Conveying bed grading dry distillation coking reactor

Abstract

The utility model discloses a conveying bed grading dry distillation coking reactor which comprises at least two conveying bed sections, at least one conveying bed section is a conveying bed expanding section, and the through-flow area of the conveying bed expanding section is larger than that of the other conveying bed sections. The conveying bed section located on the lower side is a conveying bed lower section, and the conveying bed lower section is provided with a raw material inlet, a heavy oil inlet, a heat carrier inlet and a fluidizing gas inlet. According to the utility model, the raw material airflow speed is reduced due to the increase of the through-flow area at the expanded section of the conveying bed, so that the residence time and the reaction time of the large-particle-size raw material are prolonged. The raw materials with small particle sizes are light in weight, the flow speed of the raw materials can be reduced in the expanded section of the conveying bed, but the raw materials cannot slide down, namely, the raw materials with different particle sizes are different in retention time and reaction time in the reactor, so that low yield and incomplete reaction of the raw materials with large particle sizes caused by over-reaction of the raw materials with small particle sizes are avoided; the raw material utilization rate is low, and the oil yield and the oil yield are improved.

Description

Technical Field

[0001] The utility model relates to the technical field of retorting equipment, and more specifically, to a conveying bed staged retorting coking reactor. Background Art

[0002] Retorting is a reaction process in which solids or organic substances are heated and decomposed under anaerobic conditions. The result of retorting is the generation of various gases, vapors, and solid residues. The mixture of gases and vapors is cooled and separated into gases and liquids. Retorting is a complex chemical reaction process, including dehydration, pyrolysis, dehydrogenation, thermal condensation, hydrogenation, coking, and other reactions. The production purpose of the retorting process is to produce as many high-value liquid products (such as gasoline, diesel, etc.) and sub-high-value fuel gases (including methane, carbon monoxide, hydrogen, etc.) as possible from low-value solids through retorting.

[0003] The retorting process is an ancient production process, originally used to provide fuel oil for lighting. With technological progress, the retorting process has developed. New process technologies and methods have emerged continuously to achieve higher energy utilization efficiency, maximum high-value liquid product yield, better environmental protection, and other technical and economic indicators.

[0004] The existing retorting processes mainly use low-rank lump coal as raw materials. With the development of fully mechanized coal mining technology, the proportion of fine coal has increased, resulting in low raw material utilization rate and oil yield. This is because when raw materials of different particle sizes are retorted, although smaller particle sizes produce more oil, they further increase the particle size ratio (the particle size ratio refers to the ratio of the particle size of large particle raw materials to the particle size of small particle raw materials). Generally, the particle size ratio of lump raw materials is less than 10, while the particle size ratio of fine raw materials can reach about 100. Due to the large particle size ratio of fine raw materials, the difference in complete retorting time is further increased, affecting the raw material utilization rate and oil yield.

[0005] Therefore, how to improve the raw material utilization rate, control the complete retorting time of different particle sizes, comprehensively avoid oil and gas losses, improve the oil yield, and maximize the oil and gas production has become an urgent technical problem for those skilled in the art. Summary of the Utility Model

[0006] In view of this, the purpose of the present utility model is to provide a conveying bed staged retorting coking reactor to improve the raw material utilization rate, control the complete retorting time of different particle sizes, comprehensively avoid oil and gas losses, improve the oil yield, and maximize the oil and gas production.

[0007] To achieve the above purpose, the present utility model provides the following technical solutions:

[0008] A conveying bed staged dry distillation coking reactor, comprising at least two conveying bed sections connected in series from bottom to top, wherein at least one of the conveying bed sections is a conveying bed expansion section, and the flow-through area of the conveying bed expansion section is larger than that of the other conveying bed sections;

[0009] The conveying bed section at the lower side is the lower conveying bed section, and the lower conveying bed section is provided with a raw material inlet, a heavy oil inlet, a heat carrier inlet and a fluidizing gas inlet.

[0010] Optionally, in the above-mentioned conveying bed staged dry distillation coking reactor, there are three conveying bed sections, and the conveying bed expansion section is located in the middle, the lower conveying bed section is located below the conveying bed expansion section, and the upper side of the conveying bed expansion section is the upper conveying bed section.

[0011] Optionally, in the above-mentioned conveying bed staged dry distillation coking reactor, the coarse powder feed inlet is located below the fine powder feed inlet.

