A device and process for coking using waste heat from dry coke quenching

Abstract

The present invention discloses a device and process for coking using the waste heat from dry coke quenching, and belongs to the field of coking technology. It includes: the inner cavity of the furnace body is divided into a dry distillation preheating section, a dry distillation gas collection section, a medium-low temperature dry distillation section and a high temperature dry distillation section from top to bottom; the silo is arranged at the upper end of the furnace body; the control chamber is located below the high temperature dry distillation section of the furnace body; a plurality of carbonization unit furnace pipes are arranged vertically in the inner cavity of the furnace body, and the carbonization unit furnace pipes are connected to the silo and the control chamber; the carbonization unit furnace pipes pass through the dry distillation gas collection box, and the carbonization unit furnace pipes in the dry distillation gas collection box are provided with air outlets. The present invention utilizes eddy current sedimentation dust removal to reduce the erosion and corrosion of each section of the furnace pipe; the inside and outside of the carbonization unit furnace pipe are heated simultaneously, and the high temperature of the circulating flue gas and the oxidative gasification of the smoke dust are fully utilized in sections; the overlapping area of ​​the pyrolysis and dry distillation gas flow direction and the heat transfer direction in time and space is reduced, the secondary cracking reaction of the volatile matter is reduced, and at the same time, a partial coal hydrogenation reaction is achieved.

Description

Technical Field

[0001] The invention relates to the technical field of coking, and in particular to a device and a process for coking using waste heat from dry coke quenching. Background Art

[0002] At present, dry coke quenching is an environmentally friendly, energy-saving and coke quality quenching method in the coking industry. Its biggest advantage is that it can recover the sensible heat of red coke. The sensible heat of red coke out of the coke oven accounts for about 35% to 40% of the energy consumption of the coke oven, which is equivalent to 5% of the energy of coking coal. The use of dry coke quenching can maximize the recovery of this part of heat (about 80% of the sensible heat of red coke can be recovered). In addition, compared with conventional wet coke quenching, the quality of coke after dry quenching is good, and M40 and M10 can be increased by 3% to 8% and 0.3% to 0.8% respectively, which is extremely beneficial for metallurgical blast furnaces to reduce ironmaking costs and increase pig iron production.

[0003] However, compared with wet quenching, dry quenching also has some disadvantages:

[0004] First, as far as the negative pressure system is concerned, the primary dust collector system is located in the negative pressure section of the CDQ system. Due to leakage in this section, a large amount of air enters the system. The oxygen in the air burns with carbon monoxide, hydrogen, methane, coke powder, etc. in the circulating gas, generating a large amount of heat, causing local high temperature, resulting in the fall of castables in the leakage area, shell erosion, weld burn-through, and reduced dust removal efficiency.

[0005] Secondly, the CDQ waste heat boiler system is located in the negative pressure section at the outlet of the primary dust collector of the CDQ system. Due to the furnace building materials, construction quality, coke powder combustion corrosion and flushing in this section, the boiler castables may fall off, and the superheater and evaporator tubes may burst. Due to the above reasons, the coke powder and castables at the tail of the CDQ waste heat boiler will be blocked, and the channel flow will be poor, which will further cause the dust removal efficiency of the secondary dust collector to decrease, and then the fine coke powder will be brought into the circulating fan, causing mechanical wear and difficulty in controlling the air volume, making it difficult for the CDQ system to maintain stable production for a long period of time. Summary of the invention

[0006] In view of the shortcomings of the negative pressure section of the dry coke quenching system in the prior art, the present invention provides a device and process for coking using the waste heat from dry coke quenching, which is suitable for producing carbonized coal, lump coal, iron coke, foundry coke and other products.

[0007] The present invention adopts the following technical solution: a device for coking using waste heat from dry coke quenching, comprising:

[0008] The furnace body, the inner cavity of the furnace body is divided into a dry distillation preheating section, a dry distillation gas collection section, a medium-low temperature dry distillation section and a high temperature dry distillation section from top to bottom; an air inlet is provided on one side of the high temperature dry distillation section, and a return air pipe is connected to one side of the dry distillation preheating section;

[0009] A silo, arranged at the upper end of the furnace body;

[0010] A regulating chamber is located below the high-temperature dry distillation section of the furnace body;

[0011] A plurality of carbonization unit furnace tubes are vertically arranged in the furnace body cavity; the upper ends of the carbonization unit furnace tubes are connected to the silo, and the lower ends of the carbonization unit furnace tubes are connected to the regulating chamber;

[0012] A dry distillation gas collecting box is arranged in the dry distillation gas collecting section of the furnace body cavity and isolated from the furnace body cavity; the carbonization unit furnace pipe passes through the dry distillation gas collecting box, and the carbonization unit furnace pipe in the dry distillation gas collecting box is provided with an air outlet; the dry distillation gas collecting box is connected to a gas collecting pipe that runs through the furnace body.

[0013] The high temperature dry distillation section has a collecting gasification cavity at the lower side, and a V-shaped bottom plate is provided at the connection between the collecting gasification cavity and the high temperature dry distillation section to separate the upper and lower sides of the furnace body, and a coke powder outlet is provided at the lowest position of the V-shaped bottom plate to connect the high temperature dry distillation section and the collecting gasification cavity;

[0014] The lower end of the carbonization unit furnace tube is connected to the collecting gasification chamber, and the lower side of the collecting gasification chamber is communicated with the regulating chamber.

[0015] A plurality of baffles are fixed to the inner cavity of the furnace body; an air vent is arranged between one end of the baffle and the inner wall of the furnace body, and the air vents of adjacent baffles are arranged alternately; a settling port is arranged between one end of the baffle away from the air vent and the inner wall of the furnace body.

[0016] The control chamber is divided into a steam cooling section, a water evaporation preheating section and a coke discharge section from top to bottom; water and preheating gas of a certain temperature are sprayed into the water evaporation preheating section, and the temperature of the high-temperature distillation section is controlled according to the ratio of water and preheating gas.

