A liquid level and production flow control system and control method for a reaction system

Abstract

The application provides a liquid level and production flow control system and control method of a reaction system, and belongs to the technical field of chemical production. The system comprises: a reaction system liquid level controller which adopts a split-range control method to process process input; the output end of the reaction system liquid level controller is connected with a first calculation module and a third calculation module; a production pipeline flow controller which adopts a split-range control method to process process input, the output end of the production pipeline flow controller is connected with a second calculation module and a fourth calculation module; two ends of a low selection module are connected with the first calculation module and the second calculation module; two ends of a direct production regulating valve are in communication with a reaction system and a downstream user, two ends of a production buffer regulating valve are in communication with the reaction system and a buffer system, and two ends of a buffer production regulating valve are in communication with the buffer system and the downstream user. The application can reduce energy consumption and save cost.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of chemical production, in particular to a liquid level and production flow control system and control method of a reaction system. BACKGROUND

[0002] In a chemical device, in order to maintain the liquid level of the reaction system, the material needs to be taken out to the buffer system for buffering, in order to avoid the situation of over-temperature or over-pressure of the buffer system, the material needs to be cooled before being sent to the buffer system, and when the downstream user needs it, the material in the buffer system is taken out to the downstream user through the heat exchanger for heating, so as to maintain normal production, and the demand of the downstream user for the material is more or less, therefore, in the process of transporting the material to the downstream user, it is more necessary to control the liquid level and the production flow of the reaction system to avoid over-temperature or over-pressure.

[0003] At present, in order to meet the production process requirements, the control method combining the liquid level control loop of the rectification system and the production pipeline flow control loop is often used, but in actual operation, when the material in the reaction system is taken out to the buffer system, the material in the buffer system needs to be taken out to the downstream user, which is equivalent to that the material taken out from the reaction system is first cooled and then heated before being taken out to the downstream user, resulting in the problems of energy waste and increased operation cost.

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

[0005] The present application provides a liquid level and production flow control system and control method of a reaction system, by introducing a split-range control and flow decoupling calculation module, the use amount of cold and hot medium can be reduced on the basis of liquid level control and flow control, and the purpose of reducing system energy consumption and operation cost is achieved.

[0006] In a first aspect, the present application provides a liquid level and production flow control system of a reaction system, comprising: 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 buffer 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, the reaction system liquid level controller is used for monitoring the liquid level of the material in the reaction system and controlling the flow taken out to the downstream system, wherein the downstream system comprises a buffer system and a downstream user; the output end of the reaction system liquid level controller is connected with the first calculation module and the third calculation module respectively;

[0008] The production pipeline flow controller adopts a split-range control method to process process input, an input end of the production pipeline flow controller is connected with a pipeline for production to a downstream user through a flow transmitter, the production pipeline flow controller is used for monitoring and controlling total flow of production to the downstream user, and output ends of the production pipeline flow controller are connected with the second calculation module and the fourth calculation module respectively.

[0009] The low selection module is connected with the first calculation module and the second calculation module respectively, and is used for low selection of the first calculation module and the second calculation module to obtain a minimum value output by the first calculation module and the second calculation module.

[0010] The direct production regulating valve is connected with the reaction system and the downstream user respectively, the production buffer regulating valve is connected with the reaction system and the buffer system respectively, and the buffer production regulating valve is connected with the buffer system and the downstream user respectively.

[0011] In a possible implementation manner, the direct production regulating valve, the production buffer regulating valve and the buffer production regulating valve are all gas opening valves.

[0012] In a possible implementation manner, the reaction system liquid level controller is positive action, and the production pipeline flow controller is reverse action.

[0013] In a possible implementation manner, 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 possible implementation manner, 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.

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

[0016] When the output of the reaction system liquid level controller is less than the demand of the downstream user, i.e. a / x

[0017] When the output of the reaction system liquid level controller is greater than the demand of the downstream user, i.e. a / x

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

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

[0020] wherein 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, and e = min{a / x, b / y}, i.e. e takes the smaller value of a / x and b / y.

[0021] In a possible implementation, the fourth calculation module outputs a value 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, and e is the output value of the low selection module, e = min{a / x, b / y}, i.e. e takes the smaller value of a / x and b / y.

[0024] In a possible implementation, the calculation formula of 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 reaction system liquid level controller, q1 is the full opening flow of the direct production regulating valve, and q2 is the full opening flow of the production buffer regulating valve.

