Multi-reactor feed control method, electronic equipment and storage medium for direct coal liquefaction

Abstract

This invention discloses a method for controlling the feed of a multi-reactor system in direct coal liquefaction, electronic equipment, and a storage medium. The method includes: controlling the flow rate of pulverized coal and the flow rate of pulverized coal solvent using a dual closed-loop ratio and injecting the pulverized coal into an oil-coal slurry tank; controlling the flow rate of catalyst pulverized coal and the flow rate of catalyst solvent using a dual closed-loop ratio and injecting the catalyst oil-coal slurry obtained from mixing in the catalyst oil-coal slurry tank into the oil-coal slurry tank; injecting the oil-coal slurry output from the oil-coal slurry tank into an oil-coal slurry heater; injecting liquid sulfur into the oil-coal slurry heater and hydrogen into a hydrogen heater; and inputting the intermediate product output from the oil-coal slurry heater and the heated hydrogen output from the hydrogen heater into the reactor to obtain the product output from the reactor. This invention achieves automatic control of the feed to the direct coal liquefaction reactor, reducing the workload of operators and avoiding deviations caused by the lag of manual adjustments and lack of experience, thus ensuring the efficient operation of the direct coal liquefaction reaction process.

Description

Technical Field

[0001] This invention relates to the field of coal-related technologies, and in particular to a method for controlling the feed of a multi-reactor system for direct coal liquefaction, electronic equipment, and storage medium. Background Technology

[0002] Since the beginning of the 20th century, a number of representative direct coal liquefaction processes have been developed abroad, such as the IGOR+ process jointly developed by the German Mining and Metallurgical Technology and Testing Company, Ruhr Coal Company, and FIBOR Oil Company; the H-Coal process developed by the American Hydrocarbons Research Company; and the NEDOL process developed by the New Energy and Industrial Technology Development Organization of Japan. However, all of these processes only completed small-scale and pilot-scale tests and have not yet been put into industrial-scale production.

[0003] Currently, the mixing ratios of oil-coal slurry, catalyst, liquid sulfur, and hydrogen in industrial reactor feeds are all manually adjusted without automatic control, which easily leads to adjustment lags and deviations of the mixing ratios from production targets.

[0004] In actual production, the following issues exist: Large fluctuations in the concentration of the coal-oil slurry; large fluctuations in the concentration of the catalyst coal-oil slurry, resulting in a mismatch between the injection flow rate and the system's processing capacity. Excessive injection leads to an increase in tetrahydrofuran insolubles at the bottom of the vacuum distillation tower, reducing the system's distilled oil yield; insufficient injection leads to insufficient depth of the direct liquefaction reaction, also reducing the system's distilled oil yield. Similarly, a mismatch between the liquid sulfur injection flow rate and the system's processing capacity results in excessive liquid sulfur injection causing excessive concentrations of hydrogen sulfide in the gas phase, increasing the risk of corrosion in the gas phase pipelines and the difficulty of subsequent tail gas treatment units; insufficient liquid sulfur injection leads to insufficient depth of the direct liquefaction reaction, reducing the system's distilled oil yield. Finally, a mismatch between the hydrogen injection flow rate and the system's processing capacity results in excessive hydrogen injection leading to a useless increase in system energy consumption; insufficient hydrogen injection leads to low hydrogen partial pressure, insufficient reaction depth, and reduced system distilled oil yield. Summary of the Invention

[0005] Therefore, it is necessary to address the lack of automatic control for feed in existing multi-reactor systems for direct coal liquefaction by providing a feed control method, electronic equipment, and storage medium for direct coal liquefaction.

[0006] This invention provides a multi-reactor feed control method for direct coal liquefaction, comprising:

[0007] The flow rate of pulverized coal and the flow rate of pulverized coal solvent are controlled by a double closed-loop ratio and injected into the oil-coal slurry tank. The flow rate of catalyst pulverized coal and the flow rate of catalyst solvent are controlled by a double closed-loop ratio and injected into the catalyst oil-coal slurry tank.

[0008] The catalyst oil-coal slurry obtained from mixing in the catalyst oil-coal slurry tank is injected into the oil-coal slurry tank;

[0009] The oil-coal slurry output from the oil-coal slurry tank is injected into the oil-coal slurry heating furnace;

[0010] Liquid sulfur is injected into an oil-coal slurry heater, and hydrogen is injected into a hydrogen heater.

[0011] The intermediate product output from the oil-coal slurry heater and the heated hydrogen output from the hydrogen heater are fed into the reactor to obtain the product output from the reactor.

[0012] Furthermore, the step of controlling the pulverized coal feed flow rate and the pulverized coal solvent flow rate using a dual closed-loop ratio and injecting the pulverized coal slurry into the oil-coal slurry tank includes:

[0013] Calculate the setpoint for pulverized coal solvent flow rate based on system load and oil-coal slurry concentration;

[0014] The set value of the coal powder solvent flow rate is used as the given value of the coal powder solvent flow rate PID controller. The coal powder solvent supply control valve is controlled by the coal powder solvent flow rate PID controller. The coal powder solvent supply control valve controls the connection between the coal powder solvent and the first input end of the oil-coal slurry mixer.

[0015] The actual coal powder solvent flow rate is detected, and the coal powder feed flow rate set value is calculated based on the actual coal powder solvent flow rate and the oil-coal slurry concentration.

[0016] The set value of the coal powder discharge flow rate is used as the given value of the coal powder discharge flow rate PID controller. The coal powder discharge flow rate PID controller controls the coal powder silo discharge control valve. The coal powder silo discharge control valve controls the connection between the coal powder and the second input terminal of the oil-coal slurry mixer. The oil-coal slurry mixer mixes the coal powder and the coal powder solvent and then injects the mixture into the oil-coal slurry tank.

[0017] Furthermore, the step of controlling the ratio of catalyst pulverized coal flow rate to catalyst solvent flow rate in a dual closed-loop manner and injecting the pulverized coal-catalyst slurry into the catalyst oil-coal slurry tank includes:

[0018] Calculate the catalyst solvent flow rate setpoint based on the system load and catalyst oil-coal slurry concentration;

[0019] The catalyst solvent flow rate setpoint is used as the given value of the catalyst solvent flow rate PID controller. The catalyst solvent supply control valve is controlled by the catalyst solvent flow rate PID controller. The catalyst solvent supply control valve controls the connection between the catalyst solvent and the first input end of the catalyst oil-coal slurry mixer.

[0020] The actual catalyst solvent flow rate is detected, and the catalyst coal powder flow rate set value is calculated based on the actual catalyst solvent flow rate and the catalyst oil-coal slurry concentration.

[0021] The set value of the catalyst pulverized coal flow rate is used as the given value of the catalyst pulverized coal feed flow rate PID controller. The catalyst pulverized coal feed flow rate PID controller controls the catalyst pulverized coal silo feed control valve. The catalyst pulverized coal silo feed control valve controls the connection between the catalyst pulverized coal and the second input end of the catalyst oil-coal slurry mixer. The catalyst oil-coal slurry mixer mixes the catalyst pulverized coal with the catalyst solvent and then injects it into the catalyst oil-coal slurry tank.

[0022] Furthermore:

[0023] The step of injecting the catalyst oil-coal slurry obtained from mixing the catalyst oil-coal slurry tank into the oil-coal slurry tank includes: calculating the catalyst oil-coal slurry flow rate according to the system load, using the catalyst oil-coal slurry flow rate as the setpoint of the catalyst oil-coal slurry flow rate PID controller, controlling the catalyst oil-coal slurry tank bottom pump outlet control valve through the catalyst oil-coal slurry flow rate PID controller, and controlling the connection between the catalyst oil-coal slurry tank and the oil-coal slurry tank through the catalyst oil-coal slurry tank bottom pump outlet control valve;

[0024] The step of injecting the oil-coal slurry output from the oil-coal slurry tank into the oil-coal slurry heater includes: calculating the oil-coal slurry flow rate based on the system load, using the oil-coal slurry flow rate as the setpoint of the oil-coal slurry flow rate PID controller, controlling the high-pressure feed pump frequency converter through the oil-coal slurry flow rate PID controller, controlling the speed of the high-pressure feed pump through the high-pressure feed pump frequency converter, and injecting the oil-coal slurry output from the oil-coal slurry tank into the oil-coal slurry heater by the high-pressure feed pump.

