CN101818092B - Integrated fluidized bed mild-gasification lignite upgrading system and technology - Google Patents

Abstract

Integral fluidized bed mild gasification lignite upgrading system and process, using high temperature air generated by low-value gas incinerators to pre-dry lignite to remove part of the moisture in lignite; then lignite is sent to the fluidized bed for light High-degree gasification lignite upgrading reactor, lignite undergoes partial gasification, dry distillation and combustion reactions in the fluidized bed mild gasification lignite upgrading reactor, part of the heat generated by the reaction is used to maintain the temperature in the reactor, and part of it is used to For the removal of lignite moisture, the lignite upgraded by the fluidized bed light gasification lignite upgrading reactor is sent to the finished product cooler to cool and then sent to the finished product warehouse, and the low-value gas generated is sent to the subsequent low-value gas incinerator Incineration utilization; it has the characteristics of simple process, convenient operation, low energy consumption, less pollutant discharge and no waste water discharge.

Description

Integrated fluidized bed mild gasification lignite upgrading system and process

technical field

The invention relates to a material drying and upgrading system and process, in particular to an integral fluidized bed mild gasification lignite upgrading system and process.

Background technique

Lignite is a common coal with a low degree of coalification. It is the initial product of organic biorock after peat deposition after dehydration and compaction. It is named for its brown or dark brown appearance. Lignite is mostly dull, with a true density of 1.10-1.40g/cm ³ , a moisture content of 30-60%, high volatile content, low ignition point, non-bonding, easy weathering and deterioration, containing native humic acid, and high oxygen content , strong chemical reactivity, poor thermal stability, is a flammable fossil fuel. Primary humic acid is the main characteristic component that distinguishes lignite from other coals.

China's proven lignite reserves have reached 130 billion tons, accounting for about 13% of the country's total coal reserves. China's lignite resources are mainly distributed in Yunnan Province in the east and southwest of the Inner Mongolia Autonomous Region.

From the perspective of the formation age of lignite in China, the Mesozoic Jurassic (about 205 million years ago to 144 million years ago) lignite reserves accounted for the largest proportion, accounting for about 4/5 of the national lignite reserves, mainly distributed in eastern Inner Mongolia and northeast China The three provinces are closely connected to the East Tri-Alliance area. Cenozoic Tertiary (65 million years ago to 1.8 million years ago) lignite resources account for about 1/5 of the national lignite reserves, mainly distributed in Yunnan Province. In addition, Sichuan, Guangdong, Guangxi, Hainan and other provinces also have a small amount of Tertiary lignite. The Tertiary lignite in East China is mainly distributed in Shandong Province, and there are also some Tertiary lignite in the three northeastern provinces. In the Jurassic lignite, there are very few early and middle Jurassic lignites, and they are generally Late Jurassic lignite, or old lignite, which are mainly distributed in the Huolinhe Basin in the Hailaer coal-bearing area in the eastern Inner Mongolia Autonomous Region of my country and Sanjiang, Heilongjiang. - Mulinhe coal-bearing area, which is the concentrated area of lignite resources in my country.

The Inner Mongolia Autonomous Region is a province with an absolute majority of lignite reserves in my country, accounting for more than 3/4 of the national lignite resources. Some of the lignite coal fields with the largest reserves in my country are almost concentrated in the eastern part of Inner Mongolia near the border areas of the three northeastern provinces. Among them, coal fields such as Zhalainuoer, Yuanbaoshan, and Pingzhuang were developed earlier, followed by Huolinhe, Yimin, and Dayan coal fields. Coal reserves are in the range of several billion tons to tens of billion tons.

As the world's high-quality coal resources are becoming less and less and mining costs are increasing, many countries have begun or paid more attention to the development of rich lignite resources. Compared with other types of coal, lignite has high oxygen content, large changes in ash content and ash melting point, low density, easy spontaneous combustion, and easy explosion of coal powder. There are many problems in the direct utilization of lignite. The high moisture content in lignite increases the transportation cost of lignite and limits the transportation of lignite from mining areas to users in remote areas. Lignite is a kind of coal that is highly prone to spontaneous combustion, so it will also cause problems of spontaneous combustion and explosion during long-distance transportation.