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

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

[0029] wherein y is a split point of the production line flow controller, q1 is a full open flow of the direct production control valve, and q3 is a full open flow of the buffer production control 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 production 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, which stores a computer-executable instruction, and when a processor executes the computer-executable instruction, the liquid level and production flow control method of the reaction system as described in the second aspect above is realized.

[0034] The present application provides a liquid level and production flow control system and control method of a reaction system, wherein the method controls the liquid level and production flow of the reaction system by using the split control and low selection module of the production line flow controller and the reaction system liquid level controller, the first calculation module, the second calculation module, the third calculation module and the fourth calculation module to decouple the flow when the demand of the downstream user changes, so that the production buffer control valve and the buffer production control valve do not exist in the state of simultaneous opening of the valve, and the reaction system can quickly respond to the change of the production and the demand of the downstream user, adjust the production flow of the reaction system, reduce the energy consumption, and save the cost. BRIEF DESCRIPTION OF DRAWINGS

[0035] In order to more clearly illustrate the technical solutions in the embodiments of the present application or the prior art, the drawings needed to be used in the embodiments or prior art description will be briefly introduced. Obviously, the drawings in the following description are some embodiments of the present application, and other drawings can be obtained by those skilled in the art without creative labor.

[0036] Figure 1 The connection structure diagram of the prior reaction system liquid level and production flow control method provided by the embodiments of the present application;

[0037] Figure 2 The connection structure diagram of the reaction system liquid level and production flow control system provided by the embodiments of the present application;

[0038] Figure 3A schematic flowchart illustrating the liquid level and outflow control method of the reaction system provided in this application embodiment;

[0039] Figure 4 This is a schematic diagram of the hardware structure of the electronic device provided in the embodiments of this application. Detailed Implementation

[0040] To make the objectives, technical solutions, and advantages of the embodiments of this application clearer, the technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this application, not all embodiments. Based on the embodiments of this application, all other embodiments obtained by those skilled in the art without creative effort 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 output flow control method provided in the embodiments of this application.

[0042] Currently, existing technologies employ a control scheme that combines the reaction system's liquid level control loop with the produced pipeline's flow control loop, such as... Figure 1 As shown, the system includes a reaction system level controller LIC1, a product pipeline flow controller FIC1, a regulating valve V1 directly supplying the product from the reaction system to the downstream user, a regulating valve V2 between the reaction system and the buffer system, and a regulating valve V3 between the buffer system and the downstream user. The level controller controls the flow rate from the reaction system to the buffer system by adjusting the opening of V2 to stabilize the level. The flow controller ensures that the flow rate from the buffer system to the downstream user meets the user's requirements by adjusting the opening of V3. Figure 1 During the production process shown, there is a situation where materials from the reaction system are drawn into the buffer system, and then the materials from the buffer system need to be drawn into the downstream user. This is equivalent to the materials drawn from the reaction / distillation system being cooled and then heated before being drawn into the downstream user, resulting in energy waste and increased operating costs.

[0043] To address the aforementioned technical problems, this application provides the following technical concept: by introducing a split-range control and flow decoupling calculation module, when downstream user demand is high, the output from the reaction / distillation system and the output from the buffer system can be jointly delivered to the downstream user; when downstream user demand is low, the materials in the reaction / distillation system can be separately extracted to the downstream user and the buffer system, thereby reducing the usage of cooling and heating media. This achieves the goal of reducing the usage of cold and hot media based on level control and flow control, thus reducing system energy consumption and operating costs.

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

[0045] As shown in Figure 2 , an embodiment of the present application provides a reaction system liquid level and production flow control system, as shown in Figure 2 , the system comprises 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 buffer production regulating valve V6.

[0046] The reaction system liquid level controller LIC2 adopts a split-range control method to process process input, the input end of the reaction system liquid level controller LIC2 is connected to the reaction system through a 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 of production to the downstream system, wherein the downstream system comprises a buffer system and a downstream user; the output end of the reaction system liquid level controller LIC2 is connected with the first calculation module Y1 and the third calculation module Y3 respectively.

[0047] In this embodiment, the reaction system can be a device, a container or equipment used in a chemical production process, for example, a rectification system or a reaction kettle.

