CN111154518A

CN111154518A - Coal hydro-gasification safety monitoring system and monitoring method thereof

Info

Publication number: CN111154518A
Application number: CN201910295875.1A
Authority: CN
Inventors: 晁澄; 曹晶; 田洋洋; 李美喜; 王凤彬
Original assignee: Zhejiang Supcon Technology Co Ltd; Xinneng Energy Co Ltd
Current assignee: Zhejiang Supcon Technology Co Ltd; Xinneng Energy Co Ltd
Priority date: 2019-04-12
Filing date: 2019-04-12
Publication date: 2020-05-15

Abstract

The invention discloses a coal hydrogasification safety monitoring system, which comprises a coal hydrogasification device, a detection mechanism, a PLC (programmable logic controller) and an execution mechanism, wherein the detection mechanism is connected with the detection mechanism; through the reasonable position that sets up all kinds of detection device, can carry out real-time detection to the behavior, the risk that can predict to exist has improved the degree of accuracy of risk prediction through the reasonable quantity that sets up all kinds of detection device, avoids the maloperation, whole automatic control guarantees the safe and stable operation of system, can realize the construction of coal hydrogasification technical industry device. The invention also discloses a monitoring method of the coal hydro-gasification safety monitoring system, which can execute the stop action in time when abnormal conditions occur through reasonable logic judgment by comparing each detected parameter with the preset parameter value; the system can effectively avoid the parking caused by misoperation, and also can avoid the serious consequences caused by not timely parking due to the conditions of leakage, over-temperature, over-pressure and the like in the production process.

Description

Coal hydro-gasification safety monitoring system and monitoring method thereof

The technical field is as follows:

the invention relates to the field of coal powder hydro-gasification, in particular to a coal hydro-gasification safety monitoring system and a monitoring method thereof.

Background art:

coal hydro-gasification is one of coal gasification, which refers to a process of reacting raw coal powder with hydrogen-containing reaction gas at high temperature and high pressure (800-1000 ℃, 3-8 MPa) to generate methane-rich gas and light oil products. Compared with the traditional coal gasification, the coal hydro-gasification has the characteristics of simple process, high thermal efficiency and little pollution, thereby being widely concerned. However, in the coal hydro-gasification process, the operation pressure is 7.0MPa, the operation temperature is 800-870 ℃, and the medium contains a large amount of CO and H₂And if leakage, over-temperature, over-pressure and the like occur in the production process of flammable and explosive gases, serious consequences such as equipment damage, fire hazard, explosion and the like are caused, wherein carbon monoxide can also cause poisoning of people. Because the hydro-gasification reaction needs to be triggered at a higher temperature, if abnormal reaction conditions exist, the temperature condition of continuous reaction cannot be maintained, and malignant consequences are caused; and when the pressure of the raw materials is low, the materials in the gasification furnace can be caused to flow backwards and flow backwards to cause fire explosion. The key for preventing dangerous accidents is to combine the coal hydro-gasification process to predict risks and design a corresponding detailed safety instrument control system. However, because the coal hydro-gasification technology has extremely harsh process conditions, the technology is still in the test and simulation stages at present, and no corresponding industrial device is provided.

The invention content is as follows:

the first purpose of the invention is to provide a safe and reliable coal hydro-gasification safety monitoring system with stable operation;

the first purpose of the invention is to provide a monitoring method of a coal hydro-gasification safety monitoring system, which can accurately predict risks and has reasonable logic control.

The first purpose of the invention is implemented by the following technical scheme:

the coal hydrogasification safety monitoring system comprises a coal hydrogasification device, a detection mechanism, a PLC (programmable logic controller) and an execution mechanism;

the detection mechanism is connected with the PLC in a wired or wireless mode; the detection mechanism is used for detecting the operating temperature, the operating pressure, the flow data, the liquid level data and the pressure difference data of the coal hydrogenation gasification device and transmitting the detected operating temperature, operating pressure, flow data, liquid level data and pressure difference data to the PLC;

the PLC is connected with the actuating mechanism in a wired or wireless mode, analyzes the received operating temperature, operating pressure, flow data, liquid level data and pressure difference data, and controls the actuating mechanism to execute actions.

Further, the coal hydrogasification device comprises a high-pressure coal hopper, a hydrogen heating furnace, an oxygen source, a hydrogasification furnace, a semicoke cooling fluidized bed, a semicoke storage tank, a semicoke fluidized bed steam drum, a cyclone dust collector, a waste boiler steam drum, a filter, a hydrogen source, a secondary hydrogen heater, a high-pressure nitrogen source, a replacement coal powder pipeline and a replacement oxygen pipeline;

the discharge hole of the high-pressure coal hopper is communicated with the feed inlet of the process burner of the hydrogenation gasification furnace through a coal powder pipeline, the gas outlet of the hydrogen heating furnace is communicated with the coal powder pipeline close to the high-pressure coal hopper through a hydrogen pipeline, and the gas outlet of the oxygen source is communicated with the coal powder pipeline close to the hydrogen heating furnace through an oxygen pipeline;

a semicoke outlet of the hydrogenation gasification furnace is communicated with a semicoke inlet of the semicoke cooling fluidized bed through a semicoke pipeline, a semicoke outlet of the semicoke cooling fluidized bed is communicated with an inlet of the semicoke storage tank through a semicoke storage pipeline, a steam outlet of the semicoke cooling fluidized bed is communicated with a steam inlet of a semicoke fluidized bed steam drum through a steam pipeline, and a water outlet of the semicoke fluidized bed steam drum is communicated with a water inlet of the semicoke cooling fluidized bed through a water supply pipeline;

the raw gas outlet of the hydrogenation gasification furnace is communicated with the inlet of the cyclone dust collector through a raw gas pipeline, the outlet of the cyclone dust collector is communicated with the gas inlet of the waste boiler through a pipeline, the steam outlet of the waste boiler is communicated with the steam inlet of the waste boiler drum through a pipeline, the water outlet of the waste boiler drum is communicated with the water inlet of the waste boiler through a pipeline, the gas outlet of the waste boiler is communicated with the gas inlet of the filter through a pipeline of a filter, the gas outlet of the filter is communicated with the heat medium inlet of the secondary hydrogen heater through a pipeline, and the heat medium outlet of the secondary hydrogen heater is communicated with the raw gas storage tank through a pipeline; the gas outlet of the hydrogen source is communicated with the cold medium inlet of the secondary hydrogen heater through a pipeline, and the cold medium outlet of the secondary hydrogen heater is communicated with the gas inlet of the hydrogen heating furnace through a pipeline;

the gas outlet of the high-pressure nitrogen source is divided into two paths, one path is communicated with the gas inlet of the replacement pulverized coal pipeline through a pipeline, and the other path is communicated with the gas inlet of the replacement oxygen pipeline through a pipeline;

