Liquid level and extraction flow control system and control method of reaction system

Abstract

The invention provides a liquid level and extraction flow control system and control method of a reaction system, and belongs to the technical field of chemical production, and the system is characterized in that a reaction system liquid level controller adopts a split-range control method to treat process input; the output end of the reaction system liquid level controller is respectively connected with the first calculation module and the third calculation module; the extraction pipeline flow controller adopts a split-range control method to process the process input, and the output end of the extraction pipeline flow controller is connected with the second calculation module and the fourth calculation module respectively; two ends of the low selection module are respectively connected with the first calculation module and the second calculation module; two ends of the direct extraction regulating valve are respectively communicated with the reaction system and the downstream user, two ends of the extraction buffer regulating valve are respectively communicated with the reaction system and the buffer system, and two ends of the buffer extraction regulating valve are respectively communicated with the buffer system and the downstream user. The energy consumption can be reduced, and the cost is saved.

Description

Technical Field

[0001] The present application relates to the field of chemical production technology, and in particular to a liquid level and extraction flow control system and a control method for a reaction system. Background Art

[0002] In a chemical plant, in order to maintain the liquid level of the reaction system, materials need to be taken out of the buffer system for buffering. In order to avoid over-temperature or over-pressure in the buffer system, the materials need to be cooled and then sent to the buffer system. When downstream users need them, they are heated by a heat exchanger and taken out of the buffer system to maintain normal production. Downstream users have different demands for materials, sometimes more and sometimes less. Therefore, in the process of transporting materials to downstream users, it is even more necessary to control the liquid level and extraction flow rate of the reaction system to avoid over-temperature or over-pressure.

[0003] At present, in order to meet the needs of production processes, a control method that combines the distillation system level control loop and the production pipeline flow control loop is often used. However, in actual operation, when the material in the reaction system is produced to the cache system, the material in the cache system needs to be produced to the downstream users. This is equivalent to the material produced in the reaction system being cooled first and then heated before being produced to the downstream users, resulting in energy waste and increased operating costs.

[0004] Therefore, there is an urgent need for a liquid level and extraction flow control method for a reaction system to solve the above technical problems. Summary of the invention

[0005] The present application provides a liquid level and extraction flow control system and control method for a reaction system. By introducing a split-range control and flow decoupling calculation module, the usage of cold and hot media can be reduced on the basis of liquid level control and flow control, thereby achieving the purpose of reducing system energy consumption and operating costs.

[0006] In a first aspect, the present application provides a liquid level and production flow control system for a reaction system, including: a reaction system liquid level controller, a production pipeline flow controller, a low selection module, a first calculation module, a second calculation module, a third calculation module, a fourth calculation module, a direct production regulating valve, a production buffer regulating valve, and a cache production regulating valve;

[0007] The reaction system liquid level controller adopts a split-range control method to process process input, the input end of the reaction system liquid level controller is connected to the reaction system through a liquid level transmitter, and the reaction system liquid level controller is used to monitor the liquid level of the material in the reaction system and control the flow rate of the material to the downstream system, wherein the downstream system includes a cache system and a downstream user; the output end of the reaction system liquid level controller is respectively connected to the first calculation module and the third calculation module;

[0008] The production pipeline flow controller adopts a split-range control method to process process input, the input end of the production pipeline flow controller is connected to the pipeline produced to the downstream user through a flow transmitter, the production pipeline flow controller is used to monitor and control the total flow produced to the downstream user, and the output end of the production pipeline flow controller is respectively connected to the second calculation module and the fourth calculation module;

[0009] The two ends of the low selection module are respectively connected to the first calculation module and the second calculation module, and are used to perform low selection on the first calculation module and the second calculation module to obtain the minimum value output by the first calculation module and the second calculation module;

[0010] The two ends of the direct production regulating valve are connected to the reaction system and the downstream user respectively, the two ends of the production buffer regulating valve are connected to the reaction system and the cache system respectively, and the two ends of the cache production regulating valve are connected to the cache system and the downstream user respectively.

[0011] In a possible implementation, the direct production regulating valve, the production buffer regulating valve and the cache production regulating valve are all air-opened valves.

[0012] In a possible implementation, the reaction system liquid level controller is positive acting, and the production line flow controller is negative acting.

[0013] In a possible implementation, the low selection module, the first calculation module, the second calculation module, the third calculation module, and the fourth calculation module are integrated into a flow decoupling calculation device.

[0014] In a second aspect, the present application provides a method for controlling the liquid level and production flow rate of a reaction system, using the liquid level and production flow rate control system of the reaction system described in the first aspect, the method comprising:

[0015] When the output of the liquid level controller of the liquid level controller reaction system is equal to the demand of the downstream user, the output value of the liquid level controller of the reaction system is a, the split point of the liquid level controller of the reaction system is x, and the output of the first calculation module is a / x, the output value of the production pipeline flow controller is b, the split point of the production pipeline flow controller is y, and the output of the second calculation module is b / y, at this time a / x=b / y, and the opening of the direct production regulating valve is controlled to be the opening value obtained based on the output value of the liquid level controller of the reaction system or the output value of the production pipeline flow controller;

[0016] When the output of the liquid level controller of the reaction system is less than the demand of the downstream user, at this time a / x<b / y, the low selection module outputs a first low selection result, and the fourth calculation module outputs an adjustment based on the output of the low selection result, so that the cache production regulating valve is opened wide, so that the sum of the production flow of the reaction system and the production flow of the cache system is equal to the demand of the downstream user;

[0017] When the output of the liquid level controller of the reaction system is greater than the demand of the downstream user, at this time a / x>b / y, the low selection module outputs the second low selection result, and the output of the third calculation module is adjusted based on the output of the low selection module to open the production buffer regulating valve so that the production flow of the reaction system is the sum of the flow produced to the cache device and the demand of the downstream user.