[0017] A rotary sealing valve is arranged at the lower end of the coke discharge section, and a conveyor belt is arranged below the rotary sealing valve.

[0018] The gas collecting pipe is connected with a washing and cooling device; the air inlet is introduced with the uncooled circulating flue gas from the annular flue of the dry quenching coke oven, and the return air pipe is connected with a flue gas waste heat recovery and processing device.

[0019] A process for coking using waste heat from dry coke quenching, comprising the following steps:

[0020] A. The coking blank is transported to the silo, and then goes down into the furnace tube of the carbonization unit;

[0021] B. The coking embryo material goes down to the dry distillation preheating section, where the temperature rises and dehydration and degassing begins;

[0022] C. The coking raw material goes down to the dry distillation gas collection section; the dry distillation gas collection box provides a certain negative pressure, and the dry distillation gas and the water vapor from the preheating section are mixed and led out of the furnace body through the gas collecting pipe;

[0023] D. The coking material goes down to the medium and low temperature dry distillation section, where coal pyrolysis and dry distillation begin. The dry distillation gas generated rises along the carbonization unit furnace tube and enters the dry distillation gas collection section on the upper side;

[0024] E. The coking raw material goes down to the high-temperature dry distillation section, where the coal is pyrolyzed and dry distilled to form coke or semi-coke. The dry distillation coal gas generated rises along the carbonization unit furnace tube and enters the medium- and low-temperature dry distillation section on the upper side;

[0025] F. The coke or semi-coke descends to the steam cooling section of the regulating chamber, where the steam cools the coke or semi-coke. At the same time, the steam temperature is increased under the action of the coke or semi-coke, and the high-temperature steam rises and enters the high-temperature dry distillation section on the upper side;

[0026] G. The coke or semi-coke descends to the water evaporation preheating section of the regulating chamber, where the coke or semi-coke is cooled by water evaporation, and a certain amount of preheating gas is added to regulate the temperature of the high-temperature dry distillation section, and the generated steam rises and enters the steam cooling section on the upper side;

[0027] H. The coke or semi-coke descends to the coke discharge section of the regulating chamber and is transported out of the furnace body.

[0028] The invention further comprises the following steps: the air inlet is introduced with uncooled circulating flue gas from the annular flue of the dry quenching coke oven, the circulating flue gas temperature being 950°C-1100°C; the circulating flue gas heats the high-temperature dry distillation section, the medium-low temperature dry distillation section, the dry distillation gas collection section and the dry distillation preheating section in sequence from the outside of the carbonization unit furnace tube;

[0029] The steam in the regulating chamber rises along the carbonization unit furnace tube, and the steam heats the high-temperature dry distillation section, the medium-low temperature dry distillation section and the dry distillation coal gas collection section in sequence from the inside of the carbonization unit furnace tube.

[0030] In the step E, when the coke or semi-coke descends to the collecting gasification chamber at the lower part of the high-temperature dry distillation section, the coke powder discharged from the circulating flue gas enters the collecting gasification chamber by its own weight and negative pressure, and partially gasifies with the coke or semi-coke;

[0031] In the step F, the temperature of steam is increased under the action of coke or semi-coke to provide conditions for the gasification reaction, and a certain amount of hydrogen is generated to provide a hydrogen source for subsequent reactions.

[0032] In the step B, the temperature of the coking stock in the dry distillation preheating section is 150-350° C.;

[0033] In the step C, the temperature of the coking stock in the dry distillation gas collection section is 450-500° C.;

[0034] In the step D, the temperature of the coking stock in the medium and low temperature dry distillation section is 500-850° C., and under the action of hydrogen, the coking stock undergoes a certain hydrogenation pyrolysis reaction;

[0035] In the step E, the temperature in the furnace tube of the carbonization unit in the high-temperature dry distillation section is 900-1050°C, and polycondensation pyrolysis occurs; wherein the temperature in the concentrated gasification chamber is 950-1050°C;

[0036] In the step F, the temperature in the steam cooling section is 500-750°C, and the temperature of the coke or semi-coke therein drops to 500-650°C;

[0037] In step G, the temperature of the coke or semi-coke is reduced to 120-150°C.

[0038] The beneficial effects of the present invention are:

[0039] (1) In the furnace body, the CDQ circulating flue gas is blocked by the baffles and collides with the furnace tubes of each carbonization unit, so that the coke dust is settled and removed. The baffle vents are arranged in a staggered manner, and the circulating flue gas rises in each heating section, forming a vortex settling and dust removal effect, which further removes the circulating flue gas. This optimizes the inlet conditions of the CDQ waste heat boiler, thereby protecting the furnace tubes of each section and reducing erosion and corrosion.

[0040] (2) Outside the carbonization unit furnace tube, the circulating flue gas rises in a circuitous manner and is heated in sections from bottom to top. The temperature field of the carbonization unit furnace tube is relatively stable and the heating speed is relatively fast. The high temperature of the CDQ circulating flue gas of 1100-500°C is well utilized in sections.

