A caking coal pyrolysis device and method

Abstract

The present invention provides a pyrolysis device and method for caking coal, the device comprising a pyrolysis reaction device, a gas-solid separation device and an oil-gas recovery device connected in sequence, the solid outlet of the gas-solid separation device is connected to the inlet of the pyrolysis reaction device, and the pyrolysis reaction device is provided with a jacketed feeding nozzle. The present invention improves the feeding part of the pyrolysis reaction device, controls the temperature of the pulverized coal in the feeding nozzle, and avoids the caking of the nozzle by the caking coal due to the high temperature during feeding; after feeding, the device can achieve instant full mixing and heating with the solid heat carrier, avoid staying in the bonding temperature range for a long time, and achieve rapid pyrolysis. At the same time, the structural design of the pyrolysis reaction device facilitates the use and separation of non-caking solid heat carriers, thereby achieving efficient utilization of caking coal.

Description

Technical Field

[0001] The invention belongs to the technical field of energy utilization and relates to a caking coal pyrolysis device and method. Background Art

[0002] As energy shortage and environmental pollution become increasingly serious, the development of clean and efficient chemical raw material technology has become a consensus. In the chemical raw material structure, hydrocarbon materials account for a large proportion, especially coal. Therefore, the development and promotion of clean coal technology and the realization of graded transformation and rational and effective utilization of coal resources have become research hotspots. Extracting high-value-added chemicals and oil products from coal through pyrolysis is an important technology to improve the utilization value of coal.

[0003] At present, various coal pyrolysis technologies have been industrialized, which has led to the vigorous development of clean and efficient comprehensive utilization of coal. However, different types and characteristics of coal require different treatment methods, and it is often difficult to make breakthroughs by only using existing processes. For example, for the pyrolysis of coal with high volatility and high cohesion, after the temperature reaches a certain temperature range, the cohesive coal will stick together, agglomerate, and clump, making it difficult for the pyrolysis device to operate normally. Therefore, a large amount of coal rich in oil and gas and with cohesion cannot take the route of clean and efficient comprehensive utilization of coal and graded and quality-based utilization, and the high value-added oil and gas in the coal cannot be directly and efficiently utilized.

[0004] The annual domestic coal consumption is about 3 to 4 billion tons, of which weakly sticky coal, gas coal and other sticky coal with high volatile content account for a high proportion. However, there is currently no technology suitable for the clean and efficient comprehensive utilization and graded and quality-based utilization of sticky coal. Due to the tightening of environmental protection policies in recent years, the subsequent utilization of such coal with a sulfur content greater than 1% has become increasingly limited and the conversion cost has become increasingly high. A technology is urgently needed to solve this problem. Coal pyrolysis technology can extract high-value-added chemicals and oil products from coal, and convert part of the sulfur into gas and liquid products, and then recycle and produce sulfur products. It is a very suitable utilization method, but sticky coal is easy to stick together. Traditional coal pyrolysis technology cannot achieve high dispersion, rapid and sufficient mixing and heating of sticky coal, and cannot achieve efficient utilization of sticky coal.

[0005] At present, although there are studies on the utilization of caking energy fuels, the progress is not obvious. CN 205635492U discloses a device for rapid hydrogenation pyrolysis of pulverized coal to produce oil and gas, which includes a partial oxidation furnace, a coal hydrogenation pyrolysis reactor, and a cyclone separator, which are arranged in order from top to bottom, and are provided with a pulverized coal nozzle and a cooling nozzle. The device also includes a high-efficiency cyclone separator, a fly ash filter, and a semi-coke collection tank; although the device is provided with a pulverized coal nozzle and a cooling nozzle, the two are arranged separately, and the cooling nozzle is used to cool the pyrolysis product, and cannot cool the pulverized coal feed, and is still not well suitable for the pyrolysis of caking coal.

[0006] CN 102758035A discloses a spray gun for spraying waste plastic pyrolysis gas premixed with coal powder, comprising a straight blowing pipe, the rear end of which is a blowing inlet end, and the front end of which is a blowing outlet end; a plastic preheating and pre-swirl chamber, which is sleeved on the periphery of the straight blowing pipe and is connected to a plastic particle nozzle; a premixing chamber, which is located in front of the plastic preheating and pre-swirl chamber and is connected to a plurality of coal powder nozzles; a pyrolysis gas delivery pipe, which connects the plastic preheating and pre-swirl chamber with the premixing chamber; and a plurality of mixed material delivery pipes extending backward from the premixing chamber, the other end of which is connected to the rear end of the straight blowing pipe. The spray gun can quickly pyrolyze waste plastics and burn them together with pulverized coal to avoid clogging the spray gun port, but it is mainly an improvement on the spraying system, and does not involve the problem of coal pyrolysis and its feeding.

