Method for coal liquefaction system to respond to hydrogen fluctuation and coal liquefaction system

Abstract

The present disclosure relates to a coal liquefaction system hydrogen fluctuation response method and a coal liquefaction system, comprising the following steps: reducing the load of the coal liquefaction system, and supplementing hydrogen to the system through a backup hydrogen source; reducing the temperature of the reaction coal slurry, and controlling the opening of the feed valve to control the flow of the coal slurry to the coal slurry heating furnace; controlling the vacuum degree in the vacuum fractionating tower, reducing the solid content of the material entering the vacuum fractionating tower; controlling the liquid level of the separator to be not less than 20%; and controlling the liquid level in the fractionating tower to be not less than 50%. The coal liquefaction system hydrogen fluctuation response method of the present disclosure can ensure the normal operation of the coal liquefaction system when hydrogen fluctuation occurs in the coal liquefaction system, by reducing the load in the system and the corresponding vacuum degree and liquid level in each component in the system, increasing the reaction time of the coal slurry in the coal liquefaction system, thereby reducing the impact of hydrogen fluctuation on the system.

Description

Technical Field

[0001] This disclosure relates to the field of coal liquefaction technology, and more specifically, to a method for a coal liquefaction system to cope with hydrogen fluctuations, and a coal liquefaction system. Background Technology

[0002] In coal liquefaction systems, the coal undergoes hydrocracking with the help of hydrogen and catalysts, ultimately transforming it into liquid fuel. During processing, malfunctions in hydrogen production equipment or hydrogen transport pipelines can affect the hydrogen content in the coal liquefaction system, causing fluctuations in hydrogen levels. This can hinder the full progress of the coal liquefaction reaction, reduce the yield and quality of liquefied oil, potentially trigger side reactions, increase production costs, and create safety hazards. Summary of the Invention

[0003] The purpose of this disclosure is to provide a method for dealing with hydrogen fluctuations in a coal liquefaction system, which can effectively cope with hydrogen fluctuations during the operation of the coal liquefaction system, avoid the impact of hydrogen fluctuations on the yield and output of the coal liquefaction system, and avoid damage to the coal liquefaction system.

[0004] To achieve the above objectives, a first aspect of this disclosure provides a method for a coal liquefaction system to cope with hydrogen fluctuations, comprising the following steps: Reduce the load on the coal liquefaction system and replenish hydrogen to the system through a backup hydrogen source; Lower the temperature of the reaction coal slurry and control the opening of the feed valve to control the flow rate of the coal slurry flowing to the coal slurry heater; Controlling the vacuum level in the vacuum distillation tower reduces the solid content of the material entering the vacuum distillation tower; Control the liquid level in the separator to be no lower than 20%; The liquid level in the fractionation tower should be controlled to be no lower than 50%.

[0005] Optionally, reducing the load on the coal liquefaction system and replenishing the system with hydrogen from a backup hydrogen source includes: The system pressure is restored to 2.5-3 MPa within 5-10 minutes using the backup hydrogen source, and the system load is reduced from 100% to 45-55% within 30 minutes.

[0006] Optionally, reducing the system load from 100% to 45-55% within 30 minutes includes: The material level in the coal slurry catalyst tank is controlled at 30-50%, the coal powder silo is operated at a material level of 80-100T, the capacity of the catalyst silo is controlled below 150T, and the material level in the catalyst tank is controlled at 50-70%.

[0007] Optionally, reducing the system load from 100% to 45-55% within 30 minutes includes: The sulfide content in the system is detected at preset intervals.

[0008] Optionally, the method of reducing the temperature of the reacting coal slurry and deflecting the coal slurry flowing to the coal slurry heater includes: Flushing oil is introduced into the coal slurry catalyst tank to mix with coal powder, and the opening of the four feed valves connected to the coal slurry heater and arranged in sequence along the vertical direction is adjusted to an asymmetrical distribution of 40%-60%, and the temperature difference of the furnace tubes of the coal slurry heater is controlled to be ±5℃.

