CN211015169U - Control system for temperature of pipeline confluence liquid - Google Patents
Control system for temperature of pipeline confluence liquid Download PDFInfo
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- CN211015169U CN211015169U CN201921821384.8U CN201921821384U CN211015169U CN 211015169 U CN211015169 U CN 211015169U CN 201921821384 U CN201921821384 U CN 201921821384U CN 211015169 U CN211015169 U CN 211015169U
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Abstract
A control system for the temperature of pipeline confluence liquid comprises a control console, a control valve, a first differential pressure sensor, a second differential pressure sensor, a first temperature sensor, a second temperature sensor, a third temperature sensor, a first flowmeter and a second flowmeter; on the basis of measuring the flow field characteristics of the pipeline, the flow of the liquid before confluence is automatically calculated and controlled in real time by applying the thermodynamic principle according to the working condition of the liquid before confluence, so that the temperature of the liquid after confluence is accurately reached and stably kept at the set target temperature. The utility model discloses a pipeline converges real-time accurate control of back liquid temperature to when the operating mode of the liquid that converges changes, can the aperture of automatic adjustment control valve, in order to keep converging the temperature stability of back liquid unchangeable, improved pipe-line system's stability, thereby avoided prior art to converge back liquid temperature detection feedback existence time difference, lead to the pipeline to converge the defect that liquid temperature stability descends, have the advantage that control is quick, accurate, stable.
Description
Technical Field
The utility model relates to a liquid temperature's control, concretely relates to pipeline confluence liquid temperature's control system belongs to automatic control technical field.
Background
In recent years, with the development of socio-economic, the application of industrial pipelines is more and more extensive, and the control requirement on the fluid in the pipelines is higher and higher. In a pipeline for conveying liquid, two liquid streams are often mixed and converged, and certain requirements are imposed on the temperature of the mixed liquid stream. In the prior art, a temperature sensor is usually used for detecting the temperature of fluid in a pipeline, and then the opening of the temperature control valve is directly controlled according to a preset simple program.
However, when the fluid condition changes, the above-mentioned fluid control method often generates two error situations: 1. the action of the temperature control valve and the feedback of the fluid temperature sensor after confluence generally have a certain time difference, and if the time difference is not properly set, the fluctuation of a confluence fluid temperature curve can be caused, so that the temperature stability is reduced. 2. The conventional control method uses the temperature of the merged fluid as a control basis, and the temperature of the merged fluid deviates from the target temperature at this time, and the merged fluid can be recovered after a period of time elapses after the opening degree of the temperature control valve is adjusted. Both of these situations may have the following serious consequences: 1) improper setting of the time difference may cause the temperature of the converged fluid to oscillate or even diverge, resulting in the loss of the temperature control capability of the thermostatic valve. 2) Sudden changes in the liquid conditions before confluence result in sudden changes in the liquid conditions after confluence, and at this time, the fluid has already flowed to the rear, which can have a significant adverse effect on the rear system.
SUMMERY OF THE UTILITY MODEL
For solving the above-mentioned problem that prior art arouses, the utility model provides a pipeline converges control system of liquid temperature realizes converging the real-time accurate control of liquid temperature to improve the stability of pipe-line system temperature.
In order to achieve the above purpose, the technical scheme of the utility model is as follows:
a system for controlling the temperature of a liquid flowing in a pipe comprising a first pipe for flowing a first fluid, a second pipe for flowing a second fluid, and a manifold pipe for flowing the fluid out of the pipe, the first pipe and the second pipe being connected downstream of the first pipe and downstream of the second pipe and upstream of the manifold pipe, the system comprising: the control system comprises a console, a control valve, a first differential pressure sensor, a second differential pressure sensor, a first temperature sensor, a second temperature sensor, a third temperature sensor, a first flowmeter and a second flowmeter; the control valve is connected to the first pipeline for regulating the flow of the first fluid, the first differential pressure sensor is connected to the first pipeline and connected in parallel to two ends of the control valve for measuring the pressure difference of the first fluid, the second differential pressure sensor is connected to the second pipeline for measuring the pressure difference of the second fluid, the first temperature sensor is connected to the first pipeline for measuring the temperature of the first fluid, the second temperature sensor is connected to the second pipeline for measuring the temperature of the second fluid, the third temperature sensor is connected to the confluence pipeline for measuring the temperature of the confluence liquid, the first flowmeter is connected to the first pipeline for measuring the flow of the first fluid, and the second flowmeter is connected to the second pipeline, the first differential pressure sensor, the second differential pressure sensor, the first temperature sensor, the second temperature sensor, the third temperature sensor, the first flowmeter and the second flowmeter are respectively connected with the console and used for conveying real-time test data, and the console is connected with the control valve and used for controlling the opening of the control valve so as to adjust the flow of the first fluid and accurately control the temperature of the confluence liquid after confluence in real time.
