Hydrogenation process control system for producing sorbitol

Abstract

The utility model provides a hydrogenation process control system for producing sorbitol, which comprises a feed tank, a hydrogenation reaction kettle, a gas-liquid separation tank, a settling tank and a control system, the feed tank is used for preparing glucose liquid, an outlet of the feed tank is connected to a feed port of the hydrogenation reaction kettle through a pipeline, the hydrogenation reaction kettle is provided with a hydrogen inlet and a NaOH feed port, and the gas-liquid separation tank is connected with the settling tank through a pipeline. The system is used for providing hydrogen and NaOH for a hydrogenation reaction kettle, the hydrogenation reaction kettle is respectively connected with a steam inlet pipeline and a cooling water supply pipeline, an outlet of the hydrogenation reaction kettle is connected with a gas-liquid separation tank, a liquid outlet of the gas-liquid separation tank is connected to a settling tank, a bottom outlet of the settling tank is in reflux connection with a feeding tank, and the feeding tank is connected with a steam outlet of the gas-liquid separation tank. And a clear liquid outlet of the settling tank is connected to the next production process of sorbitol. The process design is reasonable, the production efficiency is improved by automatically controlling the process of producing sorbitol through glucose hydrogenation, and safe production can be realized.

Description

Technical Field

[0001] The utility model relates to the technical field of sorbitol production, in particular to a hydrogenation process control system for producing sorbitol. Background Art

[0002] Sorbitol has the function of hygroscopic and water retention, and is widely used in the food industry. For example, adding a small amount in the production of chewing gum and candy can keep the food soft, improve the texture and reduce hardening and sanding; it is used for water retention in bread and pastries; it can be used in sweets and foods to prevent taste change during logistics, and it can also chelate metal ions; it can be used in canned drinks and wine to prevent food turbidity caused by metal ions.

[0003] The industrial production of sorbitol is generally produced by starch hydrolysis, bioconversion, glucose hydrogenation and other methods. Among them, glucose hydrogenation is currently the most commonly used production method. Glucose hydrogenation produces sorbitol, and hydrogenation is the most important process. The initial hydrogenation process is completed manually by the operator, which requires frequent operations by on-site operators, is time-consuming and labor-intensive, and cannot effectively control the reaction process. It is easy to have incomplete reactions or low efficiency problems, which is not conducive to actual production and also poses other safety hazards. Utility Model Content

[0004] In view of the above-mentioned deficiencies in the prior art, the utility model provides a hydrogenation process control system for producing sorbitol, which improves production efficiency and achieves safe production by automatically controlling the process of producing sorbitol by hydrogenating glucose.

[0005] The utility model provides a technical solution: a control system for a hydrogenation process for producing sorbitol, comprising a feed tank, a hydrogenation reactor, a gas-liquid separation tank, a sedimentation tank and a control system, wherein the feed tank is used to configure glucose solution, the outlet of the feed tank is connected to the feed port of the hydrogenation reactor through a pipeline, the hydrogenation reactor is provided with a hydrogen inlet and a NaOH feed port, which are used to provide hydrogen and NaOH to the hydrogenation reactor, the hydrogenation reactor is respectively connected to a steam air inlet pipeline and a cooling water supply pipeline, the outlet of the hydrogenation reactor is connected to the gas-liquid separation tank, the liquid outlet of the gas-liquid separation tank is connected to the sedimentation tank, the bottom outlet of the sedimentation tank is refluxed and connected to the feed tank, and the clear liquid outlet of the sedimentation tank is connected to a subsequent production process of sorbitol.

[0006] Furthermore, the control system includes a SIS production safety system and a DCS production control system for controlling the hydrogenation process. The DCS production control system includes a control cabinet and an operation display system for receiving data from instruments and meters in the hydrogenation reaction and controlling the operation of various equipment and instruments and meters.

[0007] Furthermore, the feed tank is connected to a NaOH metering tank for adjusting the pH value of the glucose solution in the feed tank. The inlet of the feed tank is connected to a feed pipeline for supplying glucose. A feed tank feed valve is provided on the feed pipeline. A first liquid level gauge, an agitator and an online pH meter are provided in the feed tank. The feed tank feed valve, the first liquid level gauge, the agitator and the online pH meter are respectively connected to a DCS production control system. The feed tank feed valve is interlocked with the first liquid level gauge, and a high limit liquid level is set to control the feed liquid level.