the gas outlet of the replacement coal powder pipeline is divided into two paths which are respectively communicated with a nitrogen plug pipeline of the coal powder pipeline and the gas inlet of a small-flow nitrogen blowing pipeline of the coal powder pipeline, and the gas outlet of the nitrogen plug pipeline of the coal powder pipeline is divided into two paths which are respectively communicated with the coal powder pipeline arranged between a coal powder upstream cut-off valve of the actuating mechanism and a coal powder downstream cut-off valve of the actuating mechanism and the coal powder pipeline arranged between the coal powder downstream cut-off valve and a coal powder upstream cut-off valve of a nozzle of the actuating mechanism; the air outlet of the small-flow nitrogen blowing pipeline of the coal dust pipeline is divided into two paths which are respectively communicated with the coal dust pipeline arranged between the coal dust downstream cut-off valve and the inlet nozzle coal dust upstream cut-off valve and the coal dust pipeline arranged between the inlet nozzle coal dust upstream cut-off valve and the inlet nozzle coal dust downstream cut-off valve of the actuating mechanism;

a pulverized coal pipeline nitrogen plug valve is arranged on the pulverized coal pipeline nitrogen plug pipeline, a pulverized coal pipeline small-flow nitrogen blowing valve is arranged on the pulverized coal pipeline small-flow nitrogen blowing pipe, and a pulverized coal inlet pipeline nitrogen upstream cut-off valve is arranged on the replaced pulverized coal pipeline;

the gas outlet of replacement oxygen pipeline divide three routes respectively with oxygen pipeline nitrogen stopper pipeline, oxygen pipeline nitrogen gas blow pipeline, the air inlet intercommunication of oxygen pipeline low discharge nitrogen blow pipeline, the gas outlet of oxygen pipeline nitrogen stopper pipeline with arrange in oxygen upper reaches trip valve with between the oxygen low reaches trip valve the oxygen pipeline intercommunication, the gas outlet of oxygen pipeline nitrogen gas blow pipeline with the gas outlet of oxygen pipeline low discharge nitrogen blow pipeline all with oxygen low reaches trip valve low reaches oxygen pipeline intercommunication, just the gas outlet of oxygen pipeline low discharge nitrogen blow pipeline is located the low reaches of the gas outlet of oxygen pipeline nitrogen gas blow pipeline.

Further, the detection mechanism comprises at least one first temperature measuring device and at least one first pressure measuring device which are arranged on the crude gas pipeline, at least one second temperature measuring device which is arranged on the hydrogen pipeline, at least one third temperature measuring device which is arranged on the filter removing pipeline, at least one second pressure measuring device which is arranged on the oxygen pipeline, at least one third pressure measuring device which is arranged on the secondary hydrogen heater cold medium outlet pipeline, a fourth pressure measuring device which is arranged in the semicoke fluidized bed steam pocket, at least one first flow measuring device which is arranged on the secondary hydrogen heater cold medium inlet pipeline, at least one second flow measuring device which is arranged on the water supply pipeline, a third flow measuring device which is arranged on the semicoke fluidized bed steam outlet pipeline, and at least one first liquid level measuring device which is arranged in the semicoke fluidized bed steam pocket, at least one second liquid level measuring device arranged in the waste boiler drum and at least one differential pressure measuring device arranged in the filter;

the first temperature measuring device, the second temperature measuring device, the third temperature measuring device, the first pressure measuring device, the second pressure measuring device, the third pressure measuring device, the fourth pressure measuring device, the first flow measuring device, the second flow measuring device, the third flow measuring device, the first liquid level measuring device, the second liquid level measuring device and the differential pressure measuring device are all connected with the input end of the PLC.

Further, the number of the first temperature measuring device, the second temperature measuring device, the third temperature measuring device, the first pressure measuring device, the second pressure measuring device, the third pressure measuring device, the first flow measuring device, the second flow measuring device, the first liquid level measuring device, the second liquid level measuring device and the differential pressure measuring device is 3.

Further, the first temperature measuring device, the second temperature measuring device and the third temperature measuring device are temperature sensors, the first pressure measuring device, the second pressure measuring device, the third pressure measuring device and the fourth pressure measuring device are pressure sensors, the first flow measuring device, the second flow measuring device and the third flow measuring device are flow velocity sensors, and the differential pressure measuring device is a differential pressure sensor.

Further, the executing mechanism comprises a pulverized coal upstream cut-off valve and a pulverized coal downstream cut-off valve which are arranged on the pulverized coal pipeline close to the high-pressure coal hopper, a nozzle pulverized coal upstream cut-off valve and a nozzle pulverized coal downstream cut-off valve which are arranged on the pulverized coal pipeline close to the hydrogenation gasification furnace, a pulverized coal conveying gas cut-off valve and a pulverized coal conveying air flow regulating valve which are arranged on the hydrogen pipeline, an oxygen upstream cut-off valve, an oxygen downstream cut-off valve and an oxygen flow regulating valve which are arranged on the oxygen pipeline, an oxygen pipeline nitrogen plug valve which is arranged on the oxygen pipeline nitrogen plug pipeline, an oxygen pipeline nitrogen purging valve which is arranged on the oxygen pipeline nitrogen purging pipeline, and an oxygen pipeline small-flow nitrogen purging valve which is arranged on the oxygen pipeline small-flow nitrogen;

the pulverized coal conveying air flow regulating valve is positioned at the downstream of the pulverized coal conveying air cut-off valve, the oxygen flow regulating valve is positioned at the upstream of the oxygen upstream cut-off valve, the oxygen upstream cut-off valve is positioned at the upstream of the oxygen downstream cut-off valve, and the pulverized coal upstream cut-off valve is positioned at the upstream of the pulverized coal downstream cut-off valve;

buggy upper reaches trip valve buggy low reaches trip valve into nozzle buggy upper reaches trip valve into nozzle buggy low reaches trip valve the buggy carries the gas trip valve the buggy carries wind flow control valve oxygen upper reaches trip valve oxygen low reaches trip valve oxygen flow control valve pulverized coal pipeline nitrogen plug valve pulverized coal pipeline low discharge nitrogen blows the valve into pulverized coal pipeline nitrogen gas upper reaches trip valve oxygen pipeline nitrogen plug valve oxygen pipeline nitrogen blow the valve and oxygen pipeline low discharge nitrogen blows the valve all with the output of PLC controller is connected.

The second purpose of the invention is implemented by the following technical scheme:

in the monitoring method of the coal hydrogasification safety monitoring system, the detection mechanism detects the operating temperature, the operating pressure, the flow data, the liquid level data and the pressure difference data of the coal hydrogasification device and transmits the detected operating temperature, operating pressure, flow data, liquid level data and pressure difference data to the PLC; the PLC analyzes the received operating temperature, operating pressure, flow data, liquid level data and pressure difference data, and controls the actuating mechanism to execute actions.

