Dry distillation system

Abstract

The invention belongs to the technical field of dry distillation, and discloses a dry distillation system, which comprises a furnace body and a transportation mechanism, the furnace body is internally provided with a first heating section, a second heating section, a cooling section and a coke quenching section which are of tunnel type structures; the conveying mechanism is movably arranged in the furnace body and can move to the first heating section, move to the second heating section from the first heating section, move to the cooling section from the second heating section and move to the coke quenching section from the cooling section, and the conveying mechanism is used for conveying raw coal; the first heating section, the second heating section, the cooling section and the coke quenching section are sequentially arranged in the conveying direction of the raw coal. According to the invention, the production efficiency and quality of products are improved.

Description

Technical Field

[0001] This invention relates to the field of dry distillation technology, and more particularly to a dry distillation system. Background Technology

[0002] Semi-coke, also known as semi-coke or coke powder, is produced by burning high-quality Jurassic coal lumps. As a new type of carbon material, it is gradually replacing metallurgical coke due to its characteristics of high fixed carbon content, high resistivity, high chemical activity, low ash content, low aluminum, low sulfur, and low phosphorus. It is widely used in the production of products such as calcium carbide, ferroalloys, ferrosilicon, and silicon carbide, and is gradually becoming an irreplaceable carbon material.

[0003] In existing technology, coal briquettes are burned using a vertical carbonization cylinder. The inlet of the cylinder is at the top, and the coal briquettes are poured into the cylinder from the top. They move downwards under their own weight, accumulating inside the cylinder and burning to produce semi-coke. However, due to the large diameter of the vertical carbonization cylinder, the temperature of the coal briquettes near the cylinder's axis is lower than that near the inner wall. This results in incomplete combustion of the coal briquettes near the axis, while the coal briquettes near the inner wall undergo over-burning, leading to uneven burning and affecting both the production efficiency and quality of the semi-coke. Summary of the Invention

[0004] The purpose of this invention is to provide a dry distillation system to solve the technical problems of low production efficiency and low quality of semi-coke in the prior art.

[0005] Based on the above concept, the technical solution adopted by this invention is as follows:

[0006] A dry distillation system, including:

[0007] The furnace body is provided with a first heating section, a second heating section, a cooling section, and a coke quenching section, all of which are tunnel-type structures.

[0008] The transport mechanism is movably placed inside the furnace body and can move to the first heating section, from the first heating section to the second heating section, from the second heating section to the cooling section, and from the cooling section to the quenching section. The transport mechanism is used to transport raw coal. The first heating section, the second heating section, the cooling section, and the quenching section are arranged sequentially along the conveying direction of the raw coal.

[0009] Optionally, the transport mechanism includes a power unit and a grate, the grate passing through the first heating section, the second heating section, the cooling section and the quenching section, the power unit being driven and connected to the grate and used to drive the grate to move, and the grate being used to support the raw coal;

[0010] Alternatively, the transport mechanism includes a kiln car, and the furnace body is provided with a track that passes through the first heating section, the second heating section, the cooling section, and the quenching section. The kiln car is movably disposed on the track along the extension direction of the track, and the kiln car is used to support the raw coal.

[0011] Optionally, the furnace body is annular, and the first heating section, the second heating section, the cooling section, and the quenching section are arranged sequentially along the circumference of the furnace body;

[0012] Alternatively, the furnace body is linear, and the first heating section, the second heating section, the cooling section, and the quenching section are arranged sequentially along the extension direction of the furnace body;

[0013] Alternatively, the furnace body may include a multi-layer tunnel structure arranged sequentially along the vertical direction. The dry distillation system may also include a lifting and transfer mechanism for transferring the raw coal between two adjacent tunnel structures. Each tunnel structure may include at least one processing section, which may be the first heating section, the second heating section, the cooling section, or the quenching section.

[0014] Optionally, the pyrolysis system further includes a porous medium burner disposed in the second heating section, and the pyrolysis system further includes a combustion-supporting device for inputting combustion-supporting gas into the second heating section, wherein the volume fraction of oxygen in the combustion-supporting gas is 21%-100%.

[0015] Optionally, the combustion-supporting device includes an oxygen-generating module, which has an oxygen outlet for discharging oxygen and a nitrogen outlet for discharging nitrogen. The oxygen outlet is connected to the second heating section, and the nitrogen outlet is connected to the quenching section.

[0016] Optionally, the furnace body is provided with a flue gas outlet, which is located in the first heating section and near the inlet of the first heating section. The flue gas from the first heating section, the second heating section and the cooling section is discharged through the flue gas outlet, and the flow direction of the flue gas is opposite to the conveying direction of the raw coal. The flue gas in the first heating section and the second heating section is used to heat the raw coal.

[0017] Optionally, the dry distillation system further includes a purification device, the inlet of which is connected to the flue gas outlet. The purification device is used to purify the flue gas to obtain a preset product, the preset product including tar and processed gas, and the processed gas including product gas and / or recycled gas.

[0018] The first outlet of the purification device is selectively connected to the second heating section, and the connection between the first outlet and the second heating section is used to input the recycled gas into the second heating section; and / or, the second outlet of the purification device is selectively connected to the quenching section, and the connection between the second outlet and the quenching section is used to input the recycled gas into the quenching section.

[0019] Optionally, the furnace body is provided with a gas passage, which selectively connects the second heating section and the cooling section;

[0020] The gas channel connects the second heating section and the cooling section to transport the cooling generated gas from the cooling section to the second heating section. The cooling generated gas includes water gas and / or water vapor.

[0021] Optionally, the dry distillation system further includes a heat exchange device, wherein the raw coal is heated in the second heating section to generate the main product, and the heat exchange device is located in the cooling section. The heat exchange device can absorb the heat of the main product in the cooling section, thereby reducing the temperature of the main product by 320°C-380°C.

[0022] Optionally, the distillation system further includes a water mist device installed in the furnace body and used to spray water mist onto the main product in the transport mechanism located in the cooling section.