[0009] Optionally, controlling the vacuum level in the vacuum distillation column to reduce the solids content of the material entering the vacuum distillation column includes: The temperature in the reactor is controlled to not exceed 456℃, the vacuum degree in the vacuum distillation tower is controlled to 1.0-1.5kPa, and the solid content of the material entering the vacuum distillation tower is controlled to be less than 50%.

[0010] Optionally, the vacuum feed heater is connected to the vacuum fractionation tower for feeding material into the vacuum fractionation tower, and controlling the solid content of the material entering the vacuum fractionation tower to be less than 50% includes: The outlet temperature of the vacuum-pressure feeding furnace is controlled to be 390-400℃.

[0011] Optionally, controlling the liquid level in the separator to be not lower than 20% includes: Control the liquid levels of the hot high-pressure separator, warm high-pressure separator, cold high-pressure separator, hot medium-pressure separator, warm medium-pressure separator, and cold medium-pressure separator, and open the membrane separation line when the gas pressure in the separator is high.

[0012] Optionally, ensuring that the liquid level in the fractionation column is not lower than 50% includes: Control the liquid levels in the atmospheric distillation column and the vacuum distillation column, and adjust the flow rates of the materials in the first and second transport lines according to the liquid levels in the atmospheric distillation column and the vacuum distillation column.

[0013] A second aspect of this disclosure also provides a coal liquefaction system as described in the above-mentioned method for coping with hydrogen fluctuations in a coal liquefaction system, comprising: The coal powder unit includes a catalyst tank, a coal slurry catalyst tank, a coal powder silo, and a catalyst silo. A liquefaction unit, comprising a heating furnace, a reactor, a separator, and a fractionation tower; A backup hydrogen source is provided, which is connected to the liquefaction unit.

[0014] The advantages of this disclosure through the above technical solution are as follows: The method of this disclosure for dealing with hydrogen fluctuations in a coal liquefaction system can increase the reaction time of coal slurry in the coal liquefaction system by reducing the load in the system and correspondingly reducing the vacuum and liquid level in each component of the system when hydrogen fluctuations occur. This ensures the normal operation of the coal liquefaction system, buys enough time for emergency repairs of hydrogen fluctuations, thereby reducing the impact of hydrogen fluctuations on the system and avoiding damage to equipment in the coal liquefaction system caused by hydrogen fluctuations.

[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 coal liquefaction system provided in the exemplary embodiments of this disclosure; Figure 2 This is a flowchart of a method for a coal liquefaction system to cope with hydrogen fluctuations provided in an exemplary embodiment of this disclosure.

[0017] Explanation of reference numerals in the attached figures 1-Pulverized coal unit; 11-Catalyst tank; 12-Coal slurry catalyst tank; 13-Pulverized coal silo; 131-Coal slurry heater; 14-Catalyst silo; 2-Liquefaction Unit; 21-Heating Furnace; 211-Coal Slurry Heating Furnace; 212-Feed Valve; 213-Reduced Pressure Feeding Heating Furnace; 22-Reactor; 23-Separator; 231-Hot High Pressure Separator; 232-Warm High Pressure Separator; 233-Cold High Pressure Separator; 234-Hot Medium Pressure Separator; 235-Warm Medium Pressure Separator; 236-Cold Medium Pressure Separator; 24-Fracturing Tower; 241-Reduced Pressure Fractionating Tower; 242-Ambient Pressure Fractionating Tower; 25-First Conveyor Line; 26-Second Conveyor Line; 3-Backup hydrogen source; 4-Membrane separation line. 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, directional terms such as "upper," "lower," "higher," "lower," "top," and "bottom" generally refer to the orientation of the corresponding component or structure in the direction of gravity. "Inner" and "outer" refer to the inner and outer contours of the corresponding component. Furthermore, it should be noted that terms such as "first" and "second" are used to distinguish one element from another and do not indicate sequence or importance. Additionally, in the description with reference to the accompanying drawings, the same reference numerals in different drawings denote the same element. The above definitions are for explanation and illustration only and should not be construed as limiting this disclosure.

