CN108940134B - Continuous reaction device and method for coal tar pitch ball oxidation infusibility - Google Patents

Continuous reaction device and method for coal tar pitch ball oxidation infusibility Download PDF

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CN108940134B
CN108940134B CN201810637418.1A CN201810637418A CN108940134B CN 108940134 B CN108940134 B CN 108940134B CN 201810637418 A CN201810637418 A CN 201810637418A CN 108940134 B CN108940134 B CN 108940134B
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chamber
reaction
air
coal tar
tar pitch
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CN108940134A (en
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刘沁雯
邵应娟
刘雪娇
钟文琪
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Southeast University
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Southeast University
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1872—Details of the fluidised bed reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1809—Controlling processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00548—Flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00938—Flow distribution elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/06—Details of tube reactors containing solid particles
    • B01J2208/065—Heating or cooling the reactor

Abstract

The invention discloses a continuous reaction device and a method for coal tar pitch ball oxidation infusibility, wherein the reaction device comprises a plurality of reaction chambers used for coal tar pitch ball oxidation infusibility reaction from top to bottom, the top of the uppermost reaction chamber is provided with a feed inlet, the bottom of the lowermost reaction chamber is provided with a discharge outlet, the adjacent reaction chambers are communicated through a material sealing chamber, and a moving part used for controlling the falling speed of the coal tar pitch ball and further controlling the retention time of the coal tar pitch ball in the reaction chamber is arranged in the material sealing chamber. The arrangement mode of the reaction device of the invention realizes the continuous operation of the coal tar pitch oxidation non-melting process, accurately controls the material retention time in different stages of the reaction process, and the circulating temperature control air supply unit can realize the step-by-step temperature rise/constant temperature air supply, and the coal tar pitch balls are in cross flow contact with the air medium, so that the mechanical efficiency and the thermal efficiency are high, the oxidation time is obviously shortened, the damage rate of the coal tar pitch balls is greatly reduced, and the energy-saving effect is good.

Description

Continuous reaction device and method for coal tar pitch ball oxidation infusibility
Technical Field
The invention relates to a reaction device and a method, in particular to a continuous reaction device and a method for coal tar pitch ball oxidation infusibility.
Background
The spherical activated carbon is a representative porous adsorption material, has excellent performances of highly developed pore structure, good fluidity, high mechanical strength, controllable pore size distribution, high adsorption and desorption speed, uniform filling density and the like, is widely applied to the fields of petrochemical industry, medicine, environmental management and the like, and is also widely applied to the fields of national defense and military industry, civil high technology and the like.
At present, the processing method of coal tar is mainly separation and purification, and the utilization of coal pitch accounting for more than 55 percent of the weight of the coal tar is limited to the production of modified pitch and carbon black with low added value. If the coal pitch can be used as a raw material for producing the spherical activated carbon with high added value, a new way can be provided for the high added value utilization of the coal pitch, the urgent need of high-quality activated carbon can be met, and the method has important significance for developing the modern coal chemical industry and the like taking coal coking as a source.
The most critical step in the process of preparing the spherical activated carbon by the coal tar pitch balls is an oxidation non-melting process, the process comprises a long air heating process, only intermittent feeding and secondary production in batches can be performed in the production process, continuous operation cannot be realized, product performances of different batches possibly have differences, the whole reaction process consumes long time and consumes much energy, and the subsequent preparation process and the final product performance are seriously influenced.
Disclosure of Invention
The purpose of the invention is as follows: the first purpose of the invention is to provide a reaction device which can improve the oxidation efficiency and realize the continuous operation of the coal tar pitch ball oxidation non-melting process; the second purpose of the invention is to provide a reaction method of the reaction device.
The technical scheme is as follows: the continuous reaction device for coal tar pitch ball oxidation infusibility comprises a plurality of reaction chambers used for coal tar pitch ball oxidation infusibility reaction from top to bottom, wherein the top of the uppermost reaction chamber is provided with a feed inlet, the bottom of the lowermost reaction chamber is provided with a discharge outlet, the adjacent reaction chambers are communicated through a material sealing chamber, and a moving part used for controlling the falling speed of the coal tar pitch ball and further controlling the retention time of the coal tar pitch ball in the reaction chamber is arranged in the material sealing chamber.
