Coal direct liquefaction separation apparatus and process

Abstract

The present disclosure relates to a coal direct liquefaction separation device and process method, the coal direct liquefaction separation device comprising a first reactor, a second reactor, a buffer tank and a hot high-pressure separator, the first reactor being connected in series with the second reactor; the buffer tank being connected to the outlet end of the second reactor; the hot high-pressure separator being connected to the top material outlet of the buffer tank, which is conducive to solving the problem of system blockage caused by "sudden boiling" of the hot high-pressure separator.

Description

Technical Field

[0001] This disclosure relates to the field of chemical equipment technology, specifically to a direct coal liquefaction separation device and process. Background Technology

[0002] The second-generation direct coal liquefaction technology includes a large-circulation reaction system comprising a reactor and a high-temperature, high-pressure separator. This eliminates the gas-liquid interface within the reactor, extends the operating cycle, and improves the economic efficiency of the unit. However, in related technologies, if the feed flow rate and temperature of the high-temperature, high-pressure separator exceed a certain limit, "sudden boiling" can easily occur, causing a large amount of pulverized coal from the top material to be carried to the top gas phase system, resulting in blockage of subsequent systems. Summary of the Invention

[0003] The purpose of this disclosure is to provide a direct coal liquefaction separation device and process method, which helps to solve the problem of system blockage caused by "sudden boiling" in hot high-pressure separators.

[0004] To achieve the above objectives, this disclosure provides a direct coal liquefaction separation device, which includes a first reactor, a second reactor, a buffer tank, and a hot high-pressure separator. The first reactor and the second reactor are connected in series. The buffer tank is connected to the outlet end of the second reactor. The hot high-pressure separator is connected to the top material outlet of the buffer tank.

[0005] Optionally, the top material outlet of the buffer tank is connected to the inlet of the hot high-pressure separator via a first connecting pipe, the first connecting pipe being provided with a quench oil inlet, the direct coal liquefaction separation equipment including a circulating pump, the bottom material outlet of the buffer tank being connected to the inlet of the circulating pump, and the outlet of the circulating pump being connected to the first reactor.

[0006] Optionally, the direct coal liquefaction separation equipment includes a hot medium-pressure separator, a warm medium-pressure separator, a high-pressure quench oil pump, and a high-pressure quench oil air cooler connected in series with the bottom material outlet of the hot high-pressure separator. The outlet end of the high-pressure quench oil air cooler is connected to a second connecting pipeline. The first branch of the second connecting pipeline is connected to the inlet end of the second reactor, and the second branch of the second connecting pipeline is connected to the quench oil inlet.

[0007] According to a second aspect of this disclosure, a process method for direct coal liquefaction and separation is provided, applied to a direct coal liquefaction and separation device, the direct coal liquefaction and separation device comprising a first reactor, a second reactor, a buffer tank, and a hot high-pressure separator, the method comprising: sequentially liquefying pretreated material through the first reactor and the second reactor; feeding the material processed by the second reactor into the buffer tank; and feeding the top material of the buffer tank into the hot high-pressure separator through the top material outlet of the buffer tank.

[0008] Optionally, the direct coal liquefaction separation equipment further includes a circulation pump, and the method further includes: conveying the bottom material of the buffer tank to the first reactor via the circulation pump through the bottom material outlet of the buffer tank.

[0009] Optionally, the bottom material outlet temperature of the buffer tank is 450℃~460℃ and the pressure is 19-20 MPa, and the outlet temperature of the first reactor is 450℃~460℃ and the pressure is 19-20 MPa.

[0010] Optionally, the step of feeding the top material of the buffer tank into the hot high-pressure separator through the top material outlet of the buffer tank further includes: feeding quench oil into the hot high-pressure separator through the quench oil inlet.

[0011] Optionally, the temperature of the hot high-pressure separator is 410℃~420℃, and the pressure is 19-20MPa.

