CN213895723U

CN213895723U - Tube shell floating assembly type semi-coke oven device

Info

Publication number: CN213895723U
Application number: CN202022558173.9U
Authority: CN
Inventors: 赵祖良; 黄子欣; 赵赶超
Original assignee: Individual
Current assignee: JIANGSU BAOLI HEAVY INDUSTRY TECHNOLOGY CO LTD
Priority date: 2020-11-09
Filing date: 2020-11-09
Publication date: 2021-08-06
Anticipated expiration: 2030-11-09

Abstract

The utility model relates to a tube shell floating assembly type semi-coke oven device, which comprises a coal feeding device, a heat exchanger device and a coke discharging device; a heat exchanger device is arranged below the coal feeding device and comprises an A-type module and a B-type module which are sequentially arranged from top to bottom at intervals, and the A-type module on the uppermost layer is arranged below the coal distribution shunting cone; the A-type module comprises a plurality of U-shaped tubes, a conical diversion cone is arranged above the U-shaped tubes, a fractionation gas outlet channel is arranged below the U-shaped tubes, two sides and the middle of the conical diversion cone are respectively provided with a bearing strip, the lower part of each bearing strip is connected with a bearing block, and the bearing block is connected with the fractionation gas outlet channel; the B-type module and the A-type module are only different in arrangement position of the U-shaped tubes and the diversion cone, and the diversion cone of the B-type module is arranged between the two U-shaped tubes of the upper A-type module. The utility model discloses adopt the U-shaped tubulation in the module, the deformation that makes the tubulation produce after receiving the cold and hot does not have the influence to the module, avoids expend with heat and contract with cold to the influence of whole furnace body.

Description

Tube shell floating assembly type semi-coke oven device

Technical Field

The utility model relates to a coal chemical industry technical field especially relates to a tube shell assembled semi coke oven device that floats.

Background

The energy structure mainly based on coal in China cannot be changed in a long time in the future, low-price coal (brown coal, long flame coal, weakly caking coal and non-caking coal) accounts for about 50 percent of the coal reserves in China (wherein the brown coal accounts for about 13 percent), and the yield accounts for about 30 percent of the total amount at present.

The low-price coal is high in water content and volatile components, and spontaneous combustion is easily generated when the stacking height is more than 2 meters, so that the low-price coal cannot be transported in a long distance and can only be processed near a coal mine, and the processing mode mainly comprises drying, upgrading and fractionating the coal. The low-price coal is dried at a temperature of below 200 ℃, and can be transported for a long distance after certain volatile components and moisture are removed. The quality improvement of the low-price coal is that the coal is heated to the temperature of 500-650 ℃ in a dry distillation device under the condition of isolating the air, so that the moisture, the organic gas and the coal tar in the coal are separated, the coal is changed into semicoke which is commonly called semi-coke, and the low-price coal is efficiently and cleanly utilized. The quality improvement of the low-price coal is carried out in a dry distillation device, and the quality improvement is carried out by internal heating and external heating.

The internal heating type directly heats coal by using combustion flue gas, the coal used by the flue gas to penetrate through a coal bed must be lump coal, pulverized coal must be screened off, the generated coal gas is mixed with the combustion flue gas, so the heat value is low and the utilization rate is not high, most coke quenching methods adopt water to quench the coke, the coke is dried after being discharged, a large amount of waste water and waste gas are generated, and the pollution is serious, thereby restricting the development of the industry.

The low-price coal in China is mainly distributed in northern Shaanxi, Ningxia, Nemeng, Xinjiang and other places in Shaanxi, and the problem is that less than 30 percent of lump coal which can be used for producing semicoke in an internal heating mode is mechanically mined, and more than 70 percent of pulverized coal is efficiently and cleanly utilized. In China, universities, research institutes and production enterprises develop various devices for clean utilization of pulverized coal, such as a heat carrier technology, a fluidized bed technology, an external heating type rotary furnace technology and the like, and a series of problems are caused by mechanical transmission of coal at high temperature in a furnace, such as sealing, abrasion, too much coal dust in coal gas and the like; therefore, it cannot be used for a long period of time and cannot be industrially produced.

In the coke ovens and semi-coke ovens which are normally produced at present, coal is almost not mechanically driven in the coking process, for example, the coke ovens only have coal charging and coke pushing, and the coal is not moved in the coking process; the coal in the semi-coke oven moves downwards under the self gravity of the coal in the coking process, and no external force is needed for the coal movement, so the coal is stable and reliable in the production process, but a plurality of problems which need to be improved exist, such as the problem of smoke leakage caused by insufficient sealing performance, the semi-coke oven main body is made of stainless heat-resistant steel, the furnace body is damaged by the deformation of the steel after expansion with heat and contraction with cold, and the like, and the problems are urgently needed to be solved.

SUMMERY OF THE UTILITY MODEL

An object of the utility model is to overcome above-mentioned not enough, provide a tube shell assembled semi coke oven device that floats, heat, the fractionation of gas, the cooling of semicoke to fine coal, heating, cooling gas walk the tube side, fine coal heating, fractionation gas outlet, semicoke cooling walk the shell side.