[0025] The process of injecting liquid sulfur into the oil-coal slurry heating furnace includes: calculating the liquid sulfur flow rate based on the system load, using the liquid sulfur flow rate as the setpoint of the liquid sulfur flow rate PID controller, controlling the liquid sulfur pump stroke regulator through the liquid sulfur flow rate PID controller, controlling the stroke of the liquid sulfur pump through the liquid sulfur pump stroke regulator, and injecting liquid sulfur into the oil-coal slurry heating furnace through the liquid sulfur pump.

[0026] The process of injecting hydrogen into the hydrogen heating furnace includes: calculating the hydrogen flow rate based on the system load, using the hydrogen flow rate as the setpoint of the hydrogen flow rate PID controller, controlling the compressor continuously variable speed regulator through the hydrogen flow rate PID controller, controlling the discharge volume of the hydrogen compressor through the compressor continuously variable speed regulator, and injecting hydrogen into the hydrogen heating furnace through the compressor.

[0027] Further, the reactor includes a first reactor and a second reactor, wherein the intermediate product output from the oil-coal slurry heater and the heated hydrogen output from the hydrogen heater are input into the reactor, comprising:

[0028] Set the gas flow rate of the oil-coal slurry heater and the hydrogen heater, input the intermediate product output from the oil-coal slurry heater and the heated hydrogen output from the hydrogen heater into the input end of the first reactor, connect the output end of the first reactor to the input end of the second reactor, output the product from the output end of the second reactor, and inject quench oil and / or quench hydrogen into the reactor connection pipeline connecting the first reactor and the second reactor.

[0029] The temperature of the first reactor connected to the first reactor of the oil-coal slurry heater and the hydrogen heater is detected, and the gas flow rate of the oil-coal slurry heater and the hydrogen heater is adjusted according to the temperature of the first reactor.

[0030] Furthermore, the step of detecting the temperature of the first reactor connected to the first reactor respectively with the oil-coal slurry heater and the hydrogen heater, and adjusting the gas flow rate of the oil-coal slurry heater and the hydrogen heater according to the temperature of the first reactor includes:

[0031] The temperature of the first reactor, which is respectively connected to the oil-coal slurry heater and the hydrogen heater, is detected.

[0032] When the temperature of the first reactor is lower than the first temperature threshold, the gas flow rate of the gas control valve of the oil-coal slurry heater is increased at a first gas rate, and the gas flow rate of the gas control valve of the hydrogen heater is increased at a second gas rate.

[0033] When the temperature of the first reactor is higher than the first temperature threshold, the gas flow rate of the gas control valve of the oil-coal slurry heater is reduced at a first gas rate, and the gas flow rate of the gas control valve of the hydrogen heater is reduced at a second gas rate.

[0034] Furthermore, the method also includes:

[0035] Set the quench oil flow rate and / or quench hydrogen flow rate entering the reactor connection pipeline, detect the temperature of the second reactor connected to the first reactor, and adjust the quench oil flow rate and / or the quench hydrogen flow rate according to the temperature of the second reactor.

[0036] Furthermore, the step of detecting the temperature of the second reactor connected to the first reactor, and adjusting the quench oil flow rate and / or the quench hydrogen flow rate based on the second reactor temperature, includes:

[0037] Detect the temperature of the second reactor connected to the first reactor;

[0038] When the temperature of the second reactor is lower than the second temperature threshold, the quench oil flow rate is controlled to decrease at the quench oil rate and / or the quench hydrogen flow rate is controlled to decrease at the quench hydrogen rate.

[0039] When the temperature of the second reactor is higher than the second temperature threshold, the quench oil flow rate is controlled to increase at the quench oil rate and / or the quench hydrogen flow rate is controlled to increase at the quench hydrogen rate.

[0040] This invention provides an electronic device, comprising:

[0041] At least one processor; and,

[0042] A memory communicatively connected to at least one of the processors; wherein,

[0043] The memory stores instructions that can be executed by at least one of the processors to enable the at least one of the processors to perform the coal direct liquefaction multi-reactor feed control method as described above.

[0044] This invention provides a storage medium that stores computer instructions, which, when executed by a computer, are used to perform all steps of the coal direct liquefaction multi-reactor feed control method as described above.

[0045] This invention solves the problem of maintaining stable and uniform oil-coal slurry concentration and catalyst-oil-coal slurry concentration by implementing dual closed-loop ratio control of the pulverized coal feed flow rate and the pulverized coal solvent flow rate, as well as dual closed-loop ratio control of the catalyst-pulverized coal flow rate and the catalyst-oil-coal slurry concentration. This ensures the stability of raw material properties, reduces errors caused by human factors, and improves system stability. This invention achieves automatic control of the feed to the direct coal liquefaction reactor, reducing the workload of operators and avoiding deviations caused by the lag of manual adjustments and lack of experience. This ensures the efficient operation of the direct coal liquefaction reaction process and increases the economic benefits of the equipment. Attached Figure Description

[0046] Figure 1 This is a flowchart illustrating the process of a multi-reactor feed control method for direct coal liquefaction according to an embodiment of the present invention.

[0047] Figure 2 This is a flowchart illustrating a multi-reactor feed control method for direct coal liquefaction, according to another embodiment of the present invention.

[0048] Figure 3 This is a system schematic diagram of a multi-reactor direct coal liquefaction system according to the preferred embodiment of the present invention.

[0049] Figure 4 This is a system module diagram of a multi-reactor coal direct liquefaction system according to the preferred embodiment of the present invention.

[0050] Figure 5 This is a schematic diagram of the hardware structure of an electronic device according to the present invention.

[0051] Marker description

[0052] 1-Catalyst pulverized coal; 2-Catalyst solvent; 3-Pulverized coal; 4-Solvent; 5-Catalyst oil-coal slurry mixer; 6-Oil-coal slurry mixer; 7-Catalyst oil-coal slurry tank; 8-Oil-coal slurry tank; 9-Catalyst oil-coal slurry tank bottom pump; 10-Oil-coal slurry tank bottom pump; 11-High-pressure feed pump; 12-Liquid sulfur; 13-Liquid sulfur tank; 14-Liquid sulfur pump; 15-Hydrogen; 16-Hydrogen compressor; 17-Oil-coal slurry heater; 18-Hydrogen heater; 19-First reactor; 20-Second reactor; 21-Reaction product ; 22-Quick cooling oil; 23-Quick cooling hydrogen; 24-Catalyst coal powder silo discharge control valve; 25-Catalyst solvent supply control valve; 26-Coal powder silo discharge control valve; 27-Solvent supply control valve; 28-Catalyst oil-coal slurry tank bottom pump outlet control valve; 29-High pressure feed pump frequency converter; 30-Liquid sulfur pump stroke regulator; 31-Compressor stepless speed regulator; 32-Oil-coal slurry heater gas control valve; 33-Hydrogen heater gas control valve; 34-Quick cooling oil control valve; 35-Quick cooling hydrogen control valve. Detailed Implementation

[0053] The specific embodiments of the present invention will be further described below with reference to the accompanying drawings. Identical components are indicated by the same reference numerals. It should be noted that the terms "front," "rear," "left," "right," "up," and "down" used in the following description refer to directions in the accompanying drawings, while the terms "inner" and "outer" refer to directions toward or away from the geometric center of a specific component, respectively.

[0054] like Figure 1 The diagram shown is a flowchart of a multi-reactor feed control method for direct coal liquefaction according to an embodiment of the present invention, including:

[0055] Step S101: The flow rate of pulverized coal and the flow rate of pulverized coal solvent are controlled by a double closed loop ratio and injected into the oil-coal slurry tank; the flow rate of catalyst pulverized coal and the flow rate of catalyst solvent are controlled by a double closed loop ratio and injected into the catalyst oil-coal slurry tank.

[0056] Step S102: Inject the catalyst oil-coal slurry obtained from mixing the catalyst oil-coal slurry tank into the oil-coal slurry tank;

[0057] Step S103: The oil-coal slurry output from the oil-coal slurry tank is injected into the oil-coal slurry heating furnace;

[0058] Step S104: Liquid sulfur is injected into the oil-coal slurry heater, and hydrogen is injected into the hydrogen heater.

[0059] Step S105: The intermediate product output from the oil-coal slurry heater and the heated hydrogen output from the hydrogen heater are input into the reactor to obtain the product output from the reactor.

[0060] Specifically, the present invention can be applied to electronic devices with processing capabilities, such as computers equipped with a distributed control system (DCS).

[0061] like Figure 3 and Figure 4 As shown, this embodiment implements feed control for a multi-reactor system for direct coal liquefaction. The multi-reactor system includes an oil-coal slurry mixing device, a catalyst-oil-coal slurry mixing device, an oil-coal slurry conveying device, a catalyst-oil-coal slurry conveying device, a liquid sulfur feed conveying device, a hydrogen feed conveying device, an oil-coal slurry heating device, and a hydrogen heating device, etc.