[0018] In a possible implementation, the output of the third calculation module is adjusted based on the output of the low selection module, and the calculation formula is:

[0019] f=(a-xe) / (1-x)

[0020] In the formula, f is the output value of the third calculation module, a is the output value of the reaction system liquid level controller, x is the split point of the reaction system liquid level controller, e is the output value of the low selection module, e=min{a / x,b / y}, that is, e takes the smaller value of a / x and b / y.

[0021] In a possible implementation, the output of the fourth calculation module is adjusted based on the output of the low selection module, and the calculation formula is:

[0022] g = (b-ye) / (1-y)

[0023] Wherein, g is the output value of the fourth calculation module, b is the output value of the production pipeline flow controller, y is the split point of the production pipeline flow controller, e is the output value of the low selection module, e = min{a / x, b / y}, that is, e takes the smaller value of a / x and b / y.

[0024] In a possible implementation, the calculation formula for the split point x of the reaction system liquid level controller is:

[0025] x=q1 / (q1+q2)

[0026] Wherein, x is the split point of the liquid level controller of the reaction system, q1 is the full-open flow rate of the direct production regulating valve, and q2 is the full-open flow rate of the production buffer regulating valve;

[0027] The calculation formula of the split point y of the production line flow controller is:

[0028] y=q1 / (q1+q3)

[0029] Wherein, y is the split point of the production pipeline flow controller, q1 is the full-open flow of the direct production regulating valve, and q3 is the full-open flow of the buffer production regulating valve.

[0030] In a third aspect, the present application provides an electronic device, comprising: at least one processor and a memory;

[0031] The memory stores computer-executable instructions;

[0032] The at least one processor executes the computer-executable instructions stored in the memory, so that the at least one processor executes the liquid level and extraction flow control method of the reaction system as described in the second aspect above.

[0033] In a fourth aspect, the present application provides a computer-readable storage medium, wherein the computer-readable storage medium stores a computer-executed instruction. When a processor executes the computer-executed instruction, the liquid level and extraction flow control method of the reaction system described in the second aspect above is implemented.

[0034] The present application provides a liquid level and production flow control system and control method for a reaction system, wherein the method controls the liquid level and production flow of the reaction system by utilizing the split-range control of the production pipeline flow controller and the reaction system liquid level controller and the low selection module, the first calculation module, the second calculation module, the third calculation module and the fourth calculation module to perform flow decoupling when the demand of downstream users changes, so that the production buffer regulating valve and the cache production regulating valve do not have a state where the valves are open at the same time, and can quickly respond to changes in the production of the reaction system and the demand of downstream users, adjust the production flow of the reaction system, reduce energy consumption, and thus save costs. BRIEF DESCRIPTION OF THE DRAWINGS

[0035] In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, a brief introduction will be given below to the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present application. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative labor.

[0036] Figure 1 A schematic diagram of the connection structure of the existing reaction system liquid level and extraction flow control method provided in the embodiment of the present application;

[0037] Figure 2 A schematic diagram of the connection structure of the reaction system liquid level and extraction flow control system provided in the embodiment of the present application;

[0038] Figure 3A schematic flow chart of a method for controlling the liquid level and extraction flow rate of a reaction system provided in an embodiment of the present application;

[0039] Figure 4 A schematic diagram of the hardware structure of an electronic device provided in an embodiment of the present application. DETAILED DESCRIPTION

[0040] In order to make the purpose, technical solution and advantages of the embodiments of the present application clearer, the technical solution in the embodiments of the present application will be clearly and completely described below in conjunction with the drawings in the embodiments of the present application. Obviously, the described embodiments are part of the embodiments of the present application, not all of the embodiments. Based on the embodiments in the present application, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of this application.

[0041] Figure 1 A schematic diagram of the connection structure of the existing reaction system liquid level and extraction flow control method provided in an embodiment of the present application.

[0042] At present, the existing technology adopts a control scheme that combines the reaction system liquid level control loop with the production pipeline flow control loop, such as Figure 1 As shown, it includes the reaction system liquid level controller LIC1, the production pipeline flow controller FIC1, the regulating valve V1 for the reaction system to directly produce to the downstream user, the regulating valve V2 between the reaction system and the cache system, and the regulating valve V3 between the cache system and the downstream user. The liquid level controller controls the flow from the reaction system to the cache system to stabilize the liquid level by adjusting the opening of V2, and the flow controller ensures that the flow from the cache system to the downstream user meets the demand by adjusting the opening of V3. Figure 1 In the production operation process shown, when materials in the reaction system are extracted to the cache system, the materials in the cache system need to be extracted to the downstream users. This is equivalent to the materials extracted from the reaction / distillation system being first cooled and then heated before being extracted to the downstream users, resulting in energy waste and increased operating costs.