Further, a first temperature set value, a second temperature set value, a third temperature set value, a first liquid level set value, a second liquid level set value, a first flow set value, a second flow set value, a third pressure set value, a fourth pressure set value, a first pressure difference set value, a second pressure difference set value and a third pressure difference set value are preset in the PLC;

a first temperature measuring device monitors a first temperature value of crude gas at an outlet of the hydrogenation gasification furnace and transmits the monitored first temperature value to the PLC controller, a second temperature measuring device monitors a second temperature value of hydrogen at an outlet of the hydrogen heating furnace and transmits the monitored second temperature value to the PLC controller, a third temperature measuring device monitors a third temperature value of crude gas at an outlet of the waste boiler and transmits the monitored third temperature value to the PLC controller, a first pressure measuring device monitors a first pressure value of the hydrogenation gasification furnace and transmits the monitored first pressure value to the PLC controller, a second pressure measuring device monitors a second pressure value of an oxygen pipeline and transmits the monitored second pressure value to the PLC controller, a third pressure measuring device monitors a third pressure value at a cold medium outlet of the secondary hydrogen heater and transmits the monitored third pressure value to the PLC controller, a fourth pressure measuring device monitors a fourth pressure value in a semicoke fluidized bed steam pocket and transmits the monitored fourth pressure value to the PLC controller, a first flow measuring device monitors a first flow value entering a secondary hydrogen heater cold medium inlet and transmits the monitored first flow value to the PLC controller, a second flow measuring device monitors a second flow value of feed water entering a semicoke cooling fluidized bed and transmits the monitored second flow value to the PLC controller, a third flow measuring device monitors a third flow value of a semicoke fluidized bed steam pocket steam outlet and transmits the monitored third flow value to the PLC controller, a first liquid level measuring device monitors a first liquid level value in the semicoke fluidized bed steam pocket and transmits the monitored first liquid level value to the PLC controller, a second liquid level measuring device monitors a second liquid level value in a waste boiler steam pocket and transmits the monitored second liquid level value to the PLC controller, the pressure difference measuring device monitors a first pressure difference value of an inlet and an outlet of the filter and transmits the monitored first pressure difference value to the PLC;

when one of the following 13 conditions is satisfied, the parking action is executed:

condition 1: the first temperature value is greater than or equal to a first temperature set value;

condition 2: the second temperature value is less than or equal to a second temperature set value;

condition 3: the third temperature value is greater than or equal to a third temperature set value;

condition 4: the first liquid level value is less than or equal to a first liquid level set value;

condition 5: the second liquid level value is less than or equal to a second liquid level set value;

condition 6: the first flow value is less than or equal to a first flow set value;

condition 7: the second flow value is less than or equal to a second flow set value;

condition 8: the third flow value is less than or equal to a third flow set value;

condition 9: the third pressure value is less than or equal to a third pressure set value;

condition 10: the fourth pressure value is greater than or equal to a fourth pressure set value;

condition 11: the first pressure difference value is greater than or equal to a first pressure difference set value;

condition 12: the second pressure value-the first pressure value is less than or equal to a second pressure difference set value;

condition 13: and the third pressure value-the first pressure value is less than or equal to a third pressure difference set value.

Further, the parking action includes:

(1) closing the oxygen upstream cut-off valve;

(2) closing the oxygen downstream cut-off valve after delaying for 15 seconds;

(3) closing the oxygen pipeline nitrogen purging valve after delaying for 40 seconds;

(4) closing the oxygen flow regulating valve;

(5) closing the coal powder upstream cut-off valve;

(6) closing a coal dust downstream cut-off valve;

(7) opening a pulverized coal conveying air flow regulating valve to enable the opening degree of the pulverized coal conveying air flow regulating valve to be 100%; when the opening feedback of the pulverized coal conveying air flow regulating valve is more than 95%, delaying for 10 seconds, closing the pulverized coal conveying air flow regulating valve, and simultaneously closing a pulverized coal upstream cut-off valve and a pulverized coal conveying air cut-off valve of a nozzle;

(8) opening a nitrogen upstream cut-off valve of a coal powder inlet pipeline, opening a nitrogen plug valve of the coal powder pipeline when the nitrogen upstream cut-off valve of the coal powder pipeline reaches a full-open state, closing the nitrogen plug valve of the coal powder pipeline after delaying for 25 seconds, closing a coal powder downstream cut-off valve of a nozzle inlet and opening a small-flow nitrogen blowing valve of the coal powder pipeline;

(9) opening a nitrogen upstream cut-off valve of a pulverized coal inlet pipeline;

(10) opening a small-flow nitrogen blowing valve of an oxygen pipeline;

(11) opening an oxygen line nitrogen plug valve;

(12) opening an oxygen pipeline nitrogen purging valve, and closing the oxygen pipeline nitrogen purging valve after delaying for 40 seconds;

(13) and stopping the hydrogen heating furnace.

Further, the first temperature set value is 1000 ℃; the second temperature set value is 800 ℃; the third temperature set point is 380 ℃; the first liquid level set value is 3.1%; the second liquid level set value is 3.1%; the first flow rate set point is 5000Nm³H; the second flow rate set value is 5m³H; the third flow setting value is 550 kg/h; the third pressure setting value is 7.3 MPa; the fourth pressure set value is 3 MPa; the first pressure differential set point is 100 kPa; the second pressure differential set point is 100 kPa; the third pressure differential set point is 100 kPa.

Further, any two first temperature values in 3 first temperature values monitored by 3 first temperature measuring devices are more than or equal to a first temperature set value, and the condition 1 is judged to be met;

any two second temperature values in the 3 second temperature values monitored by the 3 second temperature measuring devices are less than or equal to a second temperature set value, and the condition 2 is judged to be met;

any two third temperature values in 3 third temperature values monitored by 3 third temperature measuring devices are more than or equal to a third temperature set value, namely the condition 3 is judged to be met;

any two of the 3 first liquid level values monitored by the 3 first liquid level measuring devices are less than or equal to a first liquid level set value, and the condition 4 is judged to be met;

in 3 second liquid level values monitored by the 3 second liquid level measuring devices, any two second liquid level values are less than or equal to a second liquid level set value, and the condition 5 is judged to be met;

any two first flow values in the 3 first flow values monitored by the 3 first flow measuring devices are less than or equal to a first flow set value, and the condition 6 is judged to be met;

any two second flow values in the 3 second flow values monitored by the 3 second flow measuring devices are less than or equal to a second flow set value, and the condition 7 is judged to be met;

any two third flow values in the 3 third flow values monitored by the 3 third flow measuring devices are less than or equal to a third flow set value, and the condition 8 is judged to be met;

any two third pressure values in the 3 third pressure values monitored by the 3 third pressure measuring devices are less than or equal to a third pressure set value, and the condition 9 is judged to be met;

any two fourth pressure values in 3 fourth pressure values monitored by 3 fourth pressure measuring devices are more than or equal to a fourth pressure set value, namely the condition 10 is judged to be met;

any two of 3 first differential pressure values monitored by the 3 differential pressure measuring devices are more than or equal to a first differential pressure set value, namely the condition 11 is judged to be met;

any two of second pressure difference values obtained by subtracting 3 first pressure values measured by the 3 first pressure measuring devices from 3 second pressure values measured by the 3 second pressure measuring devices are less than or equal to a second pressure difference set value, that is, the condition 12 is satisfied;

and in second pressure difference values obtained by subtracting 3 third pressure values measured by the 3 third pressure measuring devices from 3 first pressure values measured by the 3 first pressure measuring devices, judging that the condition 13 is met if any two third pressure difference values are less than or equal to a third pressure difference set value.