[0012] Optionally, the direct coal liquefaction separation equipment further includes a high-temperature high-pressure separator connected to the top material outlet of the high-temperature high-pressure separator, and a medium-temperature high-pressure separator connected to the bottom material outlet of the high-temperature high-pressure separator. The method further includes: feeding the top material of the high-temperature high-pressure separator into the high-temperature high-pressure separator through the top material outlet of the high-temperature high-pressure separator; and feeding the bottom material of the high-temperature high-pressure separator into the medium-temperature high-pressure separator through the bottom material outlet of the high-temperature high-pressure separator.

[0013] Optionally, the direct coal liquefaction separation equipment includes a medium-temperature separator, a high-pressure quench oil pump, and a high-pressure quench oil air cooler connected in series with the hot medium-pressure separator. The outlet end of the high-pressure quench oil air cooler is connected to a second connecting pipeline. The first branch of the second connecting pipeline is connected to the inlet end of the second reactor, and the second branch of the second connecting pipeline is connected to the inlet end of the hot high-pressure separator. The step of feeding the bottom material of the hot high-pressure separator into the hot medium-pressure separator through the bottom material outlet of the hot high-pressure separator further includes: feeding the quench oil generated after the material entering the hot medium-pressure separator passes through the medium-temperature separator, the high-pressure quench oil pump, and the high-pressure quench oil air cooler in sequence into the inlet end of the second reactor through the first branch and into the inlet end of the hot high-pressure separator through the second branch.

[0014] Through the above technical solution, the material after liquefaction treatment in the first and second reactors needs to be sent to a high-pressure thermal separator for separation. By setting a buffer tank between the second reactor and the high-pressure thermal separator, the material generated in the second reactor can be transported to the buffer tank and undergo gas-liquid separation. The separated gaseous material is then transported to the high-pressure thermal separator for further separation through the top material outlet of the buffer tank. Therefore, the material output from the second reactor can have most of its liquid phase separated by the buffer tank before entering the high-pressure thermal separator, thereby reducing the flow rate of liquid phase material entering the high-pressure thermal separator. This reduces the risk of the high-pressure thermal separator feed carrying a large amount of coal powder, which could easily lead to "sudden boiling" during operation, causing a large amount of coal powder to be carried to the top gas phase system, resulting in blockage of subsequent systems. This helps ensure the reliability of system operation.

[0015] Other features and advantages of this disclosure will be described in detail in the following detailed description section. Attached Figure Description

[0016] The accompanying drawings are provided to further illustrate the present disclosure and form part of the specification. They are used together with the following detailed description to explain the present disclosure, but do not constitute a limitation thereof. In the drawings: Figure 1 This is a schematic diagram of the structure of a direct coal liquefaction and separation device provided according to an embodiment of this disclosure; Figure 2 This is a schematic diagram of the steps of the direct coal liquefaction and separation process provided according to the embodiments of this disclosure.

[0017] Explanation of reference numerals in the attached figures 1-First reactor, 2-Second reactor, 3-Buffer tank, 4-Hot high-pressure separator, 5-Circulating pump, 6-Warm high-pressure separator, 7-Hot medium-pressure separator, 8-Warm medium-pressure separator, 9-High-pressure quench oil pump, 10-High-pressure quench oil air cooler, 20-First connecting pipeline, 30-Second connecting pipeline, 301-First branch, 302-Second branch, 401-Catalyst coal slurry tank, 402-Catalyst coal slurry pump, 403-Coal slurry tank, 404-Coal slurry pump, 405-High-pressure coal slurry pump one, 406-High-pressure coal slurry Pump 2, 407-Coal slurry heater 1, 408-Coal slurry heat exchanger, 409-Coal slurry heater 2, 410-Hydrogen heater, 411-Hydrogen heat exchanger, 412-High-pressure air cooler, 413-Cold high-pressure separator, 414-Cold medium-pressure separator, 415-Medium-pressure air cooler, 416-Atmospheric pressure tower, 417-Atmospheric pressure pump 1, 418-Atmospheric pressure pump 2, 419-Atmospheric pressure pump 3, 420-Atmospheric pressure bottom pump, 421-Depressurization tower heater, 422-Depressurization tower, 423-Depressurization pump 1, 424-Depressurization pump 2, 425-Depressurization bottom pump. Detailed Implementation

[0018] The specific embodiments of this disclosure will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for illustration and explanation only and are not intended to limit this disclosure.