[0008] Furthermore, a second liquid level gauge is provided in the NaOH metering tank, a NaOH discharge valve is provided on the pipeline connecting the NaOH metering tank to the feed tank, a NaOH feed valve is provided on the feed pipeline of the NaOH metering tank, the NaOH feed valve, the second liquid level gauge and the NaOH discharge valve are respectively connected to the DCS production control system, the NaOH discharge valve is interlocked with the first liquid level gauge, the pH value of the feed tank is set to control the pH value, the NaOH feed valve is interlocked with the second liquid level gauge, and the high limit liquid level is set to control the NaOH liquid level.

[0009] Furthermore, a feed pump, a frequency-converter-controlled high-pressure injection pump and a reactor feed valve are arranged on the pipeline connecting the feed tank to the hydrogenation reactor; a reactor hydrogenation valve, a reactor steam valve and a reactor cold water valve are respectively arranged on the hydrogen inlet pipeline, the steam inlet pipeline and the cooling water supply pipeline of the hydrogenation reactor; a magnetic stirrer is arranged in the hydrogenation reactor; the feed pump, the frequency-converter-controlled high-pressure injection pump, the reactor feed valve, the reactor hydrogenation valve, the reactor steam valve, the reactor cold water valve and the magnetic stirrer are respectively connected to the DCS production control system; the first liquid level gauge is interlocked with the reactor feed valve, the feed pump, the high-pressure injection pump and the magnetic stirrer; the liquid level is set to control the feed liquid level of the hydrogenation reactor, the start and stop of the feed pump and the high-pressure injection pump and the start of the magnetic stirrer.

[0010] Furthermore, a first temperature sensor, a second temperature sensor and a pressure sensor are provided in the hydrogenation reactor, a reactor steam regulating valve is provided in the steam inlet pipeline, the first temperature sensor is interlocked with the reactor steam regulating valve and the reactor steam valve, and the temperature parameter is set to control the reactor temperature, a reactor hydrogenation regulating valve is provided on the hydrogen inlet pipeline, a pressure sensor is interlocked with the reactor hydrogenation regulating valve and the reactor hydrogenation valve, and a pressure parameter is set to control the reactor hydrogenation pressure, the second temperature sensor is interlocked with the reactor cold water valve, and a high limit temperature parameter is set to control the maximum reaction temperature of the reactor, and a reactor discharge valve and a reactor discharge regulating valve are provided on the discharge pipeline of the hydrogenation reactor connected to the gas-liquid separation tank, the reactor pressure sensor is interlocked with the reactor discharge regulating valve and the reactor discharge valve, and the pressure parameter is set to control the reactor discharge pressure.

[0011] Furthermore, the outlet of the hydrogenation reactor is respectively connected to a condensed water outlet pipe and a cooling water return pipe, the hydrogenation reactor is provided with a sampling port, and the feed tank is provided with a catalyst inlet and a steam inlet.

[0012] Furthermore, a spray head is provided on the top of the gas-liquid separation tank, and the spray head is connected to a spray water pipe. Two settling tanks are provided in parallel, and a feed pipe of each settling tank is connected to the gas-liquid separation tank. The feed pipe of the settling tank is provided with a settling tank feed valve. A third liquid level gauge is provided in each settling tank, and the third liquid level gauge is interlocked with the settling tank feed valve, the reactor discharge regulating valve and the reactor discharge valve. The liquid level parameters of the third liquid level gauge are set to control the reactor discharge liquid level.

[0013] Furthermore, the temperature control component in each of the settling tanks is connected to a cooling water inlet pipe with a settling tank cooling water valve, the outlet of the temperature control component is connected to a cooling water return pipe, a third temperature sensor is provided in the settling tank, the third temperature sensor is interlocked with the settling tank cooling water valve, and the temperature parameters are set to control the temperature of the settling tank; the third liquid level meter is interlocked with the settling tank cooling water valve, and the liquid level parameters are set to control the opening of the settling tank cooling water valve, a settling tank bottom material discharge valve is provided on the pipeline from the settling tank back to the feed tank, a nitrogen inlet is provided above the bottom outlet of the settling tank, and a settling tank clear liquid discharge valve is provided at the clear liquid outlet of the settling tank.