[0062] First, step S101 is executed, where the pulverized coal feed flow rate and pulverized coal solvent flow rate are controlled by a double closed-loop ratio and injected into the oil-coal slurry tank, and the catalyst pulverized coal flow rate and catalyst solvent flow rate are controlled by a double closed-loop ratio and injected into the catalyst oil-coal slurry tank.

[0063] This embodiment uses an oil-coal slurry mixing device to mix the oil-coal slurry. The oil-coal slurry mixing device includes an oil-coal slurry kneader 6, an oil-coal slurry tank 8, a coal powder silo discharge control valve 26, and a solvent supply control valve 27. The oil-coal slurry kneader 6 drives the plow blade to rotate via a horizontal shaft, thoroughly mixing the received coal powder and solvent to form an oil-coal slurry. The oil-coal slurry tank 8 receives and stores the oil-coal slurry from the oil-coal slurry kneader 6. The coal powder silo discharge control valve 26 and the solvent supply control valve 27 are controlled by a dual closed-loop ratio to control the flow rate of coal powder and solvent entering the system.

[0064] In this embodiment, the catalyst oil-coal slurry is mixed using a catalyst oil-coal slurry mixing device. This device includes a catalyst oil-coal slurry kneader 5, a catalyst oil-coal slurry tank 7, a catalyst coal powder silo discharge control valve 24, and a catalyst solvent supply control valve 25. The catalyst oil-coal slurry kneader 5 uses a transverse shaft to drive the plow blades to rotate, thoroughly mixing the received catalyst coal powder and solvent to form a catalyst oil-coal slurry. The catalyst oil-coal slurry tank 7 receives and stores the catalyst oil-coal slurry from the catalyst oil-coal slurry kneader 5. The catalyst coal powder silo discharge control valve 24 and the catalyst solvent supply control valve 25 are controlled by a dual closed-loop ratio to regulate the flow rate of catalyst coal powder and catalyst solvent entering the system.

[0065] Then, step S102 is performed to inject the catalyst oil-coal slurry obtained from mixing the catalyst oil-coal slurry tank into the oil-coal slurry tank.

[0066] In this embodiment, catalyst kerosene is transported via a catalyst oil-coal slurry conveying device. The device includes a catalyst oil-coal slurry tank bottom pump 9 and a catalyst oil-coal slurry tank bottom pump outlet control valve 28. The catalyst oil-coal slurry tank bottom pump 9 pressurizes the catalyst oil-coal slurry, and the catalyst oil-coal slurry delivery rate injected into the oil-coal slurry tank 8 is controlled by the catalyst oil-coal slurry tank bottom pump outlet control valve 28.

[0067] Then, step S103 is executed, in which the oil-coal slurry output from the oil-coal slurry tank is injected into the oil-coal slurry heating furnace.

[0068] In this embodiment, oil-coal slurry is transported via an oil-coal slurry feeding and conveying device, which includes a high-pressure feed pump 11 and a high-pressure feed pump frequency converter 29. The high-pressure feed pump 11 pressurizes the oil-coal slurry and sends it into the oil-coal slurry heater 17, while the high-pressure feed pump frequency converter 29 controls its speed, thereby controlling the amount of oil-coal slurry transported.

[0069] Next, step S104 is executed, in which liquid sulfur is injected into the oil-coal slurry heater and hydrogen is injected into the hydrogen heater.

[0070] In this embodiment, liquid sulfur is fed through a liquid sulfur feeding and conveying device. The liquid sulfur feeding and conveying device includes at least a liquid sulfur pump 14. The liquid sulfur pump 14 pressurizes the fed liquid sulfur and injects it into the oil-coal slurry heater 17.

[0071] In this embodiment, hydrogen is fed through a hydrogen feeding and conveying device. The hydrogen feeding and conveying device includes at least a hydrogen compressor 16. The hydrogen compressor 16 pressurizes the hydrogen and injects it into the hydrogen heater 18.

[0072] Finally, step S105 is executed, in which the intermediate product output from the oil-coal slurry heater and the heated hydrogen output from the hydrogen heater are input into the reactor to obtain the product output from the reactor.

[0073] In this embodiment, a coal-oil slurry heating device provides heat to the raw coal-oil slurry, catalyst coal-oil slurry, and liquid sulfur, and a hydrogen heating device provides heat to the hydrogen.

[0074] The oil-coal slurry heating device includes at least one oil-coal slurry heater 17. The oil-coal slurry heater 17 provides heat to the feed oil-coal slurry, catalyst oil-coal slurry, and liquid sulfur.

[0075] The hydrogen heating device includes at least a hydrogen heater 18. The hydrogen heater 18 provides heat to the feed hydrogen.

[0076] This invention solves the problem of maintaining stable and uniform oil-coal slurry concentration and catalyst-oil-coal slurry concentration by controlling the flow rate of pulverized coal and the flow rate of pulverized coal solvent in a dual closed-loop ratio, thereby ensuring the stability of raw material properties, reducing errors caused by human factors, and improving the stability of the system.

[0077] like Figure 2 The diagram shown is a flowchart of a multi-reactor feed control method for direct coal liquefaction according to another embodiment of the present invention, including:

[0078] Step S201: The flow rate of pulverized coal and the flow rate of pulverized coal solvent are controlled by a double closed-loop ratio and injected into the oil-coal slurry tank. The flow rate of catalyst pulverized coal and the flow rate of catalyst solvent are controlled by a double closed-loop ratio and injected into the catalyst oil-coal slurry tank.

[0079] In one embodiment, the step of controlling the pulverized coal feed flow rate and the pulverized coal solvent flow rate using a dual closed-loop ratio and injecting the pulverized coal slurry into the oil-coal slurry tank includes:

[0080] Calculate the setpoint for pulverized coal solvent flow rate based on system load and oil-coal slurry concentration;

[0081] The set value of the coal powder solvent flow rate is used as the given value of the coal powder solvent flow rate PID controller. The coal powder solvent supply control valve is controlled by the coal powder solvent flow rate PID controller. The coal powder solvent supply control valve controls the connection between the coal powder solvent and the first input end of the oil-coal slurry mixer.

[0082] The actual coal powder solvent flow rate is detected, and the coal powder feed flow rate set value is calculated based on the actual coal powder solvent flow rate and the oil-coal slurry concentration.

[0083] The set value of the coal powder discharge flow rate is used as the given value of the coal powder discharge flow rate PID controller. The coal powder discharge flow rate PID controller controls the coal powder silo discharge control valve. The coal powder silo discharge control valve controls the connection between the coal powder and the second input terminal of the oil-coal slurry mixer. The oil-coal slurry mixer mixes the coal powder and the coal powder solvent and then injects the mixture into the oil-coal slurry tank.

[0084] In one embodiment, the step of controlling the ratio of catalyst pulverized coal flow rate to catalyst solvent flow rate in a dual closed-loop manner and injecting the catalyst oil-coal slurry into the tank includes:

[0085] Calculate the catalyst solvent flow rate setpoint based on the system load and catalyst oil-coal slurry concentration;

[0086] The catalyst solvent flow rate setpoint is used as the given value of the catalyst solvent flow rate PID controller. The catalyst solvent supply control valve is controlled by the catalyst solvent flow rate PID controller. The catalyst solvent supply control valve controls the connection between the catalyst solvent and the first input end of the catalyst oil-coal slurry mixer.

[0087] The actual catalyst solvent flow rate is detected, and the catalyst coal powder flow rate set value is calculated based on the actual catalyst solvent flow rate and the catalyst oil-coal slurry concentration.

[0088] The set value of the catalyst pulverized coal flow rate is used as the given value of the catalyst pulverized coal feed flow rate PID controller. The catalyst pulverized coal feed flow rate PID controller controls the catalyst pulverized coal silo feed control valve. The catalyst pulverized coal silo feed control valve controls the connection between the catalyst pulverized coal and the second input end of the catalyst oil-coal slurry mixer. The catalyst oil-coal slurry mixer mixes the catalyst pulverized coal with the catalyst solvent and then injects it into the catalyst oil-coal slurry tank.

[0089] Step S202: Calculate the catalyst oil-coal slurry flow rate based on the system load, use the catalyst oil-coal slurry flow rate as the setpoint for the catalyst oil-coal slurry flow rate PID controller, and control the catalyst oil-coal slurry tank bottom pump outlet control valve through the catalyst oil-coal slurry flow rate PID controller. The catalyst oil-coal slurry tank bottom pump outlet control valve controls the connection between the catalyst oil-coal slurry tank and the oil-coal slurry tank.