[0019] In this disclosure, unless otherwise stated, the directional terms "inner" and "outer" refer to the "inner" and "outer" relative to the contour of the corresponding component itself. "Top" and "bottom" generally refer to the "top" and "bottom" relative to the corresponding component in its operational state along the height direction. Furthermore, the use of terms such as "first" and "second" is intended to distinguish different components and does not imply sequentiality or importance. Additionally, in the following description, when referring to the accompanying drawings, the same reference numerals in different drawings denote the same elements. Those skilled in the art should understand that the above definitions are for explanation and illustration only and should not be construed as limiting the scope of this disclosure.

[0020] According to the first aspect of this disclosure, reference to Figure 1 and Figure 2 As shown, a direct coal liquefaction separation device is provided, which includes a first reactor 1, a second reactor 2, a buffer tank 3, and a hot high-pressure separator 4. The first reactor 1 and the second reactor 2 are connected in series; the buffer tank 3 is connected to the outlet end of the second reactor 2; and the hot high-pressure separator 4 is connected to the top material outlet of the buffer tank 3.

[0021] Through the above technical solution, the material after liquefaction treatment by the first reactor 1 and the second reactor 2 needs to be sent to the thermal high-pressure separator 4 for separation. By setting a buffer tank 3 between the second reactor 2 and the thermal high-pressure separator 4, the material generated by the second reactor 2 can be transported to the buffer tank 3 and undergo gas-liquid separation. The separated gaseous material is then transported to the thermal high-pressure separator 4 for further separation through the top material outlet of the buffer tank 3. Thus, the material output from the second reactor 2 can have most of the liquid phase separated by the buffer tank 3 before entering the thermal high-pressure separator 4, thereby reducing the amount of liquid phase material entering the thermal high-pressure separator 4. This reduces the risk of the feed carrying a large amount of coal powder, which could easily cause "sudden boiling" during the operation of the thermal high-pressure separator 4, and the top gaseous material carrying a large amount of coal powder to the top gas phase system, leading to blockage of the subsequent system. This helps to ensure the reliability of the system operation.

[0022] In related technologies, a circulation pump 5 is installed at the bottom of the hot high-pressure separator 4, so that the material at the bottom of the hot high-pressure separator 4 is directly transported to the circulation pump 5 and returned to the first reactor 1. Since the reaction temperature inside the hot high-pressure separator 4 is lower than the inlet temperature of the first reactor 1, when the output material enters the circulation pump 5, the inlet temperature of the circulation pump 5 decreases, thereby causing the inlet temperature of the first reactor 1 to decrease. Therefore, in order to ensure the temperature of the first reactor 1, it is necessary to increase the heating capacity through coal slurry heater 407, coal slurry heater 409 and hydrogen heater 410, which easily leads to energy waste.

[0023] In some embodiments of this disclosure, reference is made to Figure 1 As shown, the top material outlet of the buffer tank 3 is connected to the inlet of the hot high-pressure separator 4 through the first connecting pipe 20. The first connecting pipe 20 is provided with a quench oil inlet. The coal direct liquefaction separation equipment includes a circulating pump 5. The bottom material outlet of the buffer tank 3 is connected to the inlet of the circulating pump 5, and the outlet of the circulating pump 5 is connected to the first reactor 1.