[0014] Furthermore, the SIS production safety system includes a control unit, a detection unit connected to the control unit, and an execution unit. The detection unit includes a gas detector, a smoke sensor, and an overheating sensor installed above or near each device or pipeline in the production workshop. The execution unit includes an alarm and equipment for implementing fire spraying, spraying or inert gas dilution, and steam spraying. The control cabinet of the DCS production control system is connected to the control unit. When the power supply or instrumentation of the DCS production control system is abnormal, the control unit controls the emergency valve to cut off / open or the motor power supply to cut off.

[0015] Beneficial effects of the utility model:

[0016] (1) The production system of the utility model realizes continuous production, and realizes automatic control in the production process through the DCS production control system, so that the reaction is thorough, the side reaction is less, the residual sugar in the product is low, the product yield is improved, and time and labor are saved, the labor intensity is reduced, and the labor cost is saved;

[0017] (2) The SIS production safety system is used to realize the alarm and interlocking parts of the factory control system, and implement alarm actions, adjustments or shutdown controls on the detection results in the control system, thereby ensuring the safety of the production process, preventing accidents, and reducing the hazards and impacts caused by accidents. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1 It is a production process diagram of the utility model;

[0019] Figure 2 It is the principle block diagram of the SIS production safety system of the utility model;

[0020] Figure 3 This is the principle block diagram of the DCS production control system of the utility model; DETAILED DESCRIPTION

[0021] The present invention is further described below in conjunction with specific implementation methods, wherein the accompanying drawings are only used for exemplary descriptions and represent only schematic diagrams rather than actual drawings, and should not be understood as limiting the present invention. In order to better illustrate the specific implementation methods of the present invention, some parts of the accompanying drawings may be omitted, enlarged or reduced, and do not represent the size of the actual product. For those skilled in the art, it is understandable that some well-known structures and their descriptions in the accompanying drawings may be omitted. Based on the specific implementation methods of the present invention, all other specific implementation methods obtained by ordinary technicians in this field without making creative work are within the scope of protection of the present invention.

[0022] like Figure 1-3 A hydrogenation process control system for producing sorbitol is shown, comprising a feed tank 1, a hydrogenation reactor 2, a gas-liquid separation tank 3, a sedimentation tank 4 and a control system, wherein the feed tank 1 is used to prepare glucose solution, and the outlet of the feed tank 1 is connected to the feed port of the hydrogenation reactor 2 through a pipeline, and the hydrogenation reactor 2 is provided with a hydrogen inlet and a NaOH feed port for providing hydrogen and NaOH to the hydrogenation reactor 2, the temperature control components of the hydrogenation reactor 1 are respectively connected to the steam inlet pipeline 5 and the cooling water supply pipeline 6, the outlet of the hydrogenation reactor 2 is connected to the gas-liquid separation tank 3, the liquid outlet of the gas-liquid separation tank 3 is connected to the sedimentation tank 4, the bottom outlet of the sedimentation tank 4 is refluxed and connected to the feed tank 1, and the clear liquid outlet of the sedimentation tank 4 is connected to the subsequent production process of sorbitol.

[0023] The feed tank 1 is connected to the NaOH metering tank 7, which is used to adjust the pH value of the glucose solution in the feed tank 1. The inlet of the feed tank 1 is connected to the feed pipeline for supplying glucose, and a feed tank feed valve 8 is provided on the feed pipeline. A first liquid level gauge 9, an agitator 10 and an online pH meter 11 are provided in the feed tank 1. The feed tank feed valve 8, the first liquid level gauge 9, the agitator 10 and the online pH meter 11 are respectively connected to the DCS production control system. The feed tank feed valve 8 is interlocked with the first liquid level gauge 9, and the upper limit liquid level is set to control the feed liquid level.