[0041] In the carbonization unit furnace tube, the coke powder generated by the circulating flue gas falls and gathers, and enters the collecting gasification chamber under the high-temperature dry distillation section, where oxidation and gasification are fully utilized, and oxidation raises the temperature and gasifies and cools down to maintain the optimal dry distillation temperature; at the same time, with the negative pressure rising heating of a small amount of gasification gas in the steam cooling section and water evaporation preheating section below, the carbonization unit furnace tube is heated from the bottom to the top in sections, so that the temperature field inside and outside the carbonization unit furnace tube is relatively stable and the heating speed is relatively fast;

[0042] (3) A small amount of gasification gas at the lower end of the carbonization unit furnace tube rises under negative pressure and is heated, which changes the angle between the pyrolysis and dry distillation gas flow directions and the heat transfer direction, reduces the overlapping area between the two in time and space, reduces the secondary cracking reaction of volatiles, and realizes partial coal hydrogenation reaction, so that more dry distillation gas can be obtained, and coal tar products with better quality can be obtained;

[0043] (4) The furnace body of the present invention is well sealed, with few leakage points, and the furnace tubes of the carbonization unit can be replaced separately, with a low failure rate and convenient maintenance. The problem of the negative pressure section of the existing CDQ system is solved, and hidden dangers are reduced or minimized, ensuring the safe, stable and long-term production of the system. At the same time, relevant coke, molded coke, foundry coke, semi-coke, pyrolysis gas and high-quality tar products can be obtained, and the thermal efficiency of the materials in the CDQ system can be effectively improved, and the investment in the CDQ system can be reduced. The present invention is very suitable for the construction or reconstruction of a CDQ system. BRIEF DESCRIPTION OF THE DRAWINGS

[0044] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0045] Figure 1 The present invention is a schematic structural diagram of a device for coking using waste heat from dry coke quenching.

[0046] Figure 2 for Figure 1 Enlarged view of point A in the middle.

[0047] Figure 3 It is a schematic structural diagram of a washing and cooling device in an embodiment of the present invention.

[0048] Figure 4 It is a schematic structural diagram of the first blank of the present invention.

[0049] Figure 5 for Figure 4 Middle BB view.

[0050] Figure 6 It is a schematic structural diagram of the second blank of the present invention.

[0051] Figure 7 for Figure 6 Center CC view.

[0052] Description of the accompanying drawings: 1. Silo;

[0053] 2. Furnace body; 21. Dry distillation preheating section; 22. Dry distillation coal gas collection section; 23. Medium and low temperature dry distillation section; 24. High temperature dry distillation section; 241. Collecting gasification chamber; 25. Air inlet; 26. Air return pipe; 27. Baffle; 271. Air vent; 272. Settling port; 28. V-shaped bottom plate; 281. Coke powder outlet;

[0054] 3. Control chamber; 31. Steam cooling section; 32. Water evaporation preheating section; 33. Coke removal section;

[0055] 4. Carbonization unit furnace tube;

[0056] 5. Dry distillation gas collection box; 51. Gas collecting pipe;

[0057] 6. Rotary sealing valve;

[0058] 7. Conveyor belt;

[0059] 8. Washing and cooling device; 81. Primary cooler; 82. Recovered coal tar outlet; 83. Cooling and washing oil inlet; 84. Drying distillation coal gas outlet;

[0060] 9. Flue gas waste heat recovery and treatment device. DETAILED DESCRIPTION

[0061] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0062] Embodiment 1:

[0063] like Figure 1 As shown, the present invention provides a device for coking using the waste heat from dry coke quenching, which is suitable for processing products such as carbonized coal, lump coal, iron coke, and foundry coke. The device mainly includes a furnace body 2, a coal gas collection and processing device, a circulating flue gas dust collector, a flue gas waste heat recovery and processing device, etc.

[0064] The silo 1 is arranged at the upper end of the furnace body 2 and is used for loading coking raw materials, carbonized coal briquettes, lump coal materials, iron coke briquettes, and foundry coke briquettes, as well as for evenly distributing the materials in the furnace tubes 4 of each carbonization unit.

[0065] Combination Figure 1 and Figure 2 As shown, the inner cavity of the furnace body 2 is divided into a dry distillation preheating section 21, a dry distillation gas collection section 22, a medium and low temperature dry distillation section 23 and a high temperature dry distillation section 24 from top to bottom. The lower side of the high temperature dry distillation section 24 has a collecting gasification chamber 241 for gasification and temperature raising. The collecting gasification chamber 241 and the high temperature dry distillation section 24 are separated by a V-shaped bottom plate 28 fixed in the furnace body 2, and a coke powder outlet 281 is provided at the lowest position of the V-shaped bottom plate 28; in this way, the settled coke powder can enter the collecting gasification chamber 241 through the coke powder outlet 281 under its own weight and negative pressure, and mix with mature coke to serve as a gasification raw material. Among them, an air inlet 25 is provided on one side of the high temperature dry distillation section 24, and a return air pipe 26 is connected to one side of the dry distillation preheating section 21. During operation, the air inlet 25 is introduced into the circulating flue gas from the annular flue of the dry quenching coke oven without cooling, and the return air pipe 26 is connected to the flue gas waste heat recovery and treatment device 9.

[0066] The carbonization unit furnace tube 4 is evenly arranged vertically in the inner cavity of the furnace body 2. The upper end of the carbonization unit furnace tube 4 is connected to the silo 1, and the lower end of the carbonization unit furnace tube 4 passes through the V-shaped bottom plate 28 to be connected to the collecting gasification chamber 241, and the collecting gasification chamber 241 is connected to the regulating chamber 3 below. The V-shaped bottom plate 28 is cast as a whole by the casting material, and the carbonization unit furnace tube 4 and the V-shaped bottom plate 28 can be freely extended and slid. A multi-layer baffle 27 is fixed in the inner cavity of the furnace body 2, and a vent 271 is arranged between one end of the baffle 27 and the inner wall of the furnace body 2. The vents 271 of adjacent baffles 27 are arranged in a staggered manner, so that the circulating flue gas rises circuitously, separates the dust of the dry quenching circulating flue gas, and improves the dust reduction effect. A settling port 272 is arranged between the end of the baffle 27 away from the vent 271 and the inner wall of the furnace body 2 to facilitate the falling of coke powder.