At present, lignite upgrading technology is in the stage of experimental research and initial application of engineering. While various lignite upgrading technologies have their own advantages, they also have obvious defects. Most of the technical process systems are very complex, lignite upgrading costs are high, the system operation reliability is low, and there is a lot of pollution to the environment. There is still a long way to go before the real large-scale industrial application.

After dehydration and upgrading, the composition and properties of lignite tend to be similar to those of bituminous coal, which will be more conducive to utilization, transportation and storage. There are a large number of units designed to burn bituminous coal in active service in my country. Due to changes in coal sources, fuel supply is tight, and the cost is said to be high. If the fuel made from lignite upgrading can be directly blended and used without major technical transformation of the original boiler unit, lignite resources can be effectively utilized and the utilization value of lignite can be greatly improved, which has very important practical significance and Good economy.

Contents of the invention

In order to overcome the above-mentioned shortcomings of the prior art, the object of the present invention is to provide a system and process for upgrading the quality of lignite by integral fluidized bed light gasification, which has the advantages of simple process, convenient operation, low energy consumption, less water consumption, and can meet the needs of large-scale characteristics of chemical production requirements.

In order to achieve the above object, the technical solution adopted in the present invention is:

The integrated fluidized bed light gasification lignite upgrading system includes a crushing and screening system 1, the material outlet of the crushing and screening system 1, the raw coal bunker 2 of the pre-dryer and the raw coal bunker 20 of the low-value gas incinerator. The outlet end of the raw coal bunker 2 of the pre-dryer is connected with the inlet end of the feeder 3, the outlet end of the feeder 3 is connected with the inlet end of the pre-dryer 4, and the blower The air outlet end of 6 is connected to the air inlet end of the air preheater 5 of the low-value gas incinerator, and the air outlet end of the air preheater 5 of the low-value gas incinerator is connected to the air inlet end of the pre-dryer 4. The air outlet end of the dryer 4 is connected with the inlet end of the cyclone separator 7, the air outlet end of the cyclone separator 7 is connected with the inlet end of the dust collector 8, and the outlet end of the cyclone separator 7 is connected with the semi-finished product warehouse 10. The feed port is connected, the outlet port of the dust collector 8 is connected with the inlet port of the induced draft fan 9 , and the material outlet port of the dust collector 8 is connected with the feed port port of the semi-finished product bin 10 .

In the integrated fluidized bed mild gasification lignite upgrading system, the discharge port of the semi-finished product bin 10 is connected to the feed port of the feeder 11, and the discharge port of the feeder 11 is connected to the fluidized bed light The feed inlet end of the gasification lignite upgrading reactor 12 is connected, and the coarse particle product outlet end of the fluidized bed mild gasification lignite upgrading reactor 12 is connected with the feed port end of the coarse particle product cooler 13 Connected, the outlet end of the coarse particle finished product cooler 13 is connected with the feed port end of the coarse particle finished product bin 14; The flue gas inlet end of the cyclone separator 19 is connected with the low-value gas inlet end of the low-value gas incinerator 22, and the discharge port end of the cyclone separator 19 is connected with the inlet end of the fine particle product cooler 18. The feed port end is connected, and the discharge port end of the fine particle finished product cooler 18 is connected with the feed port end of the fine particle finished product bin 17; The tuyere ends are connected, and the air outlet end of the air preheater 15 of the low-value gas incinerator is connected with the air chamber of the fluidized bed mild gasification lignite upgrading reactor 12 .