[0023] The beneficial effects of this invention are:

[0024] The dry distillation system provided by this invention has a furnace body with a first heating section, a second heating section, a cooling section, and a quenching section arranged sequentially in a tunnel-like structure. Raw coal is transported within the furnace body via a conveying mechanism, ensuring that the transfer of raw coal between the first heating section, the second heating section, the cooling section, and the quenching section is all achieved through the conveying mechanism. The raw coal on the conveying mechanism does not experience significant relative movement, thus reducing the risk of cracking and breakage due to impact. This results in less broken coke and coke powder in the product, leading to higher quality main products (e.g., semi-coke). Furthermore, the flat distribution of raw coal on the conveying mechanism provides a larger heating area, improving the heating efficiency of the raw coal. The thickness of the raw coal is also not excessive, allowing heat to be better transferred to the interior of the raw coal during the heating process, reducing the probability of "short circuits" and "uneven burning," improving the uniformity of the temperature field within the furnace body, and further enhancing the quality of the main product.

[0025] Furthermore, due to the change in transportation methods, the limitation on the size of lump coal has been eliminated, allowing the use of inexpensive small-diameter coal. This enables coal of all sizes to be heated and decomposed evenly and quickly, without the problems of "short circuit" and "uneven burning".

[0026] In addition, this invention transforms stacked distillation into sheet distillation. The slicing process allows for precise control of temperature and atmosphere throughout the entire process. With the adoption of a matching DCS control system, the level of automation is high, ensuring safe and stable production and controllable product quality. Attached Figure Description

[0027] To more clearly illustrate the technical solutions in the embodiments of the present invention, the accompanying drawings used in the description of the embodiments of the present invention will be briefly introduced below. Obviously, the accompanying drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on the content of the embodiments of the present invention and these drawings without creative effort.

[0028] Figure 1 This is a first schematic diagram of the distillation system provided in an embodiment of the present invention;

[0029] Figure 2 This is a first structural schematic diagram of the furnace body provided in an embodiment of the present invention;

[0030] Figure 3 This is a schematic diagram of the second structure of the furnace body provided in an embodiment of the present invention;

[0031] Figure 4 This is a schematic diagram of the third structure of the furnace body provided in an embodiment of the present invention;

[0032] Figure 5 This is a second schematic diagram of the distillation system provided in an embodiment of the present invention.

[0033] In the picture:

[0034] 100. Furnace body; 110. First heating section; 120. Second heating section; 130. Cooling section; 140. Quenching section; 150. Tunnel structure; 160. Lifting and conveying mechanism;

[0035] 200. Porous media burner; 300. Oxygen generation module; 400. Purification device; 500. Heat exchange device; 600. Water mist device. Detailed Implementation

[0036] To make the technical problems solved by the present invention, the technical solutions adopted, and the technical effects achieved clearer, the technical solutions of the present invention will be further described below in conjunction with the accompanying drawings and specific embodiments. It should be understood that the specific embodiments described herein are merely for explaining the present invention and are not intended to limit the present invention. Furthermore, it should be noted that, for ease of description, only the parts related to the present invention are shown in the accompanying drawings, not all of them.

[0037] It should be noted that similar labels and letters in the following figures indicate similar items. Therefore, once an item is defined in one figure, it does not need to be further defined and explained in subsequent figures.

[0038] In the description of this invention, unless otherwise explicitly specified and limited, the terms "connected," "linked," and "fixed" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.

[0039] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can include direct contact between the first and second features, or contact between the first and second features through another feature between them. Furthermore, "above," "over," and "on top" of the second feature includes the first feature directly above or diagonally above the second feature, or simply indicates that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature includes the first feature directly below or diagonally below the second feature, or simply indicates that the first feature is at a lower horizontal level than the second feature. In the description of this embodiment, unless otherwise specified, "multiple" specifically refers to two or more.

[0040] In the description of this embodiment, the terms "upper," "lower," "right," etc., refer to the orientation or positional relationship shown in the accompanying drawings. They are used only for ease of description and simplification of operation, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on the present invention. In addition, the terms "first" and "second" are used only for distinction in description and have no special meaning.

[0041] It should be noted that when a component is referred to as "fixed to" or "set on" another component, it can be directly on the other component or it can be located in between the component.

[0042] The technical solution of the present invention will be further described below with reference to the accompanying drawings and specific embodiments.

[0043] Example 1

[0044] The current semi-coke furnace type and production method, with the retorting furnace extending vertically, limits the use of large-sized lump coal as raw material. Furthermore, as the lump coal falls from the top of the coal bunker into the retorting furnace, it is prone to cracking and breaking due to impact, heating, and water quenching during its downward movement through the drying, retorting, cooling, and quenching sections. This results in a higher content of broken coke and coke powder in the product, lowering the quality of the semi-coke. Moreover, the uneven particle size and random packing of the lump coal create uneven resistance to flue gas flow within the pores. Combustion gas passes through pores with lower resistance, leading to "short circuits" and "uneven burning," resulting in an uneven temperature field within the furnace. Some areas are overburned while others are under-carbonized, leading to poor product quality and poor controllability of the retorting process.

[0045] This embodiment provides a dry distillation system that can improve the production efficiency of semi-coke and produce semi-coke of high quality.

[0046] For example, such as Figure 1 As shown, the dry distillation system includes a furnace body 100 and a conveying mechanism (not shown in the figure). The furnace body 100 contains a first heating section 110, a second heating section 120, a cooling section 130, and a quenching section 140. Both the first heating section 110 and the second heating section 120 heat the raw coal. After heating in the second heating section 120, the raw coal yields the main product. The cooling section 130 cools the main product, and the quenching section 140 quenches the cooled main product to obtain semi-coke that meets the requirements. In this embodiment, the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140 are all tunnel-type structures to create a relatively sealed processing space, reduce heat loss, and improve heat utilization.

[0047] For example, the first heating section 110, the second heating section 120, the cooling section 130 and the quenching section 140 are arranged in sequence, with the first heating section 110 being closest to the inlet of the furnace body 100 and the quenching section 140 being closest to the outlet of the furnace body 100. This allows the raw coal to enter from the inlet of the furnace body 100, pass through the first heating section 110, the second heating section 120, the cooling section 130 and the quenching section 140 in sequence, and then be output from the outlet of the furnace body 100.