[0012] Optionally, in the above-mentioned conveying bed staged dry distillation coking reactor, the heavy oil inlet is arranged between the fine powder feed inlet and the coarse powder feed inlet;

[0013] Alternatively, the heavy oil inlet and the fine powder feed inlet are coaxially arranged.

[0014] Optionally, in the above-mentioned conveying bed staged dry distillation coking reactor, the heavy oil inlet is provided with a heavy oil atomizer.

[0015] Optionally, in the above-mentioned conveying bed staged dry distillation coking reactor, the flow-through area of the conveying bed expansion section is larger than that of the upper conveying bed section.

[0016] Optionally, in the above-mentioned conveying bed staged dry distillation coking reactor, one end of the upper conveying bed section far from the conveying bed expansion section is provided with a gas-solid separator, and the gas-solid separator has an oil-gas outlet and a solid outlet.

[0017] Optionally, in the above-mentioned conveying bed staged dry distillation coking reactor, the gas-solid separator is a cyclone separator or an umbrella separator.

[0018] Optionally, in the above-mentioned conveying bed staged dry distillation coking reactor, the cross-sections of the lower conveying bed section, the conveying bed expansion section and the upper conveying bed section are all circular; and / or, [[ID=32]]

[0019] The particle size range of the raw materials entering the lower conveying bed section from the raw material inlet is 0 - 3000um.

[0020] Optionally, in the above-mentioned conveying bed staged dry distillation coking reactor, when the particle size range of the raw materials entering the lower conveying bed section from the raw material inlet is 0 - 100um, the dry distillation time is within 1s;

[0021] When the particle size range of the raw materials entering the lower section of the conveying bed from the raw material inlet is 100 - 500 um, the dry distillation time is within 1 s - 3 s.

[0022] When the particle size range of the raw materials entering the lower section of the conveying bed from the raw material inlet is 500 - 1000 um, the dry distillation time is within 3 s - 5 s.

[0023] In the conveying bed staged dry distillation coking reactor provided by the present utility model, the raw materials and the heat carrier enter the lower section of the conveying bed through the raw material inlet and the heat carrier inlet respectively, and under the action of the fluidizing gas entering from the fluidizing gas inlet, rapid mixing heat transfer is carried out, and they ascend along the enlarged section of the conveying bed and the upper section of the conveying bed in sequence. The gas flow velocity decreases in the enlarged section of the conveying bed due to the increase in the flow-through area, so that the raw materials with larger particle sizes slide downward and circulate due to gravity, prolonging the residence time of the raw materials with larger particle sizes. The larger the particle size, the longer the residence time and the reaction time. For the raw materials with smaller particle sizes, due to their smaller weight, although their flow velocity will also decrease in the enlarged section of the conveying bed, they will not slide downward. That is, according to the different particle sizes of the raw materials, the residence time and reaction time in the reactor are different, thus avoiding the low output caused by over-reaction of the raw materials with smaller particle sizes and the low raw material utilization rate caused by incomplete reaction of the raw materials with larger particle sizes, and improving the oil output and oil yield.

[0024] The fine powder raw materials with smaller particle sizes are in direct contact with the atomized heavy oil entering from the heavy oil inlet, and rapid mixing heat transfer is carried out under the combined action of the fluidizing gas and the heat carrier and they ascend along the enlarged section of the conveying bed and the upper section of the variable-diameter conveying bed. The atomized oil plays a role in reducing the dust content of the fine powder raw materials, so that the unusable ultra-fine raw material powder can be used for dry distillation to produce oil, and the organic matter contained in the ultra-fine powder raw materials undergoes pyrolysis reaction, improving the utilization rate of the raw materials. Description of the Drawings

[0025] In order to more clearly illustrate the technical solutions in the embodiments of the present utility model or the prior art, the following will briefly introduce the drawings required for the description of the embodiments or the prior art. Obviously, the drawings in the following description are only some embodiments of the present utility model. For those of ordinary skill in the art, without creative efforts, other drawings can also be obtained based on these drawings.

[0026] Figure 1 It is a schematic structural diagram of the conveying bed staged dry distillation coking reactor disclosed in the embodiments of the present utility model.

[0027] The meanings of the various reference numerals in the drawings are as follows:

[0028] 101 - Upper section of the conveying bed; 102 - Enlarged section of the conveying bed; 103 - Fine powder feed inlet; 104 - Coarse powder feed inlet; 105 - Fluidizing gas inlet; 106 - Oil and gas outlet; 107 - Gas-solid separator; 108 - Solid outlet; 109 - Heavy oil atomizer; 110 - Heat carrier inlet; 111 - Lower section of the conveying bed. Detailed implementation mode

[0029] The core of the present utility model lies in providing a conveying bed staged dry distillation coking reactor to improve the raw material utilization rate, control the complete dry distillation time of different particle sizes, comprehensively avoid oil and gas losses, increase the oil yield, and maximize the oil and gas production.