The purpose of the utility model is realized like this:

a tube shell floating assembly type semi-coke oven device comprises a coal feeding device, a heat exchanger device and a coke discharging device; the coal feeding device comprises a straight coal hopper and a coal distribution spreader cone, the coal distribution spreader cone is arranged below the straight coal hopper,

a heat exchanger device is arranged below the coal feeding device and comprises an A-type module and a B-type module which are sequentially arranged from top to bottom at intervals, the uppermost A-type module is arranged below the coal distribution shunting cone, and the lowermost B-type module is arranged above the coke discharging device;

the A-type module comprises a plurality of U-shaped tubes, a conical diversion cone is arranged above the U-shaped tubes, a fractionated gas outlet channel is arranged below the U-shaped tubes, two sides and the middle of the conical diversion cone are respectively provided with a bearing strip, the lower part of each bearing strip is connected with a bearing block, each bearing block is connected with the fractionated gas outlet channel, and the diversion cone and the fractionated gas outlet channel are rigidly connected with the bearing strips and the bearing blocks; the B-type module and the A-type module are only different in arrangement position of the U-shaped array tubes and the diversion cone, and the diversion cone of the B-type module is arranged between the two U-shaped array tubes of the upper A-type module; the lower layer opening of the U-shaped tube array is set as a U-shaped tube gas inlet, and the upper layer opening is set as a U-shaped tube gas outlet; a gas connecting container is arranged between the gas outlet of the U-shaped tube array and the gas inlet of the U-shaped tube array above the gas outlet of the U-shaped tube array;

the A-type module and the B-type module are positioned through cross positioning pins, so that the two modules cannot move front and back, left and right and are locked up and down by the self gravity of the modules; the inner seal between the A-type module and the B-type module is sealed by the pulverized coal in the modules, the periphery of the inner seal is sealed by an upper sealing flange and a lower sealing flange, and a sealing strip is arranged between the upper sealing flange and the lower sealing flange.

Furthermore, the front end of the fractionating gas outlet channel is welded and sealed together with one end of the U-shaped tube array, a nitrogen purging port is arranged, the rear end of the fractionating gas outlet channel is connected with a dust settling container, and the other end of the dust settling container is connected with the single-module fractionating gas collecting tube.

Furthermore, 4 cross positioning pins are arranged between the upper and lower A-type modules and the B-type modules, wherein one module is fixedly provided with a positioning pin, and the corresponding position of the other module is provided with an XY-direction long groove; when the positioning pin is inserted, the X direction can move, the Y direction can not move, and the X direction can not move after the positioning pin is inserted; when the temperature difference between the upper module and the lower module is large, the expansion with heat and the contraction with cold in the upper X, Y direction are increased to cause stress, and the cross positioning pin can not be constrained by the expansion with heat and the contraction with cold in the XY direction and can move.

Furthermore, the heat exchanger device is divided into an upper preheating and drying section, a middle fractionation section and a lower cooling section, wherein a U-shaped pipe gas outlet in the uppermost module in the cooling section is connected with a U-shaped pipe gas inlet in the lowermost module in the preheating and drying section through a hot gas channel; a gas outlet of a U-shaped pipe in the uppermost module of the fractionation section is set as a heating and cooling flue gas outlet, and hot flue gas is subjected to heat exchange by coal to obtain cooled flue gas, and then enters an air heat exchanger to preheat air and coal gas of the gas furnace; a U-shaped pipe gas inlet in the lowest module of the fractionating section is set as a heating hot flue gas inlet, so that the entering hot flue gas heats the coal and is cooled by the coal heat exchange and then is discharged from a heating cold flue gas outlet.

Further, the gas inlet of the U-shaped tube of the lowermost B-shaped module is set as a cold gas inlet, and the gas outlet of the U-shaped tube of the uppermost a-shaped module is set as a cold gas outlet.

Further, an outer fixing frame is arranged on the periphery of the heat exchanger device.

Furthermore, the coke discharging device comprises a transmission gear, a coke discharging shunt cone, a coke discharging shaft and a bearing square tube, the coke discharging device is arranged below a fractionation gas outlet channel of the lowest module of the heat exchanger device, the structure of the coke discharging device is similar to that of the A-type module and the B-type module of the heat exchanger device, and only the U-shaped tube array and the fractionation gas outlet channel of the modules are replaced by the bearing square tube for bearing the whole furnace body.

Furthermore, two ends of the bearing square pipe are fixedly connected with the outer fixing frame; be equipped with a burnt spreader cone between two adjacent bearing side pipes, the both sides of going out burnt spreader cone are equipped with a burnt axle respectively, it is driven by drive gear to go out the burnt axle, control out the burnt.

Furthermore, a coke powder storage groove is formed in the coke discharging shaft, and a distance is reserved between the coke discharging shaft and the coke discharging shunting cone and the bearing square pipe on the coke discharging shaft, so that coke flows into the distance.

Further, the interior of the heat exchanger device is coated with a wear-resistant ceramic coating, and the thickness of the coating is 0.1-0.8 mm.