[0024] In this way, after gas-liquid separation, the gaseous material entering the buffer tank 3 accumulates at the top of the buffer tank 3, allowing it to be transported to the thermal high-pressure separator 4 through the top material outlet. The liquid material separated from the buffer tank 3 settles at the bottom of the buffer tank 3, allowing it to be transported to the first reactor 1 via the circulation pump 5 through the bottom material outlet. By providing a quench oil inlet, quench oil is injected into the inlet of the thermal high-pressure separator 4, thereby cooling the inlet of the thermal high-pressure separator 4 and controlling its inlet temperature to prevent excessively high internal temperatures that could damage the equipment or pose safety risks. Furthermore, the liquid material can be directly transported to the circulation pump 5 through the bottom material outlet of the buffer tank 3 and returned to the first reactor 1 via the circulation pump 5. This avoids the situation where the inlet temperature of the circulation pump 5 decreases when the separated liquid material is transported from the thermal high-pressure separator 4 to the circulation pump 5, resulting in a decrease in the inlet temperature of the first reactor 1 upon return. This would otherwise require increasing the heating furnace capacity to maintain the temperature of the first reactor 1, leading to energy waste.

[0025] In some embodiments of this disclosure, reference is made to Figure 1 As shown, the direct coal liquefaction separation equipment includes a hot medium-pressure separator 7, a warm medium-pressure separator 8, a high-pressure quench oil pump 9, and a high-pressure quench oil air cooler 10 connected in series with the bottom material outlet of the hot high-pressure separator 4. The outlet end of the high-pressure quench oil air cooler 10 is connected to a second connecting pipe 30. The first branch 301 of the second connecting pipe 30 is connected to the inlet end of the second reactor 2, and the second branch 302 of the second connecting pipe 30 is connected to the quench oil inlet. In this way, the liquid material separated by the hot high-pressure separator 4 can sequentially enter the hot medium-pressure separator 7, the warm medium-pressure separator 8, the high-pressure quench oil pump 9, and the high-pressure quench oil air cooler 10, and then enter the second connecting pipeline 30. It is then transported to the second reactor 2 through the first branch 301 to cool the inlet of the second reactor 2 and control the inlet temperature of the second reactor 2, thereby ensuring the reliability of the liquefaction operation in the second reactor. Alternatively, the liquid material separated by the hot high-pressure separator 4 can also enter the hot high-pressure separator 4 after being cooled by the quench oil inlet through the second branch 302, so as to control the inlet temperature of the hot high-pressure separator 4 with quench oil.

[0026] According to the second aspect of this disclosure, reference to Figure 1 and Figure 2 As shown, a process method for direct coal liquefaction and separation is provided, applied to a direct coal liquefaction and separation equipment. The direct coal liquefaction and separation equipment includes a first reactor 1, a second reactor 2, a buffer tank 3, and a hot high-pressure separator 4. The direct coal liquefaction and separation equipment can be the one provided in the first aspect above.

[0027] The method includes the following steps: Step S1: The pretreated material is sequentially liquefied through the first reactor 1 and the second reactor 2; Step S2: Pass the material processed by the second reactor 2 into the buffer tank 3; Step S3: Pass the top material of buffer tank 3 into the hot high-pressure separator 4 through the top material outlet of buffer tank 3.

[0028] Thus, when coal liquefaction is required, coal powder, supplementary sulfur, catalyst, and hydrogen-donating solvent are prepared into a catalyst oil-coal slurry. This slurry is then mixed with hydrogen and heated before being sequentially fed into the first reactor 1 and the second reactor 2. Liquefaction of coal powder, hydrogen, catalyst, and liquid sulfur occurs under high temperature and pressure within the first and second reactors 1 and 2, producing liquefied oil. The material processed in the second reactor 2 is then fed into a buffer tank 3 for preliminary gas-liquid separation. The separated gaseous material accumulates at the top of the buffer tank 3 and is then transported via the top material outlet to a thermal high-pressure separator 4 for further separation. Therefore, the material output from the second reactor 2 can first enter the buffer tank 3 for pre-gas-liquid separation before entering the hot high-pressure separator 4. This allows the buffer tank 3 to transport the separated gaseous material to the hot high-pressure separator 4 for further gas-liquid separation. This reduces the flow rate of the material entering the hot high-pressure separator 4, thereby avoiding the risk of blockage in the subsequent system caused by a large amount of coal powder carried to the top gas phase system by the material in the hot high-pressure separator 4 when the material exceeds a certain flow rate and temperature.