[0048] In this embodiment, the transport mechanism is movably placed inside the furnace body 100 and can move to the first heating section 110, from the first heating section 110 to the second heating section 120, from the second heating section 120 to the cooling section 130, and from the cooling section 130 to the quenching section 140. The transport mechanism is used to transport raw coal, thereby driving the raw coal into the furnace body 100 and sequentially passing through the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140. This allows the raw coal to be heated in the first heating section 110 and the second heating section 120, cooled in the cooling section 130, and quenched in the quenching section 140. It can be seen that in this embodiment, the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140 are arranged sequentially along the raw coal conveying direction.

[0049] The dry distillation system provided in this embodiment has a furnace body 100 with a first heating section 110, a second heating section 120, a cooling section 130, and a quenching section 140 arranged sequentially in a tunnel-like structure. Raw coal is transported within the furnace body 100 via a conveying mechanism. The transfer of raw coal between the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140 is all achieved through this conveying mechanism. There is no significant relative movement between the raw coal particles on the conveying mechanism, thus reducing the risk of cracking and breakage due to impact. The product contains less broken coke and coke powder, resulting in higher quality main products (such as semi-coke). Furthermore, the flat distribution of raw coal on the conveyor provides a larger heating surface area, improving heating efficiency and shortening the residence time of raw coal in the furnace, ensuring sufficient carbonization without excessive burn-off. The thickness of the raw coal is also not excessive, allowing heat to be better transferred to the interior of the coal during heating, reducing the likelihood of short circuits and uneven burning, and improving the uniformity of the temperature field within the furnace, further enhancing the quality of the main product.

[0050] Furthermore, the change in transportation method eliminates the limitation on the size of raw coal. In addition to lump coal, inexpensive small-diameter coal can also be used, ensuring that coal of all sizes can be heated and decomposed uniformly and quickly without the problems of "short circuit" and "uneven burning". This transportation method eliminates the step of screening raw coal by particle size, and small-diameter coal is not wasted. The main product includes coal of different particle sizes, and the output is increased, resulting in higher economic benefits.

[0051] In addition, this embodiment transforms stacked carbonization into sheet carbonization. The slicing process allows for precise control of temperature and atmosphere throughout the entire process. A matching DCS control system is used, and each section of the furnace can independently control parameters such as temperature, atmosphere, and conveying speed. The high level of automation ensures safe and stable production and controllable product quality.

[0052] It should be noted that the temperature of the second heating section 120 is higher than that of the first heating section 110, which allows the raw coal to be heated to high temperature semi-coke after being heated in the second heating section 120.

[0053] Exemplarily, the first heating section 110 may include a preheating section and a volatilization section, wherein the preheating section is located upstream of the volatilization section and closer to the inlet of the furnace body 100, and the volatilization section is closer to the second heating section 120. The heat source of the first heating section 110 is the hot flue gas from the second heating section 120. The hot flue gas flows sequentially from the second heating section 120 through the volatilization section and the preheating section, and then flows out from the flue gas outlet of the preheating section. The preheating section is used to preheat the raw coal that has just entered the furnace body 100 to increase the temperature of the raw coal. The volatilization section is used to further heat the raw coal, so that substances with lower vaporization temperatures in the raw coal vaporize and volatilize first. In this embodiment, the temperature in the volatilization section is 100℃-200℃. It should be noted that the temperature in the volatilization section is low, therefore, the raw coal will not burn in the volatilization section. The second heating section in this embodiment may also be called a dry distillation section.

[0054] Example 2

[0055] This embodiment provides a distillation system, and based on Embodiment 1, this embodiment provides a transportation mechanism.

[0056] For example, the transport mechanism includes a power unit and a grate. The grate passes through the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140. The power unit is driven and connected to the grate and is used to drive the grate to move. The grate supports the raw coal. When the power unit drives the grate to move, the grate carries the raw coal on it through the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140 in sequence. By setting up the power unit and the grate, the raw coal can be stably transported. The grate can be cyclically arranged, that is, the grate located in the first heating section 110, the grate located in the second heating section 120, the grate located in the cooling section, and the grate located in the quenching section 140 all have raw coal, realizing the continuity of the dry distillation process and further improving the efficiency of dry distillation and the utilization rate of heat within the furnace body 100.

[0057] For example, the specific method by which the power assembly drives the grate movement can be found in the prior art. This embodiment provides a driving method in which the power assembly includes a motor, a drive gear, and a transmission gear. The grate may include a transmission chain and a support row disposed on the transmission chain. The motor drives the drive gear to rotate, and the transmission gear meshing with the drive gear also rotates. The transmission chain connected to the transmission gear rotates, thereby driving the support row to move within the furnace body 100, thereby driving the raw coal to move in the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140.

[0058] It should be noted that the duration of the raw coal's stay in the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140 can be controlled by controlling the start and stop of the motor, so as to ensure that the raw coal is fully preheated, heated, cooled, and quenched.

[0059] Example 3

[0060] This embodiment provides a distillation system, and based on Embodiment 1, this embodiment provides a transportation mechanism.

[0061] For example, the transport mechanism includes a kiln car. A track is provided within the furnace body 100, passing through the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140. Specifically, the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140 are all provided with tracks, and the extension direction of the track in the first heating section 110 is the same as the extension direction of the first heating section 110, the extension direction of the track in the second heating section 120 is the same as the extension direction of the second heating section 120, the extension direction of the track in the cooling section 130 is the same as the extension direction of the cooling section 130, and the extension direction of the track in the quenching section 140 is the same as the extension direction of the quenching section 140. The kiln car is movably mounted on the track along its extension direction for guidance. The kiln car supports the raw coal; that is, the raw coal is carried in the kiln car. As the kiln car moves, it carries the raw coal sequentially through the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140. The kiln car's flexibility enhances the flexibility of the dry distillation process.

[0062] Optionally, the kiln car can move automatically, that is, it has an internal drive system, or the kiln car can be pulled or pushed by other power devices. This embodiment does not limit this.

[0063] In this embodiment, multiple kiln cars can be provided, and multiple kiln cars can operate simultaneously and be located at different positions in the furnace body 100. This means that at the same time, there is a kiln car located in the first heating section 110, a kiln car located in the second heating section 120, a kiln car located in the cooling section 130, and a kiln car located in the quenching section 140. This achieves the continuity of the dry distillation process and further improves the efficiency of dry distillation and the utilization rate of heat in the furnace body 100.