Compared with the prior art, the beneficial effects of the utility model are that:

(1) the utility model discloses a set up the coal distribution spreader-cone in the coaling device below the coal scuttle, during the coaling fine coal adds the coal scuttle, and the coal position is by sensor control, and on the coal flowed the coal distribution spreader-cone, the coal on the spreader-cone realized automatic coaling through the angle of repose natural flow to the heat exchanger device of stacking of fine coal.

(2) The heat exchanger device of the utility model does not need rigid connection, the outer sealing of the modules is sealed by the sealing strips in the sealing flanges on the upper and lower modules, and the inner sealing is sealed by the powder (coal and coke) in each layer of modules; the modules are not rigidly connected and only are positioned in a cross way, so that the modules cannot move front and back and left and right after being assembled; the heating and cooling pipelines in the module adopt U-shaped tubes, so that the tubes are not influenced by the deformation generated after being cooled and heated on the module, and the influence of thermal expansion and cold contraction on the whole furnace body can be avoided.

(3) The heat exchanger device of the utility model is formed by assembling A, B type heat exchange modules, and is combined into an upper preheating and drying section, a middle heating and fractionating section and a lower coke quenching and cooling section according to different heat exchange modes; the preheating drying section is used for preheating the pulverized coal flowing to the fractionating section by reversely exchanging heat of the hot gas from the coke quenching cooling section below through the upward pulverized coal in the U-shaped tube array and the downward pulverized coal outside the U-shaped tube array in the module; in the heating fractionation section, the gas hot flue gas further exchanges heat and heats the preheated pulverized coal going down outside the pipe through a U-shaped tube array in the module, and the hot flue gas going up reversely is discharged outside the furnace for reuse after being cooled; the coke quenching cooling section is characterized in that cold air is introduced into a U-shaped tube array in the lowest module, heat exchange is reversely carried out on hot semicoke flowing down from the fractionation section outside the tube, and the cold air is heated through the heat exchange and then introduced into the upper preheating and drying section; the inner layer and the outer layer of the coal are exchanged when the coal flow exchanges heat in the furnace, thereby improving the heat exchange efficiency and greatly reducing the cost of fuel.

(4) The utility model discloses a U-shaped tubulation in A type and the B type module waits the position and staggers (triangle-shaped in the tubulation heat exchanger is arranged), makes fine coal obtain the replacement from A to B module intermediate position when down, makes rate of heating accelerate and even, has left the space and the passageway of gas fractionation simultaneously, has still avoided the compaction phenomenon of fine coal.

(5) The utility model discloses every U-shaped tubulation below all has a fractionation gas outlet channel, makes fine coal flow through every U-shaped tubulation and heats the back and will fractionate gaseous outside timely access to stove, has avoided the problem that the gas flow rate that the fractionation gas is concentrated in the stove and is discharged and the too big dust content of coal gas that brings of the gas velocity of flow that arouses reaches tar secondary decomposition.

(6) The coke discharging device of the utility model controls the coke discharging speed by the coke discharging shaft, the coke discharging shaft does not move and can not discharge coke, and the shaft rotates to discharge coke quickly.

(7) The utility model can realize production automation, and has the characteristics of energy saving, water saving, less waste water and waste gas generation, controllable semicoke quality, good coal gas and tar quality, less coal dust and the like; the coal does not need mechanical action in the processes of preheating, drying, fractionating into coke, quenching and cooling, and the unstable factors caused by the mechanical action at high temperature are avoided.

Drawings

Fig. 1 is a schematic structural diagram of the present invention.

Fig. 2 is a sectional view taken along line a-a of the present invention.

Fig. 3 is a schematic structural diagram of the coal distribution device of the present invention.

Fig. 4 is a partial enlarged view of fig. 3 at I.

Fig. 5 is a schematic structural diagram of the heat exchange module of the present invention.

Fig. 6 is a schematic structural view of a U-shaped tube array of the present invention.

Fig. 7 is a schematic view of the load-bearing structure of the present invention.

Fig. 8 is a schematic view of the coke discharging device of the present invention.

Fig. 9 is the cross positioning schematic diagram of the upper and lower module pins of the present invention.

Fig. 10 is a schematic view showing a state where pulverized coal of the present invention flows in the furnace body.

Wherein:

the device comprises a straight coal hopper 1, a coal level sensor 1-1, a coal distribution shunt cone 2, an A-shaped module 3, a cold air outlet 4, a B-shaped module 5, a hot air channel 6, a heating and cooling flue gas outlet 7, a heating flue gas inlet 8, an external fixing frame 9, a cold air inlet 10, a coke discharging device 11, a transmission gear 11-1, a coke discharging shunt cone 11-2, a coke discharging shaft 11-3, a bearing square pipe 11-4, a sealing upper flange 12, a sealing lower flange 13, a sealing strip 14, a gas connecting container 15, a U-shaped array pipe 16, a U-shaped pipe gas inlet 16-1, a U-shaped pipe gas outlet 16-2, a dust settling container 17, a single-module fractional gas collecting pipe 18, a fractional gas outlet channel 19, a bearing block 20, a bearing strip 21, a cross positioning pin 23 and a nitrogen purging port 24.