[0029] Specifically, the material pretreatment may include preparing the catalyst into a catalyst coal slurry in the catalyst coal slurry tank 401, pressurizing and conveying it to the coal slurry tank 403 via the catalyst coal slurry pump 402, and pressurizing and conveying the catalyst oil coal slurry to the inlet of the high-pressure coal slurry pump 405 and the high-pressure coal slurry pump 406 via the coal slurry pump 405 and the high-pressure coal slurry pump 406. After being pressurized by the high-pressure coal slurry pump 405 and the high-pressure coal slurry pump 406, the slurry is mixed with hydrogen from the hydrogen heater 410 through the coal slurry heater 407, the coal slurry heat exchanger 408, the coal slurry heater 409, and the first reactor 1 and the second reactor 2.

[0030] In some embodiments of this disclosure, reference is made to Figure 1 and Figure 2As shown, the direct coal liquefaction separation equipment also includes a circulating pump 5. The method further includes: conveying the bottom material of the buffer tank 3 to the first reactor 1 via the circulating pump 5 through the bottom material outlet of the buffer tank 3. In this way, the liquid phase material separated by the buffer tank 3 can settle at the bottom. By conveying the bottom material separated by the buffer tank 3 to the circulating pump 5, compared to conveying the bottom material separated by the hot high-pressure separator 4 to the first reactor 1 via the circulating pump 5, the bottom material separated by the buffer tank 3 does not need to be cooled by quench oil. This avoids the situation where the inlet temperature of the circulating pump 5 decreases upon entering the circulating pump 5, leading to a decrease in the inlet temperature of the first reactor 1. This helps to avoid the need to increase the heating furnace capacity to maintain the temperature of the first reactor 1, resulting in energy waste. Therefore, the setting of the circulating pump 5 is beneficial for buffering and heating the liquid phase material entering the inlet of the circulating pump 5, thereby reducing energy consumption.

[0031] In some embodiments of this disclosure, the bottom material outlet temperature of the buffer tank 3 is 450℃~460℃, and the pressure is 19-20 MPa. The outlet temperature of the first reactor 1 is also 450℃~460℃, and the pressure is 19-20 MPa. This ensures that the bottom material outlet temperature of the buffer tank 3 is kept consistent with the outlet temperature of the first reactor 1, preventing fluctuations in local temperature or pressure within the first reactor 1 caused by the entry of low-temperature or low-pressure materials. Therefore, by recirculating the bottom material of the buffer tank 3 back into the first reactor 1, there is no need to add a heating furnace for reheating, thus reducing energy waste in the heating process. Simultaneously, maintaining the high temperature and high pressure of the recirculated material helps ensure the stability of the operating conditions within the first reactor 1.

[0032] In some embodiments of this disclosure, reference is made to Figure 1 As shown, the material at the top of the buffer tank 3 is fed into the hot high-pressure separator 4 through the material outlet at the top of the buffer tank 3. The process also includes: introducing quench oil into the hot high-pressure separator 4 through the quench oil inlet. Thus, when the material at the top of the buffer tank 3 is fed into the hot high-pressure separator 4, the quench oil inlet is injected into the hot high-pressure separator 4 for cooling, which lowers the reaction temperature inside the hot high-pressure separator 4. This is beneficial for improving the separation speed and efficiency of the hot high-pressure separator 4. Simultaneously, it avoids the risk of "sudden boiling" caused by high-temperature material directly entering the hot high-pressure separator 4, which could lead to a large amount of coal powder being carried to the subsequent gas phase system, causing blockage of the subsequent system.