[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 of the material produced from the reaction system according to the electrical signal, in order to monitor and control the liquid level. The buffer system comprises a buffer container, a cooling device communicating with the feed port of the buffer container, a pump communicating with the discharge port of the buffer container and a heating device communicating with the pump. The production buffer regulating valve V5 is located between the cooling device and the reaction system, and the buffer production regulating valve V6 is located between the heating device and the downstream user.

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

[0050] In the embodiment, the reaction system liquid level controller LIC2 and the production pipeline flow controller FIC2 are both split-range controllers. Compared with the traditional split-range control, when the downstream user demand is equal to the output of the reaction system liquid level controller LIC2, the split-range control can control the production buffer regulating valve V5 and the buffer production regulating valve V6 to be in the fully closed state; when the downstream user demand is greater than the output of the reaction system liquid level controller LIC2, the split-range control can control the opening of the buffer production regulating valve V6 to be larger, and control the production buffer regulating valve V5 to be in the fully closed state; when the downstream user demand is less than the output of the reaction system liquid level controller LIC2, the split-range control can control the opening of the production buffer regulating valve V5 to be larger, and control the buffer production regulating valve V6 to be in the fully closed state. At any time, there is no state in which the production buffer regulating valve V5 and the buffer production regulating valve V6 are opened at the same time, and the reaction system can quickly respond to changes in the production amount and the downstream user demand, thereby avoiding the situation in which part of the material in the reaction system enters the buffer system through the cooling device while the material in the buffer system enters the downstream user after being heated by the heating device, and achieving energy saving and environmental protection.

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

[0052] In the embodiment, when the liquid level of the material in the reaction system is high, the material can be discharged by increasing the opening of the direct production regulating valve V4 and the production buffer regulating valve V5, so that the liquid level of the material in the reaction system is stabilized in a preset liquid level interval, and therefore the reaction system liquid level controller LIC2 needs to be positive. When the opening of the direct production regulating valve V4 and the buffer production regulating valve V6 is increased, the flow rate is increased, and at this time, the flow rate can be controlled by reducing the opening of the direct production regulating valve V4 and the buffer production regulating valve V6, and therefore the production pipeline flow controller FIC2 needs to be negative.

[0053] The low selection module is connected with the first calculation module Y1 and the second calculation module Y2 respectively, and is used for low selection of 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 the embodiment, the calculation formula of the low selection module is e = min{a / x, b / y}, where e is the output value of the low selection module, and the output value 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 respectively connected with the reaction system and the downstream user, the two ends of the production buffer regulating valve V5 are respectively connected with the reaction system and the buffer system, and the two ends of the buffer production regulating valve V6 are respectively connected with the buffer system and the downstream user.

[0056] In the 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 for material flow.

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

[0058] In the embodiment, when the control instruction received by the air opening valve is to increase the opening, the air opening valve will increase the air supply to make the valve be pushed open. In order to facilitate PID control, when the direct production regulating valve V4, the production buffer regulating valve V5 and the buffer production regulating valve V6 have no air source, they will be automatically closed 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 capable of receiving control instructions, such as air closing valves. In this regard, the embodiments of the present application do not make special limitations 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 the embodiment, the flow decoupling calculation device can be a device, a processor or a controller capable of inputting the selection result of the low selection module into the fourth calculation module Y4 and the third calculation module Y3 for split-range control calculation to obtain a calculation result, and controlling the device, the processor or the controller to change the opening of the direct production regulating valve V4, the production buffer regulating valve V5 and the buffer production regulating valve V6 according to the calculation result. For example, the flow decoupling calculation device can be a server, a controller or a chip.

[0062] In summary, the reaction system liquid level and production flow control system provided by the embodiments of the present application uses the production pipeline flow controller FIC2 and the reaction system liquid level controller LIC2, and uses the low selection module to obtain the minimum value of the output of the first calculation module Y1 and the second calculation module Y2, and controls the opening degree of the direct production regulating valve V4, the production buffer regulating valve V5 and the buffer production regulating valve V6 based on the minimum value, so that the state in which the production buffer regulating valve V5 and the buffer production regulating valve V6 are simultaneously opened does not exist, the reaction system production and downstream user demand can be quickly responded to, the production flow of the reaction / distillation system and the buffer system can be adjusted, the energy consumption is reduced, and the cost is saved.

[0063] Figure 3 The flowchart of the reaction system liquid level and production flow control method provided by the embodiments of the present application can be a server, a processor or a controller, or other computer-related devices, and the embodiments are not particularly limited.