[0067] The dry distillation gas collection box 5 is arranged in the dry distillation gas collection section 22 of the inner cavity of the furnace body 2, and the dry distillation gas collection box 5 is completely isolated from the inner cavity of the furnace body 2 by a high-temperature resistant special steel plate. The carbonization unit furnace pipe 4 passes through the dry distillation gas collection box 5, and the upper and lower joints are sealed to ensure that the dry distillation gas does not leak from the circulating flue gas. An air outlet is provided on the carbonization unit furnace pipe 4 in the dry distillation gas collection box 5, and the dry distillation gas collection box 5 is connected to a gas collecting pipe 51 that runs through the outside of the furnace body 2. The dry distillation gas collection box 5 is set with a certain negative pressure to collect the coal gas and volatiles of about 420-450°C generated in the upper and lower carbonization unit furnace pipes 4, and lead them out through the gas collecting pipe 51 to enter the washing and cooling device 8. In order to ensure safe and stable production, the dry distillation gas collection box 5 can be equipped with a single gas blower to provide power.

[0068] The control chamber 3 is divided into a steam cooling section 31, a water evaporation preheating section 32 and a coke discharge section 33 from top to bottom. The water evaporation preheating section 32 sprays water and preheated gas at a certain temperature, and controls the temperature of the high-temperature carbonization section 24 according to the ratio of water and preheated gas. A rotary sealing valve 6 is provided at the lower end of the coke discharge section 33, and a conveyor belt 7 is provided below the rotary sealing valve 6.

[0069] In this embodiment, the furnace body 2 is a rectangular steel structure, which is fully steel-enclosed on all sides, and the inner lining furnace wall is insulated. It is divided into multiple sections from bottom to top, which are the corresponding control chamber 3, high-temperature distillation section 24, medium and low-temperature distillation section 23, distillation gas collection section 22 and distillation preheating section 21. The outside of the furnace body 2 is formed by splicing ordinary steel plates, the force-bearing part is H-shaped steel, the heat-resistant part is a casting, and the furnace is partially built with clay bricks, silicon carbide refractory bricks, castables and fire-retardant coatings. Among them, the collecting gasification chamber 241 in the high-temperature distillation section 24 is isolated by one or more of clay bricks, silicon bricks, refractory castables, fire-retardant coatings and silicon nitride. The return air pipe 26 is made of ordinary heat-resistant steel with external insulation until it enters the flue gas waste heat recovery and treatment device 9. The collecting pipe 51 is made of ordinary heat-resistant steel with external insulation until it enters the washing and cooling device 8.

[0070] The carbonization unit furnace tubes 4 are arranged side by side, and the specific number is determined according to the dry coke quenching production capacity to achieve the purpose of optimization. Such as: the amount of steam, temperature, pressure, etc. required for coking. The carbonization unit furnace tube 4 is welded from different materials, and the main body is a special stainless steel that is resistant to high temperature, corrosion, oxidation, and flushing. Among them, the high-temperature dry distillation section 24 and the medium and low-temperature dry distillation section 23 are made by centrifugal casting technology, and the remaining medium and low-temperature dry distillation sections 23, the dry distillation gas collection section 22, and the dry distillation preheating section 21 are made of ordinary heat-resistant, corrosion-resistant, and wear-resistant stainless steel. The carbonization unit furnace tube 4 is an integrally welded tubular structure, and a spiral gap is opened in part of the dry distillation gas collection box 5 to facilitate the collection or overflow of dry distillation gas.

[0071] During operation, the coking blanks in the silo 1 gradually move downward along the carbonization unit furnace tube 4, enter the regulating chamber 3, and are finally discharged from the coke discharge section 33;

[0072] The CDQ circulating flue gas exchanges heat with the carbonization unit furnace tubes 4 of each section from bottom to top. The CDQ circulating flue gas does not need to be cooled down and sequentially passes through the high-temperature dry distillation section 24, the medium-low temperature dry distillation section 23, the dry distillation preheating section 21, and the circulating flue gas dust collector for dust removal, and then reaches the subsequent flue gas waste heat recovery and treatment device 9;

[0073] The carbonization unit furnace tube 4 uses most of the residual heat from dry quenching to carry out high-temperature dry distillation, medium-low-temperature dry distillation, preheating, dehydration and degassing of various raw materials from bottom to top;

[0074] The water evaporation preheating section 32 in the control chamber 3 is fed with carbon dioxide, air, oxygen or coking wastewater atomized by an atomizer to cool the coke or carbonized material (molded coke, iron coke, foundry coke, etc.) to 150-200°C, while preheating itself, and the mixed gas rises; the ratio of the mixed gas of water, carbon dioxide, air or oxygen is automatically controlled based on ensuring that the temperature range of the high-temperature dry distillation section 24 is 950-1050°C. This process can also achieve pure dry quenching without water evaporation;

[0075] In the collecting gasification chamber 241 under the high-temperature dry distillation section 24, the raw materials are gasified by using preheated water vapor, carbon dioxide, air or oxygen. This part mainly consumes large particles of dust and a small amount of dust from high-temperature dry distillation and medium-low temperature dry distillation. The gasified coal gas will pass through the high-temperature dry distillation section 24 and the medium-low temperature dry distillation section 23 in turn to transfer heat to various raw materials, and at the same time, hydrogenation dry distillation of some of the dry distillation raw materials can be achieved; then it is mixed with the dry distillation coal gas and led out through the dry distillation coal gas collecting box 5.

[0076] Embodiment 2:

[0077] On the basis of the above-mentioned embodiment 1, this embodiment 2 provides a process for coking using the residual heat from dry coke quenching, comprising the following steps:

[0078] The air inlet 25 introduces the uncooled circulating flue gas from the annular flue of the dry quenching coke oven, and the circulating flue gas temperature is 950℃-1100℃; the circulating flue gas heats the high-temperature dry distillation section 24, the medium-low temperature dry distillation section 23, the dry distillation coal gas collection section 22 and the dry distillation preheating section 21 in sequence from the outside of the carbonization unit furnace tube 4, and then enters the flue gas waste heat recovery and treatment device 9.