[0033] In some embodiments of this disclosure, reference is made to Figure 1As shown, the temperature of the hot high-pressure separator 4 is 410℃~420℃, and the pressure is 19-20MPa. This ensures that the internal temperature of the hot high-pressure separator 4 is lower than the temperature of the material output from the second reactor 2, allowing the coking and polymerization reactions of heavy oil and unreacted coal particles in the material to enter the liquid phase of the hot high-pressure separator 4. This reduces the risk of pipeline blockage in the subsequent system due to coal powder carried by the gas phase at the top of the hot high-pressure separator 4. Simultaneously, maintaining the temperature at 410℃~420℃ avoids insufficient heat in the subsequent system due to excessive temperature drops, resulting in a reduced oil extraction rate and incomplete asphalt formation at the bottom of the pressure reducing tower. Since the pressure of the hot high-pressure separator 4 is consistent with the pressure of the first reactor 1 and the buffer tank 3, pressure fluctuations during material flow are minimized, which helps reduce energy losses caused by pressure regulation.

[0034] In some embodiments of this disclosure, reference is made to Figure 1 As shown, the direct coal liquefaction separation equipment also includes a high-temperature high-pressure separator 6 connected to the top material outlet of the high-temperature high-pressure separator 4, and a medium-temperature high-pressure separator 7 connected to the bottom material outlet of the high-temperature high-pressure separator 4. The method further includes: feeding the top material of the high-temperature high-pressure separator 4 into the high-temperature high-pressure separator 6 through the top material outlet of the high-temperature high-pressure separator 4; and feeding the bottom material of the high-temperature high-pressure separator 4 into the medium-temperature high-pressure separator 7 through the bottom material outlet of the high-temperature high-pressure separator 4. In this way, by conveying the top material of the high-temperature high-pressure separator 4 to the high-temperature high-pressure separator 6, the high-temperature high-pressure separator 6 can further separate the conveyed material to increase the gas concentration and improve the material recycling efficiency. By conveying the bottom material to the medium-temperature high-pressure separator 7, the pressure is reduced by the medium-temperature high-pressure separator 7 to release the dissolved gas, reducing resource waste and helping to ensure oil quality.

[0035] The top of the hot high-pressure separator 4 can also be equipped with spray oil. The top gas phase material separated by the hot high-pressure separator 4 is washed by the spray oil and then passes through the hydrogen heat exchanger 411 and the coal slurry heat exchanger 408 in sequence before entering the warm high-pressure separator 6. It is then further processed by the high-pressure air cooler 412 and the cold high-pressure separator 413.

[0036] In some embodiments of this disclosure, reference is made to Figure 1As shown, the direct coal liquefaction separation equipment includes a medium-temperature and medium-pressure separator 8, a high-pressure quench oil pump 9, and a high-pressure quench oil air cooler 10 connected in series with the hot medium-pressure separator 7. The outlet end of the high-pressure quench oil air cooler 10 is connected to a second connecting pipe 30. The first branch 301 of the second connecting pipe 30 is connected to the inlet end of the second reactor 2, and the second branch 302 of the second connecting pipe 30 is connected to the inlet end of the hot high-pressure separator 4. The bottom material of the hot high-pressure separator 4 is fed into the hot medium-pressure separator 7 through the bottom material outlet of the hot high-pressure separator 4. The equipment also includes: quench oil generated after the material entering the hot medium-pressure separator 7 passes through the medium-temperature and medium-pressure separator 8, the high-pressure quench oil pump 9, and the high-pressure quench oil air cooler 10 in sequence is fed into the inlet end of the second reactor 2 through the first branch 301 and into the inlet end of the hot high-pressure separator 4 through the second branch 302.