[0020] This disclosure relates to a method for coping with hydrogen fluctuations in a coal liquefaction system. This method can be used when hydrogen fluctuations occur in the coal liquefaction system to prevent excessive impact of hydrogen fluctuations on the entire system. See [link to relevant documentation]. Figure 1 and Figure 2 The method disclosed herein includes the following steps: By reducing the load on the coal liquefaction system and replenishing the system with hydrogen from the backup hydrogen source 3, the overall hydrogen consumption in the system can be reduced, thus avoiding the problem of reduced hydrogen supply due to hydrogen fluctuations. Replenishing the system with hydrogen from the backup hydrogen source 3 can alleviate the problem of reduced hydrogen supply due to hydrogen fluctuations to a certain extent and buy enough time to repair the hydrogen fluctuations. The backup hydrogen source 3 can be a backup hydrogen source 3 known to those skilled in the art, such as a PSA hydrogen extraction unit, and will not be described in detail here.

[0021] Lowering the temperature of the reacting coal slurry and controlling the opening of the feed valve 212 controls the flow rate of the coal slurry to the coal slurry heater 211. By reducing the reaction temperature of the coal slurry, the reaction time of the coal slurry in the system can be increased, providing more time to repair hydrogen fluctuations. Controlling the opening of the feed valve 212 controls the flow rate of the coal slurry to the coal slurry heater 211. Due to the reduced load and raw material of the coal liquefaction system, if the feed inlets at different heights connected to the coal slurry heater 211 operate at their original flow rates, flow deviation will occur. By adjusting the opening of the feed valve 212 according to the height of the feed inlet, it can be ensured that the material entering the coal slurry heater 211 will not have flow deviation, thus ensuring the accuracy of the quality of the coal slurry entering the coal slurry heater 211.

[0022] Controlling the vacuum level in the vacuum fractionation tower 241 reduces the solid content of the material entering the vacuum fractionation tower 241. Due to the reduced load of the entire coal liquefaction system, if the original vacuum level and solid content of the material are maintained, the material residence time in the vacuum fractionation tower 241 will be longer, and the material will crystallize in the vacuum fractionation tower 241, affecting the system's output and the safety of the equipment in the system.

[0023] The liquid level in separator 23 of the coal liquefaction system is controlled to be no lower than 20%, and the liquid level in fractionation tower 24 is controlled to be no lower than 50%. This setting can prevent the liquid in separator 23 and fractionation tower 24 from being drained during the separation and fractionation process, which could lead to communication and damage between separator 23 and fractionation tower 24 at different pressures.

[0024] The method disclosed herein for dealing with hydrogen fluctuations in a coal liquefaction system increases the reaction time of the coal slurry by reducing the load on the system and correspondingly reducing the vacuum and liquid level in each component when hydrogen fluctuations occur. This ensures the normal operation of the coal liquefaction system, provides sufficient time for emergency repairs of hydrogen fluctuations, reduces the impact of hydrogen fluctuations on the system, and prevents damage to equipment in the coal liquefaction system caused by hydrogen fluctuations.

[0025] In some embodiments of this disclosure, see Figure 1 and Figure 2 To reduce the load on the coal liquefaction system and replenish hydrogen to the system through backup hydrogen source 3, the following measures are taken: By using backup hydrogen source 3, the system pressure is restored to 2.5-3 MPa within 5-10 minutes, and the system load is reduced from 100% to 45-55% within 30 minutes. Restoring the system pressure to 2.5-3 MPa within 5-10 minutes prevents a rapid pressure drop that could lead to a rapid temperature decrease, thus affecting the coal slurry reaction. Reducing the system load from 100% to 45-55% within 30 minutes rapidly reduces the system load, decreasing the amount of hydrogen required for the reaction. This avoids insufficient hydrogen for the liquefaction reaction due to a slow load reduction, which could hinder subsequent normal system operation and allow sufficient time for emergency repairs.

[0026] In some embodiments of this disclosure, see Figure 1 and Figure 2 Reducing the system load from 100% to 45-55% within 30 minutes includes: The material level in the coal slurry catalyst tank 12 is controlled at 30-50%, the coal powder silo 13 operates at a material level of 80-100T, the capacity of the catalyst silo 14 is controlled below 150T, and the material level in the catalyst tank 11 is controlled at 50-70%. By controlling the material levels in the coal slurry catalyst tank 12, coal powder silo 13, catalyst silo 14, and catalyst tank 11, the load in the coal liquefaction system can be accurately reduced. This avoids situations where the material levels in the coal slurry catalyst tank 12, coal powder silo 13, catalyst silo 14, and catalyst tank 11 are too high or too low. In such cases, after hydrogen fluctuations, the system may be unable to maintain normal operation due to insufficient hydrogen supply or insufficient replenishment of hydrogen to sustain the normal liquefaction reaction. This can lead to insufficient time for emergency repairs due to hydrogen fluctuations, affecting the subsequent use of the coal liquefaction system and causing damage to the equipment within the system.