[0079] A. The coking blank is transported to the silo 1, and the coking blank goes down into the carbonization unit furnace tube 4;

[0080] The prefabricated coking blanks or lump coal are transported to the silo by the conveying device, and enter the furnace tubes 4 of each carbonization unit by the distribution device, and gradually move from top to bottom. The coking blanks are shaped coal blanks with certain specifications that are tamped or compressed, such as cylindrical blanks with cross grooves, six grooves or eight grooves with holes in the middle, elliptical blanks or other shapes, and the lump coal is 5-100mm.

[0081] B. The coking embryo material descends to the dry distillation preheating section 21;

[0082] The temperature of the dry distillation preheating section 21 is 150-350° C. The coking billet is heated by the hot circulating flue gas of the dry quenching outside the carbonization unit furnace tube 4, and the temperature rises. The coking billet moves downward and is gradually heated to 300-350° C., and dehydration and degassing begin.

[0083] C. The coking embryo material descends to the dry distillation gas collecting section 22;

[0084] The temperature of the dry distillation gas collection section 22 is 450-500°C. The coking stock is then directly heated by the dry distillation (including gasification) gas rising from the lower section of the carbonization unit furnace tube 4, and continues to be dehydrated and degassed, and mixed with the dry distillation gas. The dry distillation gas collection box 5 provides a certain negative pressure, and the dry distillation gas and the water vapor in the preheating section are mixed and led out through the gas collecting pipe 51 and enter the washing and cooling device 8.

[0085] D. The coking material moves downward to the medium and low temperature dry distillation section 23;

[0086] The temperature of the medium and low temperature dry distillation section 23 is 500-850°C. The coking billet is heated by the circulating flue gas of 600-900°C, and the temperature continues to rise to 750°C, and the coal pyrolysis and dry distillation begin, and the generated dry distillation gas rises. At this time, the coking billet is heated by the hydrogenation of the lower section dry distillation gas in the carbonization unit furnace tube 4, and a certain hydrogenation pyrolysis reaction occurs; on the other hand, it is also heated by the dry quenching circulating flue gas outside the carbonization unit furnace tube 4. The coking billet is heated and heated from both sides, and the pyrolysis is sufficient. A hole is set in the center of the coking billet, and there are grooves on the plane, which can reduce secondary reactions and make the heating more uniform and stable.

[0087] E. The coking embryo material descends to the high temperature dry distillation section 24;

[0088] The temperature of the high-temperature dry distillation section 24 is 900-1050°C. The coking stock descends and is heated by the upward gasified coal gas, and the coal pyrolysis and dry distillation continue, and polycondensation occurs; in addition, under the external 950-1100°C circulating flue gas heating, it is gradually heated to 1000°C, and the large coking stock polycondenses to produce cracks, the coke matures, and the stock or lump coal is basically coked to obtain coke or semi-coke. At this time, the carbonization unit furnace tube 4 is heated by the gasified coal gas below the carbonization unit furnace tube 4 on the one hand, and is also heated by the high-temperature circulating flue gas of dry quenching outside the carbonization unit furnace tube 4 on the other hand. The coking stock is heated and heated from both sides, and the pyrolysis and dry distillation are sufficient, and the coke maturity is good.

[0089] The temperature in the lower section of the collecting gasification chamber 241 is 950-1050°C, where the gasification reaction of high-temperature water vapor is carried out and the reaction temperature is controlled;

[0090] When the coke or semi-coke descends to the collecting gasification chamber 241, the coke powder that falls off the circulating flue gas enters the collecting gasification chamber 241 by its own weight and negative pressure, and partially gasifies with the coke or semi-coke. The reaction mainly occurs on the coke powder, which has a large contact area and reacts quickly, and there is little reaction on the surface of large coke. When the maturity is insufficient or the temperature is not reached, air or oxygen can be added for temperature-raising reaction, and the temperature of this area is always kept stable through instruments and control valve devices.

[0091] F. The coke or semi-coke descends to the steam cooling section 31 of the regulating chamber 3;

[0092] The temperature in the steam cooling section 31 is 500-750° C., and the temperature of the coke or semi-coke therein drops to 500-650° C. After the high-temperature coke or semi-coke steam cooling section 31, the coke or semi-coke is cooled down, and the temperature of the steam (carbon dioxide, air or oxygen) is increased, providing conditions for the gasification reaction and providing a hydrogen source for hydrogenation dry distillation and volatile hydrogenation.

[0093] G. The coke or semi-coke descends to the water evaporation preheating section 32 of the regulating chamber 3;

[0094] The temperature of coke or semi-coke is reduced to 120-150°C. Carbon dioxide, air or oxygen is used as an atomizer for water spraying or direct water spraying to absorb the heat of coke, increase the temperature of the steam, carbon dioxide, air or oxygen mixed gas in the furnace, and reduce the discharge temperature; and a certain amount of preheating gas (carbon dioxide, air or oxygen) is added to increase the temperature of the mixed gas. The temperature of the high-temperature dry distillation section 24 is regulated by different gas proportions, providing convenient conditions for controlling the high-temperature dry distillation temperature and gasification reaction.

[0095] H. The coke or semi-coke descends to the coke discharge section 33 of the regulating chamber 3 ; the coke or semi-coke is discharged to the conveyor belt 7 through the rotary sealing valve 6 .

[0096] Corresponding to the source of coke powder in the above step E: After the CDQ circulating flue gas directly enters the furnace body 2, the outer side of the carbonization unit furnace tube 4 is heated. In this process, gravity dust removal and eddy current sedimentation dust removal are first performed, and finally the coke powder is settled at the bottom of the V-shaped bottom plate 28 and discharged, which is equivalent to the primary dust collector of CDQ. The obtained coke powder is mixed with the high-temperature coke or semi-coke collected in the gasification chamber 241, and after a small amount of gasification, it continues to descend, preheats steam, carbon dioxide, air or oxygen, and cools itself until it is discharged in the discharge section.