The invention has the advantages that:

the system can detect the operation condition in real time by reasonably setting the positions of various detection devices, can predict the possible risks, improves the accuracy of risk prediction, avoids misoperation, automatically controls the whole process, ensures the safe and stable operation of the system and can realize the construction of coal hydro-gasification industrial devices.

The method of the invention compares each detected parameter with the preset parameter value, and can execute the parking action in time when the abnormal condition occurs through reasonable logic judgment, thereby avoiding the occurrence of dangerous accidents; and various preset parameter values are reasonably and accurately set, so that the parking caused by misoperation can be effectively avoided, and the serious consequences caused by the fact that the vehicle is not parked in time due to the conditions of leakage, over-temperature, over-pressure and the like in the production process can also be avoided.

Description of the drawings:

in order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.

FIG. 1 is a schematic view of the system configuration of embodiment 1;

FIG. 2 is a control schematic diagram of embodiment 1;

in the figure: a high-pressure coal bunker 1, a hydrogen heating furnace 2, an oxygen source 3, a hydrogenation gasification furnace 4, a semicoke cooling fluidized bed 5, a semicoke storage tank 6, a semicoke fluidized bed steam drum 7, a cyclone dust collector 8, a waste boiler 9, a waste boiler steam drum 10, a filter 11, a hydrogen source 12, a secondary hydrogen heater 13, a coal powder pipeline 14, a hydrogen pipeline 15, an oxygen pipeline 16, a semicoke pipeline 17, a semicoke storage pipeline 18, a steam pipeline 19, a water supply pipeline 20, a crude gas pipeline 21, a filter removal pipeline 22, a first temperature measuring device 23, a second temperature measuring device 24, a third temperature measuring device 25, a first pressure measuring device 26, a second pressure measuring device 27, a third pressure measuring device 28, a fourth pressure measuring device 29, a first flow measuring device 30, a second flow measuring device 31, a third flow measuring device 32, a first liquid level measuring device 33, a second liquid level measuring device 34, a second liquid level measuring device, A differential pressure measuring device 35, a PLC 36, a coal dust upstream cut-off valve 37, a coal dust downstream cut-off valve 38, a coal dust upstream cut-off valve 39 of a nozzle inlet, a coal dust downstream cut-off valve 40 of a nozzle inlet, a coal dust conveying gas cut-off valve 41, a coal dust conveying air flow regulating valve 42, an oxygen upstream cut-off valve 43, an oxygen downstream cut-off valve 44, an oxygen flow regulating valve 45, a high-pressure nitrogen source 46 and a coal replacement pipeline 47, a replacement oxygen pipeline 48, a pulverized coal pipeline nitrogen plug pipeline 49, a pulverized coal pipeline small-flow nitrogen blowing pipeline 50, an oxygen pipeline nitrogen plug pipeline 51, an oxygen pipeline nitrogen blowing pipeline 52, an oxygen pipeline small-flow nitrogen blowing pipeline 53, a pulverized coal pipeline nitrogen plug valve 54, a pulverized coal pipeline small-flow nitrogen blowing valve 55, a pulverized coal inlet pipeline nitrogen upstream cut-off valve 56, an oxygen pipeline nitrogen plug valve 57, an oxygen pipeline nitrogen blowing valve 58, an oxygen pipeline small-flow nitrogen blowing valve 59 and a crude gas storage tank 60.

The specific implementation mode is as follows:

the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

Example 1:

the coal hydrogasification safety monitoring system shown in fig. 1 and 2 comprises a coal hydrogasification device, a detection mechanism, a PLC controller 36 and an execution mechanism;

the detection mechanism is connected with the PLC 36 in a wired or wireless mode; the detection mechanism is used for detecting the operating temperature, the operating pressure, the flow data, the liquid level data and the pressure difference data of the coal hydrogenation gasification device and transmitting the detected operating temperature, operating pressure, flow data, liquid level data and pressure difference data to the PLC 36;

the PLC 36 is connected with the actuator in a wired or wireless manner, and the PLC 36 analyzes the received operating temperature, operating pressure, flow data, liquid level data and pressure difference data and controls the actuator to execute actions.

The coal hydrogenation gasification device comprises a high-pressure coal hopper 1, a hydrogen heating furnace 2, an oxygen source 3, a hydrogenation gasification furnace 4, a semicoke cooling fluidized bed 5, a semicoke storage tank 6, a semicoke fluidized bed steam drum 7, a cyclone dust collector 8, a waste boiler 9, a waste boiler steam drum 10, a filter 11, a hydrogen source 12, a secondary hydrogen heater 13, a high-pressure nitrogen source 46, a replacement coal powder pipeline 47 and a replacement oxygen pipeline 48;

the discharge hole of the high-pressure coal hopper 1 is communicated with the process burner feed inlet of the hydrogenation gasification furnace 4 through a coal powder pipeline 14, the gas outlet of the hydrogen heating furnace 2 is communicated with the coal powder pipeline 14 close to the high-pressure coal hopper 1 through a hydrogen pipeline 15, and the gas outlet of the oxygen source 3 is communicated with the coal powder pipeline 14 close to the hydrogen heating furnace 2 through an oxygen pipeline 16;

a semicoke outlet of the hydrogenation gasification furnace 4 is communicated with a semicoke inlet of the semicoke cooling fluidized bed 5 through a semicoke pipeline 17, a semicoke outlet of the semicoke cooling fluidized bed 5 is communicated with an inlet of the semicoke storage tank 6 through a semicoke storage pipeline 18, a steam outlet of the semicoke cooling fluidized bed 5 is communicated with a steam inlet of a semicoke fluidized bed steam drum 7 through a steam pipeline 19, and a water outlet of the semicoke fluidized bed steam drum 7 is communicated with a water inlet of the semicoke cooling fluidized bed 5 through a water supply pipeline 20;