Preferably, the moving part is a conveyor belt or a rolling ball.
The material sealing cavity is an equal-diameter cavity which is equal to the diameter of the adjacent reaction cavity or a variable-diameter cavity which is different from the diameter of the adjacent reaction cavity. When the material sealing cavity is a diameter-variable cavity, at least two rows of rolling balls are arranged in the material sealing cavity from top to bottom, so that a coal pitch ball inclined falling channel is formed, and the coal pitch ball passes through the gap between the rollers from the previous reaction cavity to the next reaction cavity through the material sealing cavity. Furthermore, a guide plate is arranged between the upper rolling ball and the lower rolling ball, so that the materials are uniformly distributed in the falling process, and the materials are prevented from being stacked.
The reaction chamber is provided with a circulating temperature control air supply unit; the arrangement mode is preferably transverse arrangement, and the same reaction chamber can be provided with a plurality of circulating temperature control air supply units side by side in a transverse arrangement mode.
The circulating temperature control unit comprises an air inlet pipe connected with one side of the reaction chamber and an air outlet pipe connected with the other side of the reaction chamber, wherein the air outlet pipe is divided into two branches, one branch is connected with the waste gas treatment system, and the other branch is returned to be connected into the air inlet pipe. The circulating temperature control air supply unit adopts a circulating mode that part of fresh air and return air are mixed and then are sent into the reaction chamber, so that the oxygen content consumed in the oxidation process in the reaction chamber is supplemented, and meanwhile, the energy is saved through heat recovery.
One side of the reaction chamber is connected with an air chamber, and an air inlet pipe is connected with the air chamber. Preferably, the air chamber is internally provided with a flow dispersion shutter, air enters the air chamber through the air inlet pipe, the air field flow is uniformly distributed through the flow dispersion shutter in the air chamber, and then the air is blown out of the air chamber and enters the reaction chamber to carry out oxidation non-melting treatment on the coal tar pitch balls.
The air inlet pipe is provided with an air blower, a gas preheater, a pressure gauge, a thermometer, a flowmeter and a valve; a return air fan, an air filter and a check valve are arranged on a branch connected to the air inlet pipe.
The invention relates to a reaction method of a coal pitch ball oxidation non-melting continuous reaction device, wherein coal pitch balls enter from a feed inlet of the uppermost reaction chamber, enter a sealing chamber after undergoing oxidation non-melting reaction in the reaction chamber, enter the next reaction chamber at a certain speed under the control of a moving part of the sealing chamber to continue reaction, and are finally discharged from a discharge outlet of the lowermost reaction chamber.
Has the advantages that: compared with the prior art, the invention has the following remarkable advantages: (1) according to the invention, the reaction chamber and the material sealing chamber are arranged at intervals up and down, so that the continuous operation of the coal tar pitch oxidation non-melting process is realized, and the production benefit is obviously improved; (2) according to the characteristics and requirements of each actual oxidation process, the movement speed of the moving part in the material sealing cavity is flexibly adjusted, the material retention time of different stages of the coal pitch ball oxidation infusibility process is accurately controlled, the adjustment elasticity is large, and the application range is wide; (3) the invention arranges the circulating temperature control air supply unit in the reaction chamber to realize the gradual temperature rise/constant temperature air supply, the gas in the chamber flows horizontally in a pushing way, the structure is stable, the coal tar pitch ball is contacted with the air medium in a cross flow way, the coal tar pitch ball approximately flows in a piston way, the violent back mixing is avoided, the abrasion to the surface of the material is small, the mechanical efficiency and the thermal efficiency are high, the energy-saving effect is good, the oxidation time is obviously shortened, and the damage rate of the coal tar pitch ball is greatly reduced; (4) the circulating temperature control air supply unit adopts an air distribution mode that circulating air and air are mixed and then are sent into the cavity, so that the oxygen content consumed in the oxidation process of the small asphalt balls is supplemented, meanwhile, the heat is recovered, and the energy consumption is reduced; (5) the device can be a vertical structure, the occupied area is reduced, and the space is saved.