[0090] Step S203: Calculate the oil-coal slurry flow rate based on the system load, and use the oil-coal slurry flow rate as the setpoint for the oil-coal slurry flow rate PID controller. Control the high-pressure feed pump frequency converter through the oil-coal slurry flow rate PID controller. The high-pressure feed pump frequency converter controls the speed of the high-pressure feed pump. The high-pressure feed pump injects the oil-coal slurry output from the oil-coal slurry tank into the oil-coal slurry heating furnace.

[0091] Step S204: Calculate the liquid sulfur flow rate based on the system load, use the liquid sulfur flow rate as the setpoint of the liquid sulfur flow rate PID controller, control the liquid sulfur pump stroke regulator through the liquid sulfur flow rate PID controller, control the stroke of the liquid sulfur pump through the liquid sulfur pump stroke regulator, and inject the liquid sulfur into the oil-coal slurry heating furnace.

[0092] Step S205: Calculate the hydrogen flow rate based on the system load, use the hydrogen flow rate as the setpoint for the hydrogen flow rate PID controller, control the compressor continuously variable speed regulator through the hydrogen flow rate PID controller, control the discharge volume of the hydrogen compressor through the compressor continuously variable speed regulator, and inject hydrogen into the hydrogen heating furnace through the compressor.

[0093] Step S206: Set the gas flow rate of the oil-coal slurry heater and the hydrogen heater; input the intermediate product output from the oil-coal slurry heater and the heated hydrogen output from the hydrogen heater into the input end of the first reactor; connect the output end of the first reactor to the input end of the second reactor; output the product from the output end of the second reactor; and inject quench oil and / or quench hydrogen into the reactor connection pipeline connecting the first reactor and the second reactor.

[0094] Step S207: Detect the temperature of the first reactor connected to the first reactor of the oil-coal slurry heater and the hydrogen heater respectively, and adjust the gas flow rate of the oil-coal slurry heater and the hydrogen heater according to the temperature of the first reactor.

[0095] In one embodiment, detecting the temperature of a first reactor connected to the first reactor respectively of the oil-coal slurry heater and the hydrogen heater, and adjusting the gas flow rate of the oil-coal slurry heater and the hydrogen heater according to the first reactor temperature includes:

[0096] The temperature of the first reactor, which is respectively connected to the oil-coal slurry heater and the hydrogen heater, is detected.

[0097] When the temperature of the first reactor is lower than the first temperature threshold, the gas flow rate of the gas control valve of the oil-coal slurry heater is increased at a first gas rate, and the gas flow rate of the gas control valve of the hydrogen heater is increased at a second gas rate.

[0098] When the temperature of the first reactor is higher than the first temperature threshold, the gas flow rate of the gas control valve of the oil-coal slurry heater is reduced at a first gas rate, and the gas flow rate of the gas control valve of the hydrogen heater is reduced at a second gas rate.

[0099] Step S208: Set the quench oil flow rate and / or quench hydrogen flow rate into the reactor connection pipeline, detect the temperature of the second reactor connected to the first reactor, and adjust the quench oil flow rate and / or the quench hydrogen flow rate according to the temperature of the second reactor.

[0100] In one embodiment, detecting the temperature of the second reactor connected to the first reactor, and adjusting the quench oil flow rate and / or the quench hydrogen flow rate based on the second reactor temperature, includes:

[0101] Detect the temperature of the second reactor connected to the first reactor;

[0102] When the temperature of the second reactor is lower than the second temperature threshold, the quench oil flow rate is controlled to decrease at the quench oil rate and / or the quench hydrogen flow rate is controlled to decrease at the quench hydrogen rate.

[0103] When the temperature of the second reactor is higher than the second temperature threshold, the quench oil flow rate is controlled to increase at the quench oil rate and / or the quench hydrogen flow rate is controlled to increase at the quench hydrogen rate.

[0104] Specifically, such as Figure 3 and Figure 4As shown, this embodiment implements feed control for a multi-reactor system for direct coal liquefaction. The multi-reactor system includes an oil-coal slurry mixing device, a catalyst-oil-coal slurry mixing device, an oil-coal slurry conveying device, a catalyst-oil-coal slurry conveying device, a liquid sulfur feed conveying device, a hydrogen feed conveying device, an oil-coal slurry heating device, and a hydrogen heating device, etc., wherein:

[0105] The oil-coal slurry mixing device includes an oil-coal slurry kneader 6, an oil-coal slurry tank 8, a coal powder silo discharge control valve 26, and a solvent supply control valve 27. The oil-coal slurry kneader 6 drives the plow blades to rotate via a transverse shaft, thoroughly mixing the received coal powder and solvent to form an oil-coal slurry. The oil-coal slurry tank 8 receives and stores the oil-coal slurry from the oil-coal slurry kneader 6. The coal powder silo discharge control valve 26 and the solvent supply control valve 27 are controlled by a dual closed-loop ratio to control the flow rate of coal powder and solvent entering the system.

[0106] The catalyst oil-coal slurry mixing device includes a catalyst oil-coal slurry kneader 5, a catalyst oil-coal slurry tank 7, a catalyst coal powder silo discharge control valve 24, and a catalyst solvent supply control valve 25. The catalyst oil-coal slurry kneader 5 drives the plow blade to rotate via a transverse shaft, thoroughly mixing the received catalyst coal powder and solvent to form a catalyst oil-coal slurry. The catalyst oil-coal slurry tank 7 receives and stores the catalyst oil-coal slurry from the catalyst oil-coal slurry kneader 5. The catalyst coal powder silo discharge control valve 24 and the catalyst solvent supply control valve 25 are controlled by a dual closed-loop ratio to control the flow rate of catalyst coal powder and catalyst solvent entering the system.

[0107] The catalyst oil-coal slurry conveying device includes a catalyst oil-coal slurry tank bottom pump 9 and a catalyst oil-coal slurry tank bottom pump outlet control valve 28. The catalyst oil-coal slurry tank bottom pump 9 pressurizes the catalyst oil-coal slurry, and the catalyst oil-coal slurry conveying rate injected into the oil-coal slurry tank 8 is controlled by the catalyst oil-coal slurry tank bottom pump outlet control valve 28.

[0108] The oil-coal slurry feeding and conveying device consists of a high-pressure feed pump 11 and a high-pressure feed pump frequency converter 29. The high-pressure feed pump 11 pressurizes the oil-coal slurry and sends it into the oil-coal slurry heater 17. The high-pressure feed pump frequency converter 29 controls its speed, thereby controlling the conveying volume of the oil-coal slurry.

[0109] The liquid sulfur feed conveying device includes a liquid sulfur pump 14 and a liquid sulfur pump stroke regulator 30. The liquid sulfur pump 14 pressurizes the fed liquid sulfur, and the liquid sulfur pump stroke regulator 30 controls its conveying volume and injects it into the oil-coal slurry heater 17.

[0110] The hydrogen feeding and conveying device includes a hydrogen compressor 16 and a compressor continuously variable speed regulator 31. The hydrogen compressor 16 pressurizes the hydrogen, controls its delivery rate through the compressor continuously variable speed regulator 31, and injects it into the hydrogen heater 18.

[0111] The oil-coal slurry heating device includes: an oil-coal slurry heater 17 and an oil-coal slurry heater gas control valve 32. The oil-coal slurry heater 17 provides heat to the feed oil-coal slurry, catalyst oil-coal slurry, and liquid sulfur, and controls the gas flow rate through the oil-coal slurry heater gas control valve 32.

[0112] The hydrogen heating device includes a hydrogen heater 18 and a hydrogen heater gas control valve 33. The hydrogen heater 18 provides heat to the feed hydrogen, and the gas flow is controlled by the hydrogen heater gas control valve 33.

[0113] The control valve, frequency converter, stroke regulator, etc. mentioned are only the flow control methods in the embodiments, and bypass regulation and other forms can also be selected.

[0114] The oil-coal slurry heater and hydrogen heater mentioned are only heating methods in this embodiment. Similarly, electric heating or heat exchange can also be selected for controlling the temperature of the reactor raw materials.

[0115] The coal direct liquefaction multi-reactor feed control method provided in this embodiment is an organic integration of control methods and devices, forming a fully automated feed control system. By inputting four variables—system load, coal-oil slurry concentration, catalyst coal-oil slurry concentration, and reactor temperature—automatic control of the feed flow rate and temperature of the coal direct liquefaction multi-reactor can be achieved.