a crude gas outlet of the hydrogenation gasification furnace 4 is communicated with an inlet of a cyclone dust collector 8 through a crude gas pipeline 21, an outlet of the cyclone dust collector 8 is communicated with an air inlet of a waste boiler 9 through a pipeline, a steam outlet of the waste boiler 9 is communicated with a steam inlet of a waste boiler drum 10 through a pipeline, a water outlet of the waste boiler drum 10 is communicated with a water inlet of the waste boiler 9 through a pipeline, an air outlet of the waste boiler 9 is communicated with an air inlet of a filter 11 through a filter removing pipeline 22, an air outlet of the filter 11 is communicated with a heat medium inlet of a secondary hydrogen heater 13 through a pipeline, and a heat medium outlet of the secondary hydrogen heater 13 is communicated with a crude gas storage tank 60 through a pipeline; the gas outlet of the hydrogen source 12 is communicated with the cold medium inlet of the secondary hydrogen heater 13 through a pipeline, and the cold medium outlet of the secondary hydrogen heater 13 is communicated with the gas inlet of the hydrogen heating furnace 2 through a pipeline;

the air outlet of the high-pressure nitrogen source 46 is divided into two paths, one path is communicated with the air inlet of a replacement pulverized coal pipeline 47 through a pipeline, and the other path is communicated with the air inlet of a replacement oxygen pipeline 48 through a pipeline;

the gas outlet of the replacement coal powder pipeline 47 is divided into two paths to be respectively communicated with the gas inlets of a coal powder pipeline nitrogen plug pipeline 49 and a coal powder pipeline small-flow nitrogen blowing pipeline 50, and the gas outlet of the coal powder pipeline nitrogen plug pipeline 49 is divided into two paths to be respectively communicated with a coal powder pipeline 14 arranged between a coal powder upstream cut-off valve 37 and a coal powder downstream cut-off valve 38 and a coal powder pipeline 14 arranged between a coal powder downstream cut-off valve 38 and a nozzle coal powder upstream cut-off valve 39; the air outlet of the small-flow nitrogen blowing pipeline 50 of the coal dust pipeline is divided into two paths which are respectively communicated with the coal dust pipeline 14 arranged between the coal dust downstream cut-off valve 38 and the inlet nozzle coal dust upstream cut-off valve 39 and the coal dust pipeline 14 arranged between the inlet nozzle coal dust upstream cut-off valve 39 and the inlet nozzle coal dust downstream cut-off valve 40;

a pulverized coal pipeline nitrogen plug valve 54 is arranged on the pulverized coal pipeline nitrogen plug pipeline 49, a pulverized coal pipeline small flow nitrogen blowing valve 55 is arranged on the pulverized coal pipeline small flow nitrogen blowing pipeline 50, and a pulverized coal inlet pipeline nitrogen upstream cut-off valve 56 is arranged on the replacement pulverized coal pipeline 47;

the gas outlet of the replacement oxygen pipeline 48 is divided into three paths and is respectively communicated with the gas inlets of an oxygen pipeline nitrogen plug pipeline 51, an oxygen pipeline nitrogen purging pipeline 52 and an oxygen pipeline small-flow nitrogen blowpipe line 53, the gas outlet of the oxygen pipeline nitrogen plug pipeline 51 is communicated with the oxygen pipeline 16 arranged between the oxygen upstream stop valve 43 and the oxygen downstream stop valve 44, the gas outlet of the oxygen pipeline nitrogen purging pipeline 52 and the gas outlet of the oxygen pipeline small-flow nitrogen blowpipe line 53 are both communicated with the oxygen pipeline 16 at the downstream of the oxygen downstream stop valve 44, and the gas outlet of the oxygen pipeline small-flow nitrogen blowpipe line 53 is positioned at the downstream of the gas outlet of the oxygen pipeline nitrogen purging pipeline 52.

The detection mechanism comprises 3 first

temperature measuring devices

23 and 3 first pressure measuring devices 26 arranged on a

crude gas pipeline

21, 3 second temperature measuring devices 24 arranged on a

hydrogen pipeline

15, 3 third temperature measuring devices 25 arranged on a

filter removing pipeline

22, 3 second pressure measuring devices 27 arranged on an

oxygen pipeline

16, 3 third pressure measuring devices 28 arranged on a cold medium outlet pipeline of a secondary hydrogen heater 13, a fourth pressure measuring device 29 arranged in a semicoke fluidized bed steam pocket 7, 3 first flow measuring devices 30 arranged on a cold medium inlet pipeline of the

secondary hydrogen heater

13, 3 second flow measuring devices 31 arranged on a water supply pipeline 20, a third flow measuring device 32 arranged on a steam outlet pipeline of a semicoke fluidized bed steam pocket 7, 3 first liquid level measuring devices 33 arranged in the semicoke fluidized bed steam pocket 7, and 3 second liquid level measuring devices 34 arranged in a waste

boiler steam pocket

10, and 3 differential pressure measuring devices 35 provided in the filter 11;

the first temperature measuring device 23, the second temperature measuring device 24, the third temperature measuring device 25, the first pressure measuring device 26, the second pressure measuring device 27, the third pressure measuring device 28, the fourth pressure measuring device 29, the first flow measuring device 30, the second flow measuring device 31, the third flow measuring device 32, the first liquid level measuring device 33, the second liquid level measuring device 34 and the differential pressure measuring device 35 are all connected with an input end of the PLC controller 36.

The first temperature measuring device 23, the second temperature measuring device 24 and the third temperature measuring device 25 are all temperature sensors, the first pressure measuring device 26, the second pressure measuring device 27, the third pressure measuring device 28 and the fourth pressure measuring device 29 are all pressure sensors, the first flow measuring device 30, the second flow measuring device 31 and the third flow measuring device 32 are all flow rate sensors, and the differential pressure measuring device 35 is a differential pressure sensor.

In the embodiment, the manufacturer of the temperature sensor is Zhejiang Lunte electromechanical Co., Ltd, and the model is M-WRKK-450-T-LZ; the pressure sensor is manufactured by Honeywell GmbH, model STG74S-EIG000-1-A-CHS-HS-A-10A 0; the pressure difference sensor is manufactured by Honeywell corporation, and the model is STD720-EIAC4AS-1-A-AHS-HS-A-10A 0; the flow rate sensor was manufactured by chenodef philippit automation equipment ltd, model DM43NF1PH01N2W1 HN.