[0043] In order to solve the above technical problems, the embodiments of the present application provide the following technical concepts for solving the problems: by introducing a step-by-step control and a flow decoupling calculation module, when the demand of downstream users is large, the production of the reaction / distillation system and the production of the cache system can be delivered to the downstream users together; when the demand of downstream users is small, the materials in the reaction / distillation system can be produced to the downstream users and the cache system respectively, so as to reduce the usage of cooling medium and heating medium, thereby achieving the purpose of reducing the usage of cold and hot media on the basis of liquid level control and flow control, and reducing system energy consumption and operating costs.

[0044] Figure 2A schematic diagram of the connection structure of the reaction system liquid level and production flow control system provided in an embodiment of the present application.

[0045] like Figure 2 As shown, the embodiment of the present application provides a reaction system liquid level and extraction flow control system, such as Figure 2 As shown, the system includes: a reaction system liquid level controller LIC2, a production pipeline flow controller FIC2, a low selection module, a first calculation module Y1, a second calculation module Y2, a third calculation module Y3, a fourth calculation module Y4, a direct production regulating valve V4, a production buffer regulating valve V5 and a cache production regulating valve V6.

[0046] Among them, the reaction system liquid level controller LIC2 adopts the split-range control method to process the process input. The input end of the reaction system liquid level controller LIC2 is connected to the reaction system through the liquid level transmitter LT2. The reaction system liquid level controller LIC2 is used to monitor the liquid level of the material in the reaction system and control the flow rate extracted to the downstream system, wherein the downstream system includes the cache system and downstream users; the output end of the reaction system liquid level controller LIC2 is respectively connected to the first calculation module Y1 and the third calculation module Y3.

[0047] In this embodiment, the reaction system may be a device, container or equipment used in a chemical production process, such as a distillation system or a reactor.

[0048] In this embodiment, the liquid level transmitter LT2 is used to measure the liquid level height of the material in the reaction system, convert the liquid level information into an electrical signal and send it to the reaction system liquid level controller LIC2, so that the reaction system liquid level controller LIC2 adjusts the flow rate of the material extracted from the reaction system according to the electrical signal to monitor and control the liquid level. The cache system includes a cache container and a cooling device connected to the feed port of the cache container, a pump connected to the discharge port of the cache container, and a heating device connected to the pump. The extraction buffer regulating valve V5 is located between the cooling device and the reaction system, and the cache extraction regulating valve V6 is located between the heating device and the downstream user.

[0049] The production pipeline flow controller FIC2 adopts the split-range control method to process the process input. The input end of the production pipeline flow controller FIC2 is connected to the pipeline produced to the downstream user through the flow transmitter FT2. The production pipeline flow controller FIC2 is used to monitor and control the total flow produced to the downstream user. The output end of the production pipeline flow controller FIC2 is respectively connected to the second calculation module Y2 and the fourth calculation module Y4.

[0050] In this embodiment, the reaction system level controller LIC2 and the extraction pipeline flow controller FIC2 are both split-range controllers. Compared with the traditional split-range control, the split-range control can control the extraction buffer regulating valve V5 and the cache extraction regulating valve V6 to be fully closed when the demand of the downstream user is equal to the output of the reaction system level controller LIC2; when the demand of the downstream user is greater than the output of the reaction system level controller LIC2, the opening of the cache extraction regulating valve V6 is controlled to be larger, and the extraction buffer regulating valve V5 is controlled to be fully closed; when the demand of the downstream user is less than the output of the reaction system level controller LIC2, the opening of the extraction buffer regulating valve V5 is controlled to be larger, and the cache extraction regulating valve V6 is controlled to be fully closed. No matter when, there is no state where the extraction buffer regulating valve V5 and the cache extraction regulating valve V6 are opened at the same time, which can respond quickly when the reaction system extraction and the downstream user demand change, avoiding that when the reaction system material is extracted, part of the material enters the cache system through the cooling device, while the material in the cache system is heated by the heating device and enters the downstream user, which is more energy-saving and environmentally friendly.

[0051] In an optional embodiment of the present application, the reaction system liquid level controller LIC2 is positive acting, and the extraction pipeline flow controller FIC2 is negative acting.

[0052] In this embodiment, when the liquid level of the material in the reaction system becomes high, the material extraction operation can be performed by controlling the opening of the direct extraction regulating valve V4 and the extraction buffer regulating valve V5 to increase, so that the liquid level of the material in the reaction system is stabilized within a preset liquid level range, so the reaction system liquid level controller LIC2 is required to be positive. When the opening of the direct extraction regulating valve V4 and the buffer extraction regulating valve V6 increases, the flow rate will become higher. At this time, the flow rate can be controlled by controlling the opening of the direct extraction regulating valve V4 and the buffer extraction regulating valve V6 to decrease, so the extraction pipeline flow controller FIC2 is negative.

[0053] Two ends of the low selection module are respectively connected to the first calculation module Y1 and the second calculation module Y2 for performing low selection on the first calculation module Y1 and the second calculation module Y2 to obtain the minimum value output by the first calculation module Y1 and the second calculation module Y2.

[0054] In this embodiment, the calculation formula used by the low selection module is e=min{a / x,b / y}, where e is the output value of the low selection module, which is the minimum value output by the first calculation module Y1 and the second calculation module Y2.