In the overall fluidized bed mild gasification lignite upgrading system, the discharge port of the raw coal bunker 20 is connected to the feed port of the feeder 21, and the discharge port of the feeder 21 is connected to the low-value gas incinerator 22 are connected to each other, the flue gas outlet port of the low-value gas incinerator 22 is connected to the inlet port of the cyclone separator 24, and the air outlet port of the cyclone separator 24 is connected to the inlet port of the tail flue 32, The outlet end of tail flue 32 is connected with the inlet end of dust collector 29, the outlet end of dust collector 29 is connected with the inlet end of induced draft fan 30, and the outlet end of induced draft fan 30 is connected with the inlet end of chimney 31; The slag outlet end of the gas incinerator 22 is connected with the inlet end of the slag cooler 25; the air outlet end of the blower 27 is connected with the air inlet end of the air preheater 26 of the low-value gas incinerator 22, and the air preheater The outlet end of 26 is connected with the wind chamber of low-value gas incinerator 22; The air chamber at the bottom of the feeder of the value gas incinerator 22 is connected.

Integral fluidized bed mild gasification lignite upgrading process. After the lignite is crushed into particles smaller than 50mm in size by the crushing and screening system 1, it is transported into the raw coal bunker 2 and the raw coal bunker 20. The lignite is fed from the outlet of the raw coal bunker 2 to The feeder 3 is controlled to enter the pre-dryer 4. After the high-temperature air passes through the pre-dryer 4, the temperature drops below 100°C. After being separated by the cyclone separator 7 at the tail, it is sent to the dust collector 8, and most of the solids are removed by the dust collector 8. After the particles are removed, it is directly emptied by the induced draft fan 9, and the fine powder captured by the cyclone separator 7 and the dust collector 8 is sent to the semi-finished product bin 10; the pre-dried coal in the semi-finished product bin 10 is fed into the fluidized Bed light gasification lignite upgrading reactor 12 for deep upgrading, pre-dried coal in the fluidized bed light gasification lignite upgrading reactor 12 after hot air fluidization, in the fluidized bed light gasification lignite upgrading Slight gasification, combustion, and carbonization reactions occur in the quality reactor 12, and all the moisture in the lignite is released into the flue gas. The temperature of the fluidized bed light gasification lignite upgrading reactor 12 is generated by the chemical reaction of the lignite. heat to maintain.

After deep upgrading, two kinds of upgraded lignite with different particle sizes will be produced, i.e. coarse-grained finished product and fine-grained finished product, wherein the coarse-grained finished product is discharged from the discharge port at the bottom of the fluidized bed mild gasification lignite upgrading reactor 12. into the coarse particle finished product cooler 13, and after being cooled to a temperature lower than 75°C, it is sent to the coarse particle finished product bin 14; a part of the fine particle finished product carried by the flue gas is separated by the cyclone separator 19, most of which are separated and separated by the cyclone The discharge port at the bottom of the device 19 is discharged into the fine particle finished product cooler 18, and after being cooled to a temperature lower than 75° C., it is sent into the fine particle finished product bin 17.

The low-value gas discharged from the fluidized bed mild gasification lignite upgrading reactor 12 is sent to the low-value gas incinerator 22 for incineration after the cyclone separator 19 removes most of the coal powder; the low-value gas incinerator 22 is a furnace The adiabatic circulating fluidized bed boiler realizes the full combustion of low-value gas and reduces the emission of pollutants (SO ₂ ) by supplementary combustion of part of solid fuel and adding limestone; the high-temperature flue gas generated by the low-value combustion incinerator 22 is arranged in the The air preheaters 5, 15, 26 in the tail flue 32 are cooled by heat exchange and discharged by the dust collector 29, and then sent to the chimney 31 by the induced draft fan 30 to be emptied; the cold wind is sent into the air preheaters 5, 15, 26 After heat exchange and temperature rise, it is sent to the pre-dryer 4, the fluidized bed mild gasification lignite upgrading reactor 12 and the low-value gas incinerator 22 for utilization.

The fluidization velocity in the pre-dryer 4 is controlled between 1.0-6.0 m/s, and the temperature is controlled between 20-90°C.

The fluidization velocity in the fluidized bed mild gasification lignite upgrading reactor 12 is controlled between 1.0-6.0 m/s, and the temperature of the main reaction zone is controlled between 300°C and 700°C. The water content of the upgraded lignite can be controlled to <10%.