[0116] Specifically, step S201 is first executed, where the pulverized coal feed flow rate and pulverized coal solvent flow rate are controlled by a double closed-loop ratio and injected into the oil-coal slurry tank, and the catalyst pulverized coal flow rate and catalyst solvent flow rate are controlled by a double closed-loop ratio and injected into the catalyst oil-coal slurry tank.

[0117] In one embodiment, the step of controlling the pulverized coal feed flow rate and the pulverized coal solvent flow rate using a dual closed-loop ratio and injecting the pulverized coal slurry into the oil-coal slurry tank includes:

[0118] Calculate the setpoint for pulverized coal solvent flow rate based on system load and oil-coal slurry concentration;

[0119] The set value of the coal powder solvent flow rate is used as the given value of the coal powder solvent flow rate PID controller. The coal powder solvent supply control valve is controlled by the coal powder solvent flow rate PID controller. The coal powder solvent supply control valve controls the connection between the coal powder solvent and the first input end of the oil-coal slurry mixer.

[0120] The actual coal powder solvent flow rate is detected, and the coal powder feed flow rate set value is calculated based on the actual coal powder solvent flow rate and the oil-coal slurry concentration.

[0121] The set value of the coal powder discharge flow rate is used as the given value of the coal powder discharge flow rate PID controller. The coal powder discharge flow rate PID controller controls the coal powder silo discharge control valve. The coal powder silo discharge control valve controls the connection between the coal powder and the second input terminal of the oil-coal slurry mixer. The oil-coal slurry mixer mixes the coal powder and the coal powder solvent and then injects the mixture into the oil-coal slurry tank.

[0122] The oil-coal slurry concentration control method in this embodiment is implemented through a dual closed-loop ratio control system. The coal powder discharge flow rate is controlled by the coal powder silo discharge control valve 26, and the solvent supply flow rate is controlled by the solvent supply control valve 27. For example... Figure 4 As shown, firstly, based on the system load and coal slurry concentration, the required coal powder solvent feed flow rate is automatically calculated using a calculation module in the Distributed Control System (DCS). This calculated flow rate is used as the setpoint for the solvent flow control loop. After passing through a proportional-integral-differential (PID) controller for the coal powder solvent flow rate, the result is output to the solvent supply control valve 27, thereby controlling the coal powder solvent flow rate. Then, a dual closed-loop ratio control system is formed by combining the coal powder flow rate and the solvent flow rate. Based on the coal slurry concentration, the required coal powder flow rate is automatically calculated, and this value is used as the setpoint for the coal powder flow control loop. After passing through a PID controller for the coal powder discharge flow rate, the result is output to the coal powder silo discharge control valve 26, thereby controlling the coal powder discharge flow rate. Finally, the automatic control of the coal slurry concentration is completed. A dual-loop ratio control system is a system with two closed-loop loops: ratio control and flow control. One primary variable is controlled by the flow control loop, while the other secondary variable is controlled by the ratio control loop. The setpoint of the secondary variable depends on the measured value of the primary variable. For example, the coal powder solvent feed flow rate is the primary variable, and the control valve changes in real time according to the measured value of the coal powder solvent, adjusting the coal powder solvent feed flow rate to form an automatic control loop. The coal powder discharge flow rate is the secondary variable, which changes according to the design concentration ratio of the primary variable, the coal powder solvent flow rate, thereby indirectly controlling the opening of the coal powder discharge control valve through the secondary variable.

[0123] In some embodiments, the total oil-coal slurry flow rate is determined based on the system load, the oil-coal slurry flow rate is multiplied by the oil-coal slurry concentration to obtain the coal powder flow rate, and the oil-coal slurry flow rate is multiplied by the coal powder solvent concentration to obtain the coal powder solvent flow rate, wherein the coal powder solvent concentration = 1 - oil-coal slurry concentration.

[0124] First, the design values ​​of pulverized coal flow rate, pulverized coal solvent flow rate, catalyst flow rate, and catalyst solvent flow rate under 100% load are calculated. When the system load changes, other key parameters are changed according to the proportion of the system load change. For example, if the system load is adjusted to 85%, then all other key parameters are given at 85% of the design value.

[0125] In one embodiment, the step of controlling the ratio of catalyst pulverized coal flow rate to catalyst solvent flow rate in a dual closed-loop manner and injecting the catalyst oil-coal slurry into the tank includes:

[0126] Calculate the catalyst solvent flow rate setpoint based on the system load and catalyst oil-coal slurry concentration;

[0127] The catalyst solvent flow rate setpoint is used as the given value of the catalyst solvent flow rate PID controller. The catalyst solvent supply control valve is controlled by the catalyst solvent flow rate PID controller. The catalyst solvent supply control valve controls the connection between the catalyst solvent and the first input end of the catalyst oil-coal slurry mixer.

[0128] The actual catalyst solvent flow rate is detected, and the catalyst coal powder flow rate set value is calculated based on the actual catalyst solvent flow rate and the catalyst oil-coal slurry concentration.

[0129] The set value of the catalyst pulverized coal flow rate is used as the given value of the catalyst pulverized coal feed flow rate PID controller. The catalyst pulverized coal feed flow rate PID controller controls the catalyst pulverized coal silo feed control valve 24. The catalyst pulverized coal silo feed control valve 24 controls the connection between the catalyst pulverized coal and the second input end of the catalyst oil-coal slurry mixer. The catalyst oil-coal slurry mixer mixes the catalyst pulverized coal with the catalyst solvent and then injects it into the catalyst oil-coal slurry tank.

[0130] The catalyst oil-coal slurry concentration control method of this embodiment controls the catalyst coal powder discharge flow rate through the catalyst coal powder silo discharge control valve 24 and the solvent feed flow rate through the catalyst solvent supply control valve 25. For example... Figure 4 As shown, firstly, based on the system load and catalyst oil-coal slurry concentration, the required catalyst solvent feed flow rate is automatically calculated in the DCS using a calculation module. This calculated value is used as the setpoint for the catalyst solvent flow control loop, and after passing through the catalyst solvent flow PID controller, it is output to the catalyst solvent supply control valve 25, thereby controlling the catalyst solvent flow rate. Then, a dual closed-loop ratio control system is formed by combining the catalyst coal powder flow rate and the catalyst solvent flow rate. Based on the catalyst oil-coal slurry concentration, the required catalyst coal powder flow rate is automatically calculated, and this value is used as the setpoint for the catalyst coal powder flow control loop. After passing through the catalyst coal powder discharge flow PID controller, it is output to the catalyst coal powder silo discharge control valve 24, thereby controlling the catalyst coal powder discharge flow rate, ultimately completing the automatic control of the catalyst oil-coal slurry concentration.

[0131] In some embodiments, the total catalyst oil-coal slurry flow rate is determined based on the system load, the catalyst oil-coal slurry flow rate is multiplied by the catalyst oil-coal slurry concentration to obtain the catalyst coal powder flow rate, and the catalyst oil-coal slurry flow rate is multiplied by the catalyst solvent concentration to obtain the catalyst solvent flow rate, wherein the catalyst solvent concentration = 1 - oil-coal slurry concentration.

[0132] Then, step S202 is executed, the catalyst oil-coal slurry flow rate is calculated according to the system load, the catalyst oil-coal slurry flow rate is used as the setpoint of the catalyst oil-coal slurry flow rate PID controller, and the catalyst oil-coal slurry tank bottom pump outlet control valve is controlled by the catalyst oil-coal slurry tank bottom pump outlet control valve to control the connection between the catalyst oil-coal slurry tank and the oil-coal slurry tank.

[0133] The catalyst oil-coal slurry injection flow control method in this embodiment is implemented using a single-loop closed-loop control system. The catalyst oil-coal slurry feed flow rate is controlled by the catalyst oil-coal slurry tank bottom pump outlet control valve 28. For example... Figure 4 As shown, based on the system load, the required catalyst oil-coal slurry flow rate is automatically calculated in the DCS using a calculation module. This calculated value is used as the setpoint for the catalyst oil-coal slurry injection flow control loop. After passing through the catalyst oil-coal slurry flow PID controller, the output is sent to the catalyst oil-coal slurry tank bottom pump outlet control valve 28, thereby realizing automatic control of the catalyst oil-coal slurry injection flow rate. The catalyst oil-coal slurry enters the oil-coal slurry tank 8 via the catalyst oil-coal slurry tank bottom pump outlet control valve 28.