[0055] The two ends of the direct production regulating valve V4 are connected to the reaction system and the downstream user respectively, the two ends of the production buffer regulating valve V5 are connected to the reaction system and the cache system respectively, and the two ends of the cache production regulating valve V6 are connected to the cache system and the downstream user respectively.

[0056] In this embodiment, the direct production regulating valve V4, the production buffer regulating valve V5 and the buffer production regulating valve V6 can be connected by pipelines to allow materials to flow through.

[0057] In an optional embodiment of the present application, the direct production regulating valve V4, the production buffer regulating valve V5 and the cache production regulating valve V6 are all air-open valves.

[0058] In this embodiment, when the control instruction received by the air-open valve is to increase the opening, the air-open valve will increase the air supply to push the valve open. To facilitate PID control, the direct production regulating valve V4, the production buffer regulating valve V5 and the cache production regulating valve V6 will automatically close when there is no air source to avoid material loss.

[0059] It should be noted that the direct production regulating valve V4, the production buffer regulating valve V5 and the buffer production regulating valve V6 can also be other valves that can receive control instructions, such as air-off valves. In this regard, the embodiment of the present application does not make any special restrictions here.

[0060] In an optional embodiment of the present application, the low selection module, the first calculation module Y1, the second calculation module Y2, the third calculation module Y3, and the fourth calculation module Y4 are integrated into a flow decoupling calculation device.

[0061] In this embodiment, the flow decoupling calculation device can be: a device, processor or controller that can input the selection result of the low selection module into the fourth calculation module Y4 and the third calculation module Y3 in a flow decoupling manner to perform split-range control calculations to obtain calculation results, and control the opening of the direct production regulating valve V4, the production buffer regulating valve V5 and the cache production regulating valve V6 to change according to the calculation results. For example, the flow decoupling calculation device can be a server, a controller or a chip.

[0062] In summary, an embodiment of the present application provides a liquid level and production flow control system for a reaction system. By using a production pipeline flow controller FIC2 and a reaction system liquid level controller LIC2 that introduce a split-range control, and using a low-selection module to obtain the minimum value of the outputs of the first calculation module Y1 and the second calculation module Y2, and based on the minimum value, the opening of the direct production regulating valve V4, the production buffer regulating valve V5 and the cache production regulating valve V6 are controlled, so that there is no state in which the production buffer regulating valve V5 and the cache production regulating valve V6 are opened at the same time. When the production volume of the reaction system and the demand of downstream users change, it can respond quickly, adjust the production flow of the reaction / distillation system and the cache system, reduce energy consumption and thus save costs.

[0063] Figure 3 The present invention provides a flow chart of a method for controlling the liquid level and extraction flow rate of a reaction system in accordance with an embodiment of the present application. The execution subject of this embodiment may be a server, a processor or a controller, or may be other computer-related equipment, and there is no particular limitation on this embodiment.

[0064] like Figure 3 As shown, the liquid level and extraction flow control method of the reaction system uses the following Figure 2 The liquid level and extraction flow control system of the reaction system in the embodiment shown comprises the following steps:

[0065] S301: When the output of the liquid level controller reaction system liquid level controller LIC2 is equal to the demand of the downstream user, the output value of the reaction system liquid level controller LIC2 is a, and the split point of the reaction system liquid level controller LIC2 is x, then the output of the first calculation module Y1 is a / x, the output value of the production pipeline flow controller FIC2 is b, and the split point of the production pipeline flow controller FIC2 is y, then the output of the second calculation module Y2 is b / y, at this time a / x=b / y, and the opening of the direct production regulating valve V4 is controlled to be the opening value obtained based on the output value of the reaction system liquid level controller LIC2 or the output value of the production pipeline flow controller FIC2.

[0066] In an optional embodiment of the present application, the calculation formula of the split point x of the reaction system liquid level controller LIC2 is:

[0067] x=q1 / (q1+q2)

[0068] Wherein, x is the split point of the reaction system liquid level controller LIC2, q1 is the full-open flow of the direct production regulating valve V4, and q2 is the full-open flow of the production buffer regulating valve V5.

[0069] In an optional embodiment of the present application, the calculation formula for the split point y of the production line flow controller FIC2 is:

[0070] y=q1 / (q1+q3)

[0071] Wherein, y is the split point of the production pipeline flow controller FIC2, q1 is the full-open flow of the direct production regulating valve V4, and q3 is the full-open flow of the buffer production regulating valve V6.

[0072] In this embodiment, the output of the reaction system liquid level controller LIC2 is equal to the demand of the downstream user, indicating that the demand of the downstream user is the same as the production flow of the reaction system. At this time, the output c=a / x of the first calculation module Y1 is the same as the output d=b / y of the second calculation module Y2. After the low selection module is selected, the input of V1 is e=a / x=b / y. At the same time, the output value of the low selection module is sent to the third calculation module Y3 and the fourth calculation module Y4. At this time, the output value f=0 of the third calculation module Y3 and the output value g=0 of the fourth calculation module Y4. Correspondingly, the inputs of the production buffer regulating valve V5 and the cache production regulating valve V6 are controlled to be 0. At this time, the production buffer regulating valve V5 and the cache production regulating valve V6 are in a fully closed state, and the material flows through the open direct production regulating valve V4 and then flows to the downstream user. Therefore, the material does not need to pass through the cooling device and the heating device, avoiding energy waste.