Detailed Description

Example 1:

referring to fig. 1-10, the utility model relates to a tube shell floating assembly type semi-coke oven device, which comprises a coal feeding device, a heat exchanger device and a coke discharging device 11.

The coal feeding device comprises a straight coal hopper 1 and a coal distribution spreader cone 2, wherein the coal distribution spreader cone 2 is arranged below the straight coal hopper 1, and a coal level sensor 1-1 is installed in the straight coal hopper 1.

The coal feeder is characterized in that a heat exchanger device is arranged below the coal feeder and comprises an A-type module 3 and a B-type module 5 which are sequentially arranged from top to bottom at intervals, the A-type module 3 on the uppermost layer is arranged below the coal distribution spreader cone 2, and the B-type module 5 on the lowermost layer is arranged above the coke discharging device 11.

The A-type module 3 comprises 8U-shaped tubes 16, the B-type module 5 comprises 7U-shaped tubes 16, a conical diversion cone is arranged above the U-shaped tubes 16, a fractionation gas outlet channel 19 is arranged below the U-shaped tubes 16, two sides and the middle of the conical diversion cone are respectively provided with a bearing strip 21, the lower part of the bearing strip 21 is connected with a bearing block 20, the bearing block 20 is connected with the fractionation gas outlet channel 19, and the diversion cone and the fractionation gas outlet channel 19 are rigidly connected with the bearing strip 21 and the bearing block 20 to form a rigid module frame.

The B-type module 5 and the A-type module 3 are only different in arrangement position of the U-shaped tubes 16 and the diversion cone, and the diversion cone of the B-type module 5 is arranged between the two U-shaped tubes 16 of the upper A-type module 3.

The lower layer opening of the U-shaped tube array 16 is provided with a U-shaped tube gas inlet 16-1, and the upper layer opening is provided with a U-shaped tube gas outlet 16-2.

And a gas connecting container 15 is arranged between the U-shaped tube gas outlet 16-2 of the U-shaped tube 16 and the U-shaped tube gas inlet 16-1 of the U-shaped tube 16 above, and the gas connecting container 15 collects the gas from the U-shaped tube gas outlets 16-2 on the lower module and distributes the gas to the U-shaped tube gas inlets 16-1 on the upper module.

The front end of the fractionating gas outlet channel 19 is welded and sealed together with one end of the U-shaped tube welded and sealed, a nitrogen purging port 24 is arranged, the rear end of the fractionating gas outlet channel 19 is connected with a dust settling container 17, the other end of the dust settling container 17 is connected with a single-module fractionating gas collecting pipe 18, when the fractionated gas enters the container 17 to be decelerated so that dust is settled, a plurality of fractionated gases on one module are collected into the single-module fractionating gas collecting pipe 18, and a plurality of fractionated gases on the module are collected and then led into a total gas collecting pipe to be cooled by spraying ammonia water.

The dust settling vessel 17 and the single module fractionation gas collecting pipe 18 are provided with heating and heat insulating devices to keep the temperature above the dew point of the internal gas so as to prevent the condensation of water vapor and tar vapor in the gas.

The A-type module 3 and the B-type module 5 are positioned by a cross positioning pin 23, so that the two modules cannot move front and back, left and right and are locked up and down by the gravity of the modules; the inner seal between the A-type module 3 and the B-type module 5 is sealed by the pulverized coal in the modules, the periphery of the inner seal is sealed by an upper sealing flange 12 and a lower sealing flange 13, and a sealing strip 14 is arranged between the upper sealing flange 12 and the lower sealing flange 13.

4 cross positioning pins 23 are arranged between the upper A-type module 3 and the lower B-type module 5, wherein one module is fixedly provided with a positioning pin, and the corresponding position of the other module is provided with an XY-direction long groove; when the positioning pin is inserted, the X direction can move, the Y direction can not move, and the X direction can not move after the positioning pin is inserted; when the temperature difference between the upper module and the lower module is large, the expansion caused by heat and the contraction caused by cold in the upper direction and the lower direction of X, Y is increased to cause stress, and the cross positioning pin 23 can move in the XY direction without being constrained by the expansion caused by heat and cold.

The heat exchanger device is divided into an upper preheating and drying section, a middle fractionation section and a lower cooling section, wherein a U-shaped tube gas outlet 16-2 in the uppermost module in the cooling section is connected with a U-shaped tube gas inlet 16-1 in the lowermost module in the preheating and drying section through a hot gas channel 6; a gas outlet 16-2 of a U-shaped pipe in the uppermost module of the fractionation section is set as a heating and cooling flue gas outlet 7, and hot flue gas is subjected to heat exchange by coal to obtain cooled flue gas, and then enters an air heat exchanger to preheat air and coal gas of the gas furnace; a U-shaped pipe gas inlet 16-1 in the lowest module of the fractionating section is set as a heating flue gas inlet 8, so that the entering hot flue gas heats the coal, and the coal is cooled by heat exchange and then is discharged from a heating cold flue gas outlet 7.