[0007] In summary, for the pyrolysis treatment of binding coal, the equipment needs to be improved to avoid the influence of sufficient pulverized coal adhesion and agglomeration on the pyrolysis process. Summary of the invention

[0008] In view of the problems existing in the prior art, the purpose of the present invention is to provide a pyrolysis device and method for caking coal. The device improves the feeding part in the pyrolysis reaction device to avoid the clogging of the feeding nozzle due to the high temperature of the caking coal during feeding, thereby ensuring the normal operation of the device, and quickly mixing and heating after feeding, thereby realizing efficient pyrolysis and utilization of the caking coal.

[0009] To achieve this object, the present invention adopts the following technical solutions:

[0010] On the one hand, the present invention provides a caking coal pyrolysis device, which includes a pyrolysis reaction device, a gas-solid separation device and an oil and gas recovery device connected in sequence, the solid outlet of the gas-solid separation device is connected to the inlet of the pyrolysis reaction device, and the pyrolysis reaction device is provided with a jacketed feed nozzle.

[0011] In the present invention, the device mainly improves the feeding part of the pyrolysis reaction device. By setting a jacketed feeding nozzle, the temperature of the pulverized coal in the feeding nozzle is controlled to avoid the nozzle being blocked by the temperature at which the pulverized coal becomes sticky. After the pulverized coal is fed, it is instantly fully mixed with the solid heat carrier under the action of the airflow and the temperature is raised, avoiding staying in the sticking temperature range for a long time, thereby achieving rapid pyrolysis.

[0012] In the present invention, the device can handle the pyrolysis of various types of coal, and is particularly suitable for processing high-volatile, highly adhesive coal, wherein the volatile matter mass content reaches more than 28%, and the adhesive index is: the adhesive index G is greater than 65, such as 65, 66, 68, 70, 72 or 75, and the gelatin layer thickness Y is greater than 15 mm, such as 15 mm, 16 mm, 18 mm, 20 mm, 21 mm or 24 mm, etc.

[0013] The following are preferred technical solutions of the present invention, but are not intended to be limitations of the technical solutions provided by the present invention. Through the following technical solutions, the technical objectives and beneficial effects of the present invention can be better achieved and realized.

[0014] As a preferred technical solution of the present invention, the feed nozzle is arranged at the bottom and / or lower part of the pyrolysis reaction device.

[0015] As a preferred technical solution of the present invention, the number of the feed nozzle is at least one, for example, one, two, three or four.

[0016] In the present invention, the feed nozzle can be arranged in the middle area of ​​the bottom or the lower side of the pyrolysis reaction device. When arranged on the lower side, generally multiple feed nozzles can be arranged evenly and symmetrically.

[0017] As a preferred technical solution of the present invention, the installation direction of the feed nozzle is vertically upward, obliquely upward or horizontally;

[0018] The installation angle of the feed nozzle is 0 to 90° with the vertical direction, for example, 0°, 20°, 30°, 45°, 60°, 75° or 90°, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0019] In the present invention, the raw material pulverized coal is brought in by the conveying gas and generally enters the pyrolysis reactor from bottom to top, so the feed nozzle is installed vertically upward or obliquely upward so that the pulverized coal can be quickly dispersed after being injected. At the same time, the raw material can also enter horizontally and be dispersed after being brought in by the conveying gas.

[0020] As a preferred technical solution of the present invention, the inner tube of the jacketed feed nozzle is fed with the caking coal transported by the transporting gas, and the annular gap of the jacketed feed nozzle is fed with the cooling medium.

[0021] In the present invention, the feed nozzle is configured as a jacket structure, and a cooling medium is introduced to cool the pulverized coal raw material to prevent the high temperature in the reactor from being transmitted to the feed nozzle, causing the pulverized coal at the feed nozzle to stick and clog; the cooling medium can be selected from gases such as cold nitrogen and coal gas or liquids such as circulating water.

[0022] As a preferred technical solution of the present invention, a solid heat carrier inlet pipe is provided at the lower portion of the pyrolysis reaction device, and the solid outlet of the gas-solid separation device is connected to the solid heat carrier inlet pipe.

[0023] Preferably, a solid heat carrier regenerator is provided between the solid outlet of the gas-solid separation device and the solid heat carrier inlet pipe.

[0024] In the present invention, the pyrolysis temperature of pulverized coal is 400-650°C. In order to enable rapid heating and pyrolysis, the pulverized coke produced by the pyrolysis reactor is used as a solid heat carrier, which is partially burned in a solid heat carrier regenerator to increase its temperature to 600-800°C, and then instantly mixed with the raw pulverized coal to provide heat for the pyrolysis reaction and quickly complete the pyrolysis reaction.