[0030] Hereinafter, the embodiments will be described with reference to the drawings. In addition, the embodiments shown below do not limit the content of the utility model described in the claims in any way. Moreover, all the contents of the configurations shown in the following embodiments are not limited to those necessary for the solution of the utility model described in the claims. It should be noted that for the sake of description, only the parts related to the relevant utility model are shown in the drawings. Without conflict, the embodiments in the present utility model and the features in the embodiments can be combined with each other.

[0031] In the prior art, regarding the preparation of pulverized coal raw materials, it is impossible to prepare them into a uniform particle size, and there must be a certain particle size range in the prepared raw materials. The particle size of the pulverized coal raw materials is related to the reaction time. The larger the particle size, the longer the reaction time; on the contrary, the smaller the particle size, the shorter the reaction time.

[0032] Currently, in engineering, the process is generally carried out according to the average particle size, so there are problems that the small particle size raw materials over-react and the large particle size raw materials do not react completely. Among them, the over-reaction of the small particle size raw materials results in insufficient utilization rate of the reactor and low throughput; the incomplete reaction of the large particle size raw materials leads to large raw material consumption and low oil yield.

[0033] The embodiment of the present utility model discloses a conveying bed staged dry distillation coking reactor, which can classify raw materials with different particle sizes in the reactor, so that the reaction time of the large particle size raw materials is longer, while the reaction time of the small particle size is shorter, to improve the raw material utilization rate, control the complete dry distillation time of different particle sizes, comprehensively avoid oil and gas losses, increase the oil yield, and maximize the oil and gas production.

[0034] As Figure 1 shown, the conveying bed staged dry distillation coking reactor disclosed in the embodiment of the present utility model includes at least two conveying bed sections connected in series from bottom to top, and at least one of the conveying bed sections is the enlarged section 102 of the conveying bed. In this embodiment, the flow-through area of the enlarged section 102 of the conveying bed is larger than that of other conveying bed sections, so that the flow rate of the large particle size raw materials in the enlarged section 102 of the conveying bed is slower, or even turns back, increasing the residence time and reaction time of the large particle size raw materials.

[0035] Taking three conveying bed sections as an example, from bottom to top, the three conveying bed sections are the lower conveying bed section 111, the middle conveying bed section, and the upper conveying bed section 101. The lower conveying bed section 111, the middle conveying bed section, and the upper conveying bed section 101 can be designed as an integral structure, or can be connected by connection means such as welding.

[0036] In this embodiment, the middle conveying bed section can be designed as the enlarged conveying bed section 102, that is, the enlarged conveying bed section 102 is located in the middle conveying bed section among the three sections. The flow-through area of the enlarged conveying bed section 102 should be at least larger than the flow-through area of the lower conveying bed section 111. The enlarged conveying bed section 102 can be arranged between the lower conveying bed section 111 and the upper conveying bed section 101, that is, the enlarged conveying bed section 102 serves as the variable-diameter middle conveying bed section. The flow-through area of the enlarged conveying bed section 102 can also be larger than the flow-through area of the upper conveying bed section 101, that is, there are relatively obvious three-section changes in the lower conveying bed section 111, the enlarged conveying bed section 102, and the upper conveying bed section 101, and the enlarged conveying bed section 102 with a larger flow-through area is located in the middle section.

[0037] The cross-sections of the lower conveying bed section 111, the enlarged conveying bed section 102, and the upper conveying bed section 101 can all be circular, or can be designed into other shapes according to requirements.

[0038] It should be noted that if the flow-through area of the enlarged conveying bed section 102 is close to or equal to the flow-through area of the upper conveying bed section 101, then there are no relatively obvious three-section changes in the lower conveying bed section 111, the enlarged conveying bed section 102, and the upper conveying bed section 101, and the enlarged conveying bed section 102 and the upper conveying bed section 101 with a larger flow-through area are both visually located in the upper section.

[0039] Those skilled in the art can understand that those skilled in the art can also design the conveying bed sections into other numbers according to actual needs, not limited to the above 3 sections. Of course, the number of the enlarged conveying bed sections 102 is not limited to one section, and can also be designed into multiple sections. Conveying bed sections with a flow-through area smaller than that of the enlarged conveying bed section 102 can be designed between multiple enlarged conveying bed sections 102 to separate the two enlarged conveying bed sections 102.