The U-shaped pipe gas inlet 16-1 of the B-shaped module 5 at the lowest layer is set as a cold gas inlet 10, and the U-shaped pipe gas outlet 16-2 of the A-shaped module 3 at the uppermost layer is set as a cold gas outlet 4.

The periphery of the heat exchanger device is provided with an external fixed frame 9 which supports and fixes the furnace body, and the fixing mode adopts cross positioning along with the mode of an upper module and a lower module, so that the furnace body is not influenced by expansion after being heated.

The coke discharging device 11 comprises a transmission gear 11-1, a coke discharging shunt cone 11-2, a coke discharging shaft 11-3 and a bearing square pipe 11-4, the coke discharging device 11 is arranged below a fractionation gas outlet channel 19 of a lowermost module of the heat exchanger device, the structure of the coke discharging device is similar to that of an A-type module 3 and a B-type module 5 of the heat exchanger device, only a U-shaped array pipe 16 and the fractionation gas outlet channel 19 of the modules are replaced by the bearing square pipe 11-4 of the whole bearing furnace body, and two ends of the bearing square pipe 11-4 are fixedly connected with an external fixed frame 9; a coke discharging shunting cone 11-2 is arranged between two adjacent bearing square tubes 11-4, and the downward coke is divided into two parts when the coke moves downward; two sides of the coke discharging shunting cone 11-2 are respectively provided with a coke discharging shaft 11-3, and the coke discharging shafts 11-3 are driven by a transmission gear 11-1 to control coke discharging and non-coke discharging and fast and slow of coke;

a coke powder storage groove is formed in the coke outlet shaft 11-3, a space is reserved between the coke outlet shaft 11-3 and the coke outlet shunt cone 11-2 and the upper bearing square tube 11-4, so that coke flows into the space, and the space is determined when the shaft of the coke is static and the coke in the space is also static; the upward groove of the coke discharging shaft 11-3 is filled with coke powder, when the coke discharging shaft 11-3 rotates, the coke powder stored in the groove falls down, and meanwhile, the coke powder in the space is driven to fall down onto the lower conveying belt by the friction force of the coke discharging shaft 11-3 and the coke.

The yield and the quality of the whole furnace are controlled by the lower shaft, the yield is high when the shaft rotates quickly, the rotating speed of the shaft is about 7 minutes, and the flow rate of the pulverized coal on the shaft is about 40MM per minute.

The heat exchanger device is internally coated with a wear-resistant ceramic coating, the thickness of the coating is 0.3-0.5mm, and the problems of frictional wear, corrosion and the like of a stainless heat-resistant steel furnace body when coal flows are solved.

The working principle is as follows:

the coal hopper is arranged above the shunting cone, and a coal level sensor is arranged in the coal hopper; when coal is added, the pulverized coal is added into a coal hopper, the coal level is controlled by a sensor, the coal flows onto a coal distribution splitter cone, and the coal on the splitter cone naturally flows into a heat exchanger module through a stacking repose angle of the pulverized coal; after the lower coke discharging device discharges coke, the coal on the upper coal flows downwards to destroy the angle of repose of stacking, the coal in the coal hopper is naturally supplemented, and the coal in the coal hopper is automatically supplemented by the coal level sensor.

The heat exchanger device comprises an upper preheating and drying section, a middle fractionation section and a lower cooling section, wherein the upper preheating and drying section, the middle fractionation section and the lower cooling section are formed by a plurality of AB type heat exchange modules; in the preheating and drying section, the coal is preheated and dried by hot gas obtained by heat exchange of the lower cooling section, and the hot gas is changed into cold gas after heat exchange with the coal and then is discharged from the upper part; the middle fractionation section enters the preheating coal flowing into the module from a tube array below the fractionation section through external gas hot gas to exchange heat and heat, so that the coal reaches the required fractionation temperature, the gas after heat exchange still has a certain temperature, the gas can be reused after being discharged from the upper part of the fractionation section, and the air required by the gas boiler is preheated through the heat exchange gas device, so that the utilization of heat energy is maximized; the lower cooling section is used for cooling the hot coke descending from the upper part by cold air entering from the lower tube nest, the obtained hot air enters the preheating and drying section through a pipeline, and the cooled semi-coke is discharged from a coke discharging part. The heat required by the furnace is the heat of evaporation of water in the coal, distillation of coal gas and the heat lost in heat exchange efficiency in quenching cooling and preheating drying, thereby greatly reducing the cost of fuel.

