燥速率不高，不适宜工业推广运用。
基于以上，通过大量实验研究各种参数之间的关系，提供一种脱水率高、设备简单、运行安全、干燥效率高、通用性好、环保的物料干燥方法，是本发明的创研动机。
发明内容
本发明的目的在于克服现有技术的不足，提供一种脱水率高、设备简单、运行安全、干燥效率高、通用性好、环保的物料干燥方法。本发明的干燥方法通用性好，适宜干燥低阶煤、煤泥、城市污泥或者有色金属尾矿等多种物料。
本发明提供的一种物料的干燥方法，其技术方案为：
一种物料的干燥方法，包括以下步骤：将温度为200-1500摄氏度、含氧量小于12％的热气流从进风口引入干燥装置的腔体中，出风口尾端设有引风机，使干燥装置的腔体产生100-6000Pa的负压，腔体中热气流的流速为2-24m/s；腔体的底部设置有旋转装置，干燥装置入料口的设置位置高于旋转装置上扬料齿的顶部，旋转装置的转速为50-500转/分钟，物料和热气流并流进入腔体，扬料齿破 碎并将物料抛洒弥漫在热气流中，物料在整个腔体中的干燥时间是1-20s；物料被热气流干燥后从干燥装置排出。
优选地，干燥装置的腔体分为由挡料板分割成的多个腔室，当物料通过扬料齿解聚抛洒弥漫在腔室内，解聚后的物料随热气流在腔室中干燥后，逐步流向下一个腔室，最后经排料口排出。
优选地，干燥装置的腔体分为由交错设置的挡料板和挡风板分割成的多个腔室，使得热气流与物料在腔室中的走向为S形。
优选地，最后一个腔室的宽度大于其它腔室的宽度，使得物料流速降低。
优选地，物料通过出料端、烟气流向分离器及除尘器收集。
优选地，热气流出风口处的温度为60-200摄氏度。
优选地，物料干燥后的颗粒度为0.01-15mm。
优选地，进风口热气流的温度为800-1100摄氏度、含氧量小于8％，干燥装置的负压为900-6000Pa，腔体中热气流的流速为8-18m/s；旋转装置的转速为100-400转/分钟，物料在整个腔体中的干燥时间是1-5s。
优选地，进风口热气流的温度为600-900摄氏度、含氧量小于11％，干燥装置的负压为900-6000Pa，腔体中热气流的流速为8-14m/s；旋转装置的转速为100-400转/分钟，物料在整个腔体中的干燥时间是1-5s。
优选地，所述干燥方法用于干燥褐煤、长焰煤、不黏煤、弱黏煤、高炉喷吹煤、气煤、气肥煤、贫瘦煤、瘦煤、肥煤、无烟煤、煤泥、城市污泥或者有色金属尾矿。
优选地，上述干燥方法用于干燥低阶煤，低阶煤是褐煤、长焰煤、不黏煤、弱黏煤、高炉喷吹煤、气煤、气肥煤、贫瘦煤、瘦煤、肥煤、无烟煤中的任一种。一种低阶煤的干燥方法，其中，进风口热气流的温度为901-1100摄氏度、含氧量 小于8％，干燥装置的负压为900-6000Pa，腔体中热气流的流速为8-18m/s；旋转装置的转速为100-400转/分钟，物料在整个腔体中的干燥时间是1-5s。
优选地，上述干燥方法用于干燥煤泥。一种煤泥的干燥方法，其中，进风口热气流的温度为800-1100摄氏度、含氧量小于8％，干燥装置的负压为900-6000Pa，腔体中热气流的流速为8-18m/s；旋转装置的转速为100-400转/分钟，物料在整个腔体中的干燥时间是1-5s。
优选地，上述干燥方法用于干燥城市污泥。一种城市污泥的干燥方法，其中，进风口热气流的温度为900-1500摄氏度、含氧量小于10％，干燥装置的负压为900-6000Pa，腔体中热气流的流速为8-18m/s；旋转装置的转速为100-400转/分钟，物料在整个腔体中的干燥时间是1-5s。
优选地，上述干燥方法用于干燥有色金属尾矿。一种有色金属尾矿的干燥方法，其中，进风口热气流的温度为700-1500摄氏度、含氧量小于10％，干燥装置的负压为900-6000Pa，腔体中热气流的流速为8-14m/s；旋转装置的转速为100-400转/分钟，物料在整个腔体中的干燥时间是1-5s。
名词解释：
解聚：物料由大颗粒破碎为小颗粒的过程。
质热交换：相互之间的热量传导，质量变化的过程，具体到本发明中热气流将热量传导到物料，使物料升温，同时伴随着水分蒸发，物料被干燥的过程。
本发明的实施包括以下有益效果包括：
本发明通过对干燥装置的腔体内的负压值、温度、含氧量等参数的限定，使得本发明所限定的干燥方法脱水率大于60％；不会发生爆炸，车间运行安全；干燥速率高，能够达到600-750kg·H 20/m 3·h(每立方米干燥空间每小时能够脱出600-750千克的水)，该干燥方法每小时可干燥物料30-80立方。干燥后的煤的含 水量控制较好，物料的颗粒度均匀，有效的保证烘干后产品的质量。本发明的限定使得物料在整个腔体中的干燥时间很短，既能够保证高脱水率又不会使物料发生热解(燃烧反应)，
本发明通过干燥时间、热风温度和腔室负压参数的设置，使得物料快速干燥，不会粘黏在腔室壳体上。