[0064] As shown in the reaction system liquid level and production flow control method, Figure 3 as shown in the reaction system liquid level and production flow control system in the embodiments, Figure 2 the method 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, at this time, the output value of the reaction system liquid level controller LIC2 is a, the split point of the reaction system liquid level controller LIC2 is x, the output of the first calculation module Y1 is a / x, the output value of the production pipeline flow controller FIC2 is b, the split point of the production pipeline flow controller FIC2 is y, and the output of the second calculation module Y2 is b / y, at this time, a / x=b / y, and the opening degree of the direct production regulating valve V4 is controlled to be the opening degree 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] In the formula, x is the split point of the reaction system liquid level controller LIC2, q1 is the full opening flow of the direct production regulating valve V4, and q2 is the full opening flow of the production buffer regulating valve V5.

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

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

[0071] In the formula, y is the split point of the production line 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, which means that the demand of the downstream user is equal to the production flow of the reaction system. At this time, the output c = a / x of the first calculation module Y1 is equal to the output d = b / y of the second calculation module Y2, and the input e = a / x = b / y of the V1 is selected after the low selection module. Meanwhile, 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 are both 0. Correspondingly, the inputs of the control production buffer regulating valve V5 and the buffer production regulating valve V6 are both 0. At this time, the production buffer regulating valve V5 and the buffer production regulating valve V6 are in a full closed state, and the material flows to the downstream user after passing through the open direct production regulating valve V4. Therefore, the material does not need to pass through the cooling device and the heating device, which avoids 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 fourth calculation module Y4 adjusts the output based on the low selection result to make the buffer production regulating valve V6 open, so that the sum of the production flow of the reaction system and the production flow of the buffer system is equal to the demand of the downstream user.

[0074] In an optional embodiment of the present application, the fourth calculation module adjusts the output 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 line flow controller FIC2, y is the split point of the production line flow controller FIC2, and 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] The output of the reaction system liquid level controller LIC2 is less than the demand of the downstream user, which means the flow rate of the reaction system is lower than the demand of the downstream user, and the first calculation module Y1 outputs c=a / x, which is less than the output d=b / y of the second calculation module Y2. After the selection of the low selection module, the input of the direct production adjustment 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 adjustment valve V4 and the buffer production adjustment 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 buffer production adjustment valve V6 is larger at this time to ensure that the total flow entering the downstream user meets the demand. Since the low selection module outputs 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 output by the low selection module is sent to the third calculation module Y3, and the calculation result is f=(a-xa / x) / (1-x)=0, that is, the input of the production buffer adjustment valve V5 is 0, and the production buffer adjustment valve V5 is in the full closed state at this time.

[0079] In this embodiment, in order to better illustrate the beneficial effects of the reaction system liquid level and production flow control method provided by the present application, the traditional split range control process is also used for example, 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 the 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 adjustment valve V4 is e'=b / y, and the input of the buffer production adjustment valve V6 is g'=(b-y) / (1-y). However, if the input of the buffer production adjustment valve V6 remains g'=(b-y) / (1-y), the total flow entering the downstream user will be smaller, which will affect normal production.

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

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

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

[0084] 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 LIC2, x is the split point of the reaction system liquid level controller LIC2, and 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 the embodiment, when the output amount of the reaction system liquid level controller LIC2 is greater than the demand amount of the downstream user, it indicates that the demand flow of the downstream user is small, and the flow extracted by the reaction system to maintain the liquid level is higher than the demand amount of the downstream user. At this time, the first calculation module Y1 outputs c = a / x, which is greater than the output d = b / y of the second calculation module Y2. After selection by the low selection module, the input of the direct extraction adjustment valve V4 of the downstream user is e = b / y. It should be noted that the selection result of the low selection module will affect the opening degree of the direct extraction adjustment valve V4 and the extraction buffer adjustment valve V5. When the output a of the reaction system liquid level controller LIC2 is within the range of (x, 1), the flow decoupling mode will be adopted, and the output result of the low selection module will be 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 calculation method, in the embodiment, the valve opening degree of the extraction buffer adjustment 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 control output of the flow is not affected. The result output by the low selection module 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 buffer extraction adjustment valve V6 is 0, and at this time the valve of the buffer extraction adjustment valve V6 is in the full-closed state.