The heat exchange modules A and B consist of a plurality of tubes which are processed into U-shaped tubes by square tubes, a conical flow-dividing cone, a fractional gas outlet channel, a bearing block which bears the weight of the furnace body, a bearing strip and a sealing flange on the periphery outside the module; the conical splitter cone and the fractional gas outlet channel are rigidly connected with the bearing strip and the bearing block to form a rigid module frame; the U-shaped tube arrays are only connected with the bearing strip blocks on one side, and are not restricted by the modules in the modules when the tube arrays are heated or cold deformed; thus, after the modules AB are assembled, a tube shell floating assembly type furnace body is formed. The U-shaped tubes in the module can eliminate most of stress caused by expansion with heat and contraction with cold on the module; the AB module assembly type structure slows down the cold and hot stress of the modules at the front, back, left and right sides, and eliminates the stress caused by the upward thermal expansion deformation of each module after the furnace body is heated. The AB module is formed by staggering the position of a conical fractionating cone due to different arrangement positions of the conical shunting cone, the fractionating gas outlet channel and the U-shaped tube nest, and after the AB module is assembled into a furnace body, when coal in the A module flows into the B module, the coal flows into the B module from the coal in the A module close to the tube nest in the middle, and the middle tube nest is close to the B module, so that the replacement of a coal flowing layer is realized, the heating and cooling are uniform, and the speed is accelerated. Meanwhile, the coal in the whole furnace body flows from the module A to the module B, and the actual flowing situation of the coal is actually in a flowing state in a virtual hopper, so that the whole furnace body can be regarded as being formed by combining single coal hoppers, the coal flows from the previous coal hopper to the next coal hopper, the amount of the coal hopper on the next coal hopper is supplemented, and the coal cannot flow in multiple ways because the flowing state of the coal is the stacking state of the pulverized coal, and the coal distributing device on the coal hopper is a principle; as long as the taper of the conical shunting cone is larger than the stacking repose angle of coal, the bridging phenomenon can not occur.

A pilot furnace for processing 240 tons of pulverized coal X0.6 per day with yield =144 tons of semicoke and producing 5 ten thousand tons of semicoke per year is taken as an example; the module is sized to be 3372 long, 3000 wide and 660 high, with 480MM center to center spacing and 240MM end to end spacing between two rows of tubes in the module, and the volume of coal is 3.34 cubic × 0.8 specific gravity =2.67 tons of coal. The furnace is assembled by 22 modules, wherein 8 heating sections, 6 fractionating sections and 8 cooling sections are arranged on the furnace; coal flowing at 44MM per minute flows through a module 660/44=15 minutes, the coal is preheated by heating for 2 hours, fractionated for 1.5 hours and cooled for 2 hours from the feeding, and 22 modules take 5.5 hours in total; that is, 4 x 2.67=10.68 tons of coal in 4 modules per hour 0.6 yield =6.4 tons of semicoke, and 6.4 x 24=153.6 tons of semicoke yield per day.

During production, the coal feeding device fills the whole furnace body until the coal feeding is automatically stopped, the coke discharging device is started to observe whether the coal smoothly falls down, and the furnace body is closed after normal operation; opening a nitrogen purging port, and closing the furnace after completely replacing air in the furnace; starting a gas furnace, firstly heating coal by hot flue gas at about 300 ℃ from a heating flue gas inlet below a fractionation section, starting a coke discharging device when the temperature of a coal temperature sensor rises, simultaneously gradually increasing the temperature of the gas to 700 ℃, starting a cold air fan, and enabling cold air to enter a cooling section from a cold air inlet below the cooling section; the cold air entering the cooling module is subjected to heat exchange through the U-shaped tubes to gradually cool the descending coke, the ascending cold air is heated, the heated air enters the preheating and drying section through the hot air channel and the U-shaped tube air inlet from the U-shaped tube air outlet, and the entered hot air is discharged from the cold air outlet at the upper part after being subjected to heat exchange and cooling with the coal. Considering that the furnace body can not be heated quickly by expansion with heat and contraction with cold, the heat balance is needed for at least 7-8 hours from the process to normal coke discharging; the changes of coal, gas and coke temperature meters in the furnace are often observed in the middle, the heating and cooling air quantity is adjusted, and the coke discharging speed is adjusted; and detecting the components of the fractional gas and the semicoke in time, and determining process parameters after the components are qualified.

Coal at the lower part of the fractionation section is heated to 600 ℃ to become semicoke, each module descending to the cooling section is subjected to heat exchange and cooling by cold air passing through the U-shaped tubes one by one, and the semicoke is cooled to below 100 ℃ when going out of the coke; cold air enters from an inlet of the cooling section, and the entered cold air completely absorbs the heat released by cooling the semicoke from 600 ℃ to 100 ℃; the temperature of the gas at the outlet after the heat exchange from the normal temperature gas entering from the inlet to the cooling section is determined by the temperature of the gas entering, the flow rate of the cooling gas, the coke discharging speed and the coke discharging temperature, is a variable relation and is generally controlled at 450 ℃; the hot gas after heat exchange in the cooling section enters the preheating and drying section to preheat the coal, the preheating temperature of the finally obtained coal is also in a variable relation, the flow rate of the coal, the flow rate and the temperature of the heating gas are determined by the cooling section below, the preheating temperature of the coal is influenced by the temperature of the coal in summer and the humidity of the coal in winter, and the preheating temperature is generally 300 ℃ below 250 ℃. The coal fractionation section can adjust the coking temperature at 500-650 ℃ according to the quality requirement of the semicoke, and the temperature is controlled by the flue gas flow, the flue gas temperature and the decoking speed. Therefore, the whole production process is mainly and accurately regulated by utilizing the quality, the yield and the heat energy of the semicoke; the full utilization of the heat energy is mainly the reduction of the outlet temperature of the gas of the semicoke and the preheating section; one way of improvement is to add modules per segment.