当本发明的干燥方法用于干燥煤时，由于干燥温度、负压、流速、含氧量参数的合理设置，使得煤的可燃性成分不会挥发或燃烧，无法达到爆炸临界值，影响煤的发热值。
附图说明
图1为本发明实施例的物料干燥方法流程图。
图2为本发明实施例的干燥装置的结构示意图。
图3为图2的A-A剖面结构示意图。
图4为本发明实施例的含有挡料板的干燥装置的结构示意图。
图5为本发明实施例的含有挡料板和挡风板的干燥装置的结构示意图。
图6为本发明实施例的物料干燥方法另一种流程图。
图7为本发明实施例的随热气流排料的干燥装置的结构示意图。
图中：1、驱动装置；2、机架；3、机壳；4、扬料齿；5驱动轴；6、进风口；7、入料口；8、出风口；9、出料端；10、热气流流向曲线；11、挡料板；12、挡风板。
具体实施方式
下面将结合实施例以及附图对本发明加以详细说明，需要指出的是，所描述的实施例仅旨在便于对本发明的理解，而对其不起任何限定作用。
实施例1
本实施例提供的一种煤泥的干燥方法，参见图1至图3所示，包括以下步骤：用一种气体加热装置(常见的如热风炉)产生热气流(烟气)，将温度为200-1500摄氏度(本实施例为901摄氏度)、含氧量小于10％的热气流从进风口6引入干燥装置的腔体中，出风口8尾端设有引风机(图中未视出)，使干燥装置的腔体产生100-6000Pa(本实施例为4000Pa)的负压，腔体中热气流的流速为8-14m/s(本实施例为10m/s)；干燥装置入料口7的设置位置需要高于扬料齿4顶部，本实施例设置在壳体顶部。如此设置使物料和热气流并流进入腔体，需要特别说明的是，入料口7和进风口6可以如图2所示设置，也可以将进风口6和入料口7同时设置在壳体的一侧，只要物料和热气流能够在被扬料齿4抛洒之前汇集都属于本实施例所说的“物料和热气流并流进入腔体”的方式。腔体的底部设置有旋转装置，旋转装置设置有扬料齿4，旋转装置通过驱动装置1的驱动轴5驱动，旋转装置和驱动装置设置在机架2上，机架2上设置机壳3，旋转装置的转速为50-500转/分钟(本实施例为200转/分钟)，旋转装置上的扬料齿4抛洒物料使得物料弥漫在热气流中，物料在整个腔体中的干燥时间是1-5s(本实施例为5s)；物料被热气流干燥(质热交换)后随干燥装置排出。热气流出风口8处的温度为120-200摄氏度。热气流流向曲线10如图2所示，本实施例通过对负压值、温度、含氧量等参数的限定，使得本发明所限定的干燥方法的脱水率大大提高；达不到爆炸临界值，不会发生爆炸，车间运行安全；干燥速率高。干燥后的煤的含水量控制较好，物料的颗粒度均匀，有效的保证烘干后产品的质量。本发明的限定使得物料在整个腔体中的干燥时间短，既能够保证高脱水率又不会使物料发生热解(燃烧反应)，物料快速干燥，不会粘黏在腔室壳体上。
优选地，物料通过出料端9、烟气流向分离器及除尘器收集，最后一个腔室的宽度大于其它腔室的宽度，使得物料流速降低，大部分煤泥从出料端9排出。
本实施例驱动轴的转速可用变频器实现调速，以调节煤泥物料在壳体的抛洒的速度，进而调节热交换过程中的热气流的温度及内部的含氧量。在实际生产过程中还配合引风机的风压大小，能提高物料在腔室内空间的热交换效率，减小物料沿运动曲线解聚过程中的阻力。
煤炭开采后必须进行洗煤程序，本实施例的方法用于干燥洗煤产生的煤泥，可以完善选煤厂洗选工艺，实现由洗水闭路循环到煤泥回收利用的二次飞跃，彻底解决煤泥产品露天堆放而造成矿区环境“遇水流失、遇风飞扬”的二次污染问题，减少废弃物堆放占地面积，减少企业排污费，从而增加企业经济效益；并解决因季节变化使煤泥销售不畅，或处理困难而影响生产的被动局面。对煤干燥后，水分降低了，可以减少运输水分的成本，并避免了赛车、冻车等问题。到最终用户那里，又可以提升锅炉热效率，减少排放，降低环保投入。
使用本实施例的干燥方法干燥煤泥的数据如表1所示：
表1实施例1煤泥干燥后的数据
干燥速率 600kgH 20/m 3.h
提升热值 900kcal/kg
脱水率 60％左右
煤泥颗粒度 ≤10mm
单台每小时处理能力(湿基) 50立方
实施例2
本实施例提供一种干燥煤泥的方法，与实施例1的区别是，进风口热气流的温度为1000摄氏度、含氧量小于8％，干燥装置的负压为4500Pa，腔体中热气流的流速为10m/s；旋转装置的转速为200转/分钟，物料在整个腔体中的干燥时间是3s。参见图4所示，本实施例的干燥装置的腔体分为由挡料板11分割成的多个腔室，当物料通过扬料齿解聚抛洒弥漫在腔室内，解聚后的物料随热气流在腔室中干燥(质热交换)后，逐步流向下一个腔室，最后经排料口排出。挡料板11设置在机壳3底部。热气流流向曲线10如图4所示。本实施例的方法同样适用 于干燥低阶煤、城市污泥或者有色金属尾矿。与实施例1相同的部分，本实施例不再赘述。