Description of drawings

The accompanying drawing is a schematic diagram of the system structure of the present invention.

Detailed ways

The structural principles and process principles of the present invention will be further described in detail below in conjunction with the accompanying drawings.

Referring to the accompanying drawings, the integral fluidized bed mild gasification lignite upgrading system of the present invention includes a crushing and screening system 1, the material outlet end of the crushing and screening system 1, the raw coal bunker 2 of the pre-dryer and the low-value gas incinerator The feed port of the raw coal bunker 20 is connected, the discharge port of the raw coal bunker 2 of the pre-dryer is connected with the feed port of the feeder 3, and the discharge port of the feeder 3 is connected with the feed port of the pre-dryer 4. The feed port ends are connected, the air outlet end of the blower 6 is connected with the air inlet end of the low-value gas incinerator air preheater 5, and the air outlet end of the low-value gas incinerator air preheater 5 is connected with the air outlet end of the pre-dryer 4 The air inlet ends are connected, the air outlet of the pre-dryer 4 is connected with the inlet end of the cyclone separator 7, the air outlet end of the cyclone separator 7 is connected with the inlet end of the dust collector 8, and the discharge port of the cyclone separator 7 The outlet end of the dust collector 8 is connected with the inlet end of the induced draft fan 9, and the material outlet end of the dust collector 8 is connected with the feed port end of the semi-finished warehouse 10.

The discharge port end of the semi-finished product warehouse 10 is connected with the feed port end of the feeder 11, and the discharge port end of the feeder machine 11 is connected with the feed port end of the fluidized bed mild gasification lignite upgrading reactor 12. Connected, the coarse particle product outlet end of the fluidized bed mild gasification lignite upgrading reactor 12 is connected with the feed port end of the coarse particle product cooler 13, and the discharge port end of the coarse particle product cooler 13 is connected with the The feed port end of the coarse particle product bin 14 is connected; the flue gas outlet end of the fluidized bed mild gasification lignite upgrading reactor 12 is connected with the flue gas inlet end of the cyclone separator 19, and the outlet end of the cyclone separator 19 The tuyere end is connected with the low-value gas inlet port of the low-value gas incinerator 22, the discharge port end of the cyclone separator 19 is connected with the feed port end of the fine particle finished product cooler 18, and the discharge port end of the fine particle finished product cooler 18 The feed port end is connected to the feed port end of the fine particle finished product bin 17; the air outlet end of the blower 16 is connected to the air inlet end of the low-value gas incinerator air preheater 15, and the low-value gas incinerator air preheater The air outlet end of 15 is connected with the air chamber of the light gasification lignite upgrading reactor 12 of the fluidized bed.

The discharge port end of the raw coal bunker (20) is connected with the feed port end of the feeder 21, and the discharge port end of the feeder 21 is connected with the feed port end of the low-value gas incinerator 22, and the low-value gas The flue gas outlet of the incinerator 22 is connected to the inlet end of the cyclone separator 24, the air outlet end of the cyclone separator 24 is connected to the inlet end of the tail flue 32, and the outlet end of the tail flue 32 is connected to the inlet of the dust collector 29. The outlet end of dust collector 29 is connected with the inlet end of induced draft fan 30, and the outlet end of induced draft fan 30 is connected with the inlet end of chimney 31; the slag outlet end of low-value gas incinerator 22 is connected with slag cooler The inlet end of 25 is connected; the air outlet end of blower 27 is connected with the air inlet end of the air preheater 26 of low value gas incinerator 22, and the air outlet end of air preheater 26 is connected with the air outlet end of low value gas incinerator 22 The air chamber is connected; the discharge port of the limestone system 23 is connected with the inclined pipe of the returner of the low-value gas incinerator 22; connected.