Drawings
FIG. 1 is a schematic view of the structure of a reaction apparatus according to the present invention;
FIG. 2 is a schematic structural diagram of a circulating temperature-controlled air supply unit;
FIG. 3 is a cross-sectional view A-A of the plenum of FIG. 2;
FIG. 4 is a diagram of the morphology of the oxidized asphalt spheres obtained by the method of the present invention.
Detailed Description
The technical solution of the present invention is further explained with reference to fig. 1-4.
As shown in figure 1, the cross-flow coal tar pitch sphere oxidation infusible continuous reaction device comprises a shell 7, wherein the shell 7 comprises a plurality of reaction chambers 18 from top to bottom, four reaction chambers 18I, III, V and VI are shown in the figure, the coal tar pitch spheres are subjected to oxidation infusible reaction in the reaction chambers 18, wherein the calibers of the reaction chambers 18 can be different, for example, the chamber I can be 0.8-1.2 m long, 0.5-0.9 m wide and 0.9-1.1 m filling height; the length of the chamber III is 1.8-2.2 m, the width of the chamber III is 1.2-1.6 m, and the filling height of the chamber III is 0.9-1.1 m; the length of the chamber V is 2.3-2.7 m, the width is 1.5-1.9 m, the filling height is 0.9-1.1 m, the chamber VI is a diameter-variable chamber, the length of the cross section at the bottommost end is 0.8-1.2 m, the width is 0.7-1.1 m, and the filling height is 0.5-0.9 m.
The adjacent reaction chambers 18 are communicated through material sealing chambers 24, two material sealing chambers 24 II and IV are shown in the figure, the two material sealing chambers 24 are both diameter-variable chambers, for example, the filling height of the chamber II can be 0.3-0.7 m; the filling height of the chamber IV is 0.3-0.7 m. The variable-diameter material sealing chamber 24 can be internally provided with guide plates 10 which are uniformly distributed in the falling process of the material to prevent the material from being accumulated. The material sealing chamber 24 is internally provided with a moving part which is used for controlling the falling speed of the coal tar pitch ball and further controlling the retention time of the coal tar pitch ball in the reaction chamber 18, and the moving part is a roller 6 in the figure.
Six rows of rollers 6 are arranged in the material sealing cavity 24 shown in the figure 1 from top to bottom, the diameter of each roller 6 is 15-25 cm, the gap distance between the rollers 6 is 3-7 cm, the rotating angular speed is 1.0-1.1 rad/min, 0.30-0.40 rad/min, 0.21-0.31 rad/min, 0.16-0.27 rad/min, 0.13-0.23 rad/min and 0.48-0.58 rad/min respectively, the downward moving speed of the material is controlled by controlling the rotating speed of the rollers 6, so that the retention time of the material required in different stages of the oxidation non-melting process of the coal pitch balls is further realized, and the falling time of the coal pitch balls in the cavities I, III, V and VI is 0.8-1.2 h, 3.5-4.5 h, 5.5-6.5 h and 1.8-2.2 h respectively.
The top of the reaction device is provided with a feeder 1 and a feed inlet 2, and coal pitch balls from the feeder 1 continuously enter from the feed inlet 2 at the top of the device and sequentially pass through each reaction chamber 18 from top to bottom under the action of gravity. The bottom of the reaction device is provided with a discharge port, and the coal pitch balls which are subjected to the oxidation non-melting process fall onto the conveyor belt 8 from the discharge port.