[0040] The lower section 111 of the conveying bed is provided with a raw material inlet, a heavy oil inlet, a heat carrier inlet 110 and a fluidizing gas inlet 105. The raw material inlet is used for introducing pulverized coal raw materials (referred to as raw materials). Specifically, the pulverized coal raw materials can be added into the reactor through the raw material inlet by a feeding system. The heavy oil inlet is used for spraying heavy oil. Specifically, a heavy oil atomizer 109 can be arranged at the heavy oil inlet to atomize the heavy oil sprayed into the reactor into atomized oil, so as to increase the contact area with the ultrafine powder material. The heavy oil can be selected from the heavy part of the dry distillation pyrolysis oil produced by dry distillation and is recycled through the heavy oil inlet for washing and dust removal of the fine powder raw materials. At the same time, the heavy oil thermally cracks into lighter oil products with higher value at high temperature.

[0041] The heat carrier inlet 110 is used for introducing a heat carrier into the reactor. The heat carrier is used for heating the raw materials and heating the raw materials to the reaction temperature. The fluidizing gas inlet 105 is used for passing fluidizing gas so as to accelerate the mixing of the raw materials and the heat carrier and convey them downstream.

[0042] In the conveying bed staged dry distillation coking reactor disclosed in the embodiment of the present utility model, the raw materials and the heat carrier respectively enter the lower section 111 of the conveying bed through the raw material inlet and the heat carrier inlet 110, and under the action of the fluidizing gas entering from the fluidizing gas inlet 105, rapid mixing heat transfer is carried out, and they ascend along the conveying bed expansion section 102 and the upper section of the conveying bed in sequence. The air flow velocity decreases in the conveying bed expansion section 102 due to the increase in the flow-through area, so that the raw materials with larger particle sizes slide downward and circulate due to gravity, prolonging the residence time of the large-particle-size raw materials. The larger the particle size, the longer the residence time and the reaction time. For the raw materials with smaller particle sizes, due to their smaller weight, although their flow velocity will also decrease in the conveying bed expansion section 102, they will not slide downward. That is, according to the different particle sizes of the raw materials, the residence time and reaction time in the reactor are different, thus avoiding the low output caused by over-reaction of the small-particle-size raw materials and the low raw material utilization rate caused by incomplete reaction of the large-particle-size raw materials, and improving the oil output and oil yield.

[0043] The fine powder raw materials with smaller particle sizes are in direct contact with the atomized heavy oil entering from the heavy oil inlet, and rapid mixing heat transfer is carried out under the combined action of the fluidizing gas and the heat carrier and they ascend along the conveying bed expansion section 102 and the upper section of the variable-diameter conveying bed. The atomized oil plays a role in reducing the dust content of the fine powder raw materials. In this way, the unusable ultrafine raw material powder can be used for dry distillation to produce oil, and the organic matter contained in the ultrafine powder raw materials undergoes a pyrolysis reaction, improving the utilization rate of the raw materials.

[0044] In a specific embodiment of the present utility model, the raw material inlet includes a fine powder inlet 103 and a coarse powder inlet 104. The particle size of the raw material entering the lower section 111 of the conveying bed through the fine powder inlet 103 is smaller than that of the raw material entering the lower section 111 of the conveying bed through the coarse powder inlet 104. The coarse powder inlet 104 can be arranged below the fine powder inlet 103. Since the particle size of the raw material entering the fine powder inlet 103 is smaller, and it is arranged above the coarse powder inlet 104, it can avoid being blocked by the raw material entering through the coarse powder inlet 104, and can quickly enter the enlarged section 102 of the conveying bed and be conveyed downstream through the enlarged section 102 of the conveying bed.

[0045] Furthermore, the heavy oil inlet can be arranged between the fine powder inlet 103 and the coarse powder inlet 104. It should be noted that the heavy oil inlet and the fine powder inlet 103 can also be coaxially arranged, that is, the pipeline of the heavy oil inlet and the pipeline of the fine powder inlet 103 can be coaxially nested. For example, the pipeline of the heavy oil inlet is located in the inner circle, and the pipeline of the fine powder inlet 103 is arranged in the outer circle. Of course, it can also be set in the reverse. It only needs to arrange the heavy oil inlet adjacent to the fine powder inlet 103, so that the fine powder raw material sprayed into the reactor through the fine powder inlet 103 can be timely wrapped by the atomized heavy oil.