[0064] Example 4

[0065] This embodiment provides a dry distillation system. Based on Embodiment 1, this embodiment provides a ring-shaped furnace body 100.

[0066] like Figure 2As shown, the furnace body 100 is annular, and the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140 are arranged sequentially along the circumference of the furnace body 100. The annular furnace body 100 can be relatively short, thus making it suitable for applications with shorter and wider spaces.

[0067] In some optional embodiments, the furnace body 100 further includes a feeding section and a coking section extending radially along the furnace body 100. The feeding section is located upstream of the first heating section 110 and is used to add raw coal to the conveying mechanism located at the inlet of the first heating section 110. The coking section is located downstream of the quenching section 140 and is used to remove the generated main product from the conveying mechanism. When the furnace body 100 is annular, the feeding and coking sections are located in close proximity, facilitating the scheduling and transportation of raw coal and semi-coke. For example, an empty car that has finished unloading raw coal can be used to load semi-coke.

[0068] Example 5

[0069] This embodiment provides a dry distillation system. Based on Embodiment 1, this embodiment provides a furnace body 100 with a straight shape.

[0070] For example, such as Figure 3 As shown, the furnace body 100 is linear. The first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140 are arranged sequentially along the extension direction of the furnace body 100. The linear furnace body 100 has lower requirements for the width of the installation site and is suitable for application scenarios where the site is long but the width is limited; or for scenarios where multiple production lines are set up in parallel.

[0071] In this embodiment, the extension directions of the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140 all intersect the vertical direction. That is, in this embodiment, the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140 do not extend in the vertical direction, but in the horizontal direction. Therefore, the risk of raw coal cracking and breaking due to collision can be reduced.

[0072] For example, a coal bunker is provided on the side of the first heating section 110 facing away from the second heating section 120, and a conveying mechanism can be moved to the coal bunker so that the raw coal in the coal bunker can be placed on the conveying mechanism. A coking section 140 is provided on the side facing away from the cooling section 130 for transporting the main product.

[0073] Example 6

[0074] This embodiment provides a dry distillation system. Based on Embodiment 1, this embodiment provides a multi-layer furnace body 100.

[0075] For example, such as Figure 4As shown, the furnace body 100 includes a multi-layer tunnel structure 150, which is arranged sequentially along the vertical direction. The dry distillation system also includes a lifting and transferring mechanism 160, which is used to transfer raw coal between adjacent tunnel structures 150 to realize the transfer of raw coal between different tunnel structures 150. Each tunnel structure 150 includes at least one processing section, which may be a first heating section 110, a second heating section 120, a cooling section 130, or a quenching section 140. Each tunnel structure 150 may include only one processing section, or two or more processing sections may constitute one tunnel structure 150; this embodiment does not limit this. The furnace body 100 with a multi-layer tunnel structure 150 can be applied to installation sites with a large vertical dimension but a small length and width.

[0076] For example, in this embodiment, such as Figure 4 As shown, the furnace body 100 includes a three-layer tunnel structure 150. The uppermost tunnel structure 150 consists of a first heating section 110, meaning that the uppermost tunnel structure 150 only has the first heating section 110. The middle tunnel structure 150 consists of a second heating section 120, meaning that the middle tunnel structure only has the second heating section 120. The lowermost tunnel structure 150 consists of a cooling section 130 and a quenching section 140.

[0077] In this embodiment, the first heating section 110, the second heating section 120, the cooling section 130, and the quenching section 140 are arranged in an S-shape, enabling more continuous processing of the raw coal. Specifically, the inlet of the first heating section 110 is located on the left side of the uppermost layer, and the outlet of the first heating section 110 is located on the right side of the uppermost layer. The inlet of the second heating section 120 is located on the right side of the middle layer, and the outlet of the second heating section 120 is located on the left side of the middle layer. The raw coal exiting the outlet of the first heating section 110 is transferred to the right side of the middle layer via a lifting and conveying mechanism 160, and then moves from the right side of the middle layer to the left outlet of the middle layer. The main product at the outlet of the intermediate layer is rotated to the left side of the bottom layer by another lifting and rotating mechanism, that is, rotated to the inlet of the cooling section 130. After being processed by the cooling section 130 and the quenching section 140, it is output from the outlet of the quenching section 140 on the right side of the bottom layer, so that the transfer time of raw coal in the vertical direction can be shorter. Since the heat consumption increases by 1%-1.5% for every hour the turnover time changes, this embodiment avoids excessive heat loss during the transfer process and ensures heat utilization rate.

[0078] Optionally, the lifting and transfer mechanism 160 in this embodiment can be a lifting elevator, and the specific structure can be found in the lifting devices in the prior art.

[0079] Example 7

[0080] This embodiment provides a pyrolysis system. Based on Embodiment 1, the pyrolysis system of this embodiment also includes a porous media burner 200.

[0081] In the existing technology, the heat source of the second heating section 120 is usually set outside the furnace body 100. By introducing hot flue gas into the second heating section 120, the heat exchange between the flue gas convection and the lump coal is a contact heat exchange. When the flue gas flow is uneven, the heating effect is not good, and the temperature rise rate of the raw coal is slow, which affects the production efficiency of semi-coke.

[0082] In this embodiment, a porous media burner 200 (PMC, Porous Media Combustion Technology) is installed in the second heating section 120. Porous media combustion is a combustion method that incorporates porous media into the burner. The heat generated by the porous media at high temperatures heats the material, representing a non-contact heat exchange. Due to the presence of convection, conduction, and radiation heat exchange mechanisms, the burner with porous media achieves a more uniform temperature in the combustion zone, maintaining a relatively stable temperature gradient and exhibiting high volumetric heat intensity while ensuring stable combustion. Therefore, by installing the porous media burner 200 in the second heating section 120, the raw coal located in the second heating section 120 can be heated by infrared radiation and hot flue gas convection, resulting in rapid and uniform heating of the raw coal. This leads to more even and faster heating of the coal blocks, improving the quality of semi-coke, reducing coal consumption, shortening the dry distillation time, and enabling compact design. The coking speed is reduced from 12 hours to 2-5 hours, significantly improving the production efficiency of the dry distillation system. In addition, by setting up a porous medium burner 200, it is easier to control the dry distillation process and improve the controllability of the dry distillation process.