[0024] A second liquid level gauge 12 is provided in the NaOH metering tank 7, a NaOH discharge valve 13 is provided on the pipeline connecting the NaOH metering tank 7 to the feed tank 1, a NaOH feed valve 14 is provided on the feed pipeline of the NaOH metering tank 7, the NaOH feed valve 14, the second liquid level gauge 12 and the NaOH discharge valve 13 are respectively connected to the DCS production control system, the NaOH discharge valve 13 is interlocked with the first liquid level gauge 9, the pH value of the feed tank 1 is controlled by setting the pH value, and the NaOH feed valve 14 is interlocked with the second liquid level gauge 12, and the upper limit liquid level is set to control the NaOH liquid level.

[0025] The pipeline connecting the feed tank 1 to the hydrogenation reactor 2 is provided with a feed pump 15, a frequency conversion controlled high-pressure injection pump 16 and a reactor feed valve 17. The hydrogen inlet pipeline, the steam inlet pipeline 5 and the cooling water supply pipeline 6 of the hydrogenation reactor 2 are respectively provided with a reactor hydrogenation valve 18, a reactor steam valve 19 and a reactor cold water valve 20. A magnetic stirrer 21 is provided in the hydrogenation reactor 2. The feed pump 15, the frequency conversion controlled high-pressure injection pump 16, the reactor feed valve 17, the reactor hydrogenation valve 18, the reactor steam valve 19, the reactor cold water valve 20 and the magnetic stirrer 21 are respectively connected to the DCS production control system. The first liquid level gauge 9 is interlocked with the reactor feed valve 17, the feed pump 15, the high-pressure injection pump 16 and the magnetic stirrer 21. The liquid level is set to control the feed liquid level of the hydrogenation reactor 2, the start and stop of the feed pump 15 and the high-pressure injection pump 16 and the start of the magnetic stirrer 21.

[0026] The hydrogenation reactor 2 is provided with a first temperature sensor 22, a second temperature sensor 23 and a pressure sensor 24, the steam inlet pipeline 5 is provided with a reactor steam regulating valve 25, the first temperature sensor 22 is interlocked with the reactor steam regulating valve 25 and the reactor steam valve 19, and the temperature parameter is set to control the reactor temperature, the hydrogen inlet pipeline is provided with a reactor hydrogenation regulating valve 26, the pressure sensor 24 is interlocked with the reactor hydrogenation regulating valve 26 and the reactor hydrogenation valve 18, and the pressure parameter is set to control the reactor hydrogenation pressure, the second temperature sensor 23 is interlocked with the reactor cold water valve 20, and the upper limit temperature parameter is set to control the maximum reaction temperature of the reactor, the hydrogenation reactor 2 is connected to the gas-liquid separation tank 3. The discharge pipeline is provided with a reactor discharge valve 27 and a reactor discharge regulating valve 28, the reactor pressure sensor is interlocked with the reactor discharge regulating valve 28 and the reactor discharge valve 27, and the pressure parameter is set to control the discharge pressure of the reactor V1105.

[0027] The outlet of the temperature control component of the hydrogenation reactor 2 is respectively connected with a condensate outlet pipe 37 and a cooling water return pipe 29, and the hydrogenation reactor 2 is provided with a sampling port 30, and the feed tank 1 is provided with a catalyst inlet and a steam inlet. The feed tank 1 is connected to the CIP cleaning system to clean the feed tank, and the steam of the feed tank is mainly used for steam sterilization. The hydrogenation reactor is also provided with a catalyst addition port, and a certain catalyst is filled in the hydrogenation reactor, which is always retained in the reactor for hydrogenation production. Each batch will lose a small amount of catalyst due to chemical reaction or physical crushing, and a part of it will be recovered by sedimentation tank precipitation, and a part of new catalyst will be added to the feed tank to ensure the catalyst equivalent required for the reaction. According to the actual production situation, the catalyst should be discharged from the reactor for processing every few months, and then re-dosed. Nitrogen is usually used to press the catalyst out of the reactor.