According to the invention, a plurality of circulating temperature control air supply units are transversely arranged in parallel in each reaction chamber 18, so that heat transfer in different chambers is reduced. As shown in fig. 2, the circulating temperature control unit includes an air inlet pipe 4 connected to one side of the reaction chamber 18 and an air outlet pipe 5 connected to the other side of the reaction chamber 18, and the air inlet pipe 4 is provided with a blower 12, a gas preheater 13, a pressure gauge 15, a thermometer 16, a flow meter 17 and a valve 14; the air outlet pipe 5 is connected with an induced draft fan 19 and a three-way valve 20 and then is divided into two branches, one branch is provided with a cyclone separator 23, and then the two branches enter a waste gas treatment system; the other branch is provided with a return fan 25, an air filter 21 and a check valve 22, and then returns to the air inlet pipe 4. As shown in figure 3, one side of the reaction chamber 18 is connected with an air chamber 9, an insulating layer 3 is arranged outside the air chamber 9, a flow dispersion shutter 11 is arranged in the air chamber 9, an air inlet pipe 4 is connected with the air chamber 9, the air field flow is uniformly distributed through the flow dispersion shutter 11 in the air chamber 9, and then the air field flow is blown out from the air chamber 9 and enters the reaction chamber 18 for oxidation and non-melting treatment of the coal tar pitch balls.
The circulating temperature control air supply unit adopts a circulating mode that part of fresh air and return air are mixed and then are fed into the reaction chamber 18, so that the oxygen content consumed in the oxidation process in the reaction chamber 18 is supplemented, and meanwhile, the energy is saved through heat recovery. A plurality of circulating temperature control air supply units are arranged in the same reaction chamber 18 side by side, and the parallel arrangement of the air blowers 12 and the induced draft fans 19 in different units reduces the mixed flow phenomenon of air with different temperatures in the same chamber, thereby ensuring the stability of a flow field and a temperature field in the chamber.
Before feeding materials into the reaction device, the circulating temperature control air supply unit works for 5-10 min, so that the temperature field of each chamber in the device is stable, and after the chambers are filled with the materials, the circulating temperature control air supply unit realizes the temperature rise and constant temperature control of air along the way in the coal pitch ball oxidation non-melting treatment process in the process of slowly and vertically moving the coal pitch balls downwards. 7 left side surfaces of the casing of cavity I set up 3 air intakes, and 7 left side surfaces of the casing of cavity III set up 3 air intakes, and 7 left side surfaces of the casing of cavity V set up 3 air intakes, and 7 left side surfaces of the casing of cavity VI set up 2 air intakes, therefore whole reactor sets up 11 grades of air intakes altogether.
For each stage of air inlet, air is introduced by a blower 12, is heated to a set temperature by a gas preheater 13, enters an air chamber 9 from an air inlet on the side surface of the furnace body, is uniformly distributed in an airflow field by a flow dispersing shutter 11 in the air chamber 9, is blown out from the air chamber 9, enters a reaction chamber 18, and flows through a particle layer horizontally and rapidly under the action of an induced draft fan 19 to perform oxidation non-melting treatment on the coal tar pitch balls. An air outlet of the reaction chamber 18 is connected with an inlet of an induced draft fan 19 through a heat insulation pipeline, and an outlet of the induced draft fan 19 is connected with an inlet of a three-way valve 20 through a heat insulation pipeline. One outlet of the three-way valve 20 is connected with the cyclone separator 23 through a pipeline; one outlet is connected with the inlet of the air returning machine 25 through a heat insulation pipeline, and the outlet of the air returning machine 25 is connected with the inlet of the air filter 21 through a heat insulation pipeline. The outlet of the air filter 21 is connected with the inlet of the check valve 22 through a heat preservation pipeline, and the outlet of the check valve 22 is connected with the pipeline between the flowmeter 17 and the valve 14 through a heat preservation pipeline. The air in the reaction chamber 18 is pumped out and then passes through the three-way valve 20, a part of the air is processed by the cyclone 23 and then enters the waste gas processing system, and a part of the air is processed by the air filter 21 and then enters the reaction chamber 18 again.