[0083] In some optional embodiments, the circumferential inner wall of the second heating section 120 may be provided with a porous medium burner 200 to further increase the heating rate and further improve production efficiency.

[0084] Exemplarily, the pyrolysis system also includes a combustion-supporting device for introducing combustion-supporting gas into the second heating section 120. The combustion-supporting gas contains 21%-100% oxygen by volume; that is, the pyrolysis system in this embodiment uses oxygen-enriched combustion. Existing semi-coke production uses air for combustion, resulting in coal gas containing a large amount of nitrogen (45-48% by volume), significantly reducing the calorific value of the coal gas (1300-1900 kcal / Nm3). In this embodiment, oxygen-enriched air or pure oxygen is used instead of air for combustion (oxygen volume fraction 21-100%), ensuring that the product gas is nitrogen-free and reducing thermal nitrogen oxides in the flue gas. Depending on the process conditions, the calorific value of the coal gas can reach 3000-6000 kcal / Nm3, making it suitable for sale as a high-quality fuel gas product.

[0085] In some optional embodiments, the combustion-supporting device includes an oxygen-generating module 300, which has an oxygen outlet for discharging oxygen and a nitrogen outlet for discharging nitrogen. The oxygen outlet is connected to the second heating section 120 to introduce oxygen into the second heating section 120 for combustion of combustible materials within it. The nitrogen outlet is connected to the quenching section 140, resulting in a higher nitrogen content in the gas within the quenching section 140 and a lower oxygen content, which is beneficial for increasing the quenching speed of the high-temperature semi-coke within the quenching section 140. This embodiment provides nitrogen discharge into the quenching section 140, allowing full utilization of the byproducts generated by the oxygen-generating module 300 in oxygen production, and also improving the quenching speed while avoiding the waste of the nitrogen byproduct.

[0086] It should be noted that when nitrogen is discharged into the quenching section 140 for quenching, the quenching section 140 is isolated from the first heating section 110, the second heating section 120, and the cooling section 130. That is, the quenching section 140 is not connected to the upstream processing section, so that the nitrogen in the quenching section 140 will not enter the first heating section 110, the second heating section 120, and the cooling section 130, thus avoiding nitrogen from affecting the concentration of by-product gas and the combustion atmosphere in the second heating section 120.

[0087] In this embodiment, the oxygen generating module 300 can be an oxygen generating device in the prior art. For example, it can obtain liquid oxygen and liquid nitrogen by cooling air. The liquid nitrogen is input into the quenching section 140, which facilitates rapid quenching in the quenching section 140 and further cools the semi-coke within the quenching section 140, causing the temperature of the semi-coke to drop rapidly to a temperature suitable for coking. Of course, it is understood that the oxygen generating module 300 can also be other devices that can produce oxygen, and this embodiment does not limit this.

[0088] It should be noted that when the oxygen temperature is low, in order to prevent the oxygen from absorbing a large amount of heat after entering the second heating section 120, a steam generator can also be set in this embodiment. The steam generator is used to generate steam, which is mixed with oxygen and then sent to the PMC burner in the second heating section 120 to dilute the oxygen content of the combustion gas. Since the combustion of high-concentration oxygen or pure oxygen is very dangerous and poses a risk of explosion, adding steam to reduce the oxygen content will not introduce gases such as nitrogen. On the other hand, water vapor can produce oxygen and hydrogen after being decomposed at high temperature in the second heating section 120. The oxygen can achieve the purpose of combustion, and the hydrogen increases the hydrogen content in the flue gas, thereby forming high-calorific-value coal gas. In addition, the steam can also heat the oxygen in the second heating section 120 to ensure the temperature near the porous medium burner 200 and ensure smooth combustion.

[0089] In some optional embodiments, if air is introduced into the PMC burner of the second heating section 120 for combustion support, the resulting gas composition is: hydrogen: 10.2%; carbon monoxide: 8.6%; carbon dioxide: 6.5%; methane: 13.39%; C2-C5: 1.04%; the remainder being nitrogen. The calorific value of this gas is 1849 kcal / Nm³. 3 If the aforementioned oxygen-enriched gas is introduced into the PMC burner of the second heating section 120 to assist combustion, the composition of the produced gas is as follows: hydrogen: 16.07%; carbon monoxide: 16.08%; carbon dioxide: 11.15%; methane: 40.21%; C2-C5: 8.11%; the remainder is nitrogen. The calorific value of this gas is 5732 kcal / Nm³. 3 .

[0090] Therefore, it can be seen that after adopting oxygen-enriched combustion technology, the coal-to-coke ratio is reduced to 1.62:1, the coal tar yield is increased to about 8.5%, and the residual gas volume per ton of coal is 190 m³. 3 ~210m 3 (Shenmu coal) has a significantly increased calorific value, reaching 5600 kcal / Nm³. 3 ~6500kCal / Nm 3 The effective composition of the coal gas is significantly increased, and the thermal cycle efficiency of the generator is improved to about 42% when using gas-fired power generation, making it suitable for subsequent chemical utilization. At the same time, the high-calorific-value coal gas can be sold as a byproduct, thus keeping the overall production cost of semi-coke lower.

[0091] Example 8

[0092] This embodiment provides a dry distillation system. Based on Embodiment 1, the furnace body 100 of this embodiment is provided with a flue gas outlet.

[0093] Specifically, the furnace body 100 is equipped with a flue gas outlet located in the first heating section 110, near its inlet. Flue gas from the first heating section 110, the second heating section 120, and the cooling section 130 is discharged through this outlet, with the flow direction opposite to the coal conveying direction. The flue gas in the first heating section 110 and the second heating section 120 is used to heat the raw coal. By placing the flue gas outlet at the inlet of the first heating section 110, the flue gas passes through the entire first heating section 110 upon discharge, thus heating the raw coal within it. The opposite flow direction of the flue gas to the coal conveying direction allows the raw coal to be preheated and heated in the first heating section 110 during the first stage of heating, facilitating the volatilization of volatiles. This eliminates the need for a burner in the first heating section 110, fully utilizing the heat of the flue gas and improving the overall utilization rate of the dry distillation system. It is understandable that burners can also be installed in the first heating section 110. The number of burners can be small, just enough to achieve the purpose of preheating and volatilization.