[0027] In some embodiments of this disclosure, see Figure 1 and Figure 2 Reducing the system load from 100% to 45-55% within 30 minutes includes: During the load reduction process, the sulfide content in the system is detected at preset intervals. Since the catalyst produces harmful gases such as hydrogen sulfide during use, failure to detect these gases would pose a threat to the safety of workers. Detecting the sulfide content at preset intervals ensures the safety of workers during the load reduction process in the coal liquefaction system and subsequent load reduction operations. The preset intervals can be half an hour, one hour, etc., and the method of detecting sulfides can be any conventional technical means used by those skilled in the art. The specific method can be determined according to the actual situation, and this disclosure does not impose any restrictions on it.

[0028] In some embodiments of this disclosure, see Figure 1 and Figure 2 The measures to lower the temperature of the reacting coal slurry and to deflect the coal slurry flowing to the coal slurry heater 211 include: Flushing oil is introduced into the coal slurry catalyst tank 12 to mix with pulverized coal. The opening of the four feed valves 212, which are connected to the coal slurry heater 211 and arranged vertically in sequence, is adjusted to an asymmetrical distribution of 40%-60%, and the temperature difference of the furnace tubes of the coal slurry heater 131 is controlled to be ±5℃. Introducing flushing oil into the coal slurry catalyst tank 12 to mix with pulverized coal effectively lowers the temperature of the mixed coal slurry, preventing excessively high temperatures that could reduce the time for subsequent liquefaction reactions and thus ensure sufficient reaction even with low hydrogen levels. Adjusting the opening of the four feed valves 212, which are connected to the coal slurry heater 211 and arranged vertically in sequence in an asymmetrical distribution of 40%-60%, avoids flow deviation problems that might occur if the feed inlets at different heights connected to the coal slurry heater 211 operate at the original flow rate. This ensures the accuracy of the quality of the coal slurry entering the coal slurry heater 211. Specific adjustment parameters can be determined according to actual conditions. If the temperature difference of the furnace tubes of the coal slurry heater 131 is controlled to be ±5℃, coking will occur at the furnace tubes of the coal slurry heater 131, affecting the subsequent passage of coal slurry.

[0029] In some embodiments of this disclosure, see Figure 1 and Figure 2 Controlling the vacuum level in the vacuum distillation column 241 and reducing the solids content of the material entering the vacuum distillation column 241 includes: Reactor 22 is the reactor in liquefaction unit 2, capable of liquefying coal slurry. By controlling the temperature in reactor 22 to not exceed 456℃, crystallization of the liquefaction products after exiting reactor 22 due to excessively high temperature can be avoided, which would affect subsequent separation and fractionation of the liquefaction products and impact system output. Controlling the vacuum degree in vacuum distillation tower 241 to 1.0-1.5 kPa and ensuring the solid content of the material entering vacuum distillation tower 241 is below 50% can prevent crystallization in vacuum distillation tower 241 due to excessively low vacuum and high solid content, thus avoiding prolonged residence time and impact on output and system equipment safety.

[0030] In some embodiments of this disclosure, see Figure 1 and Figure 2 Controlling the vacuum level in the vacuum distillation column 241 and reducing the solids content of the material entering the vacuum distillation column 241 includes: The outlet temperature of the vacuum feed heater 213 is controlled at 390-400℃. The vacuum feed heater 213 is a heater that feeds materials to the vacuum fractionation tower 241. By controlling the outlet temperature of the feed heater 213, the problem of poor material flowability and coking due to deposition in the pipeline of the material being fed into the vacuum fractionation tower 241 can be avoided, thus ensuring the stability and safety of the system during operation.