Referring to the accompanying drawings, the integral fluidized bed mild gasification lignite upgrading process of the present invention is: after the lignite is broken into particles less than 50 mm in size through the crushing and screening system 1, it is transported into the raw coal bunker 2 and the raw coal bunker 20, and the lignite is extracted from the raw coal The outlet of bin 2 is controlled by the feeder 3 and enters the pre-dryer 4. After the high-temperature air passes through the pre-dryer 4, the temperature drops below 100°C. After being separated by the cyclone separator 7 at the tail, it is sent to the dust collector 8. After most of the solid particles are removed by the dust collector 8, it is directly emptied by the induced draft fan 9, and the fine powder captured by the cyclone separator 7 and the dust collector 8 is sent into the semi-finished product bin 10;

The pre-dried coal in the semi-finished product bin 10 is fed into the fluidized bed light gasification lignite upgrading reactor 12 through the feeder 11 for deep upgrading, and the pre-dried coal is in the fluidized bed light gasification lignite upgrading reactor 12 After being fluidized by hot air, mild gasification, combustion, and dry distillation reactions occur in the mild gasification lignite upgrading reactor 12 of the fluidized bed, and all the moisture in the lignite is released into the flue gas, and the mild gasification of the fluidized bed The temperature of the gasification lignite upgrading reactor 12 is maintained by the heat generated by the chemical reaction of lignite.

After deep upgrading, two kinds of upgraded lignite with different particle sizes will be produced, i.e. coarse-grained finished product and fine-grained finished product, wherein the coarse-grained finished product is discharged from the discharge port at the bottom of the fluidized bed mild gasification lignite upgrading reactor 12. into the coarse particle finished product cooler 13, and after being cooled to a temperature lower than 75°C, it is sent to the coarse particle finished product bin 14; a part of the fine particle finished product carried by the flue gas is separated by the cyclone separator 19, most of which are separated and separated by the cyclone The discharge port at the bottom of the device 19 is discharged into the fine particle finished product cooler 18, and after being cooled to a temperature lower than 75° C., it is sent into the fine particle finished product bin 17.

The low-value gas discharged from the fluidized bed mild gasification lignite upgrading reactor 12 is sent to the low-value gas incinerator 22 for incineration after the cyclone separator 19 removes most of the coal powder; the low-value gas incinerator 22 is a furnace The adiabatic circulating fluidized bed boiler realizes the full combustion of low-value gas and reduces the emission of pollutants (SO ₂ ) by supplementary combustion of part of solid fuel and adding limestone; the high-temperature flue gas generated by the low-value combustion incinerator 22 is arranged in the The air preheaters 5, 15, 26 in the tail flue 32 are cooled by exchanging heat and go out of the city through the dust collector 29, and then sent to the chimney 31 by the induced draft fan 30 to be emptied; the cold wind is sent into the air preheaters 5, 15, 26 After heat exchange and temperature rise, it is sent to the pre-dryer 4, the fluidized bed mild gasification lignite upgrading reactor 12 and the low-value gas incinerator 22 for utilization.

The fluidization velocity in the pre-dryer 4 is controlled between 1.0-6.0 m/s, and the temperature is controlled between 20-90°C.

The fluidization velocity in the fluidized bed mild gasification lignite upgrading reactor 12 is controlled between 1.0-6.0 m/s, and the temperature of the main reaction zone is controlled between 300°C and 700°C.

The water content of the upgraded lignite can be controlled to <10%.

In the accompanying drawings, 1 is a crushing and screening system; 2 is a raw coal bunker; 3 is a feeder; 4 is a pre-dryer; 5 is an air preheater; 6 is a blower; 7 is a cyclone separator; 8 is a dust collector; 9 is an induced draft fan; 10 is a semi-finished product warehouse; 11 is a feeder; 12 is a fluidized bed light gasification lignite upgrading reactor; 13 is a coarse particle finished product cooler; 14 is a coarse particle finished product warehouse; Heater; 16 is air blower; 17 is fine particle product warehouse; 18 is fine particle product cooler; 19 is cyclone separator; 20 is raw coal bunker; 21 is feeder; 22 is low-value gas incinerator; 23 is limestone 24 is cyclone separator; 25 is slag cooler; 26 is air preheater; 27 is blower; 28 is Roots fan; 29 is dust collector; 30 is induced draft fan; 31 is chimney; 32 is tail flue .