[0094] In the current technology, the semi-coke industry is experiencing slow technological upgrades, with extensive production methods, resulting in low-quality products and high energy consumption. Uneven burning leads to the ineffective consumption of raw coal; approximately 30-40% of the raw coal gas is used for reheating in the furnace, and 25% is used for drying the semi-coke. Neither the heat from the furnace nor the heat from the coal gas is effectively utilized.

[0095] In some optional embodiments, the distillation system further includes a purification device 400. The purification device 400 is used to purify the flue gas. The inlet of the purification device 400 is connected to the exhaust port, and the purification device 400 is used to purify the flue gas to obtain a predetermined product. Figure 5 As shown, the flue gas discharged from the furnace 100 can be called raw coal gas. After purification by the purification device 400, the raw coal gas can yield the preset products. The preset products include tar and processed coal gas. Processed coal gas includes product coal gas and / or recycled coal gas. It should be noted that the concentration of coal gas in product coal gas and recycled coal gas is the same, that is, their calorific values ​​are the same; the difference lies in their different uses. Specifically, as... Figure 5 As shown, product gas refers to gas that can be sold as a product. Recycled gas refers to gas that can be returned to the furnace 100 for reuse. In actual production, the amount of product gas and recycled gas in the processed gas can be divided according to demand to maximize the efficiency and minimize the cost of the dry distillation system. It should be noted that when the porous media burner 200 in Example 7 is used in conjunction with oxygen-enriched combustion, the calorific value of the processed gas is higher.

[0096] In some alternative embodiments, the first outlet of the purification device 400 is selectively connected to the second heating section 120. The connection between the first outlet and the second heating section 120 is used to input recycled coal gas into the second heating section 120. The recycled coal gas entering the second heating section 120 can be decomposed and release heat under the infrared radiation generated during combustion in the porous media burner 200. The released heat is used to heat the raw coal, making full use of the by-product gas produced by dry distillation.

[0097] For example, when the combustion in the second heating section 120 is air-assisted combustion, the calorific value of the coal gas is low, making it unsuitable for product sales and only allowing for reuse in the furnace. In this embodiment, the second outlet of the purification device 400 is selectively connected to the quenching section 140. This connection allows recycled coal gas to be introduced into the quenching section 140. Since the recycled coal gas entering the quenching section 140 is too low to burn directly, it can be used to cool the semi-coke in the quenching section 140 and achieve quenching. Furthermore, the recycled coal gas (i.e., water gas) that absorbs heat in the quenching section 140 at a higher temperature can re-enter the second heating section 120, where it decomposes and releases heat, achieving multi-stage energy utilization with high energy efficiency and realizing the recycling of flue gas and steam / water gas.

[0098] It is understandable that when the combustion in the second heating section 120 is combustion aided by oxygen-enriched air and the coke quenching section 140 uses nitrogen for coke quenching, the second outlet of the purification device 400 is not connected to the coke quenching section 140, and there is no need to input return gas into the coke quenching section 140.

[0099] In this embodiment, the method by which the purification device 400 processes flue gas to obtain a preset product is existing technology, and specific details can be found in existing purification equipment. For example, the purification device 400 may include a tar recovery module, an electrostatic precipitator module, a wet desulfurization module, a crude gas holder module, and a fine desulfurization module. The flue gas first enters the tar recovery module, and then enters the electrostatic precipitator module. Both the tar recovery module and the electrostatic precipitator module can obtain tar. After exiting the electrostatic precipitator module, the flue gas enters the desulfurization module, and then enters the crude gas holder module. After processing by the crude gas holder module, processed gas is obtained. The recycled gas in the processed gas enters the second heating section 120 and the quenching section 140. The product gas in the processed gas enters the fine desulfurization module. After processing by the fine desulfurization module, high-calorific-value fuel gas is obtained.

[0100] Example 9

[0101] This embodiment provides a dry distillation system. Based on Embodiment 1, the furnace body 100 of this embodiment is provided with a gas channel.

[0102] Specifically, the furnace body 100 is provided with a gas channel (not shown in the figure), which selectively connects the second heating section 120 and the cooling section 130. That is, the gas channel can be open or closed. For example, the gas channel can be opened or closed by setting a valve body in the gas channel.

[0103] When the gas channel connects the second heating section 120 and the cooling section 130, the gas channel can transport the cooling generated gas from the cooling section 130 to the second heating section 120. The cooling generated gas includes water gas and / or water vapor. By setting up the gas channel, the water gas generated in the quenching section 140 can enter the second heating section 120 and be heated and decomposed to release heat. The heat generated is used to heat the raw coal, which improves the utilization efficiency of the water gas generated in the cooling section 130, thereby improving the energy utilization rate of the entire dry distillation system and making the cost of the dry distillation process lower.

[0104] Example 10

[0105] This embodiment provides a dry distillation system. Based on Embodiment 1, the dry distillation system of this embodiment also includes a heat exchange device 500.

[0106] In the prior art, the high-temperature semi-coke obtained after heating in the second heating section 120 directly enters the cooling section 130 for cooling. The heat released during cooling is discharged with the flue gas, resulting in a waste of heat.

[0107] In this embodiment, as Figure 5 As shown, the distillation system also includes a heat exchanger 500, where raw coal is heated in the second heating section 120 to produce the main product (e.g., semi-coke). The heat exchanger 500 is located in the cooling section 130 and absorbs heat from the main product in the cooling section 130, causing the temperature of the main product to drop by 320℃-380℃, thus fully utilizing the heat on the main product and avoiding heat waste. For example, the heat exchanger 500 absorbs heat from the main product in the cooling section 130, causing the temperature of the main product to drop by 320℃, 340℃, 360℃, and 380℃, respectively.

[0108] In some alternative embodiments, the heat exchange device 500 may include a water-cooled jacket disposed on the inner wall of the furnace body of the cooling section 130. Water flows in the water-cooled jacket, absorbing heat from the cooling section 130 and the main product, thereby cooling the main product and the cooling section 130. The water heated by absorbing heat in the water-cooled jacket can be used as a by-product hot water or as a by-product steam. For example, the steam generated by the heat exchange device 500 can be transported to the PMC burner of the second heating section 120 to form a combustion-supporting gas mixture with pure oxygen, thereby achieving energy recovery and utilization and avoiding energy waste. Of course, it is understood that the main product may also have other uses, which are not limited in this embodiment.