[0073] S302: When the output of the reaction system liquid level controller LIC2 is less than the demand of the downstream user, at this time a / x<b / y, the low selection module outputs the first low selection result, and the output of the fourth calculation module Y4 is adjusted based on the output of the low selection result to open the cache production regulating valve V6 so that the sum of the production flow of the reaction system and the production flow of the cache system is equal to the demand of the downstream user.

[0074] In an optional embodiment of the present application, the output of the fourth calculation module is adjusted based on the output of the low selection module, and the calculation formula is:

[0075] g = (b-ye) / (1-y)

[0076] In the formula, g is the output value of the fourth calculation module, b is the output value of the production pipeline flow controller FIC2, y is the split point of the production pipeline flow controller FIC2, e is the output value of the low selection module, e = min{a / x, b / y}, that is, e takes the smaller value of a / x and b / y.

[0077] In this embodiment, when the output of the reaction system liquid level controller LIC2 is less than the demand of the downstream user, it means that the flow rate produced by the reaction system to maintain the liquid level is lower than the demand of the downstream user. At this time, the output of the first calculation module Y1 c=a / x is less than the output of the second calculation module Y2 d=b / y. After the low selection module is selected, the input of the direct production regulating valve V4 between the reaction system and the downstream user is e=a / x. It should be noted that the selection result of the low selection module will affect the opening of the direct production regulating valve V4 and the buffer production regulating valve V6. The specific process of affecting the opening is as follows:

[0078] When the output b of the production pipeline flow controller FIC2 is in the range of (y, 1), the selection result of the low selection module is input into the fourth calculation module Y4, and the calculation result of the fourth calculation module Y4 is g = (b-ay / x) / (1-y). Compared with the traditional split-range calculation method, the valve opening of the cache production regulating valve V6 is larger at this time to ensure that the total flow entering the downstream users meets the demand. Since the output of the low selection module is e = a / x, the split-range control output of the reaction system liquid level controller LIC2 is not affected at this time, and the value of the low selection module output is sent to the third calculation module Y3, and the calculation result obtained is f = (a-xa / x) / (1-x) = 0, that is, the input of the production buffer regulating valve V5 is 0, and the production buffer regulating valve V5 is in a fully closed state at this time.

[0079] In this embodiment, in order to better illustrate the beneficial effects of the liquid level and extraction flow control method of the reaction system provided in the present application, a traditional split-range control process is also used for illustration, and the process is as follows:

[0080] When the output b of the production pipeline flow controller FIC2 is in the range of (y, 1), if traditional split-range control is used instead of the split-range control in the embodiment of the present application proposed by the inventor, the input of the direct production regulating valve V4 is e'=b / y, and the input of the cache production regulating valve V6 is g'=(by) / (1-y). At present, the input of the direct production regulating valve V4 is e=a / x. If the input of the cache production regulating valve V6 still maintains g'=(by) / (1-y), the total flow entering the downstream users will be too small, affecting normal production.

[0081] S303: When the output of the reaction system liquid level controller LIC2 is greater than the demand of the downstream user, at this time a / x>b / y, the low selection module outputs the second low selection result, and the output of the third calculation module Y3 is adjusted based on the output of the low selection module to open the production buffer regulating valve V5 so that the production flow of the reaction system is the sum of the flow produced to the cache device and the demand of the downstream user.

[0082] In an optional embodiment of the present application, the output of the third calculation module Y3 is adjusted based on the output of the low selection module, and the calculation formula is:

[0083] f=(a-xe) / (1-x)

[0084] Wherein, f is the output value of the third calculation module, a is the output value of the reaction system liquid level controller LIC2, x is the split point of the reaction system liquid level controller LIC2, e is the output value of the low selection module, e=min{a / x,b / y}, that is, e takes the smaller value of a / x and b / y.

[0085] In this embodiment, when the output of the reaction system liquid level controller LIC2 is greater than the demand of the downstream user, it means that the demand flow of the downstream user is small, and the flow produced by the reaction system to maintain the liquid level is higher than the demand of the downstream user. At this time, the output c=a / x of the first calculation module Y1 is greater than the output d=b / y of the second calculation module Y2. After the low selection module is selected, the input of the direct production regulating valve V4 valve directly produced by the reaction system to the downstream user is e=b / y. It should be noted that the selection result of the low selection module will affect the opening of the direct production regulating valve V4 and the production buffer regulating valve V5. When the output a of the reaction system liquid level controller LIC2 is within the range of (x, 1), it will be used. In a flow decoupling manner, the output result of the low-selection module is input into the third calculation module Y3. The calculation result of the third calculation module Y3 is f=(a-xb / y) / (1-x). Compared with the traditional split-range calculation method, in this embodiment, the valve opening of the extraction buffer regulating valve V5 is larger to ensure that the extraction flow of the reaction system meets the requirements. Since the output of the low-selection module is e=b / y, the split-range control output of the flow is not affected at this time. The result of the low-selection module output is input into the fourth calculation module Y4, and the calculation result g=(b-yb / y) / (1-y)=0 is obtained, that is, the input of the cache extraction regulating valve V6 is 0, and the cache extraction regulating valve V6 is in a fully closed state at this time.