The executing mechanism comprises a coal powder upstream cut-off valve 37 and a coal powder downstream cut-off valve 38 which are arranged on a coal powder pipeline 14 close to the high-pressure coal hopper 1, a nozzle coal powder upstream cut-off valve 39 and a nozzle coal powder downstream cut-off valve 40 which are arranged on a coal powder pipeline 14 close to the hydrogenation gasification furnace 4, a coal powder conveying gas cut-off valve 41 and a coal powder conveying air flow regulating valve 42 which are arranged on a hydrogen pipeline 15, an oxygen upstream cut-off valve 43, an oxygen downstream cut-off valve 44 and an oxygen flow regulating valve 45 which are arranged on an oxygen pipeline 16, an oxygen pipeline nitrogen plug valve 57 which is arranged on an oxygen pipeline nitrogen plug pipeline 51, an oxygen pipeline nitrogen purging valve 58 which is arranged on an oxygen pipeline nitrogen purging pipeline 52, and an oxygen pipeline small-flow nitrogen;

the pulverized coal conveying air flow regulating valve 42 is positioned at the downstream of the pulverized coal conveying air cut-off valve 41, the oxygen flow regulating valve 45 is positioned at the upstream of the oxygen upstream cut-off valve 43, the oxygen upstream cut-off valve 43 is positioned at the upstream of the oxygen downstream cut-off valve 44, and the pulverized coal upstream cut-off valve 37 is positioned at the upstream of the pulverized coal downstream cut-off valve 38;

the coal powder upstream cut-off valve 37, the coal powder downstream cut-off valve 38, the inlet nozzle coal powder upstream cut-off valve 39, the inlet nozzle coal powder downstream cut-off valve 40, the coal powder conveying gas cut-off valve 41, the coal powder conveying wind flow regulating valve 42, the oxygen upstream cut-off valve 43, the oxygen downstream cut-off valve 44, the oxygen flow regulating valve 45, the coal powder pipeline nitrogen plug valve 54, the coal powder pipeline small-flow nitrogen blow valve 55, the coal powder pipeline nitrogen upstream cut-off valve 56, the oxygen pipeline nitrogen plug valve 57, the oxygen pipeline nitrogen blow valve 58 and the oxygen pipeline small-flow nitrogen blow valve 59 are all connected with the output end of the PLC 36.

In this embodiment, the high-pressure coal hopper 1 is used for storing and conveying pulverized coal; the hydrogenation gasification furnace 4 is used for receiving raw materials such as coal dust, hydrogen, oxygen and the like, carrying out reaction and pyrolyzing coal; the semicoke cooling fluidized bed 5 is used for recovering the semicoke heat generated in the hydrogenation gasification furnace 4, exchanging heat with boiler water and generating saturated steam by using a semicoke fluidized bed steam drum 7; the semicoke storage tank 6 is used for storing the cooled semicoke product; the cyclone dust collector 8 is used for collecting semicoke in the crude gas; the waste boiler 9 is used for recovering heat in the crude gas and generates saturated steam and superheated steam through heat exchange of a waste boiler steam drum 10; the filter 11 is used for fine dust removal and further recovering semicoke in the crude gas; the secondary hydrogen heater 13 is used for heat exchange between the crude gas and the hydrogen of the dehydrogenation gas heating furnace 2, so that the crude gas is cooled to about 216 ℃, the hydrogen is heated to about 250 ℃, and the hydrogen heating furnace 2 is used for heating the high-pressure hydrogen of 250 ℃ heated by the secondary hydrogen heater 13 to about 650 ℃, and then the high-pressure hydrogen directly enters the hydrogenation gasification furnace 4.

When the system is stopped, the high-pressure nitrogen replaces the hydrogen and the oxygen in the pipeline, so that internal combustion or explosion is avoided. When the nitrogen is replaced with the oxygen pipeline 16, opening an oxygen pipeline nitrogen plug valve 57, an oxygen pipeline nitrogen purging valve 58 and an oxygen pipeline small flow nitrogen purging valve 59, simultaneously closing the oxygen upstream cut-off valve 43 and the oxygen flow regulating valve 45, delaying for 15 seconds to close the oxygen downstream cut-off valve 44, and continuing delaying for 25 seconds to close the oxygen pipeline nitrogen purging valve 58;

when the nitrogen and hydrogen pipeline 15 is replaced, the pulverized coal conveying gas cut-off valve 41 and the pulverized coal conveying air flow regulating valve 42 are fully opened at first, and when the inlet nozzle pulverized coal upstream cut-off valve 39 is closed, the pulverized coal conveying gas cut-off valve 41 and the pulverized coal conveying air flow regulating valve 42 are closed at the same time;

when the nitrogen is replaced with the pulverized coal pipeline 14, the pulverized coal upstream cut-off valve 37 and the pulverized coal downstream cut-off valve 38 are closed, the pulverized coal inlet pipeline nitrogen upstream cut-off valve 56 is opened, the pulverized coal pipeline nitrogen plug valve 54 and the pulverized coal pipeline small flow nitrogen blow valve 55 are opened, and the nozzle pulverized coal upstream cut-off valve 39, the nozzle pulverized coal downstream cut-off valve 40 and the pulverized coal pipeline nitrogen plug valve 54 are closed.

Example 2:

in the monitoring method of the coal hydrogasification safety monitoring system implemented in embodiment 1, the detection mechanism detects the operating temperature, the operating pressure, the flow data, the liquid level data, and the pressure difference data of the coal hydrogasification apparatus, and transmits the detected operating temperature, operating pressure, flow data, liquid level data, and pressure difference data to the PLC controller 36; the PLC controller 36 analyzes the received operating temperature, operating pressure, flow data, liquid level data, and differential pressure data, and controls the actuator to perform an operation.

Presetting a first temperature set value, a second temperature set value, a third temperature set value, a first liquid level set value, a second liquid level set value, a first flow set value, a second flow set value, a third pressure set value, a fourth pressure set value, a first differential pressure set value, a second differential pressure set value and a third differential pressure set value in the PLC 36;

a first temperature measuring device 23 monitors a first temperature value of the raw gas at the outlet of the hydrogenation gasification furnace 4 and transmits the monitored first temperature value to a PLC controller 36, a second temperature measuring device 24 monitors a second temperature value of the hydrogen at the outlet of the hydrogen heating furnace 2 and transmits the monitored second temperature value to the PLC controller 36, a third temperature measuring device 25 monitors a third temperature value of the raw gas at the outlet of the waste boiler 9 and transmits the monitored third temperature value to the PLC controller 36, a first pressure measuring device 26 monitors a first pressure value of the hydrogenation gasification furnace 4 and transmits the monitored first pressure value to the PLC controller 36, a second pressure measuring device 27 monitors a second pressure value of the oxygen pipeline 16 and transmits the monitored second pressure value to the PLC controller 36, and a third pressure measuring device 28 monitors a third pressure value of the cold medium outlet of the secondary hydrogen heater 13, and transmits the monitored third pressure value to the PLC controller 36, the fourth pressure measuring device 29 monitors the fourth pressure value in the semicoke fluidized bed drum 7 and transmits the monitored fourth pressure value to the PLC controller 36, the first flow measuring device 30 monitors the first flow value of the cooling medium entering the secondary hydrogen heater 13 and transmits the monitored first flow value to the PLC controller 36, the second flow measuring device 31 monitors the second flow value of the feed water entering the semicoke cooling fluidized bed 5 and transmits the monitored second flow value to the PLC controller 36, the third flow measuring device 32 monitors the third flow value of the semicoke fluidized bed drum 7 steam outlet and transmits the monitored third flow value to the PLC controller 36, the first liquid level measuring device 33 monitors the first liquid level value in the semicoke fluidized bed drum 7 and transmits the monitored first liquid level value to the PLC controller 36, the second level measuring device 34 monitors a second level value in the waste boiler drum 10 and transmits the monitored second level value to the PLC controller 36, and the differential pressure measuring device 35 monitors a first differential pressure value at an inlet and an outlet of the filter 11 and transmits the monitored first differential pressure value to the PLC controller 36;