[0031] In some embodiments of this disclosure, see Figure 1 and Figure 2 Controlling the liquid level in separator 23 to be no less than 20% includes: The separator 23 may include a hot high-pressure separator 231, a warm high-pressure separator 232, a cold high-pressure separator 233, a hot medium-pressure separator 234, a warm medium-pressure separator 235, and a cold medium-pressure separator 236. Separators 23 with different temperature and pressure differences can separate materials with different melting points. By controlling the liquid levels of the hot high-pressure separator 231, the warm high-pressure separator 232, the cold high-pressure separator 233, the hot medium-pressure separator 234, the warm medium-pressure separator 235, and the cold medium-pressure separator 236, the problem of liquid being pumped out of the separator 23 due to low liquid levels in each separator 23, and the separation of separators 23 with different temperature and pressure differences being damaged due to liquid being pumped out, can be avoided.

[0032] Separators 23 with different temperature and pressure differences are connected in sequence. Finally, the gas in each separator 23 is discharged through the cold high-pressure separator 233. A membrane separation line 4 is provided at the outlet of the cold high-pressure separator 233. The gas is discharged through the membrane separation line 4, which can filter impurities in the gas. When the gas pressure in the separator 23 is too high, the separation membrane in the membrane separation line 4 can be opened to ensure that the gas can be discharged quickly without affecting the quality of the discharged gas, and to avoid large gas damage to the membrane separation line 4.

[0033] In some embodiments of this disclosure, see Figure 1 and Figure 2 Controlling the liquid level in fractionation column 24 to be not lower than 50% includes: The fractionation column 24 may include an atmospheric fractionation column 242 and a vacuum fractionation column 241. The fractionation columns 24 with different pressure differentials can separate materials with different melting points. By controlling the liquid levels of the atmospheric fractionation column 242 and the vacuum fractionation column 241, the problem of liquid being pumped out of the fractionation column 24 due to the liquid level in each fractionation column 24 being too low, and the fractionation columns 24 with different pressure differentials being damaged due to the liquid being pumped out, can be avoided. A first transport line 25 and a second transport line 26 can be set between the atmospheric distillation tower 242 and the vacuum distillation tower 241. The first transport line 25 and the second transport line 26 can transport materials between the two distillation towers 24. Due to the reduced load of the coal liquefaction system, the originally balanced material transport of the first transport line 25 and the second transport line 26 may result in one of the transport lines being unable to maintain its original transport volume. At this time, the material transport volume of the first transport line 25 and the second transport line 26 can be adjusted according to the actual liquid level in the atmospheric distillation tower 242 and the vacuum distillation tower 241, so as to ensure that the two transport lines do not have a flow deviation and maintain the normal operation of the two transport lines.

[0034] A second aspect of this disclosure also provides a coal liquefaction system, see [link to relevant documentation]. Figure 1 and Figure 2 It includes a pulverized coal unit 1, a liquefaction unit 2, and a backup hydrogen source 3. The pulverized coal unit 1 can perform preliminary treatment of pulverized coal and includes a catalyst tank 11, a coal slurry catalyst tank 12, a pulverized coal silo 13, and a catalyst silo 14. The catalyst silo 14 is connected to the catalyst tank 11 and can provide catalyst to the catalyst tank 11. The pulverized coal silo 13 and the catalyst tank 11 are connected to the coal slurry catalyst tank 12. Through the pulverized coal silo 13 and the catalyst tank 11, pulverized coal and catalyst can be transported to the coal slurry catalyst tank 12 for mixing, which facilitates the subsequent liquefaction reaction of the coal slurry.

[0035] The liquefaction unit 2 is capable of liquefying coal slurry and includes a heater 21, a reactor 22, a separator 23, and a fractionation tower 24. The heater 21 may include a hydrogen heater, a coal slurry heater, etc. The reactor 22 may include reactors for different types of coal slurry liquefaction reactions. The separator 23 and the fractionation tower 24 can be of the types described in the above embodiments, and can be determined according to actual conditions. This disclosure does not limit them. The backup hydrogen source 3 may be a backup hydrogen source 3 known to those skilled in the art, such as a PSA hydrogen extraction unit, and will not be described in detail here.

[0036] 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.