[0086] Similarly, in this embodiment, in order to better illustrate the beneficial effects of the liquid level and extraction flow control method of the reaction system provided in the present application, a traditional split-range control process is also used for illustration, and the process is as follows:

[0087] When the output a of the reaction system liquid level controller LIC2 is within the range of (x, 1), if traditional split-range control is used instead of the split-range control in the embodiment of the present application proposed by the inventor, the input of the direct extraction regulating valve V4 is e'=a / x, and the input of the extraction buffer regulating valve V5 is f'=(ax) / (1-x). However, the current input of the direct extraction regulating valve V4 is e=b / y, and the actual flow rate of the direct extraction regulating valve V4 is relatively low. If the input of the direct extraction regulating valve V4 is still maintained at f'=(ax) / (1-x), the total extraction flow of the reaction / distillation system will be relatively small, which will not meet the demand for the extraction flow of the material to maintain the liquid level, resulting in a continuous increase in the liquid level of the reaction system and a high liquid level risk.

[0088] In order to make the liquid level and extraction flow control method of the reaction system provided in the embodiment of the present application easier to understand and implement, in this embodiment, the reaction system is taken as an example of the extraction of the distillation system of a device in the production process, and the control method provided in the above embodiment is further explained:

[0089] Assuming that the full-open flow of the direct production regulating valve V4 is 50t / h, the full-open flow of the production buffer regulating valve V5 is 50t / h, and the full-open flow of the cache production regulating valve V6 is 100t / h, after calculation by the processor, it can be known that the split point x=50% of the reaction system liquid level controller LIC2, and the split point y=33.3% of the production pipeline flow controller FIC2.

[0090] When the demand of the downstream users is the same as the production flow of the distillation system, the output of the reaction system liquid level controller LIC2 is a=20%, and the output of the first calculation module Y1 is c=a / x=20% / 50%=40%; at this time, the output of the production pipeline flow controller FIC2 is b=13.3%, and the output of the second calculation module Y2 is d=b / y=13.3% / 33.3%=40%. After selection by the low selection module, e=b=d. At this time, the input of V1 is 40%, and the output e of the low selection module is simultaneously input to the third calculation module Y3 and the fourth calculation module Y4, and f=g=0 is obtained, that is, the inputs of the production buffer regulating valve V5 and the cache production regulating valve V6 are both 0. At this time, the production buffer regulating valve V5 and the cache production regulating valve V6 are in a fully closed state, and the material is directly produced to the downstream users through the direct production regulating valve V4.

[0091] When the demand flow of the downstream users is greater than the production flow of the distillation system to maintain the liquid level, if the output of the reaction system liquid level controller LIC2 is a=40%, and the output of the production pipeline flow controller FIC2 is b=33.3%, since a is less than the split point x, the output of the first calculation module Y1 is c=a / x=40% / 50%=80%, and the output of the second calculation module Y2 is d=33.3% / 33.3%=100%. After selection by the low selection module, e=min{c=80%, d=100%}=80%. At this time, the input of the direct production regulating valve V4 is 80%, and the output e of the low selection module is simultaneously input to the third calculation module Y3 and the fourth calculation module Y4. Then the third calculation module Y3=(40%-80%*50%) / (1-50%)=0%, and the fourth calculation module Y4=(33.3%-33.3%*80%) / (1-33.3%)=10%. At this time, the input of the production buffer regulating valve V5 is 0%, the input of the cache production regulating valve V6 is 10%, and the opening of the direct production regulating valve V4 and the cache production regulating valve V6 can ensure that the demand of downstream users is met on the basis of maintaining the stability of the distillation system liquid level. The production buffer regulating valve V5 is in a fully closed state.

[0092] When the demand of downstream users is less than the production flow of the distillation system to maintain the liquid level, the output of the reaction system liquid level controller LIC2 is a=60%. At this time, a is greater than the split point x, and the output of the first calculation module Y1 is c=a / x=60% / 50%. Since the maximum output of the first calculation module Y1 is 100%, the output of the first calculation module Y1 is c=100%. If the output of the production pipeline flow controller FIC2 is 20% at this time, the output of the second calculation module Y2 is d=b / y=20% / 33.3%=60%. After the low selection module is selected, e=min{100%, 60%}, and the production adjustment is directly performed at this time. The input of valve V4 is 60%, and the output e of the low selection module is input to the third calculation module Y3 and the fourth calculation module Y4 at the same time. Then the third calculation module Y3 = (60% - 50% * 60%) / (1-50%) = 60%, the fourth calculation module Y4 = (20% - 33.3% * 60%) / (1-33.3%) = 0%. At this time, the input of the production buffer regulating valve V5 is 60%, and the input of the cache production regulating valve V6 is 0%. The opening of the direct production regulating valve V4 and the production buffer regulating valve V5 ensures that the distillation system production maintains the stability of the liquid level on the basis of meeting the demand of downstream users, and the cache production regulating valve V6 is in a fully closed state.

[0093] In summary, the method for controlling the liquid level and production flow of the reaction system provided in the embodiment of the present application controls the liquid level and production flow of the reaction system by utilizing the split-range control of the production pipeline flow controller FIC2 and the reaction system liquid level controller LIC2 and the low selection module, the first calculation module Y1, the second calculation module Y2, the third calculation module Y3 and the fourth calculation module Y4 to perform flow decoupling when the demand of downstream users changes, so that the production buffer regulating valve V5 and the cache production regulating valve V6 are not in a state of being opened at the same time, and can respond quickly when the production of the reaction system and the demand of downstream users change, adjust the production flow of the reaction system, reduce energy consumption, and thus save costs.