表2实施例2煤泥干燥后的数据
干燥速率 600kgH 20/m 3.h
提升热值 1000kcal/kg
脱水率 65％左右
煤泥颗粒度 ≤10mm
单台每小时处理能力(湿基) 50立方
实施例3
本实施例提供一种干燥煤泥的方法，与实施例1的区别是，进风口热气流的温度为1200摄氏度、含氧量小于8％，干燥装置的负压为4000Pa，腔体中热气流的流速为10m/s；旋转装置的转速为200转/分钟，物料在整个腔体中的干燥时间是3s。参见图5所示，干燥装置的腔体分为由交错设置的挡料板11和挡风板12分割成的多个腔室，使得热气流与物料在腔室中的走向为S形，质热交换充分，热效率提高。热气流流向曲线10如图5所示，挡料板11设置在机壳3底部，挡风板12设置在壳体顶部。本实施例的方法同样适用于干燥低阶煤、城市污泥或者有色金属尾矿。与实施例1相同的部分，本实施例不再赘述。
下档板将壳体分成多个腔室，颗粒度大小及干湿度到达一定程度后才能进入后一个腔室，颗粒度大的及湿度大的物料由于自重较大，无法随同热空气移动进入下一个腔室，继续落入当前腔室由扬料齿搅动实现上扬抛洒，并实现煤泥大颗粒的不断破碎，其破碎由扬料齿、下挡板、颗粒相互撞击共同实现，分多个腔室过渡后最终达到出料闭风器，保证成品颗粒度均匀以及湿度符合要求。
通过上档板和下档板使热空气及物流构成S形走向，交换效率高，能耗小。
表3实施例3煤泥干燥后的数据
干燥速率 600kgH 20/m 3.h
提升热值 1200kcal/kg
脱水率 70％左右
煤泥颗粒度 ≤10mm
单台每小时处理能力(湿基) 50立方
实施例4
本实施例提供一种干燥褐煤的方法，参见图6和图7所示，包括以下步骤：用一种气体加热装置(常见的如热风炉)产生热气流(烟气)，将温度为200-1500摄氏度(本实施例为900摄氏度)、含氧量小于8％的热气流从进风口6引入干燥装置的腔体中，出风口8尾端设有引风机(图中未视出)，使干燥装置的腔体产生100-6000Pa(本实施例为4000Pa)的负压，腔体中热气流的流速为8-14m/s(本实施例为10m/s)；干燥装置入料口7的设置位置需要高于扬料齿4顶部，本实施例设置在壳体顶部。如此设置使物料和热气流并流进入腔体，需要特别说明的是，入料口7和进风口6可以如图7所示设置，也可以将进风口6和入料口7同时设置在壳体的一侧，只要物料和热气流能够在被扬料齿4抛洒之前汇集都属于本实施例所说的“物料和热气流并流进入腔体”的方式。腔体的底部设置有旋转装置，旋转装置设置有扬料齿4，旋转装置通过驱动装置1的驱动轴5驱动，旋转装置和驱动装置设置在机架2上，机架2上设置机壳3，旋转装置的转速为50-500转/分钟(本实施例为200转/分钟)，旋转装置上的扬料齿4抛洒物料使得物料弥漫在热气流中，物料在整个腔体中的干燥时间是1-5s(本实施例为3s)；物料被热气流干燥(质热交换)后随干燥装置排出。热气流出风口8处的温度为120-200摄氏度。热气流流向曲线10如图7所示，本实施例通过对负压值、温度、含氧量等参数的限定，使得本发明所限定的干燥方法的脱水率大大提高；达不到爆炸临界值，不会发生爆炸，车间运行安全；干燥速率高。干燥后的煤的含水量控制较好，物料的颗粒度均匀，有效的保证烘干后产品的质量。本发明的限定使得物料在整个腔体中的干燥时间短，既能够保证高脱水率又不会使物料发生热解(燃烧反应)，物料快速干燥，不会粘黏在腔室壳体上。
优选地，干燥装置的腔体分为由交错设置的挡料板和挡风板分割成的多个腔室，使得热气流与物料在腔室中的走向为S形，质热交换充分，热效率提高。挡料板设置在机壳3底部，挡风板设置在壳体顶部。物料全部随热气流带走，然后通过烟气流向分离器及除尘器收集，最后一个腔室的宽度大于其它腔室的宽度，使得物料流速降低，大部分煤泥从出料端9排出。
表4实施例4褐煤干燥后的数据
干燥速率 600kgH 20/m 3.h
提升热值 2500kcal/kg
脱水率 75％左右
颗粒度 3≤mm
单台每小时处理能力(湿基) 35立方
实施例5