[0086] Similarly, in the embodiment, in order to better illustrate the beneficial effects of the reaction system liquid level and extraction flow control method provided by the present application, the traditional split 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 in the range of (x, 1), if a conventional split-range control is used instead of the split-range control provided in the embodiments of the present application, the input of the direct withdrawal control valve V4 is e' = a / x, and the input of the withdrawal buffer control valve V5 is f' = (a-x) / (1-x). However, the input of the direct withdrawal control valve V4 is e = b / y, and the actual flow rate of the direct withdrawal control valve V4 is low. If the input of the direct withdrawal control valve V4 is still f' = (a-x) / (1-x), the total flow rate withdrawn from the reaction / distillation system is small, which cannot meet the requirement of the flow rate of the withdrawn material for maintaining the liquid level, and the liquid level of the reaction system continuously rises, which is a potential risk of high liquid level.

[0088] To make the method for controlling the liquid level and the withdrawal flow rate of the reaction system provided in the embodiments of the present application more understandable and implementable, the embodiments take the withdrawal of the distillation system of a device in a production process as an example to further illustrate the control method provided in the above embodiments.

[0089] Suppose that the full opening flow rate of the direct withdrawal control valve V4 is 50 t / h, the full opening flow rate of the withdrawal buffer control valve V5 is 50 t / h, and the full opening flow rate of the buffer withdrawal control valve V6 is 100 t / h. After the calculation of the processor, the split-range point x of the reaction system liquid level controller LIC2 is 50%, and the split-range point y of the withdrawal pipeline flow rate controller FIC2 is 33.3%.

[0090] When the demand of the downstream user is the same as the withdrawal flow rate of the distillation system, the output a of the reaction system liquid level controller LIC2 is 20%, the output c of the first calculation module Y1 is a / x = 20% / 50% = 40%, the output b of the withdrawal pipeline flow rate controller FIC2 is 13.3%, the output d of the second calculation module Y2 is b / y = 13.3% / 33.3% = 40%, e = b = d after the selection of the low selection module, 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, f = g = 0, that is, the inputs of the withdrawal buffer control valve V5 and the buffer withdrawal control valve V6 are both 0, and the withdrawal buffer control valve V5 and the buffer withdrawal control valve V6 are both in the full closed state. The material is directly withdrawn to the downstream user through the direct withdrawal control valve V4.

[0091] When the downstream user demand flow is greater than the production flow of the rectification system for maintaining the liquid level, such as the reaction system liquid level controller LIC2 output a = 40%, 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%, 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%, 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%, 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 buffer production regulating valve V6 is 10%, the opening degrees of the direct production regulating valve V4 and the buffer production regulating valve V6 can ensure that the downstream user demand is met on the basis of maintaining the stability of the liquid level of the rectification system, and the production buffer regulating valve V5 is in a full-closed state.

[0092] When the downstream user demand is less than the production flow of the rectification system for maintaining the liquid level, at this time the reaction system liquid level controller LIC2 output a = 60%, at this time a is greater than the split point x, the output of the first calculation module Y1 is c = a / x = 60% / 50%, since the output of the first calculation module Y1 is maximum 100%, therefore, at this time the output of the first calculation module Y1 is c = 100%, if the output of the production pipeline flow controller FIC2 at this time is b = 20%, the output of the second calculation module Y2 is d = b / y = 20% / 33.3% = 60%, after selection by the low selection module, e = min{100%, 60%}, at this time the input of the direct production regulating valve V4 is 60%, 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 = (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%, the input of the buffer production regulating valve V6 is 0%, the opening degrees of the direct production regulating valve V4 and the production buffer regulating valve V5 ensure that the rectification system production maintains the stability of the liquid level on the basis of meeting the downstream user demand, and the buffer production regulating valve V6 is in a full-closed state.

[0093] In summary, the reaction system liquid level and production flow control method provided by the embodiments of the present application controls the liquid level and production flow of the reaction system by using the split control and low selection module of the production pipeline flow controller FIC2 and the reaction system liquid level controller LIC2, the first calculation module Y1, the second calculation module Y2, the third calculation module Y3 and the fourth calculation module Y4 to control the flow decoupling mode when the demand of the downstream user changes, so that the production buffer regulating valve V5 and the buffer production regulating valve V6 do not exist in the state of being opened at the same time, and the reaction system production and the demand of the downstream user can be quickly responded to, the production flow of the reaction system is adjusted, the energy consumption is reduced, and the cost is saved.