Claims (9)

1. integrated fluidized bed mild-gasification brown coal upgrading system; Comprise a crushing and screening system (1); It is characterized in that; The material outlet end of crushing and screening system (1) links to each other with the feed inlet end of predrying device run coal bin (2) with low value gas-fired incinerator run coal bin (20); The discharge port end of predrying device run coal bin (2) is connected with the feed inlet end of feeding machine (3), and the discharge port end of feeding machine (3) is connected with the feeding mouth end of predrying device (4), and the air opening end of fan (6) is connected with the blast inlet end of low value gas-fired incinerator air preheater (5); The air opening end of low value gas-fired incinerator air preheater (5) is connected with the blast inlet end of predrying device (4); The air opening end of predrying device (4) is connected with the inlet end of cyclonic separator (7), and the air opening end of cyclonic separator (7) is connected with the inlet end of fly-ash separator (8), and the discharge port end of cyclonic separator (7) is connected with the feed inlet end of work in-process storehouse (10); The exit end of fly-ash separator (8) is connected with the inlet end of induced draft fan (9), and the material outlet end of fly-ash separator (8) is connected with the feed inlet end of work in-process storehouse (10).

2. integrated fluidized bed mild-gasification brown coal upgrading as claimed in claim 1 system; It is characterized in that; The discharge port end in work in-process storehouse (10) is connected with the feed inlet end of feeding machine (11); The discharge port end of feeding machine (11) is connected with the feed inlet end of fluidized bed mild-gasification brown coal upgrading reactor drum (12); The coarse particles finished product discharge port end of fluidized bed mild-gasification brown coal upgrading reactor drum (12) is connected with the feed inlet end of coarse particles finished product water cooler (13), and the discharge port end of coarse particles finished product water cooler (13) is connected with the feed inlet end of coarse particles finished bin (14); The smoke outlet of fluidized bed mild-gasification brown coal upgrading reactor drum (12) is connected with the gas approach end of cyclonic separator (19); The air opening end of cyclonic separator (19) is connected with the low value fuel gas inlet end of low value gas-fired incinerator (22); The discharge port end of cyclonic separator (19) is connected with the feeding mouth end of fine particle finished product water cooler (18), and the discharge port end of fine particle finished product water cooler (18) is connected with the feed inlet end of fine particle finished bin (17); The air opening end of fan (16) is connected with the blast inlet end of low value gas-fired incinerator air preheater (15), and the air opening end of low value gas-fired incinerator air preheater (15) is connected with the air compartment of fluidized bed mild-gasification brown coal upgrading reactor drum (12).

3. arrangement fluidized bed mild-gasification upgrading as claimed in claim 1 system; It is characterized in that; The discharge port end of run coal bin (20) is connected with the feed inlet end of feeding machine (21); The discharge port end of feeding machine (21) is connected with the feed inlet end of low value gas-fired incinerator (22); The smoke outlet of low value gas-fired incinerator (22) is connected with the entrance end of cyclonic separator (24), and the air opening end of cyclonic separator (24) is connected with the entrance end of back-end ductwork (32), and the exit end of back-end ductwork (32) is connected with the entrance end of fly-ash separator (29); The exit end of fly-ash separator (29) is connected with the entrance end of induced draft fan (30), and the exit end of induced draft fan (30) is connected with chimney (31) entrance end; The slag notch end of low value gas-fired incinerator (22) is connected with the entrance end of slag cooler (25); The air opening end of fan (27) is connected with the blast inlet end of the air preheater (26) of low value gas-fired incinerator (22), and the air opening end of air preheater (26) is connected with the air compartment of low value gas-fired incinerator (22); The discharge port end of limestone system (23) is connected with the material returning device inclined tube appropriate position of low value gas-fired incinerator (22); The air outlet of roots blower (28) is connected with the material returning device bottom air compartment of low value gas-fired incinerator (22).