[0025] In order to heat the raw materials quickly, the coal needs to be ground and crushed first, and the particle size can be controlled within the range of 50 to 300 μm.

[0026] As a preferred technical solution of the present invention, the number of the solid heat carrier inlet pipe is at least one, such as one, two, three or four.

[0027] In the present invention, in order to facilitate the solid heat carrier to enter the pyrolysis reactor and quickly mix with the pulverized coal, the solid heat carrier inlet pipe is generally arranged obliquely from top to bottom, and when multiple inlets are arranged, they are evenly and symmetrically distributed.

[0028] Preferably, the pyrolysis reaction device is provided with a ring pipe in the horizontal direction along the inner wall, the inlet of the ring pipe is connected to the solid heat carrier inlet pipe, and the position of the ring pipe facing the inner side of the pyrolysis reaction device is provided with a slit.

[0029] Preferably, the annular pipe is provided with at least one section, and the number of the annular pipes is the same as the number of the solid heat carrier inlet pipes.

[0030] In the present invention, in order to facilitate the rapid mixing and heating of the heat carrier and the caking coal raw material, an annular tube is arranged along the inner wall of the pyrolysis reaction device, and a slit is arranged on the annular tube facing inward, and the heat carrier entering through the solid heat carrier inlet pipe is sprayed in a fan-shaped surface from the slit, thereby accelerating the mixing with the raw coal.

[0031] As a preferred technical solution of the present invention, the installation direction of the solid heat carrier inlet pipe is horizontal or obliquely downward;

[0032] The installation angle of the solid heat carrier inlet pipe is less than 90° with the horizontal direction, for example 80°, 75°, 60°, 45°, 30°, 15° or 0°, but is not limited to the listed values, and other values ​​not listed within the numerical range are also applicable.

[0033] As a preferred technical solution of the present invention, the pyrolysis reaction device includes an entrained flow reactor.

[0034] Preferably, the middle portion of the pyrolysis reaction device is a diameter-reducing section, and the diameter of the diameter-reducing section is larger than the diameters of the lower portion and the upper portion.

[0035] Preferably, a return pipe is provided at the lower part of the diameter-changing section, and the return pipe is connected to the solid heat carrier regenerator.

[0036] In the present invention, the pyrolysis reaction device is provided with a variable diameter section, which is helpful for the separation of solid heat carrier particles during the pyrolysis reaction and for the pyrolysis reaction of the bonding coal.

[0037] In the present invention, a plurality of pyrolysis reaction devices can be arranged in parallel, and the outlet pipelines are connected to the gas-solid separation device after merging, which can effectively increase the processing capacity of the bonding coal without affecting the mixing and heating of the bonding coal.

[0038] As a preferred technical solution of the present invention, a fluidizing gas pipe is also provided at the bottom of the pyrolysis reaction device.

[0039] As a preferred technical solution of the present invention, a gas distribution plate is provided inside the pyrolysis reaction device and above the fluidizing gas pipe.

[0040] In the present invention, since the amount of conveying gas is relatively large, in addition to a part being used as conveying gas for pulverized coal, the other part can be directly introduced from the bottom of the pyrolysis reaction device, and a gas distribution plate is arranged above to make the gas evenly distributed, which is helpful for the dispersion of pulverized coal and heat carrier.

[0041] On the other hand, the present invention provides a method for pyrolyzing caking coal using the above-mentioned device, characterized in that the method comprises:

[0042] (1) The caking coal raw material is heat exchanged at the feed nozzle, and then undergoes a pyrolysis reaction to obtain a pyrolysis product;

[0043] (2) The pyrolysis product obtained in step (1) is subjected to gas-solid separation, the obtained gas phase product is subjected to oil-gas separation, and the obtained solid phase product is returned to step (1) as a heat carrier for the pyrolysis reaction.

[0044] As a preferred technical solution of the present invention, the caking coal raw material in step (1) is transported by conveying gas.

[0045] Preferably, the conveying gas comprises any one of coal gas, nitrogen or flue gas, or a combination of at least two of them. Typical but non-limiting examples of the combination include: a combination of coal gas and nitrogen, a combination of nitrogen and flue gas, a combination of coal gas, nitrogen and flue gas, etc.

[0046] In the present invention, the transport gas may also be pyrolysis gas obtained by separating pyrolysis oil and gas generated by the reaction of the device.

[0047] Preferably, the particle size of the caking coal raw material in step (1) is 50 to 300 μm, for example, 50 μm, 100 μm, 150 μm, 200 μm, 250 μm or 300 μm, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0048] Preferably, the heat exchange in step (1) is carried out in a jacketed feed nozzle.