Further, the first flow meter and the second flow meter are dismantled after debugging is completed.
Furthermore, the control console is internally provided with a control program in advance.
Furthermore, a plurality of pipelines form a pipeline system, and the control systems with the same number as the pipelines are respectively connected with the pipelines and control the temperature of the confluence liquid of the whole pipeline system.
Compared with the prior art, the beneficial effects of the utility model are that:
the control system for the pipeline confluence liquid temperature is based on the measurement of the flow field characteristics of the pipeline, automatically calculates and controls the flow of the liquid before confluence in real time by applying the thermodynamic principle according to the working condition of the liquid before confluence, so that the real-time accurate control of the liquid temperature after the pipeline confluence is realized, and when the working condition of the confluence liquid changes, the control system can automatically calculate and immediately adjust the opening of the control valve so as to keep the temperature of the liquid after confluence stable and unchanged, thereby improving the stability of the pipeline system.
The utility model discloses changed and used the traditional regulation and control mode that converges back liquid temperature as the foundation, avoided prior art to converge back liquid temperature detection feedback existence time difference, lead to the pipeline to converge liquid temperature stability and drop, produce the defect of great adverse effect to the rear pipeline, had that control is quick, accurate, stable advantage.
Drawings
Fig. 1 is a schematic diagram of the present invention.
Detailed Description
The invention will be further elucidated with reference to the drawings and specific embodiments, without limiting the scope of the invention.
Referring to fig. 1, the illustrated pipes include a first pipe a, a second pipe b, and a confluence pipe c, and the downstream of the first pipe a and the second pipe b are connected to the upstream of the confluence pipe c, so that a first fluid flowing into the first pipe a and a second fluid flowing into the second pipe b are merged into a confluence liquid to flow out of the confluence pipe c. Larger duct systems may be made up of multiple illustrated duct structures.
The control system for the temperature of the pipeline confluence liquid is connected to the pipeline and comprises a control console (not shown in the figure), a control valve 1, a first differential pressure sensor 2, a second differential pressure sensor 3, a first temperature sensor 4, a second temperature sensor 5, a third temperature sensor 8, a first flowmeter 6 and a second flowmeter 7.
The control valve 1 is connected to the first pipe a for regulating the flow rate of the first fluid. The first differential pressure sensor 2 is connected to the first pipe a and connected in parallel to both ends of the control valve 1, for measuring a pressure difference of the first fluid. The first temperature sensor 4 is connected to the first pipe a for measuring the temperature of the first fluid. The first flow meter 6 is connected to the first pipe a for measuring the flow rate of the first fluid.
The second differential pressure sensor 3, the second temperature sensor 5 and the second flow meter 7 are connected to the second pipeline b and are respectively used for measuring the pressure difference, the temperature and the flow of the second fluid.
The third temperature sensor 8 is connected to the confluence pipe c for measuring the temperature of the confluence liquid.
The first differential pressure sensor 2, the second differential pressure sensor 3, the first temperature sensor 4, the second temperature sensor 5, the third temperature sensor 8, the first flowmeter 6 and the second flowmeter 7 are respectively connected with the console and used for transmitting real-time test data. The first flow meter 6 and the second flow meter 7 are removed after the commissioning is completed.
The control console is internally provided with a control program in advance, is connected with the control valve 1 and controls the opening of the control valve 1 so as to adjust the flow of the first fluid and accurately control the temperature of the converged liquid.
In the pipeline system, each pipeline is connected with a control system, so that the temperature of the confluence liquid is controlled for the whole pipeline system.
The utility model discloses a through the adjustment the aperture of control valve 1 changes first fluidic flow in the first pipeline a, thereby it is right to realize the control of liquid temperature converges. The operation content comprises the following steps: measuring and recording the flow field characteristics of the pipeline in a debugging stage, and obtaining a function corresponding relation between the opening of the control valve and the resistance coefficient of the first pipeline; and in the operation stage, the pressure difference and the temperature of the first fluid and the second fluid before confluence are obtained through detection, the opening degree of a control valve necessary for reaching the target temperature of the confluent liquid after confluence is calculated according to the function corresponding relation obtained in the debugging stage, an energy conservation equation and a mass conservation equation, and the opening degree of the control valve is adjusted to control the temperature of the confluent liquid to accurately reach and stably keep the temperature at the set target temperature.