The falling process of the coal tar pitch balls in the chamber I lasts for t1 time, and the temperature along the way is increased to 130-150 ℃ from room temperature; the falling process of the coal tar pitch balls in the chamber III lasts for t3 time, and the temperature along the way is increased from room temperature to 190-210 ℃; the falling process of the coal tar pitch ball in the chamber V lasts for t5 time, and the temperature along the way is increased from room temperature to 290-310 ℃; and (3) carrying out constant temperature treatment on the coal tar pitch balls in the chamber VI at 290-310 ℃ for t6 time. The left side surface of a shell 7 of the chamber I is provided with three air inlets, and the inlet air temperature is T0, T1 and T2 from top to bottom; the total intake of cavity I is Q11, and the air output is Q12, and the amount of return air is Q13, wherein Q11: q12: q13 is 4-6: 0.6-1.4: 3 to 5. The left side surface of the shell 7 of the chamber III is provided with three air inlets, and the air inlet temperature is T3, T4 and T5 from top to bottom; the total air intake of the chamber III is Q31, the air output is Q32, and the air return rate is Q33, wherein Q31: q32: q33 is 4-6: 0.6-1.4: 3 to 5. The left side surface of a shell 7 of the chamber V is provided with three air inlets, and the inlet air temperature is T6, T7 and T8 from top to bottom; the total air intake of the chamber V is Q51, the air output is Q52, and the air return rate is Q53, wherein Q51: q52: q53 is 4-6: 0.6-1.4: 3 to 5. Two air inlets are formed in the left side surface of the shell 7 of the chamber VI, and the air inlet temperatures are T9; the total air intake of the chamber VI is Q61, the air output is Q62, and the air return rate is Q63, wherein Q61: q62: q63 is 4-6: 0.6-1.4: 3 to 5. Wherein Q11: q31: q51: q61 ═ 1: 1: 1: 1.
for example, the inlet air temperatures of 3 air inlets on the left side surface of the shell 7 of the chamber I are 60 ℃, 100 ℃ and 140 ℃ from top to bottom; the total intake of the chamber I is 16128m3H, air output is 3226m3The return air volume is 12902m3H; the coal tar pitch ball falls in the chamber I for 1h, and the temperature rises to 140 ℃ from room temperature along the way. The air inlet temperatures of 3 air inlets on the left side of a shell 7 of the chamber III are respectively 160 ℃, 180 ℃ and 200 ℃ from top to bottom; the total air intake of the chamber III is 16128m3H, air output is 3226m3The return air volume is 12902m3H; the dropping process of the coal tar pitch balls in the chamber III lasts for 4 hours, and the temperature gradually rises to 200 ℃ along the way. The inlet air temperatures of 3 air inlets on the left side surface of a shell 7 of the chamber V are respectively 240 ℃, 270 ℃ and 300 ℃ from top to bottom; the total intake of the chamber V is 16128m3H, air output is 3226m3The return air volume is 12902m3H; the dropping process of the coal tar pitch ball in the chamber V lasts for 6 hours, and the temperature gradually rises to 300 ℃ along the way. The inlet air temperature of 2 air inlets at the left side of a shell 7 of the chamber VI is 300 ℃; the total intake of the chamber VI is 16128m3H, air output is 3226m3The return air volume is 12902m3H; and (5) carrying out constant temperature treatment on the coal tar pitch balls for 2 hours.
The diameter of the asphalt balls treated by the device and the process is 0.3-0.9 mm, and the production capacity is 0.5 t/h. In the implementation process, coal tar pitch balls with the diameter of 0.3-0.9 mm sequentially fall into chambers I, II, III, IV, V and VI of the reaction device from top to bottom under the action of gravity, the temperature rise and constant temperature control of air along the way in the oxidation infusibility treatment process of the coal tar pitch balls are realized through a circulating temperature control air supply system, the oxidized pitch balls with perfect surface appearance are obtained after the oxidation process, the surface is flat and smooth, melting and cracking are hardly caused, and the pore structure is clear and visible, as shown in figure 4.