[0094] At the same time, it can avoid the situation where part of the material in the reaction system is cooled and enters the cache system when the material is taken out, while the material in the cache system is heated before entering the downstream users, thereby reducing the use of cold and hot media, thereby reducing energy waste in the material production process and achieving the purpose of reducing system energy consumption and operating costs.

[0095] Figure 4 A schematic diagram of the hardware structure of an electronic device provided in an embodiment of the present application is shown in FIG. Figure 4 As shown, the device includes: at least one processor 401 and a memory 402 .

[0096] The memory 402 is used to store computer-executable instructions.

[0097] The processor 401 is used to execute the computer-executable instructions stored in the memory 402 to implement the various steps involved in the above method embodiment. For details, please refer to the relevant description in the above method embodiment.

[0098] Optionally, the memory 402 may be independent or integrated with the processor 401 .

[0099] When the memory 402 is independently provided, the electronic device further includes a bus 403 for connecting the memory 402 and the processor 401 .

[0100] The embodiment of the present application also provides a computer-readable storage medium, in which computer-executable instructions are stored. When a processor executes the computer-executable instructions, the liquid level and extraction flow control method of the reaction system as described above is implemented.

[0101] An embodiment of the present application also provides a computer program product, including a computer program, which, when executed by a processor, implements the above-mentioned method for controlling the liquid level and production flow rate of the reaction system.

[0102] In the several embodiments provided in the present application, it should be understood that the disclosed devices and methods can be implemented in other ways. For example, the device embodiments described above are only schematic. For example, the division of the above modules is only a logical function division. There may be other division methods in actual implementation, such as multiple modules can be combined or integrated into another system, or some features can be ignored or not executed. Another point is that the mutual coupling or direct coupling or communication connection shown or discussed can be through some interfaces, indirect coupling or communication connection of devices or modules, which can be electrical, mechanical or other forms.

[0103] The modules described above as separate components may or may not be physically separated, and the components shown as modules may or may not be physical units, that is, they may be located in one place or distributed on multiple network units. Some or all of the modules may be selected according to actual needs to implement the solution of this embodiment.

[0104] In addition, each functional module in each embodiment of the present invention may be integrated into one processing unit, each module may exist physically separately, or two or more modules may be integrated into one unit. The unit composed of the above modules may be implemented in the form of hardware or in the form of hardware plus software functional units.

[0105] The above-mentioned integrated module implemented in the form of a software function module can be stored in a computer-readable storage medium. The above-mentioned software function module is stored in a storage medium, including a number of instructions for causing a computer device (which can be a personal computer, a server, or a network device, etc.) or a processor to perform some steps of the method of each embodiment of the present application.

[0106] It should be understood that the processor may be a central processing unit (CPU), or other general-purpose processors, digital signal processors (DSP), application-specific integrated circuits (ASIC), etc. A general-purpose processor may be a microprocessor or any conventional processor. The steps of the method disclosed in the invention may be directly implemented as being executed by a hardware processor, or may be implemented by a combination of hardware and software modules in the processor.

[0107] The memory may include a high-speed RAM memory, and may also include a non-volatile storage NVM, such as at least one disk memory, and may also be a USB flash drive, a mobile hard disk, a read-only memory, a magnetic disk or an optical disk, etc.

[0108] The bus may be an Industry Standard Architecture (ISA) bus, a Peripheral Component Interconnect (PCI) bus, or an Extended Industry Standard Architecture (EISA) bus, etc. The bus may be divided into an address bus, a data bus, a control bus, etc. For ease of representation, the bus in the drawings of the present application is not limited to only one bus or one type of bus.

[0109] The above storage medium can be implemented by any type of volatile or non-volatile storage device or a combination thereof, such as static random access memory (SRAM), electrically erasable programmable read-only memory (EEPROM), erasable programmable read-only memory (EPROM), programmable read-only memory (PROM), read-only memory (ROM), magnetic memory, flash memory, magnetic disk or optical disk. The storage medium can be any available medium that can be accessed by a general or special purpose computer.

[0110] An exemplary storage medium is coupled to a processor so that the processor can read information from the storage medium and write information to the storage medium. Of course, the storage medium can also be a component of the processor. The processor and the storage medium can be located in an application specific integrated circuit (ASIC). Of course, the processor and the storage medium can also exist as discrete components in an electronic device or a main control device.

[0111] Those skilled in the art can understand that all or part of the steps of implementing the above-mentioned method embodiments can be completed by hardware related to program instructions. The aforementioned program can be stored in a computer-readable storage medium. When the program is executed, the steps of the above-mentioned method embodiments are executed; and the aforementioned storage medium includes: ROM, RAM, disk or optical disk and other media that can store program codes.

[0112] The present invention is intended to illustrate the technical solution of the present application rather than to limit it. Although the present application has been described in detail with reference to the aforementioned embodiments, a person skilled in the art should understand that the technical solutions described in the aforementioned embodiments may still be modified, or some or all of the technical features may be replaced by equivalents. However, these modifications or replacements do not deviate the essence of the corresponding technical solution from the scope of the technical solutions of the embodiments of the present application.