In the whole furnace body, the temperature of the gas which can be decomposed and used by the coal after being heated is more than 200 ℃, the temperature of the gas in the furnace can be 3 modules below the preheating drying section, 6 modules in the fractionating section and 5 modules above the cooling section, the 14 modules are all separated from the fractionation gas, wherein the amount of the 3 separated gases below the cooling section is less; the gases useful in these 14 modules are passed through 7 fractional gas outlet channels 19 on each module, through 7 dust settling vessels 17 to a single module fractional gas header 18 and together to a gas primary cooling header. The upper 3, the middle 6 and the lower 2 which can normally separate out coal gas are 11 (the lower 3 are not counted), and the number of the fractionation gas outlet channels 19 in the 11 modules is 11 × 7= 77; each channel had a loading area of 0.228 x 0.09=0.02052 square, and 77 were 1.58 square; the furnace distills 10 tons of coal per hour, the coal produces 200 cubes of clean coal gas, the volume of the clean coal gas is 2.6 times under the condition that the temperature of the raw coal gas in the furnace is 330 ℃, then 200 x 2.6=520 cubes are obtained, and the steam which evaporates 80 kg of water in the coal per hour during distillation is 80 x 1.7=136 cubes. The average gas velocity in the outlet channel for the fractionated gas is (520 + 136) × 10 tonnes =6560 cubic/1.58 square/3600 sec =1.15 m/sec, and this velocity is decelerated into the dust settling vessel 17 with a loading surface of 0.228 × 0.25=0.057 square, with a ratio of 0.057/0.02052=2.78 times, and after deceleration 1.15/2.78=0.415 m/sec. This flow rate was sufficient to allow coal dust of 0.05MM diameter to sink, and the settled coal dust flowed back into the furnace coal stream.

The pressure of the coal gas fractionated in the 14 modules is controlled by a coal gas primary cooling gas collecting pipe, generally at 300-500 Pa, which is higher than the pressure of an external sealing belt of the furnace body; in order to prevent gas from communicating inside the gas, the single-module fractionation gas collecting pipes on the remaining 5 modules on the preheating drying section are connected into a container together, the pressure in the container is equal to the gas pressure, and the pressure difference is not more than or less than 50 Pa; the rest 3 modules in the lower cooling section are treated similarly, and if the pressure is not enough, water can be sprayed for pressurization; the pulverized coal in the modules is sealed by itself in such a way that the gas seal in the internal furnace is formed, so that it cannot cross gas.

After assembly, the AB modules are sealed outwards by ceramic ropes with certain elasticity between upper and lower flanges on the modules, the diameter of the ceramic ropes is 15MM, 3 ceramic ropes are arranged, the distance between the two flanges is 12MM, and the ceramic ropes are compacted by the dead weight of the modules; because the pressure of the fractionating gas in the furnace is not high, 3 ceramic ropes form step sealing under the condition of static sealing, so that the leakage is slight.

The coal is fractionated at 600 ℃ in the fractionating section, the coal preheating temperature is 250 ℃, the required heat is 250-. The furnace is used for processing 10 tons of normal temperature pulverized coal per hour, the temperature of the coal in the furnace is less than 9 tons and only 8 tons at multiple points when reaching 250 ℃, and the temperature of the coal in the furnace is about 6 tons after coking when reaching 600 ℃; the heat quantity required by ton coal is different according to the variety, temperature, humidity and fineness of coal.

The distance between two U-shaped tubes in the AB module in the furnace is 240MM for the thickness of the coal flow, and the coal flow on two sides of the B-shaped module is 120 MM; the coal between the two U-shaped tubes in the module is separated by the middle bearing block 20 to form a straight coal bucket with the length of 1320 and the height of 460 and the width of 240 and containing coal, and the coal is divided into two parts by a diversion cone positioned in the middle of the coal flow width of 240MM on the lower module when descending, and the form of the coal distribution device on the upper part of the furnace is the same, so that the coal flow is the relationship that the coal of the previous straight coal bucket is divided into half of the coal in the two lower straight coal buckets. The coal hopper can also be regarded as a virtual straight coal hopper with the distance between the top corners of the two shunting cones on the lower module being more than 480MM and 460MM high and 1320MM long, the two inner sides of the shunting cones are oblique sides of the coal hopper, and thus a virtual rectangular coal hopper with the size of 1320MM long, 480MM wide and 240MM wide coal outlet port below the total height 660 is formed; the coal at the coal outlet of the hopper flows into the lower two hoppers. The influence on the fluidity of the coal flow is mainly determined whether bridging phenomenon exists on the coal flow width of 120MM on the two sides of the B-type module, and after the test, the pulverized coal with the repose angle of 49.4 degrees is stacked below 6MM, and moves downwards at the speed of 20MM per minute without blocking and bridging phenomenon in a coal hopper with the width of 80MM, the length of 500MM and the height of 600 MM.