condition 1: the first temperature value is greater than or equal to a first temperature set value, and the first temperature set value is 1000 ℃; namely, the temperature of the crude gas at the outlet of the hydrogenation gasification furnace 4 is overhigh;

condition 2: the second temperature value is less than or equal to a second temperature set value, and the second temperature set value is 800 ℃; namely, the temperature of the hydrogen at the outlet of the hydrogen heating furnace 2 is too low;

condition 3: the third temperature value is more than or equal to a third temperature set value, and the third temperature set value is 380 ℃; namely, the temperature of the crude gas at the outlet of the waste boiler 9 is overhigh;

condition 4: the first liquid level value is less than or equal to a first liquid level set value, and the first liquid level set value is 3.1 percent; namely the liquid level in the semicoke fluidized bed steam drum 7 is too low;

condition 5: the second liquid level value is less than or equal to a second liquid level set value, and the second liquid level set value is 3.1 percent; i.e. the liquid level in the waste boiler drum 10 is too low;

condition 6: the first flow rate value is less than or equal to a first flow rate set value, and the first flow rate set value is 5000Nm³H; namely, the hydrogen flow entering the cold medium inlet of the secondary hydrogen heater 13 is too small;

condition 7: the second flow value is less than or equal to a second flow set value which is 5m³H; namely, the feed water flow entering the semicoke cooling fluidized bed 5 is too small;

condition 8: the third flow value is less than or equal to a third flow set value, and the third flow set value is 550 kg/h; namely, the flow of the steam outlet of the steam drum 7 of the semicoke fluidized bed is too small;

condition 9: the third pressure value is less than or equal to a third pressure set value, and the third pressure set value is 7.3 MPa; namely, the hydrogen pressure at the cold medium outlet of the secondary hydrogen heater 13 is too low;

condition 10: the fourth pressure value is greater than or equal to a fourth pressure set value, and the fourth pressure set value is 3 MPa; namely, monitoring the overhigh pressure in the steam drum 7 of the semicoke fluidized bed;

condition 11: the first pressure difference value is greater than or equal to a first pressure difference set value, and the first pressure difference set value is 100 kPa; namely, the pressure difference of the crude gas at the inlet and the outlet of the filter 11 is too high;

condition 12: the second pressure value-the first pressure value is less than or equal to a second pressure difference set value, and the second pressure difference set value is 100 kPa; i.e. the pressure difference between the oxygen line 16 and the hydro-gasification furnace 4 is too low;

condition 13: the third pressure value-the first pressure value is less than or equal to a third pressure difference set value, and the third pressure difference set value is 100 kPa; namely, the pressure difference between the cold medium outlet of the secondary hydrogen heater 13 and the hydrogenation gasification furnace 4 is too low.

The parking action includes:

(1) closing the oxygen upstream cut-off valve 43;

(2) the oxygen downstream cut-off valve 44 is closed after 15 seconds of delay;

(3) closing the oxygen pipeline nitrogen purge valve 58 after delaying for 40 seconds;

(4) closing the oxygen flow regulating valve 45;

(5) closing the pulverized coal upstream cut-off valve 37;

(6) closing the pulverized coal downstream shut-off valve 38;

(7) opening the coal powder conveying air flow regulating valve 42 to ensure that the opening degree of the coal powder conveying air flow regulating valve 42 is 100 percent; when the opening feedback of the coal powder conveying air flow regulating valve 42 is more than 95%, delaying for 10 seconds, closing the coal powder conveying air flow regulating valve 42, and simultaneously closing the coal powder upstream cut-off valve 39 and the coal powder conveying air cut-off valve 41 of the inlet nozzle;

(8) opening a nitrogen upstream cut-off valve 56 of the coal powder feeding pipeline, opening a nitrogen plug valve 54 of the coal powder pipeline when the nitrogen upstream cut-off valve 56 of the coal powder pipeline reaches a full open state, closing the nitrogen plug valve 54 of the coal powder pipeline after delaying for 25 seconds, closing a coal powder downstream cut-off valve 40 of the coal feeding nozzle and opening a small-flow nitrogen blowing valve 55 of the coal powder pipeline;

(9) opening a nitrogen upstream cut-off valve 56 of the coal powder inlet pipeline;

(10) opening the oxygen line small flow nitrogen purge valve 59;

(11) opening oxygen line nitrogen plug valve 57;

(12) opening the oxygen pipeline nitrogen purge valve 58, delaying for 40 seconds, and closing the oxygen pipeline nitrogen purge valve 58;

(13) the hydrogen heating furnace 2 was stopped.

In this embodiment, any two first temperature values among the 3 first temperature values monitored by the 3 first temperature measuring devices 23 are greater than or equal to a first temperature set value, that is, it is determined that the condition 1 is satisfied;

any two second temperature values in the 3 second temperature values monitored by the 3 second temperature measuring devices 24 are less than or equal to a second temperature set value, that is, the condition 2 is satisfied;

any two third temperature values in the 3 third temperature values monitored by the 3 third temperature measuring devices 25 are greater than or equal to a third temperature set value, that is, the condition 3 is satisfied;

any two of the 3 first liquid level values monitored by the 3 first liquid level measuring devices 33 are less than or equal to a first liquid level set value, and the condition 4 is judged to be met;

in the 3 second liquid level values monitored by the 3 second liquid level measuring devices 34, any two second liquid level values are less than or equal to a second liquid level set value, and the condition 5 is judged to be met;

any two first flow values in the 3 first flow values monitored by the 3 first flow measuring devices 30 are less than or equal to a first flow set value, and the condition 6 is judged to be met;

any two second flow values in the 3 second flow values monitored by the 3 second flow measuring devices 31 are less than or equal to a second flow set value, that is, the condition 7 is satisfied;

any two third flow values in the 3 third flow values monitored by the 3 third flow measuring devices 32 are less than or equal to the third flow set value, that is, the condition 8 is satisfied;

any two third pressure values in the 3 third pressure values monitored by the 3 third pressure measuring devices 28 are less than or equal to a third pressure set value, that is, the condition 9 is satisfied;

any two fourth pressure values in the 3 fourth pressure values monitored by the 3 fourth pressure measuring devices 29 are greater than or equal to a fourth pressure set value, that is, the condition 10 is satisfied;

any two of the 3 first differential pressure values monitored by the 3 differential pressure measuring devices 35 are greater than or equal to a first differential pressure set value, that is, the condition 11 is satisfied;

any two second pressure difference values out of the second pressure difference values obtained by subtracting the 3 first pressure values measured by the 3 first pressure measuring devices 26 from the 3 second pressure values measured by the 3 second pressure measuring devices 27 are less than or equal to a second pressure difference set value, that is, it is determined that the condition 12 is satisfied;

and (3) judging that the condition 13 is met if any two of second differential pressure values obtained by subtracting the 3 third pressure values measured by the 3 third pressure measuring devices 28 from the 3 first pressure values measured by the 3 first pressure measuring devices 26 are less than or equal to a third differential pressure set value.