本实施例提供一种干燥长焰煤的方法，参见图1至图3所示，包括以下步骤：用一种气体加热装置(常见的如热风炉)产生热气流(烟气)，将温度为200-1500摄氏度(本实施例为900摄氏度)、含氧量小于10％的热气流从进风口6引入干燥装置的腔体中，出风口8尾端设有引风机(图中未视出)，使干燥装置的腔体产生100-6000Pa(本实施例为4000Pa)的负压，腔体中热气流的流速为8-14m/s(本实施例为10m/s)；干燥装置入料口7的设置位置需要高于扬料齿4顶部，本实施例设置在壳体顶部。如此设置使物料和热气流并流进入腔体，需要特别说明的是，入料口7和进风口6可以如图2所示设置，也可以将进风口6和入料口7同时设置在壳体的一侧，只要物料和热气流能够在被扬料齿4抛洒之前汇集都属于本实施例所说的“物料和热气流并流进入腔体”的方式。腔体的底部设置有旋转装置，旋转装置设置有扬料齿4，旋转装置通过驱动装置1的驱动轴5驱动，旋转装置和驱动装置设置在机架2上，机架2上设置机壳3，旋转装置的转速为50-500转/分钟(本实施例为200转/分钟)，旋转装置上的扬料齿4抛洒物料使得物料弥漫在热气流中，物料在整个腔体中的干燥时间是1-5s(本实施例为3s)； 物料被热气流干燥(质热交换)后随干燥装置排出。热气流出风口8处的温度为120-200摄氏度。热气流流向曲线10如图2所示，本实施例通过对负压值、温度、含氧量等参数的限定，使得本发明所限定的干燥方法的脱水率大大提高；达不到爆炸临界值，不会发生爆炸，车间运行安全；干燥速率高。干燥后的煤的含水量控制较好，物料的颗粒度均匀，有效的保证烘干后产品的质量。本发明的限定使得物料在整个腔体中的干燥时间短，既能够保证高脱水率又不会使物料发生热解(燃烧反应)，物料快速干燥，不会粘黏在腔室壳体上。
优选地，物料通过分布在出料端9、烟气流向分离器及除尘器收集，最后一个腔室的宽度大于其它腔室的宽度，使得物料流速降低，大部分煤泥从出料端9排出。
本实施例的干燥装置也可以如图4所示，干燥装置的腔体分为由挡料板分割成的多个腔室，当物料通过扬料齿解聚抛洒弥漫在腔室内，解聚后的物料随热气流在腔室中干燥(质热交换)后，逐步流向下一个腔室，最后经排料口排出。还可以如图5所示，干燥装置的腔体分为由交错设置的挡料板和挡风板分割成的多个腔室，使得热气流与物料在腔室中的走向为S形，质热交换充分，热效率提高。
表5实施例5长焰煤干燥后的数据
干燥速率 600kgH 20/m 3.h
提升热值 900kcal/kg
脱水率 50％左右
颗粒度 6≤mm
单台每小时处理能力(湿基) 50立方
实施例6
本实施例提供一种干燥不黏煤的方法，参见图1至图3所示，包括以下步骤：用一种气体加热装置(常见的如热风炉)产生热气流(烟气)，将温度为200-1500摄氏度(本实施例为1000摄氏度)、含氧量小于10％的热气流从进风口6引入干燥装置的腔体中，出风口8尾端设有引风机(图中未视出)，使干燥装置的腔体 产生100-6000Pa(本实施例为4000Pa)的负压，腔体中热气流的流速为8-14m/s(本实施例为10m/s)；干燥装置入料口7的设置位置需要高于扬料齿4顶部，本实施例设置在壳体顶部。如此设置使物料和热气流并流进入腔体，需要特别说明的是，入料口7和进风口6可以如图2所示设置，也可以将进风口6和入料口7同时设置在壳体的一侧，只要物料和热气流能够在被扬料齿4抛洒之前汇集都属于本实施例所说的“物料和热气流并流进入腔体”的方式。腔体的底部设置有旋转装置，旋转装置设置有扬料齿4，旋转装置通过驱动装置1的驱动轴5驱动，旋转装置和驱动装置设置在机架2上，机架2上设置机壳3，旋转装置的转速为50-500转/分钟(本实施例为50转/分钟)，旋转装置上的扬料齿4抛洒物料使得物料弥漫在热气流中，物料在整个腔体中的干燥时间是1-20s(本实施例为12s)；物料被热气流干燥(质热交换)后随干燥装置排出。热气流出风口8处的温度为120-200摄氏度。热气流流向曲线10如图2所示，本实施例通过对负压值、温度、含氧量等参数的限定，使得本发明所限定的干燥方法的脱水率大大提高；达不到爆炸临界值，不会发生爆炸，车间运行安全；干燥速率高。干燥后的煤的含水量控制较好，物料的颗粒度均匀，有效的保证烘干后产品的质量。本发明的限定使得物料在整个腔体中的干燥时间短，既能够保证高脱水率又不会使物料发生热解(燃烧反应)，物料快速干燥，不会粘黏在腔室壳体上。
优选地，物料通过分布在出料端9、烟气流向分离器及除尘器收集，最后一个腔室的宽度大于其它腔室的宽度，使得物料流速降低，大部分煤泥从出料端9排出。
本实施例的干燥装置也可以如图4所示，干燥装置的腔体分为由挡料板分割成的多个腔室，当物料通过扬料齿解聚抛洒弥漫在腔室内，解聚后的物料随热气流在腔室中干燥(质热交换)后，逐步流向下一个腔室，最后经排料口排出。还 可以如图5所示，干燥装置的腔体分为由交错设置的挡料板和挡风板分割成的多个腔室，使得热气流与物料在腔室中的走向为S形，质热交换充分，热效率提高。
表6实施例6不黏煤干燥后的数据
干燥速率 600kgH 20/m 3.h
提升热值 1000kcal/kg
脱水率 60％左右
颗粒度 ≤6mm
单台每小时处理能力(湿基) 60立方
实施例7