4. integrated fluidized bed mild-gasification brown coal process for upgrading as claimed in claim 1; It is characterized in that; Brown coal deliver into run coal bin (2) and run coal bin (20) after being crushed to the particle less than the 50mm granularity through crushing and screening system (1), and brown coal get into predrying device (4) from the discharge port of run coal bin (2) by feeding machine (3) control; High temperature air through predrying device (4) afterwards; Temperature drops to below 100 ℃, after cyclonic separator (7) separation through afterbody, sends into fly-ash separator (8); After fly-ash separator (8) is most of solid removal,, send into work in-process storehouse (10) by the fine powder that cyclonic separator (7) and fly-ash separator (8) capture directly by induced draft fan (9) emptying; Predrying coal in the work in-process storehouse (10) feeds fluidized bed mild-gasification brown coal upgrading reactor drum (12) via feeding machine (11) and carries out degree of depth upgrading; Predrying coal in upgrading reactor drum (12) after the warm air fluidisation; Mild-gasification, burning, dry distillation reactor take place in fluidized bed mild-gasification brown coal upgrading reactor drum (12); Whole moisture in the brown coal are released in the flue gas, and the heat that the chemical reaction that the temperature of fluidized bed mild-gasification brown coal upgrading reactor drum (12) is taken place by brown coal produces is kept;

Through degree of depth upgrading; Can produce the upgrading brown coal of two kinds of different-grain diameters; Be coarse particles finished product and fine particle finished product; Wherein the coarse particles finished product enters coarse particles finished product water cooler (13) by the discharge gate of fluidized bed mild-gasification brown coal upgrading reactor drum (12) bottom, sends into coarse particles finished bin (14) through being cooled to after temperature is lower than 75 ℃; After a part of fine particle finished product that flue gas carries separates via cyclonic separator (19); Major part is separated gets off; Discharge gate by cyclonic separator (19) bottom enters fine particle finished product water cooler (18), sends into fine particle finished bin (17) through being cooled to after temperature is lower than 75 ℃;

Low value combustion gas by fluidized bed mild-gasification brown coal upgrading reactor drum (12) is discharged is sent into burner hearth burning utilization by low value gas-fired incinerator (22) after cyclonic separator (19) is removed most of coal dust; The high-temperature flue gas that low value burning incinerator (22) produces is via being arranged in air preheater (5,15,26) the heat exchange cooling in the back-end ductwork (32) after after fly-ash separator (29) discharge, send into chimney (31) emptying by induced draft fan (30); Cold wind is admitted to delivers to the utilizations of predrying device (4), fluidized bed mild-gasification brown coal upgrading reactor drum (12) and low value gas-fired incinerator (22) after air preheater (5,15,26) heat exchange heats up.

5. integrated fluidized bed mild-gasification brown coal process for upgrading as claimed in claim 4 is characterized in that, the fluidizing velocity in the predrying device (4) is controlled between 1.0～6.0m/s.

6. integrated fluidized bed mild-gasification brown coal process for upgrading as claimed in claim 4 is characterized in that, the temperature in the predrying device (4) is controlled between 20～90 ℃.

7. integrated fluidized bed mild-gasification brown coal process for upgrading as claimed in claim 4 is characterized in that, the fluidizing velocity in the fluidized bed mild-gasification brown coal upgrading reactor drum (12) is controlled between 1.0～6.0m/s.

8. integrated fluidized bed mild-gasification brown coal process for upgrading as claimed in claim 4 is characterized in that, the temperature of fluidized bed mild-gasification brown coal upgrading reactor drum (12) main reaction region is controlled between 300 ℃～700 ℃.

9. integrated fluidized bed mild-gasification brown coal process for upgrading as claimed in claim 4; It is characterized in that; Low value gas-fired incinerator (22) is a burner hearth adiabatic circular fluid bed; Its temperature of combustion is 800～950 ℃, realizes the abundant burning of low value combustion gas and the discharging of reduction pollutent through afterburning solid fuel and interpolation Wingdale.

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