[0046] In a specific embodiment of the present utility model, a gas-solid separator 107 is arranged at one end of the upper section 101 of the conveying bed away from the enlarged section 102 of the conveying bed. The gas-solid separator 107 has an oil-gas outlet 106 and a solid outlet 108. The gas-solid separator 107 can separate the oil-gas and solids in the reaction products. The gas-solid separator 107 can be a cyclone separator or an umbrella separator, or other types of gas-solid separators can be selected according to requirements. The specific structure of the gas-solid separator is not limited in this embodiment.

[0047] The coarse powder from the feeding system (the raw material entering through the coarse powder inlet 104 is simply referred to as coarse powder) passes through the coarse powder inlet 104, the fine powder (the raw material entering through the fine powder inlet 103 is simply referred to as fine powder) passes through the fine powder inlet 103 and the heat carrier enters the lower section 111 of the conveying bed through the heat carrier inlet 110 to carry out rapid mixing and heat transfer and move upward along the conveying bed. During the upward movement, the organic matter contained in the raw material undergoes a dry distillation reaction. Due to the wide screening of the particle size distribution of the raw material, the particle size range is 0 - 3000um, and the maximum diameter of the large particle size raw material and the small particle size raw material differ by hundreds of times, and the complete dry distillation time difference is large. In order to enable the raw materials of different particle sizes to achieve complete dry distillation, the gas velocity decreases when the raw material passes through the enlarged section 102 of the conveying bed, the residence time of the large particle size raw material is extended, and then it enters the gas-solid separator 107 through the upper section 101 of the conveying bed to achieve rapid gas-solid separation, and the liquid products of the dry distillation reaction are retained to the greatest extent.

[0048] The staged dry distillation coking reactor of the conveyor bed disclosed in the embodiments of the present utility model can preferably handle raw materials with a particle size range of 0 to 1000 um, and is also applicable to other particle size ranges within 0 to 3000 um, such as 0 to 100 um, 0 to 200 um, 0 to 500 um, etc.

[0049] When the particle size range of the raw materials entering the lower section 111 of the conveyor bed from the raw material inlet is 0 to 100 um, the dry distillation time can be controlled within 1 s; when the particle size range of the raw materials entering the lower section 111 of the conveyor bed from the raw material inlet is 100 to 500 um, the dry distillation time can be controlled within 1 s - 3 s; when the particle size range of the raw materials entering the lower section 111 of the conveyor bed from the raw material inlet is 500 to 1000 um, the dry distillation time can be controlled within 3 s - 5 s. The dry distillation time is related to the flow rate of the raw materials in the reactor, and the flow rate of the raw materials is related to the flow-through area of the enlarged section 102 of the conveyor bed. Therefore, the flow-through area of the enlarged section 102 of the conveyor bed can be determined according to conditions such as different raw materials, the particle size distribution of the raw materials, and the time required to achieve complete dry distillation.

[0050] Example 1

[0051] A pulverized coal raw material was used as the test raw material, and a comparative dry distillation reaction was carried out using the staged dry distillation coking reactor of the conveyor bed disclosed in the embodiments of the present utility model and the staged dry distillation coking reactor in the prior art.

[0052] Table 1 Raw material utilization rate of pulverized coal dry distillation pilot test

[0053]

[0054] Table 2 Product distribution data of pulverized coal fluidized dry distillation pilot test

[0055]

[0056] It should be noted that in Table 2, the temperature range behind gasoline, diesel, and heavy oil is the distillation range of the oil product.

[0057] From the data in Table 1 and Table 2, it can be seen that by using the staged dry distillation coking reactor of the conveyor bed disclosed in the embodiments of the present utility model compared with the staged dry distillation coking reactor in the prior art, the raw material utilization rate increased from 87% to 98%, an increase of 11%. The total oil production increased from 9.6396% (i.e., 87% multiplied by 11.08%) to 11.0838% (i.e., 98% multiplied by 11.31%), an increase of 1.4442%. The quality of the oil products has also been greatly improved. The gasoline component increased by 5.6% (i.e., the difference between 24.6% and 19%), the diesel component increased by 24.46% (i.e., the difference between 71.66% and 47.2%), and the heavy oil decreased by 30.06% (i.e., the difference between 33.80% and 3.74%).

[0058] Example 2

[0059] Another pulverized coal raw material was used as the test raw material, and a comparative dry distillation reaction was carried out using the transport bed staged dry distillation coking reactor disclosed in the embodiments of the present invention and the transport bed staged dry distillation coking reactor in the prior art.