本实施例提供一种干燥弱黏煤的方法，参见图1至图3所示，包括以下步骤：用一种气体加热装置(常见的如热风炉)产生热气流(烟气)，将温度为200-1500摄氏度(本实施例为1000摄氏度)、含氧量小于10％的热气流从进风口6引入干燥装置的腔体中，出风口8尾端设有引风机(图中未视出)，使干燥装置的腔体产生100-6000Pa(本实施例为4000Pa)的负压，腔体中热气流的流速为8-14m/s(本实施例为8m/s)；干燥装置入料口7的设置位置需要高于扬料齿4顶部，本实施例设置在壳体顶部。如此设置使物料和热气流并流进入腔体，需要特别说明的是，入料口7和进风口6可以如图2所示设置，也可以将进风口6和入料口7同时设置在壳体的一侧，只要物料和热气流能够在被扬料齿4抛洒之前汇集都属于本实施例所说的“物料和热气流并流进入腔体”的方式。腔体的底部设置有旋转装置，旋转装置设置有扬料齿4，旋转装置通过驱动装置1的驱动轴5驱动，旋转装置和驱动装置设置在机架2上，机架2上设置机壳3，旋转装置的转速为50-500转/分钟(本实施例为200转/分钟)，旋转装置上的扬料齿4抛洒物料使得物料弥漫在热气流中，物料在整个腔体中的干燥时间是1-5s(本实施例为3s)；物料被热气流干燥(质热交换)后随干燥装置排出。热气流出风口8处的温度为120-200摄氏度。热气流流向曲线10如图2所示，本实施例通过对负压值、温度、含氧量等参数的限定，使得本发明所限定的干燥方法的脱水率大大提高；达不到 爆炸临界值，不会发生爆炸，车间运行安全；干燥速率高。干燥后的煤的含水量控制较好，物料的颗粒度均匀，有效的保证烘干后产品的质量。本发明的限定使得物料在整个腔体中的干燥时间短，既能够保证高脱水率又不会使物料发生热解(燃烧反应)，物料快速干燥，不会粘黏在腔室壳体上。
优选地，物料通过分布在出料端9、烟气流向分离器及除尘器收集，最后一个腔室的宽度大于其它腔室的宽度，使得物料流速降低，大部分煤泥从出料端9排出。
本实施例的干燥装置也可以如图4所示，干燥装置的腔体分为由挡料板分割成的多个腔室，当物料通过扬料齿解聚抛洒弥漫在腔室内，解聚后的物料随热气流在腔室中干燥(质热交换)后，逐步流向下一个腔室，最后经排料口排出。还可以如图5所示，干燥装置的腔体分为由交错设置的挡料板和挡风板分割成的多个腔室，使得热气流与物料在腔室中的走向为S形，质热交换充分，热效率提高。
表7实施例7弱黏煤干燥后的数据
干燥速率 600kgH 20/m 3.h
提升热值 1000kcal/kg
脱水率 60％左右
颗粒度 ≤10mm
单台每小时处理能力(湿基) 50立方
实施例8
本实施例提供一种干燥气煤的方法，参见图1至图3所示，包括以下步骤：用一种气体加热装置(常见的如热风炉)产生热气流(烟气)，将温度为200-1500摄氏度(本实施例为900摄氏度)、含氧量小于10％的热气流从进风口6引入干燥装置的腔体中，出风口8尾端设有引风机(图中未视出)，使干燥装置的腔体产生100-6000Pa(本实施例为4000Pa)的负压，腔体中热气流的流速为8-14m/s(本实施例为8m/s)；干燥装置入料口7的设置位置需要高于扬料齿4顶部，本实施例设置在壳体顶部。如此设置使物料和热气流并流进入腔体，需要特别说明 的是，入料口7和进风口6可以如图2所示设置，也可以将进风口6和入料口7同时设置在壳体的一侧，只要物料和热气流能够在被扬料齿4抛洒之前汇集都属于本实施例所说的“物料和热气流并流进入腔体”的方式。腔体的底部设置有旋转装置，旋转装置设置有扬料齿4，旋转装置通过驱动装置1的驱动轴5驱动，旋转装置和驱动装置设置在机架2上，机架2上设置机壳3，旋转装置的转速为50-500转/分钟(本实施例为250转/分钟)，旋转装置上的扬料齿4抛洒物料使得物料弥漫在热气流中，物料在整个腔体中的干燥时间是1-5s(本实施例为3s)；物料被热气流干燥(质热交换)后随干燥装置排出。热气流出风口8处的温度为120-200摄氏度。热气流流向曲线10如图2所示，本实施例通过对负压值、温度、含氧量等参数的限定，使得本发明所限定的干燥方法的脱水率大大提高；达不到爆炸临界值，不会发生爆炸，车间运行安全；干燥速率高。干燥后的煤的含水量控制较好，物料的颗粒度均匀，有效的保证烘干后产品的质量。本发明的限定使得物料在整个腔体中的干燥时间短，既能够保证高脱水率又不会使物料发生热解(燃烧反应)，物料快速干燥，不会粘黏在腔室壳体上。
优选地，物料通过分布在出料端9、烟气流向分离器及除尘器收集，最后一个腔室的宽度大于其它腔室的宽度，使得物料流速降低，大部分煤泥从出料端9排出。
本实施例的干燥装置也可以如图4所示，干燥装置的腔体分为由挡料板分割成的多个腔室，当物料通过扬料齿解聚抛洒弥漫在腔室内，解聚后的物料随热气流在腔室中干燥(质热交换)后，逐步流向下一个腔室，最后经排料口排出。还可以如图5所示，干燥装置的腔体分为由交错设置的挡料板和挡风板分割成的多个腔室，使得热气流与物料在腔室中的走向为S形，质热交换充分，热效率提高。