Example 1
The length of the chamber I is 0.9m, the width of the chamber I is 0.7m, and the filling height of the chamber I is 1.0 m; the length of the chamber III is 2.0m, the width is 1.4m, and the filling height is 1.0 m; the length of the chamber V is 2.5m, the width is 1.7m, the filling height is 1.0m, the chamber VI is a diameter-variable chamber, the length of the cross section at the bottom end is 1.0m, the width is 0.9m, and the filling height is 0.7 m. The diameter of the rollers 6 is 20cm, the gap distance between the rollers 6 is 5cm, and the rotation angular speed is 1.05rad/min, 0.35rad/min, 0.26rad/min, 0.21rad/min, 0.18rad/min, 0.53rad/min respectively in sequence. The inlet air temperatures of 3 air inlets on the left side surface of a shell 7 of the chamber I are respectively 60 ℃, 100 ℃ and 140 ℃ from top to bottom; the total intake of the chamber I is 16128m3H, air output is 3226m3The return air volume is 12902m3H; the coal tar pitch ball falls in the chamber I for 1h, and the temperature rises to 140 ℃ from room temperature along the way. The air inlet temperatures of 3 air inlets on the left side of a shell 7 of the chamber III are respectively 160 ℃, 180 ℃ and 200 ℃ from top to bottom; the total air intake of the chamber III is 16128m3H, air output is 3226m3The return air volume is 12902m3H; the dropping process of the coal tar pitch balls in the chamber III lasts for 4 hours, and the temperature gradually rises to 200 ℃ along the way. ChamberThe inlet air temperatures of 3 air inlets on the left side surface of a shell 7 of the chamber V are respectively 240 ℃, 270 ℃ and 300 ℃ from top to bottom; the total intake of the chamber V is 16128m3H, air output is 3226m3The return air volume is 12902m3H; the dropping process of the coal tar pitch ball in the chamber V lasts for 6 hours, and the temperature gradually rises to 300 ℃ along the way. The inlet air temperature of 2 air inlets at the left side of a shell 7 of the chamber VI is 300 ℃; the total intake of the chamber VI is 16128m3H, air output is 3226m3The return air volume is 12902m3H; and (5) carrying out constant temperature treatment on the coal tar pitch balls for 2 hours.
The total oxidation time of the asphalt balls is 13 hours, the breakage rate of the product obtained after oxidation non-melting treatment is 0.6 percent, and the recycling heat of the circulating temperature control air supply unit is 13418 MJ.
Example 2
The length of the chamber I is 1.1m, the width of the chamber I is 0.8m, and the filling height of the chamber I is 1.1 m; the length of the chamber III is 2.1m, the width is 1.5m, and the filling height is 0.9 m; the length of the chamber V is 2.4m, the width of the chamber V is 1.6m, the filling height of the chamber V is 1.0m, the chamber VI is a diameter-variable chamber, the length of the cross section at the bottommost end is 1.1m, the width of the chamber is 1.0m, and the filling height of the chamber VI is 0.8 m. The diameter of the rollers 6 is 15cm, the gap distance between the rollers 6 is 6cm, and the rotation angular speed is 1.07rad/min, 0.37rad/min, 0.30rad/min, 0.25rad/min, 0.20rad/min, 0.55rad/min respectively in sequence. The inlet air temperatures of 3 air inlets on the left side surface of a shell 7 of the chamber I are respectively 70 ℃, 110 ℃ and 150 ℃ from top to bottom; the total air inlet volume of the chamber I is 16200m3H, air output of 3300m3H, the return air volume is 12900m3H; the coal tar pitch ball falls in the chamber I for 1.1h, and the temperature rises to 150 ℃ from room temperature along the way. The air inlet temperatures of 3 air inlets on the left side of a shell 7 of the chamber III are respectively 170 ℃, 190 ℃ and 210 ℃ from top to bottom; the total air intake of the chamber III is 16200m3H, air output of 3300m3H, the return air volume is 12900m3H; the dropping process of the coal tar pitch balls in the chamber III lasts for 4.2 hours, and the temperature gradually rises to 210 ℃ along the way. The inlet air temperatures of 3 air inlets on the left side surface of a shell 7 of the chamber V are respectively 250 ℃, 280 ℃ and 300 ℃ from top to bottom; the total air intake of the chamber V is 16200m3H, air output of 3300m3/h，The return air volume is 12900m3H; the dropping process of the coal tar pitch ball in the chamber V lasts for 5.9h, and the temperature gradually rises to 300 ℃ along the way. The inlet air temperature of 2 air inlets at the left side of a shell 7 of the chamber VI is 300 ℃; the total air inlet volume of the chamber VI is 16200m3H, air output of 3300m3H, the return air volume is 12900m3H; and (5) carrying out constant temperature treatment on the coal tar pitch balls for 2.1 h.