[0060] Table 3 Raw material utilization rate of the raw materials in the pilot test of pulverized coal dry distillation

[0061]

[0062] Table 4 Product distribution data of the pilot test of pulverized coal dry distillation

[0063]

[0064] It should be noted that in Table 4, the temperature ranges behind gasoline, diesel, and heavy oil are the distillation ranges of these oil products.

[0065] It can be seen from the data in Table 3 and Table 4 that by using the transport bed staged dry distillation coking reactor disclosed in the embodiments of the present invention compared with the transport bed staged dry distillation coking reactor in the prior art, the raw material utilization rate increased from 93% to 98%, an increase of 5%; the total oil production increased from 13.764% (i.e., 93% multiplied by 14.8%) to 13.916% (i.e., 98% multiplied by 14.2%), an increase of 0.152%; the quality of the oil products was greatly improved, the gasoline component increased by 6.1%, the diesel component increased by 24.3%, and the heavy oil decreased by 30.4%.

[0066] As shown in this application and the claims, unless the context clearly indicates an exception, words such as "a", "an", "one", and / or "the" are not specifically singular and may also include the plural. Generally speaking, the terms "comprising" and "including" only indicate the inclusion of the steps and elements that have been clearly identified, and these steps and elements do not constitute an exclusive list. The method or device may also include other steps or elements. Elements defined by the statement "including one..." do not exclude the existence of other identical elements in the process, method, commodity, or device including the element.

[0067] In the description of this application, unless otherwise clearly defined, words such as "set", "installed", "connected", etc. should be understood in a broad sense, and those skilled in the art can reasonably determine the specific meanings of the above words in this application in combination with the specific content of the technical solution.

[0068] In this specification, the various embodiments are described in a progressive manner. The key point of each embodiment is to illustrate the differences from other embodiments. The same and similar parts between the various embodiments can be referred to each other.

[0069] In this article, specific examples are used to elaborate on the principle and implementation mode of the present utility model. The description of the above embodiments is only used to help understand the method and its core idea of the present utility model. It should be pointed out that for those of ordinary skill in the art, without departing from the principle of the present utility model, several improvements and modifications can still be made to the present utility model, and these improvements and modifications also fall within the protection scope of the claims of the present utility model.

Claims

1. A conveying bed classification coking reactor by retorting, characterized in that It includes at least two conveying bed sections that are connected in sequence from bottom to top, where at least one of the conveying bed sections is a conveying bed expansion section (102), and the flow-through area of the conveying bed expansion section (102) is larger than that of the other conveying bed sections; The conveying bed section located at the lower side is the lower conveying bed section (111), and the lower conveying bed section (111) is provided with a raw material inlet, a heavy oil inlet, a heat carrier inlet (110), and a fluidizing gas inlet (105).

2. The conveying bed staged dry distillation coking reactor according to claim 1, wherein, There are three conveying bed sections, and the conveying bed expansion section (102) is located in the middle, the lower conveying bed section (111) is located below the conveying bed expansion section (102), and the upper side of the conveying bed expansion section (102) is the upper conveying bed section (101).

3. The conveying bed staged dry distillation coking reactor according to claim 1, characterized in that, The raw material inlet includes a fine powder feed port (103) and a coarse powder feed port (104), and the particle size of the raw material entering the lower conveying bed section (111) from the fine powder feed port (103) is smaller than that of the raw material entering the lower conveying bed section (111) from the coarse powder feed port (104).

4. The conveying bed classification coking reactor according to claim 3, characterized in that, The coarse powder feed port (104) is located below the fine powder feed port (103).

5. The conveying bed staged dry distillation coking reactor according to claim 4, wherein, The heavy oil inlet is arranged between the fine powder feed port (103) and the coarse powder feed port (104); Alternatively, the heavy oil inlet and the fine powder feed port (103) are coaxially arranged.

6. The conveying bed classification coking reactor as described in claim 1, wherein The heavy oil inlet is provided with a heavy oil atomizer (109).

7. The conveying bed staged dry distillation coking reactor according to claim 2, wherein, One end of the upper conveying bed section (101) far from the conveying bed expansion section (1 8. The conveying bed staged dry distillation coking reactor according to claim 7, characterized in that, ​ 9. The conveying bed staged dry distillation coking reactor according to claim 2, characterized in that, ​ ​ 10. The conveying bed staged coking reactor according to any one of claims 1-9, characterized in that, ​ ​ ​

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