表8实施例8气煤干燥后的数据
干燥速率 600kgH 20/m 3.h
提升热值 900kcal/kg
脱水率 50％左右
颗粒度 ≤10mm
单台每小时处理能力(湿基) 50立方
实施例9
本实施例提供一种干燥瘦煤的方法，参见图1至图3所示，包括以下步骤：用一种气体加热装置(常见的如热风炉)产生热气流(烟气)，将温度为200-1500摄氏度(本实施例为1000摄氏度)、含氧量小于10％的热气流从进风口6引入干燥装置的腔体中，出风口8尾端设有引风机(图中未视出)，使干燥装置的腔体产生100-6000Pa(本实施例为4000Pa)的负压，腔体中热气流的流速为8-14m/s(本实施例为8m/s)；干燥装置入料口7的设置位置需要高于扬料齿4顶部，本实施例设置在壳体顶部。如此设置使物料和热气流并流进入腔体，需要特别说明的是，入料口7和进风口6可以如图2所示设置，也可以将进风口6和入料口7同时设置在壳体的一侧，只要物料和热气流能够在被扬料齿4抛洒之前汇集都属于本实施例所说的“物料和热气流并流进入腔体”的方式。腔体的底部设置有旋转装置，旋转装置设置有扬料齿4，旋转装置通过驱动装置1的驱动轴5驱动，旋转装置和驱动装置设置在机架2上，机架2上设置机壳3，旋转装置的转速为50-500转/分钟(本实施例为180转/分钟)，旋转装置上的扬料齿4抛洒物料使得物料弥漫在热气流中，物料在整个腔体中的干燥时间是1-5s(本实施例为3s)；物料被热气流干燥(质热交换)后随干燥装置排出。热气流出风口8处的温度为120-200摄氏度。热气流流向曲线10如图2所示，本实施例通过对负压值、温度、含氧量等参数的限定，使得本发明所限定的干燥方法的脱水率大大提高；达不到爆炸临界值，不会发生爆炸，车间运行安全；干燥速率高。干燥后的煤的含水量控制较好，物料的颗粒度均匀，有效的保证烘干后产品的质量。本发明的限定使得物料在整个腔体中的干燥时间短，既能够保证高脱水率又不会使物料发生热解 (燃烧反应)，物料快速干燥，不会粘黏在腔室壳体上。
优选地，物料通过分布在出料端9、烟气流向分离器及除尘器收集，最后一个腔室的宽度大于其它腔室的宽度，使得物料流速降低，大部分煤泥从出料端9排出。
本实施例的干燥装置也可以如图4所示，干燥装置的腔体分为由挡料板分割成的多个腔室，当物料通过扬料齿解聚抛洒弥漫在腔室内，解聚后的物料随热气流在腔室中干燥(质热交换)后，逐步流向下一个腔室，最后经排料口排出。还可以如图5所示，干燥装置的腔体分为由交错设置的挡料板和挡风板分割成的多个腔室，使得热气流与物料在腔室中的走向为S形，质热交换充分，热效率提高。
表9实施例9瘦煤干燥后的数据
干燥速率 600kgH 20/m 3.h
提升热值 900kcal/kg
脱水率 60％左右
颗粒度 ≤10mm
单台每小时处理能力(湿基) 50立方
实施例10
本实施例提供一种干燥无烟煤的方法，参见图1至图3所示，包括以下步骤：用一种气体加热装置(常见的如热风炉)产生热气流(烟气)，将温度为200-1500摄氏度(本实施例为800摄氏度)、含氧量小于10％的热气流从进风口6引入干燥装置的腔体中，出风口8尾端设有引风机(图中未视出)，使干燥装置的腔体产生100-6000Pa(本实施例为4000Pa)的负压，腔体中热气流的流速为8-14m/s(本实施例为8m/s)；干燥装置入料口7的设置位置需要高于扬料齿4顶部，本实施例设置在壳体顶部。如此设置使物料和热气流并流进入腔体，需要特别说明的是，入料口7和进风口6可以如图2所示设置，也可以将进风口6和入料口7同时设置在壳体的一侧，只要物料和热气流能够在被扬料齿4抛洒之前汇集都属于本实施例所说的“物料和热气流并流进入腔体”的方式。腔体的底部设置有旋转 装置，旋转装置设置有扬料齿4，旋转装置通过驱动装置1的驱动轴5驱动，旋转装置和驱动装置设置在机架2上，机架2上设置机壳3，旋转装置的转速为50-500转/分钟(本实施例为200转/分钟)，旋转装置上的扬料齿4抛洒物料使得物料弥漫在热气流中，物料在整个腔体中的干燥时间是1-5s(本实施例为2s)；物料被热气流干燥(质热交换)后随干燥装置排出。热气流出风口8处的温度为120-200摄氏度。热气流流向曲线10如图2所示，本实施例通过对负压值、温度、含氧量等参数的限定，使得本发明所限定的干燥方法的脱水率大大提高；达不到爆炸临界值，不会发生爆炸，车间运行安全；干燥速率高。干燥后的煤的含水量控制较好，物料的颗粒度均匀，有效的保证烘干后产品的质量。本发明的限定使得物料在整个腔体中的干燥时间短，既能够保证高脱水率又不会使物料发生热解(燃烧反应)，物料快速干燥，不会粘黏在腔室壳体上。