[0109] For example, the heat exchange device 500 can also be a water-cooled wall in the prior art. For specific structure and working principle, please refer to the prior art. This embodiment does not limit it.

[0110] Example 11

[0111] This embodiment provides a pyrolysis system. Based on Embodiment 1, the pyrolysis system of this embodiment also includes a water mist device 600.

[0112] In existing technologies, the quenching method for semi-coke is usually water quenching, which involves placing the high-temperature semi-coke underwater to achieve the purpose of quenching. Water quenching consumes 0.2 tons of water per ton of semi-coke quenched. The sensible heat of the semi-coke at around 550℃ in the carbonization stage is wasted with the steam discharge, accounting for about 45% of the total heat consumption. Rapid cooling of the semi-coke generates significant thermal stress, leading to numerous cracks and pores, resulting in low strength and brittleness. Drying wet semi-coke wastes about 25% of the coal gas, and the contact between high-temperature semi-coke and water produces a large amount of wastewater containing phenols, cyanides, and sulfides, resulting in high treatment costs.

[0113] This embodiment employs water mist quenching. Specifically, the distillation system also includes a water mist device 600, installed in the furnace body 100, which sprays water mist onto the main product in the transport mechanism located in the cooling section 130 for water mist cooling and quenching. That is, most of the semi-coke can be significantly cooled and quenched in the cooling section 130, and the quenching section 140 ensures that all semi-coke is quenched and cooled to a temperature suitable for unloading. The water mist generated by the water mist device 600 cools the hot coke, saving 10% energy and 30% water, while reducing the breakage caused by rapid cooling of the coke. The semi-coke yield is increased by 2.3%, and drying is unnecessary, reducing processing costs. The generated hot water vapor can flow back to the second heating section 120, cooling the coke while increasing the water-gas reaction, recovering waste heat and generating more gas. Furthermore, the cooling section 130 discharges no wastewater, resulting in significant environmental benefits, eliminating the need for treatment equipment, and reducing costs.

[0114] For example, the water mist device 600 may include a plurality of water mist nozzles disposed in the cooling section 130, the water mist nozzles being used to spray water mist to achieve coke quenching.

[0115] As can be seen, the water mist quenching technology provided in this embodiment can recover waste heat from semi-coke, improving energy efficiency; reduce the amount of combustion gas and oxygen required, further saving energy; significantly reduce the moisture content of the semi-coke product, eliminating the need for drying; and improve the strength of the semi-coke product due to changes in cooling conditions, while significantly reducing cracking and breakage rates. Production practice shows that adopting water mist quenching technology can save 10% of energy, theoretically reduce water consumption by more than 30%, reduce the water content of the finished semi-coke to below 5%, and increase the semi-coke yield by about 2.3%. If the user's transportation costs, energy-saving benefits, and environmental and social benefits are considered, the economic benefits will be even more significant. The improved quality of the semi-coke product can bring additional revenue. In summary, water mist quenching can save drying gas, quenching water, wastewater treatment, combustion oxygen, and combustion gas, while also increasing the calorific value of the gas and improving the quality of the semi-coke.

[0116] In this embodiment, water mist is used to quench coke in the cooling section 130, which can save 10% of energy and reduce theoretical water consumption by 30%, improve energy utilization efficiency, and significantly improve the quality of semi-coke products. In addition, the reaction of water and gas to generate syngas (H2+CO) increases the production of coal gas and improves the H / C ratio of coal gas.

[0117] In this embodiment, when the water vapor generated by the water mist quenching at the cooling section 130 is not introduced into the second heating section 120, the gas composition within the second heating section 120 is: hydrogen: 40.95%; carbon monoxide: 25.04%; carbon dioxide: 12.46%; methane: 14.65%; C2-C5: 5.85%; the remainder is nitrogen. The calorific value of this gas is 3149 kcal / Nm³. 3 When steam is introduced into the second heating section 120, the gas composition within the second heating section 120 is: hydrogen: 48.95%; carbon monoxide: 20.04%; carbon dioxide: 10.46%; methane: 13.95%; C2-C5: 4.85%; the remainder is nitrogen. The calorific value of this gas is 3388 kcal / Nm³. 3 .

[0118] Therefore, by introducing steam from the cooling section 130 into the second heating section 120, the amount of cooling gas required to produce one ton of semi-coke is reduced to 60-70 m³ / h. 3 The surplus gas volume has been increased to 480m³. 3 The calorific value of the gas has increased slightly compared to before, reaching 13400–14220 kJ / Nm³. 3 Furthermore, the increased effective hydrogen content makes it suitable for subsequent chemical applications, expanding the range of applications for the product gas. Steam can lower the temperature of the second heating section, resulting in a lower distillation temperature and increasing semi-coke production by 10%–12%, with tar recovery reaching 90% (an increase of 5%), of which light oil accounts for 15%–19% of the total.

[0119] Example 12

[0120] In this embodiment, a first sealing mechanism may be provided between the first heating section 110 and the second heating section 120. The first sealing mechanism has an open state and an isolated state. When the first sealing mechanism is in the open state, the first heating section 110 and the second heating section 120 can be interconnected, facilitating the transportation of raw coal by the transport mechanism, and the flue gas from the second heating section 120 can also flow to the first heating section 110. When the first sealing mechanism is in the isolated state, the first heating section 110 and the second heating section 120 are independent of each other, allowing the temperature in the second heating section 120 to rise rapidly, so as to quickly convert the raw coal into semi-coke.

[0121] Similarly, a second sealing mechanism can be provided between the second heating section 120 and the cooling section 130. This second sealing mechanism has an open state and an isolated state. When the second sealing mechanism is open, the cooling section 130 and the second heating section 120 can be connected, facilitating the transport of raw coal by the transport mechanism, and the flue gas from the cooling section 130 can also flow to the second heating section 120. When the second sealing mechanism is in the isolated state, the cooling section 130 and the second heating section 120 cannot be connected through the second sealing mechanism, allowing the temperature in the second heating section 120 to rise rapidly, quickly converting the raw coal into semi-coke. Furthermore, the heat from the second heating section 120 will not move to the cooling section, facilitating rapid cooling of the cooling section 130. It should be noted that even if the cooling section 130 and the second heating section 120 are not connected through the second sealing mechanism, they can be connected through a gas channel to allow water vapor to be introduced into the second heating section 120.