The debugging stage comprises the following steps:
1) setting the control valve 1 at a certain opening degreeMeasuring the flow rate Q of the first fluid by the first flow meter 6 and the second flow meter 7, respectively1And flow rate Q of the second fluid2Measuring the pressure difference H of the first fluid by the first differential pressure sensor 2 and the second differential pressure sensor 3 respectively1And the pressure difference H of the second fluid2。
The pipeline has the formula H-SQ2Expressed flow field characteristics, so that the console automatically calculates the drag coefficient S of the first pipeline a by the following formula1And the drag coefficient S of the second pipe b2：
S1＝Q1 2/H1，
S2＝Q2 2/H2，
Wherein the content of the first and second substances,
S1is the drag coefficient, Q, of the first conduit a1Is the flow rate of the first fluid, measured by the first flow meter 6, H1Is the pressure difference of the first fluid, measured by the first differential pressure sensor 2;
S2is the drag coefficient, Q, of the second conduit b2Measured by a second flow meter 7 for the flow of a second fluid, H2Is the pressure difference of the second fluid, measured by the second differential pressure sensor 3, S, since there is no element in the second pipe b that changes the flow rate2、Q2And H2All are fixed values that are not changed during the debugging phase.
The console then compares the resistance coefficient S of the control valve 1 at this opening with the resistance coefficient S of the first conduit a1And the drag coefficient S of the second pipeline b2Automatic recording is performed.
2) Sequentially setting the control valve 1 at different opening degrees, and repeating the step 1) to obtain a flow rate Q of the first fluid caused by the change of the opening degree of the control valve 11And the pressure difference H1And the coefficient of resistance S of the first conduit a at each opening of the control valve 1 is recorded1So as to obtain the opening degree of the control valve 1 and the resistance coefficient S of the first pipeline a1And automatically recorded in a control program in the console.
3) And after debugging is completed, the first flow meter 6 and the second flow meter 7 are detached.
The operating phase comprises the steps of:
1) setting a target temperature T of the confluence liquid after confluence3mAnd inputting a control program of the console;
2) the real-time temperature T of the first fluid is measured by the first temperature sensor 4, the second temperature sensor 5 and the third temperature sensor 8 respectively10The real-time temperature T of the second fluid20And the real-time temperature T of the confluence liquid30And input into the console;
according to the thermodynamic principle, the console is then based on the measured real-time temperature T of the first fluid10And the real-time temperature T of the second fluid20Separately calculating the enthalpy value h of the first fluid1And enthalpy h of the second fluid2The target temperature T of the confluence liquid set according to the step 1)3mCalculating target enthalpy value h of confluence liquid3m。
3) The first differential pressure sensor 2 and the second differential pressure sensor 3 are used for respectively measuring the real-time pressure difference value H of the first fluid10And a second fluid H20And input to the console; the console calculates the real-time flow Q of the second fluid through the following formula20：
H20＝S2Q20 2，
Wherein Q is20Is the real-time flow of the second fluid, H20Is a real-time pressure difference of the second fluid, measured by the second differential pressure sensor 3, S2The resistance coefficient and the fixed value of the second pipeline b are obtained in the step 1) of the debugging stage;
4) according to an energy conservation equation and a mass conservation equation, the console calculates the target flow Q of the first fluid through the following formula1m：
Q1mh1+Q20h2＝Q3mh3m，
Q1m+Q20＝Q3m，
Wherein the content of the first and second substances,
Q1mis the target flow rate of the first fluid, Q20Calculated from step 3) for the real-time flow of the second fluid, Q3mIs the target flow rate of the confluence liquid;
h1is the enthalpy of the first fluid, h2Is the enthalpy of the second fluid, h3mThe target enthalpy value of the confluence liquid is obtained by calculation in the step 2).