[0097] Embodiment three:

[0098] On the basis of the above-mentioned embodiment 2, this example is used to illustrate the use of the present invention to produce large-block high-quality metallurgical coke, foundry coke, high calorific value dry distillation coal gas and coal tar by blending tamping coke with coal.

[0099] Combination Figure 4 and Figure 5 The blank shown is a raw coal blank with a diameter of 500 mm, a thickness of 300 mm, a middle zone aperture of 100 mm, and reserved grooves on the upper and lower planes, which is formed by tamping or shock compaction; it is sent to the silo 1 through a conveying device, loaded into each carbonization unit furnace tube 4 by mechanical stacking, and gradually descends, enters the dry distillation preheating section 21 at the upper part of the carbonization unit furnace tube 4, and is heated by 500-650°C of the dry quenching circulating flue gas outside the carbonization unit furnace tube 4, and the raw material blank is quickly heated and dried, dehydrated and degassed, and then descends;

[0100] The temperature gradually rises to 350°C and enters the dry distillation gas collection section 22; it is heated by the mixed dry distillation gas at 450-550°C in the upward medium-low temperature dry distillation section 23, and the heated dry distillation gas is mixed with the water vapor in the preheating section and led out of the furnace body 2;

[0101] After passing through the dry distillation gas collection section 22, the raw material billet descends into the medium and low temperature dry distillation section 23, the carbonization unit furnace tube 4 is heated by the dry quenching circulating flue gas at 600-800°C, and the carbonization unit furnace tube 4 is heated by the mixed dry distillation gas at 550-750°C in the upward high temperature dry distillation section 24. This section is heated bidirectionally inside and outside, heated evenly, and a certain amount of hydrogenation pyrolysis occurs. Hydrogenation pyrolysis can improve the cohesiveness of coal and avoid or reduce the occurrence of secondary cracking reactions; melt expansion squeezes up and presses down, and dry distillation pyrolysis is sufficient;

[0102] Continue to descend and enter the high-temperature dry distillation section 24, the outside of the carbonization unit furnace tube 4 is heated by the circulating flue gas at the dry quenching outlet at 950-1100°C, and the inside of the carbonization unit furnace tube 4 is heated by the upward high-temperature gasified coal gas at 950-1000°C. This section is heated bidirectionally inside and outside, heated evenly, and polycondensation pyrolysis occurs;

[0103] The mature coke continues to descend into the collecting gasification chamber 241 for high-temperature gasification and cooling. The temperature in this area must be kept stable, which is controlled by the amount of atomized wastewater, the amount of air or oxygen, the coke discharge temperature and the amount of coke discharge. The coke powder and the coke surface react with air or oxygen to increase the temperature, and react with water vapor to gasify and cool down.

[0104] The coke powder and mature coke continue to descend to the regulating chamber 3, where they are preheated with steam, air or oxygen until the wastewater is gasified and atomized. The temperature then drops to 120-150°C and they are discharged from the furnace body 2 through the rotary sealing valve 6 and sent out by the conveyor belt 7.

[0105] Similarly, combined Figure 6 and Figure 7 The blank shown in the second embodiment of the present invention is also applicable to the carbonization of shaped coal blanks to produce shaped coke and the production of iron coke from iron coke blanks. The principle and basic process are the same, and the carbonization time is not much different.

[0106] Since the present invention adopts the carbonization unit furnace tube 4 to heat both inside and outside at the same time, the heating speed is uniform and stable, and the carbonization time and speed can be controlled; the molded coke and iron coke are mature, dense, high in thermal strength and good in quality. The carbonization carbonization coal gas purification is simple, and the process control is reliable. Among them, the iron coke blank is carbonized, and the carbonization heating in the gasification coal gas atmosphere occurs, and hydrogenation pyrolysis and iron reduction reactions occur, which avoids or reduces the occurrence of secondary cracking reactions, and at the same time improves the adhesion of the blended coal to a certain extent, and the iron reduction rate in the iron coke is high; the iron coke blank carbonization process has both coal pyrolysis reaction and iron ore powder reduction reaction. The device of the present invention adopts the carbonization unit furnace tube 4 to heat both inside and outside, and has high thermal efficiency; therefore, the carbonization time of the molded coal blank and the iron coke blank in the furnace body 2 can be shortened, the production efficiency is improved, and the product has high cold strength and hot strength.

[0107] Embodiment 4:

[0108] Based on the above-mentioned embodiment 2, this example is used to illustrate the use of the present invention to produce large-scale high-quality semi-coke, high calorific value dry distillation gas and high-quality medium and low coal tar from non-caking coal and weakly caking coal, long flame coal or a mixture of the three.

[0109] Use 5-100mm non-bonding coal, weakly bonding coal, long flame coal or a mixture of the three as raw materials;

[0110] The material is sent to the upper material bin 1 of the furnace body 2 by the conveying device, and is loaded into the furnace tubes 4 of each carbonization unit by the material distribution device and gradually moves downward;

[0111] After entering the carbonization unit furnace tube 4 upper dry distillation preheating section 21, the raw material lump coal is heated to 500-650°C by the dry quenching circulating flue gas outside the carbonization unit furnace tube 4, and is quickly heated and dried, dehydrated and degassed, and then moves downward;

[0112] The temperature gradually rises to 350°C and enters the dry distillation gas collection section 22; it is heated by the mixed dry distillation gas at 450-550°C in the upward medium-low temperature dry distillation section 23, and the heated dry distillation gas is mixed with the water vapor in the preheating section and led out of the furnace body 2;