[0049] Preferably, a cooling medium is introduced into the annular gap of the jacketed feed nozzle, wherein the cooling medium may be a gas such as nitrogen, coal gas, or a liquid such as circulating water.

[0050] Preferably, the temperature of the caking coal raw material after heat exchange in step (1) is below 200°C, for example 200°C, 180°C, 160°C, 150°C or 140°C, etc., but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0051] Preferably, the temperature of the pyrolysis reaction in step (1) is 400-650°C, for example 400°C, 450°C, 500°C, 550°C, 600°C or 650°C, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0052] Preferably, the pressure of the pyrolysis reaction in step (1) is 0 to 0.5 MPaG, such as 0, 0.1 MPaG, 0.2 MPaG, 0.3 MPaG, 0.4 MPaG or 0.5 MPaG, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0053] Preferably, the pyrolysis reaction time in step (1) is 0.5 to 5 s, for example 0.5 s, 1 s, 2 s, 3 s, 4 s or 5 s, but is not limited to the listed values, and other values ​​not listed within the numerical range are also applicable.

[0054] As a preferred technical solution of the present invention, the gas-solid separation in step (2) obtains char powder and pyrolysis oil gas.

[0055] Preferably, part of the fine coke is returned to step (1) via a solid heat carrier regenerator as a heat carrier for the pyrolysis reaction.

[0056] Preferably, the powdered coke undergoes a combustion reaction in a solid heat carrier regenerator and the temperature is raised to 600-800°C, for example, 600°C, 630°C, 650°C, 680°C, 700°C, 720°C, 750°C, 780°C or 800°C, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0057] In the present invention, the temperature of the solid coke generated by the pyrolysis reaction is not enough to quickly heat the binding coal raw material to the pyrolysis temperature. Therefore, the coke can enter the heat carrier regenerator, and air is introduced to burn a small amount of coke. The remaining coke is heated to serve as a heat carrier. At the same time, not all of the coke is used as a heat carrier. Another part can also be cooled and used as a product or a raw material for downstream processing equipment.

[0058] Preferably, the heat carrier of the pyrolysis reaction also includes any one of silica sand, porcelain balls or ore, or a combination of at least two of them. Typical but non-limiting examples of the combination include: a combination of silica sand and porcelain balls, a combination of porcelain balls and ore, a combination of silica sand, porcelain balls and ore, etc.

[0059] Preferably, the silica sand and / or porcelain balls are separated when passing through the diameter-changing section of the pyrolysis reaction device and returned to the solid heat carrier regenerator.

[0060] In the present invention, in view of the characteristics of caking coal, the solid heat carrier used also includes solid particles with large heat capacity and high temperature stability such as silica sand, porcelain balls or ore. When used together with powdered coke, the ratio of non-caking particles to bonding particles can be greatly increased to adapt to the pyrolysis of coals with different caking properties.

[0061] The mixed solid heat carrier moves upward to the variable diameter section. Since the silica sand and porcelain balls are carried out at a high speed, they fall in this area and return to the heat carrier regenerator. The powdered coke continues to move upward through the variable diameter section and enters the gas-solid separation device.

[0062] In addition, if the powdered coke is not used as a solid heat carrier, and solid particles such as silica sand and porcelain balls are used alone, heat is provided by burning self-produced coal gas or heavy tar.

[0063] Compared with the prior art, the present invention has the following beneficial effects:

[0064] (1) The present invention improves the feeding part of the pyrolysis reaction device to control the temperature of the pulverized coal in the feeding nozzle, thereby preventing the caking coal from caking the nozzle due to high temperature during feeding, thereby ensuring the normal operation of the device and achieving efficient utilization of the caking coal, with an energy utilization efficiency of more than 80%;

[0065] (2) After feeding, the device of the present invention can achieve instant full mixing and temperature rise with the solid heat carrier, avoiding staying in the bonding temperature range for a long time, and achieving rapid pyrolysis;

[0066] (3) The structural design of the pyrolysis reaction device of the present invention facilitates the use and separation of non-adhesive solid heat carriers and helps the pyrolysis reaction of adhesive coal. BRIEF DESCRIPTION OF THE DRAWINGS

[0067] Figure 1 is a schematic structural diagram of a caking coal pyrolysis device provided in Example 1 of the present invention;

[0068] Figure 2 is a schematic structural diagram of the inlet portion of the pyrolysis reaction device provided in Example 1 of the present invention;

[0069] Figure 3 is a schematic structural diagram of a caking coal pyrolysis device provided in Example 2 of the present invention;

[0070] Figure 4 is a schematic structural diagram of the inlet portion of the pyrolysis reaction device provided in Example 2 of the present invention;