Claims

1. A liquid level and extraction flow control system for a reaction system, characterized in that: include: Reaction system liquid level controller, production pipeline flow controller, low selection module, first calculation module, second calculation module, third calculation module, fourth calculation module, direct production regulating valve, production buffer regulating valve and cache production regulating valve; The reaction system liquid level controller adopts a split-range control method to process process input, the input end of the reaction system liquid level controller is connected to the reaction system through a liquid level transmitter, and the reaction system liquid level controller is used to monitor the liquid level of the material in the reaction system and control the flow rate of the material to the downstream system, wherein the downstream system includes a cache system and a downstream user; the output end of the reaction system liquid level controller is respectively connected to the first calculation module and the third calculation module; The production pipeline flow controller adopts a split-range control method to process process input, the input end of the production pipeline flow controller is connected to the pipeline produced to the downstream user through a flow transmitter, the production pipeline flow controller is used to monitor and control the total flow produced to the downstream user, and the output end of the production pipeline flow controller is respectively connected to the second calculation module and the fourth calculation module; The two ends of the low selection module are respectively connected to the first calculation module and the second calculation module, and are used to perform low selection on the first calculation module and the second calculation module to obtain the minimum value output by the first calculation module and the second calculation module; The two ends of the direct production regulating valve are connected to the reaction system and the downstream user respectively, the two ends of the production buffer regulating valve are connected to the reaction system and the cache system respectively, and the two ends of the cache production regulating valve are connected to the cache system and the downstream user respectively.

2. The system according to claim 1, characterized in that The direct production regulating valve, the production buffer regulating valve and the cache production regulating valve are all air-opened valves.

3. The system according to claim 1, characterized in that The reaction system liquid level controller is positive acting, and the production line flow controller is negative acting.

4. The system according to any one of claims 1 to 3, characterized in that The low selection module, the first calculation module, the second calculation module, the third calculation module and the fourth calculation module are integrated into a flow decoupling calculation device.

5. A method for controlling the liquid level and extraction flow rate of a reaction system, using the liquid level and extraction flow rate control system of the reaction system as claimed in claim 1, characterized in that: The method comprises: When the output of the reaction system liquid level controller is equal to the demand of the downstream user, the output value of the reaction system liquid level controller is a, the split point of the reaction system liquid level controller is x, and the output of the first calculation module is a / x, the output value of the production pipeline flow controller is b, the split point of the production pipeline flow controller is y, and the output of the second calculation module is b / y, at this time a / x=b / y, and the opening of the direct production regulating valve is controlled to be the opening value obtained based on the output value of the reaction system liquid level controller or the output value of the production pipeline flow controller; When the output of the liquid level controller of the reaction system is less than the demand of the downstream user, at this time a / x<b / y, the low selection module outputs a first low selection result, and the fourth calculation module outputs an adjustment based on the output of the low selection result, so that the cache production regulating valve is opened wide, so that the sum of the production flow of the reaction system and the production flow of the cache system is equal to the demand of the downstream user; When the output of the liquid level controller of the reaction system is greater than the demand of the downstream user, at this time a / x>b / y, the low selection module outputs the second low selection result, and the output of the third calculation module is adjusted based on the output of the low selection module to open the production buffer regulating valve so that the production flow of the reaction system is the sum of the flow produced to the cache device and the demand of the downstream user.

6. The method according to claim 5, characterized in that The output of the third calculation module is adjusted based on the output of the low selection module, and the calculation formula is: f=(a-xe) / (1-x) In the formula, f is the output value of the third calculation module, a is the output value of the reaction system liquid level controller, x is the split point of the reaction system liquid level controller, e is the output value of the low selection module, e=min{a / x,b / y}, that is, e takes the smaller value of a / x and b / y.

7. The method according to claim 5, characterized in that The output of the fourth calculation module is adjusted based on the output of the low selection module, and the calculation formula is: g = (b-ye) / (1-y) Wherein, g is the output value of the fourth calculation module, b is the output value of the production pipeline flow controller, y is the split point of the production pipeline flow controller, e is the output value of the low selection module, e = min{a / x, b / y}, that is, e takes the smaller value of a / x and b / y.

8. The method according to claim 5, characterized in that The calculation formula of the split point x of the reaction system liquid level controller is: x=q1 / (q1+q2) Wherein, x is the split point of the liquid level controller of the reaction system, q1 is the full-open flow rate of the direct production regulating valve, and q2 is the full-open flow rate of the production buffer regulating valve; The calculation formula of the split point y of the production line flow controller is: y=q1 / (q1+q3) Wherein, y is the split point of the production pipeline flow controller, q1 is the full-open flow of the direct production regulating valve, and q3 is the full-open flow of the buffer production regulating valve.

9. An electronic device, characterized in that: include: at least one processor and memory; The memory stores computer-executable instructions; The at least one processor executes the computer-executable instructions stored in the memory, so that the at least one processor executes the liquid level and extraction flow control method of the reaction system as described in any one of claims 5 to 8.

10. A computer-readable storage medium, characterized in that: The computer-readable storage medium stores computer-executable instructions. When the processor executes the computer-executable instructions, the liquid level and extraction flow control method of the reaction system as described in any one of claims 5 to 8 is implemented.

Images