[0028] A spray head is provided on the top of the gas-liquid separation tank 3, and the spray head is connected to the spray water pipe. Two settling tanks 4 are provided in parallel, and the feed pipe of each settling tank 4 is connected to the gas-liquid separation tank 3. The feed pipe of the settling tank 4 is provided with a settling tank feed valve 36. A third liquid level gauge 31 is provided in each settling tank 4, and the third liquid level gauge 31 is interlocked with the settling tank feed valve 36, the reactor discharge regulating valve 28 and the reactor discharge valve 27. The liquid level parameter of the third liquid level gauge 31 is set to control the reactor discharge liquid level.

[0029] The temperature control assembly in each of the settling tanks 4 is connected to the cooling water inlet pipe with the settling tank cooling water valve 32, and the outlet of the temperature control assembly is connected to the cooling water return pipe. A third temperature sensor 33 is provided in the settling tank 4, and the third temperature sensor 33 is interlocked with the settling tank cooling water valve 32, and the temperature parameter is set to control the temperature of the settling tank; the third liquid level meter 31 is interlocked with the settling tank cooling water valve 32, and the liquid level parameter is set to control the opening of the settling tank cooling water valve 32. A settling tank bottom material discharge valve 34 is provided on the pipeline from the settling tank 4 back to the feed tank 1, and a nitrogen inlet is provided above the bottom outlet of the settling tank 4, and a settling tank clear liquid discharge valve 35 is provided at the clear liquid outlet of the settling tank 4. The nitrogen inlet is provided because the catalyst precipitation is easy to block the pipe mouth, and a small amount of nitrogen is used to quickly flush it open, and the precipitated catalyst is recovered. The use of nitrogen also prevents the catalyst from being oxidized and prevents the oxygen content of the settling tank from exceeding the standard.

[0030] The control system includes an SIS production safety system and a DCS production control system for controlling the hydrogenation process. All the instruments and components for performing operations in the hydrogenation process are connected to the DCS production control system. The DCS production control system includes a control cabinet and an operation display system for receiving data from instruments and instruments in the hydrogenation reaction and controlling the operation of various equipment and instruments and instruments. The SIS production safety system includes a control unit, a detection unit and an execution unit connected to the control unit. The detection unit includes a gas detector, a smoke sensor and an overheating sensor arranged above or near each equipment or pipeline in the production workshop. The execution unit includes an alarm and equipment for realizing fire spraying, spraying or inert gas dilution, and steam spraying. The control cabinet of the DCS production control system is connected to the control unit. When the power supply or instrument of the DCS production control system is abnormal, the control unit controls the emergency valve to cut off / open or the motor power supply to cut off.

[0031] The SIS production safety system can monitor the emerging or potential dangers in the production process, issue warning messages or directly execute predetermined procedures, and immediately enter operations to prevent accidents and reduce the hazards and impacts caused by accidents.

[0032] This system, combined with the DCS production control system, can more effectively ensure production safety, and respond to power outages, gas (instrument air), and water (auxiliary process water) outages with corresponding alarms, cutoffs, fire fighting, dilution, and other measures.

[0033] (1) Alarm

[0034] Gas detectors, smoke sensors, and overheat sensors are installed above or near each device or pipeline in the production workshop. When hydrogen leaks or abnormal operations occur, and the gas density setting value, smoke concentration setting value, and ambient temperature setting value are exceeded, the SIS system will issue an emergency alarm and make corresponding level of processing to monitor the safety of the production environment in real time.

[0035] (2) Emergency treatment such as firefighting and cutting off

[0036] According to the alarm time or the actual detection value of the detector, firefighting water spray, fog or inert gas dilution, steam spray and other treatment measures are taken. In addition to the fixed position setting of the detector, there is also random handheld detection. For example, when regular inspection or maintenance is required, the handheld detector is turned on and the system security permission is obtained before the maintenance work can be carried out, and the whole process is recorded in real time for filing.

[0037] When the DCS system stops suddenly or the power supply is cut off, the instrument gas pressure is less than 1 bar or there is no data, the cooling water or chilled water pressure is less than 1 bar or there is no data, the reactor, high-pressure hydrogen tank, low-pressure hydrogen tank and other equipment or complete sets with safety valves, the SIS system will make emergency treatments such as emergency valve cutting / opening, motor power cutting, and protective gas or steam valve opening.