[0071] Figure 5 It is a structural schematic diagram of the inlet part and the variable diameter section of the pyrolysis reaction device provided in Example 3 of the present invention;

[0072] Figure 6 is a schematic structural diagram of a pyrolysis reaction device arranged in parallel provided in Example 4 of the present invention;

[0073] Among them, 1-pyrolysis reaction device, 2-gas-solid separation device, 3-oil and gas recovery device, 4-feed nozzle, 5-solid heat carrier inlet pipe, 6-fluidizing gas pipe, 7-gas distribution plate, 8-variable section, 9-return pipe, 10-solid heat carrier regenerator. DETAILED DESCRIPTION

[0074] In order to better illustrate the present invention and facilitate understanding of the technical solution of the present invention, the present invention is further described in detail below. However, the following embodiments are only simple examples of the present invention and do not represent or limit the scope of protection of the present invention. The scope of protection of the present invention shall be subject to the claims.

[0075] The specific implementation mode of the present invention provides a caking coal pyrolysis device and method, the device comprises a pyrolysis reaction device 1, a gas-solid separation device 2 and an oil and gas recovery device 3 which are connected in sequence, the solid outlet of the gas-solid separation device 2 is connected to the inlet of the pyrolysis reaction device 1, and the pyrolysis reaction device 1 is provided with a jacketed feed nozzle 4.

[0076] The method comprises:

[0077] (1) The caking coal raw material is heat exchanged at the feed nozzle 4, and then undergoes a pyrolysis reaction to obtain a pyrolysis product;

[0078] (2) The pyrolysis product obtained in step (1) is subjected to gas-solid separation, the obtained gas phase product is subjected to oil-gas separation, and the obtained solid phase product is returned to step (1) as a heat carrier for the pyrolysis reaction.

[0079] The following are typical but non-limiting embodiments of the present invention:

[0080] Embodiment 1:

[0081] This embodiment provides a caking coal pyrolysis device. The structural schematic diagram of the device is as follows: Figure 1 As shown, it includes a pyrolysis reaction device 1, a gas-solid separation device 2 and an oil-gas recovery device 3 which are connected in sequence, the solid outlet of the gas-solid separation device 2 is connected to the inlet of the pyrolysis reaction device 1, and the pyrolysis reaction device 1 is provided with a jacketed feed nozzle 4.

[0082] The structural schematic diagram of the inlet part of the pyrolysis reaction device is as follows Figure 2 As shown, the feed nozzle 4 is arranged at the bottom of the pyrolysis reaction device 1, there is one feed nozzle 4, and it is installed vertically upward.

[0083] The inner tube of the feed nozzle 4 is fed with the caking coal transported by coal gas, and the annular gap of the feed nozzle 4 is fed with the cooling medium nitrogen.

[0084] A solid heat carrier inlet pipe 5 is provided at the lower part of the pyrolysis reaction device 1 , and a solid outlet of the gas-solid separation device 2 is connected to the solid heat carrier inlet pipe 5 .

[0085] The solid heat carrier inlet pipe 5 is one in number and is installed obliquely downward at an angle of 45 degrees to the horizontal direction.

[0086] The pyrolysis reaction device 1 is provided with a ring pipe in the horizontal direction along the inner wall, the inlet of the ring pipe is connected to the outlet of the solid heat carrier inlet pipe 5, and the position of the ring pipe facing the inner side of the pyrolysis reaction device 1 is provided with a slit; the ring pipe has a section.

[0087] A fluidizing gas pipe 6 is further provided at the bottom of the pyrolysis reaction device 1 , and a gas distribution plate 7 is provided inside the pyrolysis reaction device 1 and above the fluidizing gas pipe 6 .

[0088] Embodiment 2:

[0089] This embodiment provides a caking coal pyrolysis device. The structural schematic diagram of the device is as follows: Figure 3 As shown, it includes a pyrolysis reaction device 1, a gas-solid separation device 2 and an oil-gas recovery device 3 which are connected in sequence, the solid outlet of the gas-solid separation device 2 is connected to the inlet of the pyrolysis reaction device 1, and the pyrolysis reaction device 1 is provided with a jacketed feed nozzle 4.

[0090] The structural schematic diagram of the inlet part of the pyrolysis reaction device is as follows Figure 4 As shown, the feed nozzles 4 are arranged on the lower side of the pyrolysis reaction device 1, and there are two of them, which are symmetrically installed at an angle of 45 degrees to the vertical direction.

[0091] The inner tube of the feed nozzle 4 is fed with nitrogen-transported caking coal, and the annular gap of the feed nozzle 4 is fed with cooling medium circulating water.