The coal flow flows from the A module to the B module in the furnace, 30MM coal on two sides of the 240MM coal flow between two U-shaped tubes of the A module is heated, when the coal flow flows to the B module, 30MM hot coal on two sides flows to the middle of the next 240MM coal flow, the 60MM hot coal flow also becomes a heat source in the B module and can thermally diffuse the coal beside, and meanwhile, cold coal in the middle of the 240MM coal flow of the A module flows to the edges of the tubes of the B module to be heated and then flows to the next module to exchange the inside and the outside of the coal flow; the temperature difference between the tubes and the coal is increased, the heat conductivity coefficient of the pulverized coal is improved after the temperature of the internal coal and the external coal is raised, the heat transfer is accelerated, and the heating is uniform.

The above is only a specific application example of the present invention, and does not constitute any limitation to the protection scope of the present invention. All the technical solutions formed by equivalent transformation or equivalent replacement fall within the protection scope of the present invention.

Claims

1. The utility model provides a shell of tube floating assembly formula semi coke oven device which characterized in that: the device comprises a coal feeding device, a heat exchanger device and a coke discharging device; the coal feeding device comprises a straight coal hopper and a coal distribution spreader cone, the coal distribution spreader cone is arranged below the straight coal hopper, a heat exchanger device is arranged below the coal feeding device, the heat exchanger device comprises an A-type module and a B-type module which are sequentially arranged from top to bottom at intervals, the A-type module at the uppermost layer is arranged below the coal distribution spreader cone, and the B-type module at the lowermost layer is arranged above the coke discharging device;

2. The tube shell floating assembly type semi-coke oven device of claim 1, wherein: the front end of the fractionating gas outlet channel is welded and sealed together with one end of the U-shaped tube array, a nitrogen purging port is arranged, the rear end of the fractionating gas outlet channel is connected with a dust settling container, and the other end of the dust settling container is connected with a single-module fractionating gas collecting tube.

3. The tube shell floating assembly type semi-coke oven device of claim 1, wherein: 4 cross positioning pins are arranged between the upper A-type module and the lower B-type module, wherein one module is fixedly provided with a positioning pin, and the corresponding position of the other module is provided with an XY-direction long groove; when the positioning pin is inserted, the X direction can move, the Y direction can not move, and the X direction can not move after the positioning pin is inserted; when the temperature difference between the upper module and the lower module is large, the expansion with heat and the contraction with cold in the upper X, Y direction are increased to cause stress, and the cross positioning pin can not be constrained by the expansion with heat and the contraction with cold in the XY direction and can move.

4. The tube shell floating assembly type semi-coke oven device of claim 1, wherein: the heat exchanger device is divided into an upper preheating and drying section, a middle fractionation section and a lower cooling section, and a U-shaped pipe gas outlet in the uppermost module in the cooling section is connected with a U-shaped pipe gas inlet in the lowermost module in the preheating and drying section through a hot gas channel; a gas outlet of a U-shaped pipe in the uppermost module of the fractionation section is set as a heating and cooling flue gas outlet, and hot flue gas is subjected to heat exchange by coal to obtain cooled flue gas, and then enters an air heat exchanger to preheat air and coal gas of the gas furnace; a U-shaped pipe gas inlet in the lowest module of the fractionating section is set as a heating hot flue gas inlet, so that the entering hot flue gas heats the coal and is cooled by the coal heat exchange and then is discharged from a heating cold flue gas outlet.

5. The tube shell floating assembly type semi-coke oven device of claim 1, wherein: the air inlet of the U-shaped pipe of the B-shaped module at the lowest layer is set as a cold air inlet, and the air outlet of the U-shaped pipe of the A-shaped module at the uppermost layer is set as a cold air outlet.

6. The tube shell floating assembly type semi-coke oven device of claim 1, wherein: and an outer fixed frame is arranged on the periphery of the heat exchanger device.

7. The tube shell floating assembly type semi-coke oven device of claim 1, wherein: the coke discharging device comprises a transmission gear, a coke discharging shunt cone, a coke discharging shaft and a bearing square tube, the coke discharging device is arranged below a fractionation gas outlet channel of the lowermost module of the heat exchanger device, the structure of the coke discharging device is similar to that of an A-type module and a B-type module of the heat exchanger device, and only the U-shaped tube array and the fractionation gas outlet channel of the modules are replaced by the bearing square tube for bearing the whole furnace body.

8. The tube shell floating assembly coke oven plant of claim 7, wherein: two ends of the bearing square tube are fixedly connected with the outer fixing frame; be equipped with a burnt spreader cone between two adjacent bearing side pipes, the both sides of going out burnt spreader cone are equipped with a burnt axle respectively, it is driven by drive gear to go out the burnt axle, control out the burnt.

9. The tube shell floating assembly coke oven plant of claim 8, wherein: the coke discharging shaft is provided with a coke powder storage groove, and a distance is reserved between the coke discharging shaft and the coke discharging shunting cone and the bearing square pipe on the coke discharging shaft, so that coke flows into the distance.

10. The tube shell floating assembly type semi-coke oven device of claim 1, wherein: the interior of the heat exchanger device is coated with a wear-resistant ceramic coating, and the thickness of the coating is 0.1-0.8 mm.