[0038] The reasonable combination of DCS production control system and SIS production safety system eliminates more production safety hazards, effectively handles emergencies and reduces the error handling of personnel instability factors. The dual systems are linked with factors such as production process and equipment layout, and are targeted at the characteristics of glucose hydrogenation production process, with real-time detection and control, to improve the safety production specifications.

[0039] The production process of glucose hydrogenation includes process control steps such as batching, feeding, hydrogenation, discharging, and sedimentation.

[0040] (1) Ingredient control

[0041] When production needs to batch materials in advance, the operator enters the first step instruction <batch control>. According to the liquid level LT1101 parameter set in the feed tank, the feed pump P1102 and the agitator A1101 are automatically started / stopped, the pH value is detected online, and NaOH is added according to the material volume of the feed tank V1101, and the metering and real-time detection PHT1101 reaches 7.8-8.2. The batching control is completed and the system instruction feed control is waiting.

[0042] (2) Feed control

[0043] When the first step instruction <batch control> is completed, the program enters the second step instruction <feed control>. When the system detects and confirms that the agitator of the reactor is in a stopped state and the pressure is less than 20bar, the hydrogenation valve, steam valve, discharge valve, vent valve, and cooling valve are in a closed state, the feed pump is started, the pneumatic high-pressure injection pump is delayed, and the feed valve is opened at the same time; when the liquid level of the feed tank is at 50%, the reactor starts the magnetic agitator: when the liquid level of the feed tank is at 15%, the agitator of the feed tank is stopped; when the liquid level of the feed tank is at the set level, the feed valve is closed, the high-pressure injection pump is stopped at the same time, and the feed pump is stopped with a delay to complete the feed control.

[0044] (3) Hydrogenation control

[0045] When the second step instruction <feed control> is completed, the program enters the third step instruction <hydrogenation control>. According to the set temperature parameters and heating time parameters, and the online temperature detection signal, the opening of the steam regulating valve is controlled to control the heating process; at the same time, according to the set pressure parameters and pressurization time parameters, and the online pressure detection signal, the opening of the hydrogen regulating valve is controlled to control the hydrogenation process. The glucose hydrogenation process is an exothermic process. When the temperature reaches the highest point and does not rise, and the pressure in the kettle reaches the set value and does not drop, after a delay of 5-10 minutes, the system will preliminarily determine that the reaction is over, and send a sampling signal to close the steam shut-off valve and the hydrogen shut-off valve; at this time, manual sampling is involved, and the detection process takes about 12-15 minutes. After receiving the detection information, the operator manually enters the detection value.

[0046] (4) Discharge control

[0047] When the third step instruction <hydrogenation control> is completed, the program enters the fourth step instruction <discharging control>. First, the system sends a signal to stop the magnetic stirrer, and the program enters the reactor's 'stationary' timing; detect the liquid level parameters of the sedimentation tank (A or B), choose to open the sedimentation tank feed valve, open the sedimentation tank cooling water inlet valve (the outlet valve is normally open), and the sedimentation tank discharge valve is in a closed state. After the 'stationary' set time is completed, the reactor discharge valve gradually opens according to the opening time, and the online pressure detection discharge pressure controls the discharge valve opening; when the sedimentation tank liquid level reaches the set liquid level height, close the discharge valve to complete the discharge control.

[0048] (5) Settlement control

[0049] When the fourth step instruction <discharging control> is completed, the program enters the fifth step instruction <sedimentation control>. When the sedimentation time reaches the first set value, the liquid level of the feed tank is detected, and the bottom material discharge valve is opened and closed according to the set valve opening time and opening times, and the liquid with catalyst is recovered to the feed tank; when the sedimentation time reaches the second set value, the liquid level of the process sedimentation tank is detected, and the clear liquid discharge valve of the sedimentation tank is opened; when the sedimentation tank reaches the lower limit of the liquid level, the clear liquid discharge valve is closed, the bottom material discharge valve is opened, and the liquid with catalyst is recovered to the feed tank again.

[0050] That is to complete the control process of glucose hydrogenation. Usually, the operator can regulate the production process on a microcomputer.