[0094] At the same time, the material in the reaction system can be avoided to be cooled and enter the buffer system at the same time when the material is produced, and the material in the buffer system can be heated and then enter the downstream user, the use amount of cold and hot medium is reduced, the energy waste in the material production process is reduced, the system energy consumption and operation cost are reduced, and the purpose is achieved.

[0095] Figure 4 The hardware structure schematic diagram of the electronic device provided by the embodiments of the present application is shown in FIG. 1. Figure 4 As shown in FIG. 1, the device includes at least one processor 401 and a memory 402.

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

[0097] The processor 401 is used to execute the computer execution instructions stored in the memory 402 to realize each step involved in the above method embodiments. For details, please refer to the related description in the foregoing method embodiments.

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

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

[0100] The embodiments of the present application also provide a computer readable storage medium, and the computer readable storage medium stores computer execution instructions. When the processor executes the computer execution instructions, the reaction system liquid level and production flow control method is realized.

[0101] The embodiments of the present application also provide a computer program product, which includes a computer program. When the computer program is executed by the processor, the reaction system liquid level and production flow control method is realized.

[0102] In several embodiments provided in the present application, it should be understood that the disclosed apparatus and method can be implemented in other manners. For example, the described apparatus embodiments are merely schematic. The division of the modules is merely logical function division. There can be another division manner for the actual implementation, for example, multiple modules or components can be combined or integrated into another system, or some features can be ignored or not executed. In addition, the displayed or discussed coupling or direct coupling or communication connection between the modules can be indirect coupling or communication connection through some interfaces, devices or modules, and can be electrical, mechanical or in other forms.

[0103] The modules illustrated as separated components can or can not be physically separated, and the components illustrated as modules can or can not be physical units, i.e., can be located in one place, or can be distributed on multiple network units. Some or all of the modules can be selected according to actual needs to implement the embodiments of the present application.

[0104] In addition, each functional module in each embodiment of the present application can be integrated in one processing unit, or each module can be physically present separately, or two or more modules can be integrated in one unit. The unit composed of the above modules can be realized in the form of hardware, or in the form of hardware plus software functional unit.

[0105] The integrated modules realized in the form of software functional modules can be stored in a computer readable storage medium. The software functional modules stored in the storage medium include a plurality of instructions for causing a computer device (which can be a personal computer, a server, or a network device, etc.) or a processor to execute part of the steps of the method of each embodiment of the present application.

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

[0107] The memory can include a high-speed RAM memory, and can also include a non-volatile storage NVM, for example, at least one disk memory, and can also be a U disk, a mobile hard disk, a read-only memory, a magnetic disk or an optical disk, etc.

[0108] The bus can be an Industry Standard Architecture (ISA) bus, a Peripheral Component Interconnect (PCI) bus, or an Extended Industry Standard Architecture (EISA) bus, etc. The bus can 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 does not limit to only one bus or one type of bus.

[0109] The storage medium described above can be realized by any type of volatile or nonvolatile storage devices or a combination thereof, such as a static random access memory (SRAM), an electrically erasable programmable read-only memory (EEPROM), an erasable programmable read-only memory (EPROM), a programmable read-only memory (PROM), a read-only memory (ROM), a magnetic storage, a flash memory, a magnetic disk, or an 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 the processor so that the processor can read information from, and write information to, the storage medium. Of course, the storage medium can be part of the processor. The processor and the storage medium can be located in an application specific integrated circuits (ASIC). Of course, the processor and the storage medium can exist as discrete components in the electronic device or host device.

[0111] Those of ordinary skill in the art can understand that all or part of the steps of the above-mentioned method embodiments can be completed by relevant hardware instructed by programs. The foregoing programs can be stored in a computer readable storage medium. When the programs are executed, the steps of the above-mentioned method embodiments are executed; and the foregoing storage medium includes various storage media that can store program codes, such as ROM, RAM, magnetic disks, or optical disks.

[0112] The technical solutions of the present application are described above, but not limited to them; although the present application is described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that the technical solutions recorded in the foregoing embodiments can be modified, or some or all of the technical features can be replaced by equivalent replacements; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present application.