[0092] A solid heat carrier inlet pipe 5 is provided at the lower part of the pyrolysis reaction device 1, and the solid outlet of the gas-solid separation device 2 is connected to the solid heat carrier inlet pipe 5; a solid heat carrier regenerator 10 is provided between the solid outlet of the gas-solid separation device 2 and the solid heat carrier inlet pipe 5.

[0093] There are two solid heat carrier inlet pipes 5 , which are symmetrically installed obliquely downward and form an angle of 30 degrees with the horizontal direction.

[0094] The pyrolysis reaction device 1 is provided with a ring pipe in the horizontal direction along the inner wall, the inlet of the ring pipe is connected to the outlet of the solid heat carrier inlet pipe 5, and the ring pipe is provided with a slit at a position facing the inner side of the pyrolysis reaction device 1; the ring pipe is provided with two sections, which correspond to two solid heat carrier inlet pipes 5 respectively.

[0095] A fluidizing gas pipe 6 is further provided at the bottom of the pyrolysis reaction device 1 , and a gas distribution plate 7 is provided inside the pyrolysis reaction device 1 and above the fluidizing gas pipe 6 .

[0096] Embodiment 3:

[0097] The present embodiment provides a caking coal pyrolysis device, which includes a pyrolysis reaction device 1, a gas-solid separation device 2 and an oil and gas recovery device 3 connected in sequence, the solid outlet of the gas-solid separation device 2 is connected to the inlet of the pyrolysis reaction device 1, and the pyrolysis reaction device 1 is provided with a jacketed feed nozzle 4.

[0098] The structural schematic diagram of the inlet part and the variable diameter section of the pyrolysis reaction device is as follows Figure 5 As shown, the feed nozzles 4 are arranged on the lower side of the pyrolysis reaction device 1 , and there are four of them, which are evenly and symmetrically installed at an angle of 20 degrees to the vertical direction.

[0099] The inner tube of the feed nozzle 4 is fed with the binding coal conveyed by flue gas, and the annular gap of the feed nozzle 4 is fed with the cooling medium gas.

[0100] A solid heat carrier inlet pipe 5 is provided at the lower part of the pyrolysis reaction device 1, and the solid outlet of the gas-solid separation device 2 is connected to the solid heat carrier inlet pipe 5; a solid heat carrier regenerator 10 is provided between the solid outlet of the gas-solid separation device 2 and the solid heat carrier inlet pipe 5.

[0101] There are four solid heat carrier inlet pipes 5 , which are evenly and symmetrically distributed obliquely downward and form an angle of 20 degrees with the horizontal direction.

[0102] The pyrolysis reaction device 1 is an entrained flow reactor, the middle part of the pyrolysis reaction device 1 is a reducing section 8, the diameter of the reducing section 8 is larger than the diameters of the lower and upper parts; the lower part of the reducing section 8 is provided with a return pipe 9, and the return pipe 9 is connected to the solid heat carrier regenerator 10.

[0103] A fluidizing gas pipe 6 is further provided at the bottom of the pyrolysis reaction device 1 , and a gas distribution plate 7 is provided inside the pyrolysis reaction device 1 and above the fluidizing gas pipe 6 .

[0104] Embodiment 4:

[0105] This embodiment provides a caking coal pyrolysis device. The structure of the device refers to the structure in Example 3, except that: the device includes two pyrolysis reaction devices 1 arranged in parallel, and its structural schematic diagram is shown in FIG. Figure 6 As shown, the top outlets of the two pyrolysis reaction devices 1 are merged and connected to the inlet of the gas-solid separation device 2 .

[0106] Embodiment 5:

[0107] This embodiment provides a caking coal pyrolysis method, which is carried out in the device of embodiment 2 and includes the following steps:

[0108] (1) A caking coal raw material with a particle size of 150 μm is fed into a feed nozzle 4 under coal gas transportation, and a cooling medium nitrogen is passed through the annular gap of the feed nozzle 4 to maintain the feed temperature of the caking coal below 200° C. After the caking coal enters the pyrolysis reaction device 1, it is quickly mixed with the solid heat carrier powder coke to undergo a pyrolysis reaction. The pyrolysis reaction temperature is 500° C., the pressure is 0.2 MPaG, and the reaction time is 3 s to obtain a pyrolysis product;

[0109] (2) The pyrolysis product obtained in step (1) is subjected to gas-solid separation, and the obtained gas phase product is subjected to oil-gas separation to obtain coal gas and coal tar products. The obtained solid phase product powder coke part is subjected to combustion reaction with air, and the temperature is raised to 700° C. and returned to step (1) as a heat carrier for the pyrolysis reaction.

[0110] In this embodiment, the device is used to pyrolyze the bonding coal. Since the raw materials will not be bonded during feeding, the device can operate continuously and stably, and the energy utilization efficiency of the bonding coal can reach more than 80%.