[0037] In this way, the bottom material of the hot high-pressure separator 4 can be further separated by the hot medium-pressure separator 7 and the warm medium-pressure separator 8. After being pressurized by the high-pressure quench oil pump 9 and cooled by the high-pressure quench air cooler, it is transported as quench oil to the second reactor 2 through the first branch 301 to control the inlet temperature of the second reactor 2, avoid local overheating, and help ensure the stability of the reaction temperature inside the second reactor 2. At the same time, it can also be transported back to the hot high-pressure separator 4 through the second branch 302 to be injected into the hot high-pressure separator 4 through the quench oil inlet, thereby cooling the inlet of the hot high-pressure separator 4 and inhibiting the coking of heavy components inside the hot high-pressure separator 4, which would cause the hot high-pressure separator 4 to become clogged and require shutdown.

[0038] In addition, the bottom material separated by the hot high-pressure separator 4 is depressurized by the pressure reducing valve and then enters the hot medium-pressure separator 7 and the warm medium-pressure separator 8. Some of the material can enter the medium-pressure air cooler 415 and the cold medium-pressure separator 414, and then enter the atmospheric pressure tower 416 for separation. The material in the atmospheric pressure tower 416 is pressurized by the first atmospheric pump 417, the second atmospheric pump 418, and the third atmospheric pump 419 and then transported to the hydrogenation stabilization unit for processing. The bottom material of the atmospheric pressure tower 416 is pressurized by the bottom pump 420, heated by the pressure reducing tower heater 421, and then transported to the pressure reducing tower. The oil in the pressure reducing tower 422 is pressurized by the first pressure reducing pump 423 and the second pressure reducing pump 424 and then transported to the hydrogenation stabilization unit for processing. The bottom material of the pressure reducing tower 422 is pressurized by the bottom pump 425 and then transported to the oil residue forming device.

[0039] It should be understood that the components disclosed herein include: first reactor 1, second reactor 2, hot high-pressure separator 4, warm high-pressure separator 6, hot medium-pressure separator 7, warm medium-pressure separator 8, high-pressure quench oil pump 9, high-pressure quench oil air cooler 10, catalyst coal slurry tank 401, catalyst coal slurry pump 402, coal slurry tank 403, coal slurry pump 404, high-pressure coal slurry pump one 405, high-pressure coal slurry pump two 406, coal slurry heater one 407, coal slurry heat exchanger 408, coal slurry heater two 409, hydrogen heater 410, hydrogen heat exchanger 411, and high-pressure air cooler 412. The specific structures and names of the following components are known to those skilled in the art: cold high-pressure separator 413, cold medium-pressure separator 414, medium-pressure air cooler 415, atmospheric pressure tower 416, atmospheric pressure pump 417, atmospheric pressure pump 2, atmospheric pressure pump 3, atmospheric pressure pump 419, atmospheric pressure bottom pump 420, pressure reducing tower heater 421, pressure reducing tower 422, pressure reducing pump 1, pressure reducing pump 2, and pressure reducing pump bottom 425. These structures and names are known to those skilled in the art, and those skilled in the art can clearly understand the inventive concept of this disclosure after reading it. For the sake of brevity and to highlight the improvements of this disclosure, the structures will not be described in detail here.

[0040] The preferred embodiments of this disclosure have been described in detail above with reference to the accompanying drawings. However, this disclosure is not limited to the specific details of the above embodiments. Within the scope of the technical concept of this disclosure, various simple modifications can be made to the technical solutions of this disclosure, and these simple modifications all fall within the protection scope of this disclosure.

[0041] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, this disclosure will not describe the various possible combinations separately.

[0042] Furthermore, various different embodiments of this disclosure can be combined in any way, as long as they do not violate the spirit of this disclosure, they should also be regarded as the content disclosed in this disclosure.

Claims

1. A coal direct liquefaction and separation device, characterized in that, The direct coal liquefaction and separation equipment includes: First reactor; The second reactor is connected in series with the first reactor; A buffer tank is connected to the outlet end of the second reactor; A hot high-pressure separator is connected to the top material outlet of the buffer tank.