Claims

1. A liquid level and production flow control system for a reaction system, characterized by, The method comprises the following steps: 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 a reaction system through a liquid level transmitter, the reaction system liquid level controller is used for monitoring the liquid level of materials in the reaction system and controlling the flow rate of withdrawal to a downstream system, wherein the downstream system comprises a buffer system and a downstream user; the output end of the reaction system liquid level controller is connected with the first calculation module and the third calculation module respectively; The withdrawal pipeline flow controller adopts a split-range control method to process process input, the input end of the withdrawal pipeline flow controller is connected with a pipeline through which materials are withdrawn to the downstream user through a flow transmitter, the withdrawal pipeline flow controller is used for monitoring and controlling the total flow rate of withdrawal to the downstream user, and the output end of the withdrawal pipeline flow controller is connected with the second calculation module and the fourth calculation module respectively; The low selection module is connected with the first calculation module and the second calculation module at two ends, and is used for low selection of 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 direct withdrawal regulating valve is in communication with the reaction system and the downstream user at two ends, the withdrawal buffer regulating valve is in communication with the reaction system and the buffer system at two ends, and the buffer withdrawal regulating valve is in communication with the buffer system and the downstream user at two ends. The direct withdrawal regulating valve, the withdrawal buffer regulating valve and the buffer withdrawal regulating valve are all gas opening valves.

2. The system of claim 1, wherein, The reaction system liquid level controller is positive, and the withdrawal pipeline flow controller is negative.

3. The system of claim 1, wherein, 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.

4. The system of any one of claims 1 to 3, wherein, The method comprises the following steps:

5. A method for controlling the liquid level and production flow rate of a reaction system using the reaction system liquid level and production flow rate control system according to claim 1, characterized by, When the output quantity of the reaction system liquid level controller is equal to the demand quantity of the downstream user, the output value of the reaction system liquid level controller is a, the split-range point of the reaction system liquid level controller is x, the output of the first calculation module is a / x, the output value of the withdrawal pipeline flow controller is b, the split-range point of the withdrawal pipeline flow controller is y, the output of the second calculation module is b / y, a / x=b / y at this time, and the opening degree of the direct withdrawal regulating valve is an opening degree value obtained based on the output value of the reaction system liquid level controller or the output value of the withdrawal pipeline flow controller; When the output quantity of the reaction system liquid level controller is less than the demand quantity of the downstream user, a / x<b / y at this time, the first low selection result is output by the low selection module, the fourth calculation module adjusts the output based on the low selection result, the buffer withdrawal regulating valve is opened, so that the sum of the withdrawal flow rate of the reaction system and the withdrawal flow rate of the buffer system is equal to the demand quantity of the downstream user. ​ When the output of the reaction system liquid level controller is greater than the demand of the downstream user, i.e. a / x > b / y, the low selection module outputs a second low selection result, and the third calculation module outputs an adjustment based on the output of the low selection module, so that the production buffer regulating valve is opened to make the production flow of the reaction system be the sum of the flow produced to the buffer device and the demand of the downstream user.

6. The method of claim 5, wherein, The calculation formula of the adjustment of the output of the third calculation module based on the output of the low selection module 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, and e = min{a / x, b / y}, i.e. e takes the smaller value of a / x and b / y.

7. The method of claim 5, wherein, The calculation formula of the adjustment of the output of the fourth calculation module based on the output of the low selection module is: g = (b - ye) / (1 - y) In the formula, 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, and e = min{a / x, b / y}, i.e. e takes the smaller value of a / x and b / y.

8. The method of claim 5, wherein, The calculation formula of the split point x of the reaction system liquid level controller is: x = q1 / (q1 + q2) In the formula, x is the split point of the reaction system liquid level controller, q1 is the full opening flow of the direct production regulating valve, and q2 is the full opening flow of the production buffer regulating valve. The calculation formula of the split point y of the production pipeline flow controller is: y = q1 / (q1 + q3) In the formula, y is the split point of the production pipeline flow controller, q1 is the full opening flow of the direct production regulating valve, and q3 is the full opening flow of the buffer production regulating valve.

9. An electronic device, comprising: It comprises: at least one processor and a memory; the memory stores computer execution instructions; the at least one processor executes the computer execution instructions stored in the memory, so that the at least one processor executes the reaction system liquid level and production flow control method as claimed in any one of claims 5 to 8.

10. A computer-readable storage medium, characterized in that, The computer readable storage medium stores computer execution instructions, and when the processor executes the computer execution instructions, the reaction system liquid level and production flow control method as claimed in any one of claims 5 to 8 is realized.

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