优选地，物料通过分布在出料端9、烟气流向分离器及除尘器收集，最后一个腔室的宽度大于其它腔室的宽度，使得物料流速降低，大部分煤泥从出料端9排出。
本实施例的干燥装置也可以如图4所示，干燥装置的腔体分为由挡料板分割成的多个腔室，当物料通过扬料齿解聚抛洒弥漫在腔室内，解聚后的物料随热气流在腔室中干燥(质热交换)后，逐步流向下一个腔室，最后经排料口排出。还可以如图5所示，干燥装置的腔体分为由交错设置的挡料板和挡风板分割成的多个腔室，使得热气流与物料在腔室中的走向为S形，质热交换充分，热效率提高。
表10实施例10无烟煤干燥后的数据
干燥速率 600kgH 20/m 3.h
提升热值 1000kcal/kg
脱水率 70％左右
颗粒度 ≤10mm
单台每小时处理能力(湿基) 60立方
实施例11
本实施例提供一种干燥城市污泥的方法，参见图1至图3所示，包括以下步骤：用一种气体加热装置(常见的如热风炉)产生热气流(烟气)，将温度为900-1500摄氏度(本实施例为1000摄氏度)、含氧量小于10％的热气流从进风口6引入干燥装置的腔体中，出风口8尾端设有引风机(图中未视出)，使干燥装置的腔体产生100-6000Pa(本实施例为4000Pa)的负压，腔体中热气流的流速为8-14m/s(本实施例为8m/s)；干燥装置入料口7的设置位置需要高于扬料齿4顶部，本实施例设置在壳体顶部。如此设置使物料和热气流并流进入腔体，需要特别说明的是，入料口7和进风口6可以如图2所示设置，也可以将进风口6和入料口7同时设置在壳体的一侧，只要物料和热气流能够在被扬料齿4抛洒之前汇集都属于本实施例所说的“物料和热气流并流进入腔体”的方式。腔体的底部设置有旋转装置，旋转装置设置有扬料齿4，旋转装置通过驱动装置1的驱动轴5驱动，旋转装置和驱动装置设置在机架2上，机架2上设置机壳3，旋转装置的转速为50-500转/分钟(本实施例为200转/分钟)，旋转装置上的扬料齿4抛洒物料使得物料弥漫在热气流中，物料在整个腔体中的干燥时间是1-5s(本实施例为3s)；物料被热气流干燥(质热交换)后随干燥装置排出。热气流出风口8处的温度为120-200摄氏度。热气流流向曲线10如图2所示，本实施例通过对负压值、温度、含氧量等参数的限定，使得本发明所限定的干燥方法的脱水率大大提高；达不到爆炸临界值，不会发生爆炸，车间运行安全；干燥速率高。干燥后的煤的含水量控制较好，物料的颗粒度均匀，有效的保证烘干后产品的质量。本发明的限定使得物料在整个腔体中的干燥时间短，既能够保证高脱水率又不会使物料发生热解(燃烧反应)，物料快速干燥，不会粘黏在腔室壳体上。
优选地，物料通过分布在出料端9、烟气流向分离器及除尘器收集，最后一个腔室的宽度大于其它腔室的宽度，使得物料流速降低，大部分煤泥从出料端9排出。
本实施例的干燥装置也可以如图4所示，干燥装置的腔体分为由挡料板分割成的多个腔室，当物料通过扬料齿解聚抛洒弥漫在腔室内，解聚后的物料随热气流在腔室中干燥(质热交换)后，逐步流向下一个腔室，最后经排料口排出。还可以如图5所示，干燥装置的腔体分为由交错设置的挡料板和挡风板分割成的多个腔室，使得热气流与物料在腔室中的走向为S形，质热交换充分，热效率提高。
表11实施例11城市污泥干燥后的数据
干燥速率 600kgH 20/m 3.h
脱水率 80％左右
颗粒度 ≤10mm
单台每小时处理能力(湿基) 30立方
实施例12
本实施例提供一种干燥有色金属尾矿的方法，参见图1至图3所示，包括以下步骤：用一种气体加热装置(常见的如热风炉)产生热气流(烟气)，将温度为200-1500摄氏度，优选700-1500摄氏度(本实施例为1100摄氏度)、含氧量小于10％的热气流从进风口6引入干燥装置的腔体中，出风口8尾端设有引风机(图中未视出)，使干燥装置的腔体产生100-6000Pa(本实施例为4000Pa)的负压，腔体中热气流的流速为8-14m/s(本实施例为8m/s)；干燥装置入料口7的设置位置需要高于扬料齿4顶部，本实施例设置在壳体顶部。如此设置使物料和热气流并流进入腔体，需要特别说明的是，入料口7和进风口6可以如图2所示设置，也可以将进风口6和入料口7同时设置在壳体的一侧，只要物料和热气流能够在被扬料齿4抛洒之前汇集都属于本实施例所说的“物料和热气流并流进入腔体”的方式。腔体的底部设置有旋转装置，旋转装置设置有扬料齿4，旋转装置通 过驱动装置1的驱动轴5驱动，旋转装置和驱动装置设置在机架2上，机架2上设置机壳3，旋转装置的转速为50-500转/分钟(本实施例为200转/分钟)，旋转装置上的扬料齿4抛洒物料使得物料弥漫在热气流中，物料在整个腔体中的干燥时间是1-5s(本实施例为3s)；物料被热气流干燥(质热交换)后随干燥装置排出。热气流出风口8处的温度为120-200摄氏度。热气流流向曲线10如图2所示，本实施例通过对负压值、温度、含氧量等参数的限定，使得本发明所限定的干燥方法的脱水率大大提高；达不到爆炸临界值，不会发生爆炸，车间运行安全；干燥速率高。干燥后的煤的含水量控制较好，物料的颗粒度均匀，有效的保证烘干后产品的质量。本发明的限定使得物料在整个腔体中的干燥时间短，既能够保证高脱水率又不会使物料发生热解(燃烧反应)，物料快速干燥，不会粘黏在腔室壳体上。