[0051] Finally, it should be noted that the above is only a preferred embodiment of the present invention and is not intended to limit the present invention. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art can still modify the technical solutions described in the aforementioned embodiments or make equivalent substitutions for some of the technical features therein. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A hydrogenation process control system for producing sorbitol, characterized in that: The invention comprises a feed tank (1), a hydrogenation reactor (2), a gas-liquid separation tank (3), a sedimentation tank (4) and a control system. The feed tank (1) is used to prepare glucose solution. The outlet of the feed tank (1) is connected to the feed port of the hydrogenation reactor (2) through a pipeline. The hydrogenation reactor (2) is provided with a hydrogen inlet and a NaOH feed port for providing hydrogen and NaOH to the hydrogenation reactor (2). The temperature control component of the hydrogenation reactor (2) is connected to a steam inlet pipeline (5) and a cooling water supply pipeline (6) respectively. The outlet of the hydrogenation reactor (2) is connected to the gas-liquid separation tank (3). The liquid outlet of the gas-liquid separation tank (3) is connected to the sedimentation tank (4). The bottom outlet of the sedimentation tank (4) is refluxed and connected to the feed tank (1). The clear liquid outlet of the sedimentation tank (4) is connected to a subsequent production process of sorbitol.

2. A hydrogenation process control system for producing sorbitol according to claim 1, characterized in that: The control system includes a SIS production safety system and a DCS production control system for controlling the hydrogenation process. The DCS production control system includes a control cabinet and an operation display system for receiving data from instruments and meters in the hydrogenation reaction and controlling the operation of various equipment and instruments and meters.

3. A hydrogenation process control system for producing sorbitol according to claim 1, characterized in that: The feed tank (1) is connected to a NaOH metering tank (7) for adjusting the pH value of the glucose solution in the feed tank (1). The inlet of the feed tank (1) is connected to a feed pipeline for supplying glucose. A feed tank feed valve (8) is provided on the feed pipeline. A first liquid level meter (9), an agitator (10) and an online pH meter (11) are provided in the feed tank (1). The feed tank feed valve (8), the first liquid level meter (9), the agitator (10) and the online pH meter (11) are respectively connected to a DCS production control system. The feed tank feed valve (8) is interlocked with the first liquid level meter (9) to set a high limit liquid level to control the feed liquid level.

4. A hydrogenation process control system for producing sorbitol according to claim 3, characterized in that: The NaOH metering tank (7) is provided with a second liquid level gauge (12), a NaOH discharge valve (13) is provided on the pipeline connecting the NaOH metering tank (7) to the feed tank (1), and a NaOH feed valve (14) is provided on the feed pipeline of the NaOH metering tank (7). The NaOH feed valve (14), the second liquid level gauge (12) and the NaOH discharge valve (13) are respectively connected to a DCS production control system. The NaOH discharge valve (13) is interlocked with the first liquid level gauge (9) to set the pH value of the feed tank (1), and the NaOH feed valve (14) is interlocked with the second liquid level gauge (12) to set the upper limit liquid level to control the NaOH liquid level.

5. A hydrogenation process control system for producing sorbitol according to claim 3, characterized in that: The pipeline connecting the feed tank (1) to the hydrogenation reactor (2) is provided with a feed pump (15), a frequency conversion-controlled high-pressure injection pump (16) and a reactor feed valve (17); the hydrogen inlet pipeline, the steam inlet pipeline (5) and the cooling water supply pipeline (6) of the hydrogenation reactor (2) are respectively provided with a reactor hydrogenation valve (18), a reactor steam valve (19) and a reactor cooling water valve (20); the hydrogenation reactor (2) is provided with a magnetic stirrer (21), a feed pump (15), a frequency conversion-controlled high-pressure injection pump (16) and a reactor feed valve (17); The pump (16), the reactor feed valve (17), the reactor hydrogenation valve (18), the reactor steam valve (19), the reactor cooling water valve (20) and the magnetic stirrer (21) are respectively connected to the DCS production control system. The first liquid level meter (9) is interlocked with the reactor feed valve (17), the feed pump (15), the high-pressure injection pump (16) and the magnetic stirrer (21). The liquid level is set to control the feed liquid level of the hydrogenation reactor (2), the start and stop of the feed pump (15) and the high-pressure injection pump (16) and the start of the magnetic stirrer (21).