[0113] After the dry distillation gas collecting section 22, the raw lump coal gradually descends to enter the medium and low temperature dry distillation section 23, the carbonization unit furnace tube 4 is heated by the dry quenching circulating flue gas at 600-800°C, and the carbonization unit furnace tube 4 is heated by the mixed dry distillation gas at 550-750°C of the upward high temperature dry distillation section 24. This section is heated bidirectionally inside and outside, heated evenly, and a certain amount of hydrogenation pyrolysis occurs, avoiding or reducing the occurrence of secondary cracking reactions; due to hydrogenation pyrolysis dry distillation, the cohesiveness of the lump coal is improved, and a small amount of small particles of lump coal will be melted and agglomerated, and large lumps of coal will adhere to each other. The reason is that hydrogenation pyrolysis can increase the cohesiveness of the raw coal, especially the weakly cohesive coal, which is the most obvious. For the process of the present invention, it has little effect, but is beneficial; the upper extrusion and lower pressure make the molding more beautiful, and the edges and corners of the lump coal are reduced; the dry distillation pyrolysis in this section is more sufficient;

[0114] Continue to descend and enter the high-temperature dry distillation section 24, the carbonization unit furnace tube 4 is heated by the circulating flue gas at 950-1100°C at the CDQ outlet, and the carbonization unit furnace tube 4 is heated by the upward high-temperature gasified coal gas at 950-1000°C. This section is heated bidirectionally inside and outside, heated evenly, and polycondensation and pyrolysis occur, and the volatile matter of the semi-coke is reduced;

[0115] Continue to go down and enter the gathering gasification chamber 241. This area is a high-temperature gasification temperature-raising and cooling area. The temperature must be kept stable and is controlled by the amount of atomized wastewater, the amount of air or oxygen, the coke discharge temperature and the coke discharge amount. The coke powder and semi-coke surface react with air or oxygen to increase the temperature and react with water vapor to reduce the temperature;

[0116] The coke powder and mature semi-coke continue to descend to the regulating chamber 3, where they are preheated with steam, air or oxygen until the wastewater is gasified and atomized. The temperature then drops to 120-150°C and is discharged from the furnace body 2 through the rotary sealing valve 6 and sent out by the conveyor belt 7.

[0117] Embodiment five:

[0118] On the basis of the above-mentioned embodiment 2, this embodiment 5 provides a washing and cooling device 8. The negative pressure of the dry distillation gas collection box 5 is used to collect the coal gas and volatiles at about 420-450°C generated by the dry distillation preheating section 21, the medium and low temperature dry distillation section 23, and the high temperature dry distillation section 24 (collecting the gasification chamber 241), and lead them out of the furnace body 2 to enter the washing and cooling device 8. The dry distillation coal gas is cooled to 85°C by using coal tar or washing oil or coal tar or petroleum asphalt or other oils, and then merged into the negative pressure section of the coke oven gas system of the coking plant; the recovered coal tar is mixed with the washing oil after washing and sent to the coal tar processing device by pumping to increase pressure.

[0119] Combination Figure 1 and Figure 3 As shown, the washing and cooling device 8 is provided with a coal tar recovery outlet 82 at the lower end, a cooling washing oil inlet 83 and a pyrolysis gas outlet 84 at the upper end, and a primary cooler 81 is provided in the middle. The pyrolysis gas at 400-500°C sent from the furnace body 2 enters the lower part of the washing and cooling device 8 and flows upward in countercurrent, and contacts with the 55-65°C washing oil for washing, cooling and dust removal. After purification, the pyrolysis gas is directly incorporated into the primary cooler 81 of the coking plant at a temperature of 75-85°C and is directly incorporated into the main coke oven gas pipe, or a primary cooler 81 and a gas blower are separately provided to provide cooling power for it; in general, the chemical product purification system of the coking plant is redundant and can be used to reduce investment. According to the dry distillation temperature, the coal tar in the present invention should belong to a mixture of medium-low temperature coal tar and a small amount of high temperature coal tar. The properties and compositions of medium-low temperature coal tar and high temperature coal tar are significantly different, but there are many components with similar properties. Various fractions are cut by pre-distillation method, so that the single component products to be extracted such as phenol, naphthalene, anthracene, etc. are concentrated and concentrated in the corresponding fractions, and then further separated by physical and chemical methods. After further processing, each fraction can be separated into a variety of chemical products. The washing and cooling process is actually a distillation and cooling process. Therefore, the present invention can cut three boiling point products in this process and send them to the coal tar deep processing device respectively; mainly light oil with a boiling point of more than 230°C, washing oil part of 230-300°C and heavy oil part below 300°C; washing oil can choose low temperature coal tar, medium temperature coal tar, high temperature coal tar, and can be assisted by superheated steam 380-450°C heating stripping distillation when necessary.

[0120] Obviously, those skilled in the art can make various changes and modifications to the present invention without departing from the spirit and scope of the present invention. Thus, if these modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include these modifications and variations.