[0037] 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.

[0038] 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 method for coping with hydrogen fluctuations in a coal liquefaction system, characterized in that, Includes the following steps: Reduce the load on the coal liquefaction system and replenish hydrogen to the system through a backup hydrogen source; Lower the temperature of the reaction coal slurry and control the opening of the feed valve to control the flow rate of the coal slurry flowing to the coal slurry heater; Controlling the vacuum level in the vacuum distillation column reduces the solid content of the material entering the vacuum distillation column; Control the liquid level in the separator to be no lower than 20%; The liquid level in the fractionation tower should be controlled to be no lower than 50%.

2. The method for coping with hydrogen fluctuations in a coal liquefaction system according to claim 1, characterized in that, The reduction of the load on the coal liquefaction system and the replenishment of hydrogen to the system through a backup hydrogen source include: The system pressure is restored to 2.5-3 MPa within 5-10 minutes using the backup hydrogen source, and the system load is reduced from 100% to 45-55% within 30 minutes.

3. The method for coping with hydrogen fluctuations in a coal liquefaction system according to claim 2, characterized in that, The reduction of system load from 100% to 45-55% within 30 minutes includes: Control the material level in the coal slurry catalyst tank to 30-50%, keep the coal powder silo at a material level of 80-100T, control the capacity of the catalyst silo to below 150T, and control the material level in the catalyst tank to 50-70%.

4. The method for coping with hydrogen fluctuations in a coal liquefaction system according to claim 2, characterized in that, The reduction of system load from 100% to 45-55% within 30 minutes includes: The sulfide content in the system is detected at preset intervals.

5. The method for coping with hydrogen fluctuations in a coal liquefaction system according to claim 1, characterized in that, The method of reducing the temperature of the reacting coal slurry and deflecting the coal slurry flowing to the coal slurry heater includes: Flushing oil is introduced into the coal slurry catalyst tank to mix with coal powder, and the opening of the four feed valves connected to the coal slurry heater and arranged in sequence along the vertical direction is adjusted to an asymmetrical distribution of 40%-60%, and the temperature difference of the furnace tubes of the coal slurry heater is controlled to be ±5℃.

6. The method for coping with hydrogen fluctuations in a coal liquefaction system according to claim 1, characterized in that, Controlling the vacuum level in the vacuum distillation column to reduce the solid content of the material entering the vacuum distillation column includes: The temperature in the reactor is controlled to not exceed 456℃, the vacuum degree in the vacuum distillation tower is controlled to 1.0-1.5kPa, and the solid content of the material entering the vacuum distillation tower is controlled to be less than 50%.

7. The method for coping with hydrogen fluctuations in a coal liquefaction system according to claim 6, characterized in that, A vacuum feed heater is connected to the vacuum fractionation tower for feeding material into the vacuum fractionation tower. Controlling the solid content of the material entering the vacuum fractionation tower to be less than 50% includes: The outlet temperature of the vacuum-pressure feeding furnace is controlled to be 390-400℃.

8. The method for coping with hydrogen fluctuations in a coal liquefaction system according to claim 7, characterized in that, The control of the separator's liquid level to be not lower than 20% includes: Control the liquid levels of the hot high-pressure separator, warm high-pressure separator, cold high-pressure separator, hot medium-pressure separator, warm medium-pressure separator, and cold medium-pressure separator, and open the membrane separation line when the gas pressure in the separator is high.

9. The method for coping with hydrogen fluctuations in a coal liquefaction system according to claim 7, characterized in that, The control of the liquid level in the fractionation tower to be not lower than 50% includes: Control the liquid levels in the atmospheric distillation column and the vacuum distillation column, and adjust the flow rates of the materials in the first and second transport lines according to the liquid levels in the atmospheric distillation column and the vacuum distillation column.

10. A coal liquefaction system as described in any one of claims 1-9 for coping with hydrogen fluctuations, characterized in that, include: The coal powder unit includes a catalyst tank, a coal slurry catalyst tank, a coal powder silo, and a catalyst silo. A liquefaction unit, comprising a heating furnace, a reactor, a separator, and a fractionation tower; A backup hydrogen source is provided, which is connected to the liquefaction unit.

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