[0122] Optionally, both the first and second sealing mechanisms can be doors, and this embodiment does not limit this. In some embodiments, the sealing effect can be achieved through the structural cooperation between the outer wall of the kiln car and the inner wall of the furnace.

[0123] It should be noted that each of Embodiments 2 to 12 can be combined with Embodiment 1 to form a technical solution. Furthermore, at least two embodiments of Embodiments 2 to 12 can be arbitrarily combined and combined with Embodiment 1 to form different technical solutions. For example, Embodiment 2 can be combined with Embodiment 1, and Embodiments 7 and 8 can be combined with Embodiment 1 to form a technical solution. Embodiments 7, 8, and 9 can be combined with Embodiment 1 to form a technical solution. Embodiments 8 and 9 can be combined with Embodiment 1 to form a technical solution, and so on. These embodiments will not be listed one by one here.

[0124] Note that the above description is merely a preferred embodiment of the present invention and the technical principles employed. Those skilled in the art will understand that the present invention is not limited to the specific embodiments described herein, and various obvious changes, readjustments, and substitutions can be made without departing from the scope of protection of the present invention. Therefore, although the present invention has been described in detail through the above embodiments, the present invention is not limited to the above embodiments, and may include many other equivalent embodiments without departing from the concept of the present invention, the scope of which is determined by the scope of the appended claims.

Claims

1. A distillation system, characterized in that, include: The furnace body (100) is provided with a first heating section (110), a second heating section (120), a cooling section (130) and a quenching section (140), all of which are tunnel-type structures. The transport mechanism is movably placed inside the furnace body (100) and can move to the first heating section (110), from the first heating section (110) to the second heating section (120), from the second heating section (120) to the cooling section (130), and from the cooling section (130) to the quenching section (140). The transport mechanism is used to transport raw coal. The first heating section (110), the second heating section (120), the cooling section (130), and the quenching section (140) are arranged sequentially along the conveying direction of the raw coal.

2. The distillation system according to claim 1, characterized in that, The transport mechanism includes a power unit and a grate. The grate passes through the first heating section (110), the second heating section (120), the cooling section (130), and the quenching section (140). The power unit is driven and connected to the grate and is used to drive the grate to move. The grate is used to support the raw coal. Alternatively, the transport mechanism includes a kiln car, and the furnace body (100) is provided with a track, which passes through the first heating section (110), the second heating section (120), the cooling section (130) and the quenching section (140). The kiln car is movably disposed on the track along the extension direction of the track, and the kiln car is used to support the raw coal.

3. The distillation system according to claim 1, characterized in that, The furnace body (100) is annular, and the first heating section (110), the second heating section (120), the cooling section (130) and the quenching section (140) are arranged sequentially along the circumference of the furnace body (100); Alternatively, the furnace body (100) is linear, and the first heating section (110), the second heating section (120), the cooling section (130), and the quenching section (140) are arranged sequentially along the extension direction of the furnace body (100); Alternatively, the furnace body (100) includes a multi-layer tunnel structure (150) arranged sequentially in the vertical direction. The dry distillation system also includes a lifting and transfer mechanism (160) for transferring the raw coal in two adjacent tunnel structures (150). Each tunnel structure (150) includes at least one processing section, which is the first heating section (110), the second heating section (120), the cooling section (130), or the quenching section (140).

4. The distillation system according to claim 1, characterized in that, The pyrolysis system further includes a porous medium burner (200) disposed in the second heating section (120), and the pyrolysis system further includes a combustion-supporting device for inputting combustion-supporting gas into the second heating section (120), wherein the volume fraction of oxygen in the combustion-supporting gas is 21%-100%.

5. The distillation system according to claim 4, characterized in that, The combustion-supporting device includes an oxygen-generating module (300), which has an oxygen outlet for discharging oxygen and a nitrogen outlet for discharging nitrogen. The oxygen outlet is connected to the second heating section (120), and the nitrogen outlet is connected to the quenching section (140).

6. The distillation system according to any one of claims 1-5, characterized in that, The furnace body (100) is provided with a flue gas outlet, which is located in the first heating section (110) and close to the inlet of the first heating section (110). The flue gas from the first heating section (110), the second heating section (120) and the cooling section (130) is discharged through the flue gas outlet, and the flow direction of the flue gas is opposite to the conveying direction of the raw coal. The flue gas in the first heating section (110) and the second heating section (120) is used to heat the raw coal.

7. The distillation system according to claim 6, characterized in that, The pyrolysis system further includes a purification device (400), the inlet of which is connected to the flue gas outlet. The purification device (400) is used to purify the flue gas to obtain a preset product, the preset product including tar and processed gas, the processed gas including product gas and / or recycled gas. The first outlet of the purification device (400) is selectively connected to the second heating section (120), and the first outlet is connected to the second heating section (120) for inputting the recycled gas into the second heating section (120); and / or, the second outlet of the purification device (400) is selectively connected to the quenching section (140), and the second outlet is connected to the quenching section (140) for inputting the recycled gas into the quenching section (140).

8. The distillation system according to any one of claims 1-5, characterized in that, The furnace body (100) is provided with a gas passage, which selectively connects the second heating section (120) and the cooling section (130); The gas passage connects the second heating section (120) and the cooling section (130) to transport the cooling generated gas from the cooling section (130) to the second heating section (120), the cooling generated gas including water gas and / or water vapor.

9. The distillation system according to any one of claims 1-5, characterized in that, The distillation system also includes a heat exchange device (500). The raw coal is heated in the second heating section (120) to generate the main product. The heat exchange device (500) is located in the cooling section (130). The heat exchange device (500) can absorb the heat of the main product in the cooling section (130) and reduce the temperature of the main product by 320°C-380°C.

10. The distillation system according to any one of claims 1-5, characterized in that, The distillation system also includes a water mist device (600), which is installed in the furnace body (100) and is used to spray water mist onto the main product in the transport mechanism located in the cooling section (130).

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