[0134] Then, step S203 is executed, the oil-coal slurry flow rate is calculated according to the system load, the oil-coal slurry flow rate is used as the setpoint of the oil-coal slurry flow rate PID controller, the high-pressure feed pump frequency converter is controlled by the oil-coal slurry flow rate PID controller, the high-pressure feed pump frequency converter controls the speed of the high-pressure feed pump, and the high-pressure feed pump injects the oil-coal slurry output from the oil-coal slurry tank into the oil-coal slurry heating furnace.

[0135] The oil-coal slurry injection flow control method in this embodiment is implemented using a single-loop closed-loop control system. The speed of the high-pressure feed pump 11 is controlled by the high-pressure feed pump frequency converter 29, thereby controlling the oil-coal slurry injection flow rate. Figure 4 As shown, based on the system load, the required oil-coal slurry flow rate is automatically calculated in the DCS using a calculation module, and this calculated value is used as the setpoint for the oil-coal slurry injection flow rate control loop. After passing through the oil-coal slurry flow rate PID controller, the output is sent to the high-pressure feed pump frequency converter 29, thereby realizing the automatic control of the oil-coal slurry injection flow rate.

[0136] Then, step S204 is executed, the liquid sulfur flow rate is calculated according to the system load, the liquid sulfur flow rate is used as the setpoint of the liquid sulfur flow rate PID controller, the liquid sulfur pump stroke regulator is controlled by the liquid sulfur flow rate PID controller, the liquid sulfur pump stroke regulator controls the stroke of the liquid sulfur pump, and the liquid sulfur pump injects liquid sulfur into the oil-coal slurry heating furnace.

[0137] The liquid sulfur injection flow rate control method in this embodiment is implemented using a single-loop closed-loop control system. The outlet flow rate of the liquid sulfur pump 14 is controlled by the liquid sulfur pump stroke regulator 30, thereby controlling the injection flow rate of liquid sulfur 12. Liquid sulfur 12 is input into the liquid sulfur tank 13 and output from the liquid sulfur tank 13 via the liquid sulfur pump 14. Figure 4 As shown, based on the system load, the required liquid sulfur flow rate is automatically calculated in the DCS using a calculation module, and this calculated value is used as the setpoint for the liquid sulfur injection flow control loop. After passing through the liquid sulfur flow PID controller, the value is output to the liquid sulfur pump stroke regulator 30, thereby realizing the automatic control of the liquid sulfur injection flow rate.

[0138] Then, step S205 is executed, the hydrogen flow rate is calculated according to the system load, the hydrogen flow rate is used as the setpoint of the hydrogen flow rate PID controller, the compressor continuously variable speed regulator is controlled by the hydrogen flow rate PID controller, the compressor continuously variable speed regulator controls the discharge volume of the hydrogen compressor, and the compressor injects hydrogen into the hydrogen heating furnace.

[0139] The hydrogen injection flow rate control method in this embodiment is implemented using a single-loop closed-loop control system. The outlet flow rate of the hydrogen compressor 16 is controlled by the continuously variable speed regulator 31 of the hydrogen compressor 16, thereby controlling the injection flow rate of the hydrogen 15. Figure 4 As shown, based on the system load, the required hydrogen flow rate is automatically calculated in the DCS using a calculation module, and this calculated value is used as the setpoint for the hydrogen flow control loop. After passing through the hydrogen flow PID controller, the value is output to the compressor continuously variable speed regulator 31, thereby realizing the automatic control of the hydrogen refueling flow rate.

[0140] Then, step S206 is executed, setting the gas flow rate of the oil-coal slurry heater and the hydrogen heater, inputting the intermediate product output from the oil-coal slurry heater and the heated hydrogen output from the hydrogen heater into the input end of the first reactor, connecting the output end of the first reactor to the input end of the second reactor, outputting the product from the output end of the second reactor, and injecting quench oil and / or quench hydrogen into the reactor connection pipeline connecting the first reactor and the second reactor.

[0141] Specifically, the intermediate product output from the oil-coal slurry heater 17 and the heated hydrogen output from the hydrogen heater 18 are input into the first reactor 19 for reaction. After the intermediate product is subjected to temperature adjustment by quench oil 22 and / or quench hydrogen 23, it is injected into the second reactor 20 for reaction. The product after reaction is output from the second reactor 20.

[0142] Then, step S207 is performed to detect the temperature of the first reactor connected to the first reactor of the oil-coal slurry heater and the hydrogen heater respectively, and to adjust the gas flow rate of the oil-coal slurry heater and the hydrogen heater according to the temperature of the first reactor.

[0143] The reactor temperature control method in this embodiment utilizes a cascade control loop. The first reactor temperature is used as the main loop, and the gas flow rate as the secondary loop. The first reactor temperature is input as a setpoint to the main loop, and the output value of the main loop's PID controller is used as the setpoint for the secondary loop. The output of the secondary loop's PID controller is sent to the gas control valve to adjust the gas flow rate, thereby regulating the reactor temperature.

[0144] In one embodiment, detecting the temperature of a first reactor connected to the first reactor respectively of the oil-coal slurry heater and the hydrogen heater, and adjusting the gas flow rate of the oil-coal slurry heater and the hydrogen heater according to the first reactor temperature includes:

[0145] The temperature of the first reactor, which is respectively connected to the oil-coal slurry heater and the hydrogen heater, is detected.

[0146] When the temperature of the first reactor is lower than the first temperature threshold, the gas flow rate of the gas control valve of the oil-coal slurry heater is increased at a first gas rate, and the gas flow rate of the gas control valve of the hydrogen heater is increased at a second gas rate.

[0147] When the temperature of the first reactor is higher than the first temperature threshold, the gas flow rate of the gas control valve of the oil-coal slurry heater is reduced at a first gas rate, and the gas flow rate of the gas control valve of the hydrogen heater is reduced at a second gas rate.

[0148] Specifically, the gas flow rate of the oil-coal slurry heater 17 is controlled by the gas control valve 32 of the oil-coal slurry heater, and the gas flow rate of the hydrogen heater 18 is controlled by the gas control valve 33 of the hydrogen heater.

[0149] In this embodiment, the gas flow rates of the oil-coal slurry heater and the hydrogen heater are adjusted according to the temperature of the first reactor, so as to achieve automatic adjustment of the reactor feed oil-coal slurry, catalyst, liquid sulfur and hydrogen temperatures as the reactor temperature changes.

[0150] Additionally, step S208 can be performed to set the quench oil flow rate and / or quench hydrogen flow rate entering the reactor connection pipeline, detect the temperature of the second reactor connected to the first reactor, and adjust the quench oil flow rate and / or the quench hydrogen flow rate according to the temperature of the second reactor.

[0151] In one embodiment, detecting the temperature of the second reactor connected to the first reactor, and adjusting the quench oil flow rate and / or the quench hydrogen flow rate based on the second reactor temperature, includes:

[0152] Detect the temperature of the second reactor connected to the first reactor;

[0153] When the temperature of the second reactor is lower than the second temperature threshold, the quench oil flow rate is controlled to decrease at the quench oil rate and / or the quench hydrogen flow rate is controlled to decrease at the quench hydrogen rate.

[0154] When the temperature of the second reactor is higher than the second temperature threshold, the quench oil flow rate is controlled to increase at the quench oil rate and / or the quench hydrogen flow rate is controlled to increase at the quench hydrogen rate.

[0155] Specifically, the flow rate of quench oil is controlled by adjusting the opening of the quench oil control valve 34, and the flow rate of quench hydrogen is controlled by adjusting the opening of the quench hydrogen control valve 35. Since the direct coal liquefaction reaction is exothermic, the temperature of the second reactor is controlled by adjusting the flow rates of quench oil and / or quench hydrogen. The temperature of the feedstock at the inlet of the second reactor is indirectly controlled by adjusting the injection flow rates of quench oil and / or quench hydrogen; thus, the injection of quench oil and quench hydrogen serves as a means of controlling the temperature of the second reactor.

[0156] In this embodiment, the flow rate of quench oil and / or quench hydrogen is adjusted according to the temperature of the second reactor, so that the temperature in the reactor connecting pipeline can be adaptively adjusted to follow the temperature of the second reactor.