2. The coal direct liquefaction separation equipment according to claim 1, characterized in that, The top material outlet of the buffer tank is connected to the inlet of the hot high-pressure separator through a first connecting pipe. A quench oil inlet is provided on the first connecting pipe. The direct coal liquefaction separation equipment includes a circulating pump. The bottom material outlet of the buffer tank is connected to the inlet of the circulating pump, and the outlet of the circulating pump is connected to the first reactor.

3. The coal direct liquefaction separation equipment according to claim 2, characterized in that, The direct coal liquefaction separation equipment includes a hot medium-pressure separator, a warm medium-pressure separator, a high-pressure quench oil pump, and a high-pressure quench oil air cooler, which are connected in series with the bottom material outlet of the hot high-pressure separator. The outlet of the high-pressure quench oil air cooler is connected to a second connecting pipe. The first branch of the second connecting pipe is connected to the inlet of the second reactor, and the second branch of the second connecting pipe is connected to the quench oil inlet.

4. A process for direct coal liquefaction and separation, characterized in that, The method is applied to a direct coal liquefaction separation device, which includes a first reactor, a second reactor, a buffer tank, and a hot high-pressure separator. The pretreated material is sequentially liquefied by passing it through the first reactor and the second reactor. The material processed by the second reactor is fed into the buffer tank; The top material of the buffer tank is fed into the hot high-pressure separator through the top material outlet of the buffer tank.

5. The process method for direct coal liquefaction and separation according to claim 4, characterized in that, The direct coal liquefaction separation equipment further includes a circulating pump, and the method further includes: The bottom material of the buffer tank is transported to the first reactor via the circulating pump through the bottom material outlet of the buffer tank.

6. The process method for direct coal liquefaction and separation according to claim 5, characterized in that, The bottom material outlet temperature of the buffer tank is 450℃~460℃, and the pressure is 19-20 MPa. The outlet temperature of the first reactor is 450℃~460℃, and the pressure is 19-20 MPa.

7. The process method for direct coal liquefaction and separation according to claim 4, characterized in that, The step of introducing the top material of the buffer tank into the hot high-pressure separator through the top material outlet of the buffer tank further includes: Cooling oil is introduced into the hot high-pressure separator through the cooling oil inlet.

8. The process method for direct coal liquefaction and separation according to claim 7, characterized in that, The temperature of the hot high-pressure separator is 410℃~420℃, and the pressure is 19-20MPa.

9. The process method for direct coal liquefaction and separation according to claim 4, characterized in that, The direct coal liquefaction separation equipment further includes a high-temperature high-pressure separator connected to the top material outlet of the high-pressure thermal separator, and a medium-pressure thermal separator connected to the bottom material outlet of the high-pressure thermal separator. The method further includes: The top material of the hot high-pressure separator is fed into the warm high-pressure separator through the top material outlet of the hot high-pressure separator; the bottom material of the hot high-pressure separator is fed into the hot medium-pressure separator through the bottom material outlet of the hot high-pressure separator.

10. The process method for direct coal liquefaction and separation according to claim 9, characterized in that, The direct coal liquefaction separation equipment includes a medium-temperature separator, a high-pressure quench oil pump, and a high-pressure quench oil air cooler connected in series with the hot medium-pressure separator. The outlet end of the high-pressure quench oil air cooler is connected to a second connecting pipeline. The first branch of the second connecting pipeline is connected to the inlet end of the second reactor, and the second branch of the second connecting pipeline is connected to the inlet end of the hot high-pressure separator. The step of introducing the bottom material of the hot high-pressure separator into the hot medium-pressure separator through the bottom material outlet of the hot high-pressure separator also includes: The material entering the hot-medium pressure separator passes sequentially through the hot-medium pressure separator, the high-pressure quenching oil pump, and the quenching oil generated after the high-pressure quenching oil is air-cooled. The quenching oil is then introduced into the inlet of the second reactor through the first branch and into the inlet of the hot-high pressure separator through the second branch.

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