[0111] Embodiment 6:

[0112] This embodiment provides a caking coal pyrolysis method, which is carried out in the device of embodiment 2 and includes the following steps:

[0113] (1) A caking coal raw material with a particle size of 300 μm is fed into a feed nozzle 4 under nitrogen transport, and a cooling medium circulating water is passed through the annular gap of the feed nozzle 4 to maintain the feed temperature of the caking coal below 200° C. After the caking coal enters the pyrolysis reaction device 1, it is quickly mixed with the solid heat carrier powder coke to undergo a pyrolysis reaction. The pyrolysis reaction is performed at 400° C., a pressure of 0.5 MPaG, and a reaction time of 5 seconds to obtain a pyrolysis product;

[0114] (2) The pyrolysis product obtained in step (1) is subjected to gas-solid separation, and the obtained gas phase product is subjected to oil-gas separation to obtain coal gas and coal tar products. The obtained solid phase product powder coke part is subjected to combustion reaction with air, and the temperature is raised to 600° C. and returned to step (1) as a heat carrier for the pyrolysis reaction.

[0115] In this embodiment, the device is used to pyrolyze the bonding coal. Since the raw materials will not be bonded during feeding, the device can operate continuously and stably, and the energy utilization efficiency of the bonding coal can reach more than 80%.

[0116] Embodiment 7:

[0117] This embodiment provides a caking coal pyrolysis method, which is carried out in the device of embodiment 3 and includes the following steps:

[0118] (1) A caking coal raw material with a particle size of 50 μm is conveyed into a feed nozzle 4 under flue gas transport. A cooling medium circulating water is passed through the annular gap of the feed nozzle 4 to maintain the feed temperature of the caking coal below 200° C. After the caking coal enters the pyrolysis reaction device 1, it is quickly mixed with a solid heat carrier. The solid heat carrier includes coke powder, silica sand and porcelain balls, and a pyrolysis reaction occurs. The pyrolysis reaction is 650° C., the pressure is 0.1 MPaG, and the reaction time is 0.5 s to obtain a pyrolysis product. During the pyrolysis reaction, the silica sand and porcelain balls are separated when they pass through the reducing section 8 and are used as a heat carrier again;

[0119] (2) The pyrolysis product obtained in step (1) is subjected to gas-solid separation, and the obtained gas phase product is subjected to oil-gas separation to obtain coal gas and coal tar products. The obtained solid phase product powder coke part is subjected to combustion reaction with air, and the temperature is raised to 800° C. and returned to step (1) as a heat carrier for the pyrolysis reaction.

[0120] In this embodiment, the device is used to pyrolyze the bonding coal. Since the raw materials will not be bonded during feeding, the device can operate continuously and stably, and the energy utilization efficiency of the bonding coal can reach more than 80%.

[0121] From the above embodiments, it can be seen that the present invention improves the feeding part of the pyrolysis reaction device, controls the temperature of the pulverized coal in the feeding nozzle, avoids the clogging of the nozzle due to the adhesion of the bonding coal due to the high temperature during feeding, and realizes the efficient utilization of the bonding coal: the device can achieve instant full mixing and heating with the solid heat carrier after feeding, avoids staying in the bonding temperature range for a long time, and realizes rapid pyrolysis; the structural design of the pyrolysis reaction device facilitates the use and separation of non-bonding solid heat carriers, and is conducive to the pyrolysis reaction of bonding coal.

[0122] The applicant declares that the present invention uses the above embodiments to illustrate the detailed devices and methods of the present invention, but the present invention is not limited to the above detailed devices and methods, that is, it does not mean that the present invention must rely on the above devices and methods to be implemented. Those skilled in the art should understand that any improvement of the present invention, equivalent replacement of the device of the present invention, addition of auxiliary structures, selection of specific methods, etc., all fall within the protection scope and disclosure scope of the present invention.

Claims

1. A caking coal pyrolysis device, characterized in that: The device comprises a pyrolysis reaction device, a gas-solid separation device and an oil and gas recovery device which are connected in sequence, wherein the solid outlet of the gas-solid separation device is connected to the inlet of the pyrolysis reaction device, the pyrolysis reaction device is provided with a jacketed feed nozzle, and the feed nozzle is arranged at the bottom and / or lower part of the pyrolysis reaction device, the lower part of the pyrolysis reaction device is provided with a solid heat carrier inlet pipe, the pyrolysis reaction device is provided with a ring pipe in the horizontal direction along the inner wall, the inlet of the ring pipe is connected to the solid heat carrier inlet pipe, the ring pipe is provided with a slit at a position facing the inner side of the pyrolysis reaction device, and the bottom of the pyrolysis reaction device is also provided with a fluidizing gas pipe.