[0157] This embodiment presents a multi-reactor feed control method for direct coal liquefaction, achieving automatic control of feed flow rate, feed composition, and feed temperature. This embodiment addresses the issue of maintaining stable and uniform oil-coal slurry concentration and catalyst-oil-coal slurry concentration. This ensures the stability of raw material properties, reduces errors caused by human factors, and improves system stability. Simultaneously, it solves the problem of automatically adjusting the injection flow rates of oil-coal slurry, catalyst, liquid sulfur, and hydrogen to the multi-reactor feed according to the system's processing capacity. This reduces the workload of operators and avoids inefficient direct coal liquefaction reactions caused by human error. Finally, this embodiment solves the problem of automatically adjusting the temperatures of the reactor feed oil-coal slurry, catalyst, liquid sulfur, and hydrogen according to reactor temperature changes. This avoids the lag caused by manual adjustments, large reactor temperature fluctuations, and the resulting impact on the system's oil yield and economic benefits.

[0158] As an example, let's take a million-ton-scale direct coal liquefaction plant as an example.

[0159] According to the method described, the system load is 100%, the catalyst oil-coal slurry concentration is 50%, the oil-coal slurry concentration is 50%, the temperature of the first reactor is 455℃, and the temperature of the second reactor is 455℃.

[0160] When the catalyst coal powder silo discharge control valve 24 and the catalyst solvent supply control valve 25 receive a signal indicating a catalyst oil-coal slurry concentration of 50%, the two valves control the flow rate at a 1:1 ratio. Simultaneously, upon receiving a system load signal of 100%, the catalyst coal powder discharge control valve 24 controls the feed coal powder flow rate to 44 t / h, and the catalyst solvent supply control valve 25 controls the feed solvent flow rate to 44 tons per hour (t / h). The feed catalyst coal powder 1 and catalyst solvent 2 are uniformly mixed by the catalyst oil-coal slurry mixer 5 and then enter the catalyst oil-coal slurry tank 7.

[0161] Upon receiving a 50% concentration signal from the coal slurry, the coal powder silo discharge control valve 26 and the solvent supply control valve 27 control the flow rate at a 1:1 ratio. Simultaneously, upon receiving a 100% system load signal, the coal powder discharge control valve 26 controls the coal powder feed flow rate to 220 t / h, and the solvent supply control valve 27 controls the solvent feed flow rate to 220 t / h. The coal powder 3 and solvent 4 are then uniformly mixed by the coal slurry mixer 6 and enter the coal slurry tank 8.

[0162] When the catalyst oil-coal slurry tank bottom pump outlet control valve 28 receives the system load 100% signal, the catalyst oil-coal slurry tank bottom pump outlet control valve 28 controls the feed catalyst oil-coal slurry flow rate of 88t / h into the oil-coal slurry tank 8.

[0163] When the high-pressure feed pump frequency converter 29 receives the system load 100% signal, it controls the speed of the high-pressure feed pump 11, thereby indirectly controlling the feed oil-coal slurry to enter the oil-coal slurry heater 17 at a rate of 528 t / h.

[0164] When the liquid sulfur pump stroke regulator 30 receives the system load 100% signal, it controls the stroke of the liquid sulfur pump 14, thereby indirectly controlling the feed liquid sulfur to enter the oil-coal slurry heater 17 at a rate of 3t / h.

[0165] When the compressor continuously variable speed regulator 31 receives the system load 100% signal, it controls the compressor discharge volume of 21t / h to enter the hydrogen heater 18.

[0166] When the gas control valve 32 of the oil-coal slurry heater and the gas control valve 33 of the hydrogen heater receive a 100% system load signal, the gas control valve 32 controls the gas flow of the oil-coal slurry heater 17 to 12000 Nm³ / h. Simultaneously, it receives a signal indicating a first reactor temperature of 455℃. When the first reactor temperature is below 455℃, the gas control valve 32 will control the gas consumption to 200 cubic meters per minute (Nm³ / h).3 When the temperature of the first reactor exceeds 455℃, the gas control valve 32 of the oil-coal slurry heater will control the gas consumption to 200 Nm³ / min. 3 The gas flow rate decreases by 100 Nm³ / h, and the gas control valve 33 of the hydrogen heater controls the gas supply of the hydrogen heater to 800 Nm³ / h. Simultaneously, it receives a signal indicating the temperature of the first reactor is 455℃. When the temperature of the first reactor falls below 455℃, the gas control valve 33 will control the gas supply to 30 Nm³ / h. 3 When the temperature of the first reactor rises by 30 Nm³ / min, the gas control valve 33 of the hydrogen heater will control the gas consumption to 30 Nm³ / min. 3 / min decrease.

[0167] When the quench oil control valve 34 and the quench hydrogen control valve 35 receive a 100% system load signal, the quench oil control valve 34 controls the flow rate of quench oil 22 to 40 t / h, and the quench hydrogen control valve 35 controls the flow rate of quench oil 23 to 100,000 Nm³ / h. Simultaneously, upon receiving a signal indicating a second reactor temperature of 455℃, when the second reactor temperature drops below 455℃, the quench oil control valve 34 will reduce the quench oil flow rate by 3 t / min, and the quench hydrogen control valve 35 will reduce the quench hydrogen flow rate by 5000 Nm³ / h. 3 When the temperature of the second reactor increases by 3 t / min, and the temperature of the second reactor exceeds 455℃, the quench oil control valve 34 will control the quench oil flow rate to increase by 3 t / min, and the quench hydrogen control valve 35 will control the quench hydrogen flow rate to increase by 5000 Nm³. 3 / min increase.

[0168] like Figure 5 The diagram shown is a hardware structure schematic of an electronic device according to the present invention, comprising:

[0169] At least one processor 501; and,

[0170] A memory 502 is communicatively connected to at least one of the processors 501; wherein,

[0171] The memory 502 stores instructions that can be executed by at least one of the processors to enable the at least one of the processors to perform the coal direct liquefaction multi-reactor feed control method as described above.

[0172] Figure 5 Take a processor 501 as an example.

[0173] The electronic device may also include an input device 503 and a display device 504.

[0174] The processor 501, memory 502, input device 503 and display device 504 can be connected by a bus or other means. The figure shows an example of connection by bus.

[0175] The memory 502, as a non-volatile computer-readable storage medium, can be used to store non-volatile software programs, non-volatile computer-executable programs, and modules, such as the program instructions / modules corresponding to the coal direct liquefaction multi-reactor feed control method in the embodiments of this application, for example, Figure 1 , Figure 2 The method flow is shown. The processor 501 executes various functional applications and data processing by running non-volatile software programs, instructions, and modules stored in the memory 502, thereby realizing the coal direct liquefaction multi-reactor feed control method in the above embodiments.

[0176] Memory 502 may include a program storage area and a data storage area. The program storage area may store an operating system and application programs required for at least one function. The data storage area may store data created based on the use of the coal direct liquefaction multi-reactor feed control method. Furthermore, memory 502 may include high-speed random access memory and may also include non-volatile memory, such as at least one disk storage device, flash memory device, or other non-volatile solid-state storage device. In some embodiments, memory 502 may optionally include memory remotely located relative to processor 501, which can be connected via a network to the apparatus performing the coal direct liquefaction multi-reactor feed control method. Examples of such networks include, but are not limited to, the Internet, intranets, local area networks, mobile communication networks, and combinations thereof.

[0177] The input device 503 can receive user clicks and generate signal inputs related to user settings and function control of the coal direct liquefaction multi-reactor feed control method. The display device 504 may include a display screen or other display equipment.

[0178] The one or more modules are stored in the memory 502, and when run by the one or more processors 501, they execute the coal direct liquefaction multi-reactor feed control method in any of the above method embodiments.

[0179] This invention solves the problem of maintaining stable and uniform oil-coal slurry concentration and catalyst-oil-coal slurry concentration by controlling the flow rate of pulverized coal and the flow rate of pulverized coal solvent in a dual closed-loop ratio, thereby ensuring the stability of raw material properties, reducing errors caused by human factors, and improving the stability of the system.

[0180] One embodiment of the present invention provides a storage medium that stores computer instructions, which, when executed by a computer, are used to perform all steps of the coal direct liquefaction multi-reactor feed control method as described above.

[0181] The embodiments described above are merely illustrative of several implementations of the present invention, and while the descriptions are specific and detailed, they should not be construed as limiting the scope of the present invention. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of the present invention, and these modifications and improvements all fall within the scope of protection of the present invention. Therefore, the scope of protection of this patent should be determined by the appended claims.