6. A hydrogenation process control system for producing sorbitol according to claim 5, characterized in that: The hydrogenation reactor (2) is provided with a first temperature sensor (22), a second temperature sensor (23) and a pressure sensor (24); the steam inlet pipeline (5) is provided with a reactor steam regulating valve (25); the first temperature sensor (22) is interlocked with the reactor steam regulating valve (25) and the reactor steam valve (19); the temperature parameters are set to control the reactor temperature; the hydrogenation pipeline is provided with a reactor hydrogenation regulating valve (26); the pressure sensor (24) is interlocked with the reactor hydrogenation regulating valve (26) and the reactor hydrogenation regulating valve (19); The hydrogen valve (18) is interlocked, and a pressure parameter is set to control the hydrogenation pressure of the reactor. The second temperature sensor (23) is interlocked with the reactor cooling water valve (20), and a high limit temperature parameter is set to control the maximum reaction temperature of the reactor. The hydrogenation reactor (2) is connected to the gas-liquid separation tank (3) on the discharge pipe provided with a reactor discharge valve (27) and a reactor discharge regulating valve (28). The reactor pressure sensor is interlocked with the reactor discharge regulating valve (28) and the reactor discharge valve (27), and a pressure parameter is set to control the discharge pressure of the reactor.

7. A hydrogenation process control system for producing sorbitol according to claim 1, characterized in that: The outlet of the temperature control component of the hydrogenation reaction kettle (2) is respectively connected to a condensed water outlet pipe (37) and a cooling water return pipe (29); the hydrogenation reaction kettle (2) is provided with a sampling port (30); and the feed tank (1) is provided with a catalyst inlet and a steam inlet.

8. A hydrogenation process control system for producing sorbitol according to claim 6, characterized in that: A spray head is provided on the top of the gas-liquid separation tank (3), and the spray head is connected to a spray water pipeline. Two settling tanks (4) are provided in parallel, and the feed pipeline of each settling tank (4) is connected to the gas-liquid separation tank (3). The feed pipeline of the settling tank (4) is provided with a settling tank feed valve (36). A third liquid level meter (31) is provided in each settling tank (4), and the third liquid level meter (31) is interlocked with the settling tank feed valve (36), the reactor discharge regulating valve (28) and the reactor discharge valve (27). The liquid level parameter of the third liquid level meter (31) is set to control the reactor discharge liquid level.

9. A hydrogenation process control system for producing sorbitol according to claim 8, characterized in that: The temperature control component in each of the settling tanks (4) is connected to a cooling water inlet pipe with a settling tank cooling water valve (32), and the outlet of the temperature control component is connected to a cooling water return pipe. A third temperature sensor (33) is provided in the settling tank (4), and the third temperature sensor (33) is interlocked with the settling tank cooling water valve (32), and a temperature parameter is set to control the temperature of the settling tank; a third liquid level meter (31) is interlocked with the settling tank cooling water valve (32), and a liquid level parameter is set to control the opening of the settling tank cooling water valve (32). A settling tank bottom material discharge valve (34) is provided on the pipeline from the settling tank (4) back to the feed tank (1), a nitrogen inlet is provided above the bottom outlet of the settling tank (4), and a settling tank clear liquid discharge valve (35) is provided at the clear liquid outlet of the settling tank (4).

10. A hydrogenation process control system for producing sorbitol according to claim 2, characterized in that: The SIS production safety system includes a control unit, a detection unit and an execution unit connected to the control unit. The detection unit includes a gas detector, a smoke sensor and an overheating sensor installed above or near each equipment or pipeline in the production workshop. The execution unit includes an alarm and equipment for implementing fire spraying, spraying or inert gas dilution, and steam spraying. The control cabinet of the DCS production control system is connected to the control unit. When the power supply or instruments of the DCS production control system are abnormal, the control unit controls the emergency valve to cut off / open or cut off the power supply of the motor.

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