2. The caking coal pyrolysis device according to claim 1, characterized in that: The number of the feed nozzle is at least one.

3. The caking coal pyrolysis device according to claim 1, characterized in that The installation direction of the feed nozzle is vertically upward, obliquely upward or horizontally.

4. The caking coal pyrolysis device according to claim 1, characterized in that The included angle between the installation angle of the feed nozzle and the vertical direction is 0-90°.

5. The caking coal pyrolysis device according to claim 1, characterized in that: The inner tube of the jacketed feed nozzle is fed with the bonding coal conveyed by the conveying gas, and the annular gap of the jacketed feed nozzle is fed with the cooling medium.

6. The caking coal pyrolysis device according to claim 1, characterized in that: The solid outlet of the gas-solid separation device is connected to the solid heat carrier inlet pipe.

7. The caking coal pyrolysis device according to claim 1, characterized in that A solid heat carrier regenerator is provided between the solid outlet of the gas-solid separation device and the solid heat carrier inlet pipe.

8. The caking coal pyrolysis device according to claim 1, characterized in that The number of the solid heat carrier inlet pipe is at least one.

9. The caking coal pyrolysis device according to claim 1, characterized in that The annular pipe is provided with at least one section, and the number of the annular pipes is the same as the number of the solid heat carrier inlet pipes.

10. The caking coal pyrolysis device according to claim 1, characterized in that: The solid heat carrier inlet pipe is installed in a horizontal direction or obliquely downward.

11. The caking coal pyrolysis device according to claim 1, characterized in that The included angle between the installation angle of the solid heat carrier inlet pipe and the horizontal direction is less than 90°.

12. The caking coal pyrolysis device according to claim 1, characterized in that: The pyrolysis reaction device comprises an entrained flow reactor.

13. The caking coal pyrolysis device according to claim 1, characterized in that The middle part of the pyrolysis reaction device is a diameter-changing section, and the diameter of the diameter-changing section is larger than the diameters of the lower part and the upper part.

14. The caking coal pyrolysis device according to claim 13, characterized in that A return pipe is provided at the lower part of the diameter-changing section, and the return pipe is connected to the solid heat carrier regenerator.

15. The caking coal pyrolysis device according to claim 1, characterized in that: A gas distribution plate is arranged inside the pyrolysis reaction device and above the fluidizing gas pipe.

16. A method for pyrolyzing caking coal using the device according to any one of claims 1 to 15, characterized in that: The method comprises: (1) The caking coal raw material is heat exchanged at the feed nozzle, and then undergoes a pyrolysis reaction to obtain a pyrolysis product; (2) The pyrolysis product obtained in step (1) is subjected to gas-solid separation, the obtained gas phase product is subjected to oil-gas separation, and the obtained solid phase product is returned to step (1) as a heat carrier for the pyrolysis reaction.

17. The method according to claim 16, characterized in that The caking coal raw material in step (1) is transported by conveying gas.

18. The method according to claim 17, characterized in that The conveying gas includes any one of coal gas, nitrogen or flue gas, or a combination of at least two of them.

19. The method according to claim 16, characterized in that The particle size of the caking coal raw material in step (1) is 50 to 300 μm.

20. The method according to claim 16, characterized in that The heat exchange in step (1) is carried out in a jacketed feed nozzle.

21. The method according to claim 20, characterized in that A cooling medium is introduced into the annular gap of the jacketed feed nozzle.

22. The method according to claim 16, characterized in that After the heat exchange in step (1), the temperature of the caking coal raw material is below 200°C.

23. The method according to claim 16, characterized in that The temperature of the pyrolysis reaction in step (1) is 400-650°C.

24. The method according to claim 17, characterized in that The pressure of the pyrolysis reaction in step (1) is 0 to 0.5 MPaG.

25. The method according to claim 17, characterized in that The pyrolysis reaction time of step (1) is 0.5 to 5 seconds.

26. The method according to claim 16, characterized in that The gas-solid separation in step (2) obtains char powder and pyrolysis oil gas.

27. The method according to claim 26, characterized in that Part of the coke powder is returned to step (1) via the solid heat carrier regenerator as a heat carrier for the pyrolysis reaction.

28. The method according to claim 27, characterized in that The powdered coke undergoes a combustion reaction in the solid heat carrier regenerator and the temperature rises to 600-800°C.

29. The method according to claim 16, characterized in that The heat carrier of the pyrolysis reaction also includes any one of silica sand, porcelain balls or ores, or a combination of at least two of them.

30. The method according to claim 29, characterized in that The silica sand and / or porcelain balls are separated when passing through the diameter-changing section of the pyrolysis reaction device and returned to the solid heat carrier regenerator.

Images