The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.

Claims

1. The coal hydrogasification safety monitoring system is characterized by comprising a coal hydrogasification device, a detection mechanism, a PLC (programmable logic controller) and an execution mechanism;

2. The coal hydrogasification safety monitoring system according to claim 1, wherein the coal hydrogasification device comprises a high-pressure coal hopper, a hydrogen heating furnace, an oxygen source, a hydrogasification furnace, a semicoke cooling fluidized bed, a semicoke storage tank, a semicoke fluidized bed drum, a cyclone dust collector, a waste boiler drum, a filter, a hydrogen source, a secondary hydrogen heater, a high-pressure nitrogen source, a replacement pulverized coal pipeline and a replacement oxygen pipeline;

3. The coal hydrogasification safety monitoring system of claim 2, wherein the detection mechanism comprises at least one first temperature measuring device and at least one first pressure measuring device disposed on the raw gas line, at least one second temperature measuring device disposed on the hydrogen line, at least one third temperature measuring device disposed on the filter removal line, at least one second pressure measuring device disposed on the oxygen line, at least one third pressure measuring device disposed on the secondary hydrogen heater cold medium outlet line, a fourth pressure measuring device disposed in the semicoke fluidized bed drum, at least one first flow measuring device disposed on the secondary hydrogen heater cold medium inlet line, at least one second flow measuring device disposed on the water supply line, and a third flow measuring device disposed on the semicoke fluidized bed drum steam outlet line, the system comprises at least one first liquid level measuring device arranged in a semicoke fluidized bed steam drum, at least one second liquid level measuring device arranged in a waste boiler steam drum, and at least one differential pressure measuring device arranged in a filter;

4. The coal hydrogasification safety monitoring system of claim 3, wherein the number of the first temperature measuring device, the second temperature measuring device, the third temperature measuring device, the first pressure measuring device, the second pressure measuring device, the third pressure measuring device, the first flow measuring device, the second flow measuring device, the first liquid level measuring device, the second liquid level measuring device, and the differential pressure measuring device is 3.

5. The coal hydrogasification safety monitoring system of claim 4, wherein the first temperature measuring device, the second temperature measuring device, and the third temperature measuring device are all temperature sensors, the first pressure measuring device, the second pressure measuring device, the third pressure measuring device, and the fourth pressure measuring device are all pressure sensors, the first flow measuring device, the second flow measuring device, and the third flow measuring device are all flow rate sensors, and the differential pressure measuring device is a differential pressure sensor.

6. The coal hydrogasification safety monitoring system according to claim 2, wherein the execution mechanism comprises a pulverized coal upstream cut-off valve and a pulverized coal downstream cut-off valve which are arranged on the pulverized coal pipeline close to the high-pressure coal hopper, a nozzle pulverized coal upstream cut-off valve and a nozzle pulverized coal downstream cut-off valve which are arranged on the pulverized coal pipeline close to the hydro-gasification furnace, a pulverized coal conveying gas cut-off valve and a pulverized coal conveying air flow regulating valve which are arranged on the hydrogen pipeline, an oxygen upstream cut-off valve, an oxygen downstream cut-off valve and an oxygen flow regulating valve which are arranged on the oxygen pipeline nitrogen plug pipeline, an oxygen pipeline nitrogen plug valve which is arranged on the oxygen pipeline nitrogen plug pipeline, and an oxygen pipeline nitrogen purge valve which is arranged on the oxygen pipeline nitrogen purge pipeline, and an oxygen pipeline small-flow nitrogen blowing valve arranged on the oxygen pipeline small-flow nitrogen blowing pipe line;

7. The monitoring method of the coal hydrogasification safety monitoring system according to any one of claims 1 to 6, wherein the detection means detects an operating temperature, an operating pressure, flow rate data, liquid level data, and pressure difference data of the coal hydrogasification apparatus, and transmits the detected operating temperature, operating pressure, flow rate data, liquid level data, and pressure difference data to the PLC; the PLC analyzes the received operating temperature, operating pressure, flow data, liquid level data and pressure difference data, and controls the actuating mechanism to execute actions.

8. The monitoring method of a coal hydro-gasification safety monitoring system according to claim 7, wherein a first temperature set value, a second temperature set value, a third temperature set value, a first liquid level set value, a second liquid level set value, a first flow set value, a second flow set value, a third pressure set value, a fourth pressure set value, a first differential pressure set value, a second differential pressure set value, and a third differential pressure set value are preset in the PLC controller;

9. The method of monitoring coal hydro-gasification safety as recited in claim 8 wherein the shutdown action comprises:

(1) closing the oxygen upstream cut-off valve;

(2) closing the oxygen downstream cut-off valve after delaying for 15 seconds;

(4) closing the oxygen flow regulating valve;

(5) closing the coal powder upstream cut-off valve;

(6) closing a coal dust downstream cut-off valve;

(10) opening a small-flow nitrogen blowing valve of an oxygen pipeline;

(11) opening an oxygen line nitrogen plug valve;

(13) and stopping the hydrogen heating furnace.

10. The monitoring method for coal hydrogasification safety monitoring according to claim 8, wherein the first temperature set point is 1000 ℃; the second temperature set value is 800 ℃; the third temperature set point is 380 ℃; the first liquid level set value is 3.1%; the second liquid level set value is 3.1%; the first flow rate set point is 5000Nm³H; the second flow rate set value is 5m³H; the third flow setting value is 550 kg/h; the third pressure setting value is 7.3 MPa; the fourth pressure set value is 3 MPa; the first pressure differential set point is 100 kPa; the second pressure differential set point is 100 kPa; the third pressure differential set point is 100 kPa.

11. The monitoring method for coal hydrogasification safety monitoring according to claim 8, wherein any two of the 3 first temperature values monitored by the 3 first temperature measuring devices are greater than or equal to a first temperature set value, that is, the condition 1 is determined to be satisfied;