Claims

1. A method for controlling the feed of a multi-reactor system in direct coal liquefaction, characterized in that, include: The flow rate of pulverized coal and the flow rate of pulverized coal solvent are controlled by a double closed-loop ratio and injected into the oil-coal slurry tank. The flow rate of catalyst pulverized coal and the flow rate of catalyst solvent are controlled by a double closed-loop ratio and injected into the catalyst oil-coal slurry tank. The catalyst oil-coal slurry obtained from mixing in the catalyst oil-coal slurry tank is injected into the oil-coal slurry tank; The oil-coal slurry output from the oil-coal slurry tank is injected into the oil-coal slurry heating furnace; Liquid sulfur is injected into an oil-coal slurry heater, and hydrogen is injected into a hydrogen heater. The intermediate product output from the oil-coal slurry heater and the heated hydrogen output from the hydrogen heater are fed into the reactor to obtain the product output from the reactor. The method of controlling the pulverized coal feed flow rate and the pulverized coal solvent flow rate through a dual closed-loop ratio and injecting the pulverized coal slurry into the oil-coal slurry tank includes: Calculate the setpoint for pulverized coal solvent flow rate based on system load and oil-coal slurry concentration; The set value of the coal powder solvent flow rate is used as the given value of the coal powder solvent flow rate PID controller. The coal powder solvent supply control valve is controlled by the coal powder solvent flow rate PID controller. The coal powder solvent supply control valve controls the connection between the coal powder solvent and the first input end of the oil-coal slurry mixer. The actual coal powder solvent flow rate is detected, and the coal powder feed flow rate set value is calculated based on the actual coal powder solvent flow rate and the oil-coal slurry concentration. The set value of the coal powder discharge flow rate is used as the given value of the coal powder discharge flow rate PID controller. The coal powder discharge flow rate PID controller controls the coal powder silo discharge control valve. The coal powder silo discharge control valve controls the connection between the coal powder and the second input end of the oil-coal slurry mixer. The oil-coal slurry mixer mixes the coal powder and the coal powder solvent and then injects the mixture into the oil-coal slurry tank. The method of controlling the flow rate of pulverized coal catalyst and the flow rate of catalyst solvent through a dual closed-loop ratio and injecting the pulverized coal-oil catalyst slurry into the catalyst oil tank includes: Calculate the catalyst solvent flow rate setpoint based on the system load and catalyst oil-coal slurry concentration; The catalyst solvent flow rate setpoint is used as the given value of the catalyst solvent flow rate PID controller. The catalyst solvent supply control valve is controlled by the catalyst solvent flow rate PID controller. The catalyst solvent supply control valve controls the connection between the catalyst solvent and the first input end of the catalyst oil-coal slurry mixer. The actual catalyst solvent flow rate is detected, and the catalyst coal powder flow rate set value is calculated based on the actual catalyst solvent flow rate and the catalyst oil-coal slurry concentration. The set value of the catalyst pulverized coal flow rate is used as the given value of the catalyst pulverized coal feed flow rate PID controller. The catalyst pulverized coal feed flow rate PID controller controls the catalyst pulverized coal silo feed control valve. The catalyst pulverized coal silo feed control valve controls the connection between the catalyst pulverized coal and the second input end of the catalyst oil-coal slurry mixer. The catalyst oil-coal slurry mixer mixes the catalyst pulverized coal with the catalyst solvent and then injects it into the catalyst oil-coal slurry tank. The step of injecting the catalyst oil-coal slurry obtained from mixing the catalyst oil-coal slurry tank into the oil-coal slurry tank includes: calculating the catalyst oil-coal slurry flow rate according to the system load, using the catalyst oil-coal slurry flow rate as the setpoint of the catalyst oil-coal slurry flow rate PID controller, controlling the catalyst oil-coal slurry tank bottom pump outlet control valve through the catalyst oil-coal slurry flow rate PID controller, and controlling the connection between the catalyst oil-coal slurry tank and the oil-coal slurry tank through the catalyst oil-coal slurry tank bottom pump outlet control valve; The step of injecting the oil-coal slurry output from the oil-coal slurry tank into the oil-coal slurry heater includes: calculating the oil-coal slurry flow rate based on the system load, using the oil-coal slurry flow rate as the setpoint of the oil-coal slurry flow rate PID controller, controlling the high-pressure feed pump frequency converter through the oil-coal slurry flow rate PID controller, controlling the speed of the high-pressure feed pump through the high-pressure feed pump frequency converter, and injecting the oil-coal slurry output from the oil-coal slurry tank into the oil-coal slurry heater by the high-pressure feed pump. The process of injecting liquid sulfur into the oil-coal slurry heating furnace includes: calculating the liquid sulfur flow rate based on the system load, using the liquid sulfur flow rate as the setpoint of the liquid sulfur flow rate PID controller, controlling the liquid sulfur pump stroke regulator through the liquid sulfur flow rate PID controller, controlling the stroke of the liquid sulfur pump through the liquid sulfur pump stroke regulator, and injecting liquid sulfur into the oil-coal slurry heating furnace through the liquid sulfur pump. The process of injecting hydrogen into the hydrogen heating furnace includes: calculating the hydrogen flow rate based on the system load, using the hydrogen flow rate as the setpoint of the hydrogen flow rate PID controller, controlling the compressor continuously variable speed regulator through the hydrogen flow rate PID controller, controlling the discharge volume of the hydrogen compressor through the compressor continuously variable speed regulator, and injecting hydrogen into the hydrogen heating furnace through the compressor.

2. The coal direct liquefaction multi-reactor feed control method according to claim 1, characterized in that, The reactor includes a first reactor and a second reactor. The step of inputting the intermediate product output from the oil-coal slurry heater and the heated hydrogen output from the hydrogen heater into the reactor includes: Set the gas flow rate of the oil-coal slurry heater and the hydrogen heater, input the intermediate product output from the oil-coal slurry heater and the heated hydrogen output from the hydrogen heater into the input end of the first reactor, connect the output end of the first reactor to the input end of the second reactor, output the product from the output end of the second reactor, and inject quench oil and / or quench hydrogen into the reactor connection pipeline connecting the first reactor and the second reactor. The temperature of the first reactor connected to the first reactor of the oil-coal slurry heater and the hydrogen heater is detected, and the gas flow rate of the oil-coal slurry heater and the hydrogen heater is adjusted according to the temperature of the first reactor.

3. The coal direct liquefaction multi-reactor feed control method according to claim 2, characterized in that, The step of detecting the temperature of the first reactor connected to the first reactors of the oil-coal slurry heater and the hydrogen heater respectively, and adjusting the gas flow rate of the oil-coal slurry heater and the hydrogen heater according to the temperature of the first reactor includes: The temperature of the first reactor, which is respectively connected to the oil-coal slurry heater and the hydrogen heater, is detected. When the temperature of the first reactor is lower than the first temperature threshold, the gas flow rate of the gas control valve of the oil-coal slurry heater is increased at a first gas rate, and the gas flow rate of the gas control valve of the hydrogen heater is increased at a second gas rate. When the temperature of the first reactor is higher than the first temperature threshold, the gas flow rate of the gas control valve of the oil-coal slurry heater is reduced at a first gas rate, and the gas flow rate of the gas control valve of the hydrogen heater is reduced at a second gas rate.

4. The coal direct liquefaction multi-reactor feed control method according to claim 2, characterized in that, The method further includes: Set the quench oil flow rate and / or quench hydrogen flow rate entering the reactor connection pipeline, detect the temperature of the second reactor connected to the first reactor, and adjust the quench oil flow rate and / or the quench hydrogen flow rate according to the temperature of the second reactor.

5. The coal direct liquefaction multi-reactor feed control method according to claim 4, characterized in that, The step of detecting the temperature of the second reactor connected to the first reactor and adjusting the quench oil flow rate and / or the quench hydrogen flow rate based on the second reactor temperature includes: Detect the temperature of the second reactor connected to the first reactor; When the temperature of the second reactor is lower than the second temperature threshold, the quench oil flow rate is controlled to decrease at the quench oil rate and / or the quench hydrogen flow rate is controlled to decrease at the quench hydrogen rate. When the temperature of the second reactor is higher than the second temperature threshold, the quench oil flow rate is controlled to increase at the quench oil rate and / or the quench hydrogen flow rate is controlled to increase at the quench hydrogen rate.

6. An electronic device, characterized in that, include: At least one processor; as well as, A memory communicatively connected to at least one of the processors; wherein, The memory stores instructions executable by at least one of the processors to enable the at least one processor to perform the coal direct liquefaction multi-reactor feed control method as described in any one of claims 1 to 5.

7. A storage medium, characterized in that, The storage medium stores computer instructions, which, when executed by the computer, are used to perform all steps of the coal direct liquefaction multi-reactor feed control method as described in any one of claims 1 to 5.

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