Claims

1. A device for coking using waste heat from dry coke quenching, characterized in that: include: A furnace body (2), wherein the inner cavity of the furnace body (2) is divided into a dry distillation preheating section (21), a dry distillation coal gas collection section (22), a medium-low temperature dry distillation section (23) and a high temperature dry distillation section (24) from top to bottom; an air inlet (25) is provided on one side of the high temperature dry distillation section (24), and a return air pipe (26) is connected to one side of the dry distillation preheating section (21); A material bin (1) is arranged at the upper end of the furnace body (2); A control chamber (3) located below the high-temperature dry distillation section (24) of the furnace body (2); A plurality of carbonization unit furnace tubes (4) are vertically arranged in the inner cavity of the furnace body (2); the upper ends of the carbonization unit furnace tubes (4) are connected to the material bin (1), and the lower ends of the carbonization unit furnace tubes (4) are connected to the control cavity (3); a pyrolysis coal gas collecting box (5), arranged in a pyrolysis coal gas collecting section (22) in the inner cavity of the furnace body (2) and isolated from the inner cavity of the furnace body (2); the carbonization unit furnace pipe (4) passes through the pyrolysis coal gas collecting box (5), and a gas outlet hole is provided on the carbonization unit furnace pipe (4) in the pyrolysis coal gas collecting box (5); the pyrolysis coal gas collecting box (5) is connected to a gas collecting pipe (51) that passes through the outside of the furnace body (2); The high-temperature dry distillation section (24) has a collecting gasification chamber (241) at the lower side, and a V-shaped bottom plate (28) is provided at the connection between the collecting gasification chamber (241) and the high-temperature dry distillation section (24) for dividing the upper and lower sides of the furnace body (2), and a coke powder outlet (281) is provided at the lowest position of the V-shaped bottom plate (28) for connecting the high-temperature dry distillation section (24) and the collecting gasification chamber (241); The lower end of the carbonization unit furnace tube (4) is connected to the collecting gasification chamber (241), and the lower side of the collecting gasification chamber (241) is in communication with the regulating chamber (3); A plurality of baffles (27) are fixed to the inner cavity of the furnace body (2); a vent (271) is provided between one end of the baffle (27) and the inner wall of the furnace body (2), and the vents (271) of adjacent baffles (27) are arranged in a staggered manner; a settling port (272) is provided between one end of the baffle (27) away from the vent (271) and the inner wall of the furnace body (2); The control chamber (3) is divided into a steam cooling section (31), a water evaporation preheating section (32) and a coke removal section (33) from top to bottom; water and preheating gas of a certain temperature are sprayed into the water evaporation preheating section (32), and the temperature of the high-temperature carbonization section (24) is controlled according to the ratio of water and preheating gas; A rotary sealing valve (6) is provided at the lower end of the coke discharge section (33), and a conveyor belt (7) is provided below the rotary sealing valve (6); The gas collecting pipe (51) is connected to a washing and cooling device (8); the air inlet (25) is fed with uncooled circulating flue gas from the annular flue of the dry quenching coke oven; the return air pipe (26) is connected to a flue gas waste heat recovery and processing device (9).

2. A process for coking using waste heat from dry coke quenching, using the device for coking using waste heat from dry coke quenching as claimed in claim 1, characterized in that: The steps include: A. The coking material is transported to the silo (1), and then moves downward into the carbonization unit furnace tube (4); B. The coking material moves down to the dry distillation preheating section (21), where the temperature rises and dehydration and degassing begin; C. The coking material moves downward to the dry distillation gas collecting section (22); the dry distillation gas collecting box (5) provides a certain negative pressure, and the dry distillation gas and the water vapor from the preheating section are mixed and led out of the furnace body (2) through the gas collecting pipe (51); D. The coking material descends to the medium-low temperature dry distillation section (23), where coal pyrolysis and dry distillation begin. The dry distillation coal gas generated rises along the carbonization unit furnace tube (4) and enters the dry distillation coal gas collection section (22) on the upper side; E. The coking material descends to the high-temperature dry distillation section (24), where it continues to be pyrolyzed and dry distilled to form coke or semi-coke. The dry distillation coal gas generated rises along the carbonization unit furnace tube (4) and enters the medium-low temperature dry distillation section (23) on the upper side; F. The coke or semi-coke descends to the steam cooling section (31) of the regulating chamber (3), where the steam cools the coke or semi-coke. At the same time, the steam temperature is increased under the action of the coke or semi-coke, and the high-temperature steam rises and enters the high-temperature dry distillation section (24) on the upper side; G. The coke or semi-coke descends to the water evaporation preheating section (32) of the control chamber (3), where the coke or semi-coke is cooled by water evaporation, and a certain amount of preheating gas is added to control the temperature of the high-temperature dry distillation section (24). The generated steam rises and enters the steam cooling section (31) on the upper side; H. The coke or semi-coke descends to the coke discharge section (33) of the regulating chamber (3) and is transported to the outside of the furnace body (2).

3. A process for coking using waste heat from dry coke quenching according to claim 2, characterized in that: The air inlet (25) is fed with uncooled circulating flue gas from the annular flue of the dry quenching coke oven, the circulating flue gas temperature being 950° C.-1100° C.; the circulating flue gas heats the high-temperature dry distillation section (24), the medium-low temperature dry distillation section (23), the dry distillation coal gas collection section (22) and the dry distillation preheating section (21) in sequence from the outside of the carbonization unit furnace tube (4); The steam in the control chamber (3) rises along the carbonization unit furnace tube (4), and the steam sequentially heats the high-temperature dry distillation section (24), the medium-low temperature dry distillation section (23), and the dry distillation coal gas collection section (22) from inside the carbonization unit furnace tube (4).

4. A process for coking using waste heat from dry coke quenching according to claim 3, characterized in that: In the step E, when the coke or semi-coke descends to the collecting gasification chamber (241) at the lower part of the high-temperature dry distillation section (24), the coke powder discharged from the circulating flue gas enters the collecting gasification chamber (241) under its own weight and negative pressure, and partially gasifies with the coke or semi-coke; In the step F, the temperature of steam is increased under the action of coke or semi-coke to provide conditions for the gasification reaction, and a certain amount of hydrogen is generated to provide a hydrogen source for subsequent reactions.

5. A coking process using waste heat from dry coke quenching according to claim 4, characterized in that: In the step B, the temperature of the coking stock in the dry distillation preheating section (21) is 150-350°C; In the step C, the temperature of the coking stock in the dry distillation gas collecting section (22) is 450-500°C; In the step D, the temperature of the coking stock in the medium-low temperature carbonization section (23) is 500-850°C, and under the action of hydrogen, the coking stock undergoes a certain hydrogenation pyrolysis reaction; In the step E, the temperature in the carbonization unit furnace tube (4) in the high-temperature dry distillation section (24) is 900-1050°C, and polycondensation pyrolysis occurs; wherein the temperature in the collecting gasification chamber (241) is 950-1050°C; In step F, the temperature in the steam cooling section (31) is 500-750°C, and the temperature of the coke or semi-coke therein is reduced to 500-650°C; In step G, the temperature of the coke or semi-coke is reduced to 120-150°C.

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