优选地，物料通过分布在出料端9、烟气流向分离器及除尘器收集，最后一个腔室的宽度大于其它腔室的宽度，使得物料流速降低，大部分煤泥从出料端9排出。
本实施例的干燥装置也可以如图4所示，干燥装置的腔体分为由挡料板分割成的多个腔室，当物料通过扬料齿解聚抛洒弥漫在腔室内，解聚后的物料随热气流在腔室中干燥(质热交换)后，逐步流向下一个腔室，最后经排料口排出。还可以如图5所示，干燥装置的腔体分为由交错设置的挡料板和挡风板分割成的多个腔室，使得热气流与物料在腔室中的走向为S形，质热交换充分，热效率提高。
表12实施例12有色金属尾矿干燥后的数据
干燥速率 600kgH 20/m 3.h
脱水率 80％左右
颗粒度 6≤mm
单台每小时处理能力(湿基) 30立方
实施例13至实施例28
下述实施例仅列出与上述实施例(以实施例1为例)的差别部分，为了专利文本的简洁性，只用表格的方式列出有差别的参数，本领域技术人员结合上述实施例(以实施例1为例)和以下公开的内容，完全能够实现该些实施例的技术方案。差别如下所示：
表13实施例13至实施例28所限定的参数
Figure PCTCN2017120078-appb-000001
低阶煤是褐煤、长焰煤、不黏煤、弱黏煤、高炉喷吹煤、气煤、气肥煤、贫瘦煤、瘦煤、肥煤、无烟煤中的任一种。经过试验，上述实施例的干燥效果同样优异，本处不再赘述。
最后应当说明的是，以上实施例仅用以说明本发明的技术方案，而非对本发明保护范围的限制，尽管参照较佳实施例对本发明作了详细地说明，本领域的普通技术人员应当理解，可以对本发明的技术方案进行修改或者等同替换，而不脱离本发明技术方案的实质和范围。

Claims (10)

  1. 一种物料的干燥方法，其特征在于：包括以下步骤：将温度为200-1500摄氏度、含氧量小于12％的热气流从进风口引入干燥装置的腔体中，出风口尾端设有引风机，使干燥装置的腔体产生100-6000Pa的负压，腔体中热气流的流速为2-24m/s；腔体的底部设置有旋转装置，干燥装置入料口的设置位置高于旋转装置上的扬料齿的顶部，旋转装置的转速为50-500转/分钟，物料和热气流并流进入腔体，扬料齿破碎并将物料抛洒弥漫在热气流中，物料在整个腔体中的干燥时间是1-20s；物料被热气流干燥后从干燥装置排出。
  2. 根据权利要求1所述的一种物料的干燥方法，其特征在于：干燥装置的腔体分为由挡料板分割成的多个腔室，物料随热气流在腔室中干燥后，逐步流向下一个腔室，最后经排料口排出。
  3. 根据权利要求1所述的一种物料的干燥方法，其特征在于：干燥装置的腔体分为由交错设置的挡料板和挡风板分割成的多个腔室，使得热气流与物料在腔室中的走向为S形。
  4. 根据权利要求3所述的一种物料的干燥方法，其特征在于：最后一个腔室的宽度大于其它腔室的宽度，使得物料流速降低。
  5. 根据权利要求4所述的一种物料的干燥方法，其特征在于：物料通过出料端、烟气流向分离器及除尘器收集。
  6. 根据权利要求1-5任一项所述的一种物料的干燥方法，其特征在于：热气流出风口处的温度为60-200摄氏度。
  7. 根据权利要求1-6任一项所述的一种物料的干燥方法，其特征在于：物料干燥后的颗粒度为0.01-15mm。
  8. 根据权利要求1-5任一项所述的一种物料的干燥方法，其特征在于：进风口热气流的温度为800-1100摄氏度、含氧量小于8％，干燥装置的负压为 900-6000Pa，腔体中热气流的流速为8-18m/s；旋转装置的转速为100-400转/分钟，物料在整个腔体中的干燥时间是1-5s。
  9. 根据权利要求1-5任一项所述的一种物料的干燥方法，其特征在于：进风口热气流的温度为600-900摄氏度、含氧量小于11％，干燥装置的负压为900-6000Pa，腔体中热气流的流速为8-14m/s；旋转装置的转速为100-400转/分钟，物料在整个腔体中的干燥时间是1-5s。
  10. 根据权利要求1-5任一项所述的一种物料的干燥方法，其特征在于：所述干燥方法用于干燥褐煤、长焰煤、不黏煤、弱黏煤、高炉喷吹煤、气煤、气肥煤、贫瘦煤、瘦煤、肥煤、无烟煤、煤泥、城市污泥或者有色金属尾矿。
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