The total oxidation time of the asphalt balls is 13.3h, the breakage rate of products obtained after oxidation non-melting treatment is 0.5%, and the recycling heat of the circulating temperature control air supply unit is 13725 MJ.
In the prior art, the oxidation time of the asphalt balls is mostly 25-35 h, and the breakage rate is mostly 8% -12%. Compared with the prior art, the oxidation time of the asphalt ball is obviously shortened by about 50%, the damage rate is reduced by about 6-10%, and nearly 80% of heat is recycled by the circulating temperature control air supply unit.

Claims (7)

1. A continuous reaction device for coal tar pitch ball oxidation infusibility is characterized in that: the device comprises a plurality of reaction chambers used for coal tar pitch ball oxidation non-melting reaction from top to bottom, wherein the top of the uppermost reaction chamber is provided with a feed inlet, the bottom of the lowermost reaction chamber is provided with a discharge outlet, the adjacent reaction chambers are communicated through a material sealing chamber, and a moving part used for controlling the falling speed of the coal tar pitch ball and further controlling the retention time of the coal tar pitch ball in the reaction chamber is arranged in the material sealing chamber; the reaction chamber is provided with a circulating temperature control air supply unit; the circulating temperature control air supply unit comprises an air inlet pipe connected with one side of the reaction chamber and an air outlet pipe connected with the other side of the reaction chamber, the air outlet pipe is divided into two branches, one branch is connected with the waste gas treatment system, and the other branch is returned to be connected into the air inlet pipe; one side of the reaction chamber is connected with an air chamber, and an air inlet pipe is connected with the air chamber.
2. The reactor apparatus of claim 1, wherein: the moving part is a conveying belt or a rolling ball.
3. The reactor apparatus of claim 1, wherein: the material sealing cavity is an equal-diameter cavity which is equal to the diameter of the adjacent reaction cavity or a variable-diameter cavity which is different from the diameter of the adjacent reaction cavity.
4. The reactor apparatus of claim 3, wherein: when the material sealing cavity is a reducing cavity, at least two rows of rolling balls are arranged in the material sealing cavity up and down, so that a coal tar pitch ball inclined falling channel is formed.
5. The reactor apparatus of claim 4, wherein: a guide plate is arranged between the upper rolling ball and the lower rolling ball.
6. The reactor apparatus of claim 1, wherein: the air inlet pipe is provided with an air blower, a gas preheater, a pressure gauge, a thermometer, a flowmeter and a valve; a return air fan, an air filter and a check valve are arranged on a branch connected to the air inlet pipe.
7. A reaction method of the coal tar pitch ball oxidation non-melting continuous reaction device according to claim 1, characterized in that: the coal pitch ball enters from the feed inlet of the uppermost reaction chamber, enters into the sealed chamber after oxidation non-melting reaction in the reaction chamber, enters into the next reaction chamber at a certain speed under the control of the moving part to continue reaction, and is finally discharged from the discharge outlet of the lowermost reaction chamber.
CN201810637418.1A 2018-06-20 2018-06-20 Continuous reaction device and method for coal tar pitch ball oxidation infusibility Active CN108940134B (en)

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JPS5039636B2 (en) * 1973-05-29 1975-12-18
US4657753A (en) * 1985-04-29 1987-04-14 E. I. Du Pont De Nemours And Company Stabilization of pitch fiber
JP2645756B2 (en) * 1989-12-18 1997-08-25 日本カーボン株式会社 Method for producing spherical carbon material
JPH1095982A (en) * 1996-09-26 1998-04-14 Osaka Gas Co Ltd Production of carbonic microsphere
CN1247453C (en) * 2003-07-18 2006-03-29 中国科学院山西煤炭化学研究所 Method for preparing spherical active cardon with base of asphaltum riched in mesopores
CN100402419C (en) * 2006-08-02 2008-07-16 太原理工大学 Method of preparing nano-carbon fiber using coal tar asphalt as raw material
FI121638B (en) * 2009-06-12 2011-02-15 Foster Wheeler Energia Oy The fluidized bed reactor
CN102491320B (en) * 2011-11-28 2013-06-05 福州大学 Pitch-based active carbon with superhigh specific surface area and preparation method thereof
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