5) The console calculates a target resistance coefficient S of the first pipeline through the following formula1m：
H10＝S1mQ1m 2，
Wherein S is1mIs the target drag coefficient of the first conduit, H10Measured as a real-time pressure difference of the first fluid by the first differential pressure sensor 2, Q1mThe target flow rate of the first fluid is calculated in the step 4);
then the console obtains the opening degree of the control valve and the resistance coefficient S of the first pipeline a according to the step 2) in the debugging stage1Functional correspondence between the first and second pipes, target resistance coefficient S of the first pipe a obtained by calculation1mA target opening degree of the control valve 1 is determined.
6) The console controls and adjusts the control valve 1 to reach the target opening obtained in the step 5) in real time, so that the real-time temperature T of the converged liquid is achieved30Accurately reaches the set target temperature T3mWhen the working condition of the pipeline confluence liquid changes, the console automatically calculates and controls the control valve 1 to adjust the opening in real time, so that the temperature T of the confluence liquid30Stably maintained at the target temperature T3mIt is not changed.
The present invention is obviously not limited to the above-described embodiments, and various obvious modifications, variations and adaptations, which may be made by those skilled in the art, are intended to be included within the scope of the present invention.
Claims (4)
1. A system for controlling the temperature of a liquid flowing in a pipe comprising a first pipe for flowing a first fluid, a second pipe for flowing a second fluid, and a manifold pipe for flowing the fluid out of the pipe, the first pipe and the second pipe being connected downstream of the first pipe and downstream of the second pipe and upstream of the manifold pipe, the system comprising: the control system comprises a console, a control valve, a first differential pressure sensor, a second differential pressure sensor, a first temperature sensor, a second temperature sensor, a third temperature sensor, a first flowmeter and a second flowmeter; the control valve is connected to the first pipeline for regulating the flow of the first fluid, the first differential pressure sensor is connected to the first pipeline and connected in parallel to two ends of the control valve for measuring the pressure difference of the first fluid, the second differential pressure sensor is connected to the second pipeline for measuring the pressure difference of the second fluid, the first temperature sensor is connected to the first pipeline for measuring the temperature of the first fluid, the second temperature sensor is connected to the second pipeline for measuring the temperature of the second fluid, the third temperature sensor is connected to the confluence pipeline for measuring the temperature of the confluence liquid, the first flowmeter is connected to the first pipeline for measuring the flow of the first fluid, and the second flowmeter is connected to the second pipeline, the first differential pressure sensor, the second differential pressure sensor, the first temperature sensor, the second temperature sensor, the third temperature sensor, the first flowmeter and the second flowmeter are respectively connected with the console and used for conveying real-time test data, and the console is connected with the control valve and used for controlling the opening of the control valve so as to adjust the flow of the first fluid and accurately control the temperature of the confluence liquid after confluence.
2. The system of claim 1, wherein the controller is configured to: and the first flow meter and the second flow meter are dismantled after debugging is finished.
3. The system of claim 1, wherein the controller is configured to: the control console is internally provided with a control program in advance.
4. The system of claim 1, wherein the controller is configured to: the control systems with the same number as the pipelines are respectively connected with the pipelines and control the temperature of the confluence liquid of the whole pipeline system.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201921821384.8U CN211015169U (en) | 2019-10-28 | 2019-10-28 | Control system for temperature of pipeline confluence liquid |
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| CN201921821384.8U CN211015169U (en) | 2019-10-28 | 2019-10-28 | Control system for temperature of pipeline confluence liquid |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113653540A (en) * | 2021-08-27 | 2021-11-16 | 上海发电设备成套设计研究院有限责任公司 | Turbine dry gas sealing and cylinder cooling system device and operation method thereof |
| CN117472116A (en) * | 2023-12-26 | 2024-01-30 | 徐州鸿丰高分子材料有限公司 | Intelligent material conveying control system |
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2019
- 2019-10-28 CN CN201921821384.8U patent/CN211015169U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113653540A (en) * | 2021-08-27 | 2021-11-16 | 上海发电设备成套设计研究院有限责任公司 | Turbine dry gas sealing and cylinder cooling system device and operation method thereof |
| CN113653540B (en) * | 2021-08-27 | 2023-11-24 | 上海发电设备成套设计研究院有限责任公司 | Turbine dry gas sealing and cylinder cooling system device and operation method thereof |
| CN117472116A (en) * | 2023-12-26 | 2024-01-30 | 徐州鸿丰高分子材料有限公司 | Intelligent material conveying control system |
| CN117472116B (en) * | 2023-12-26 | 2024-03-19 | 徐州鸿丰高分子材料有限公司 | Intelligent material conveying control system |
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