CN117130406A - Method for controlling preset temperature of reactor of cracking carbon five fraction device - Google Patents
Method for controlling preset temperature of reactor of cracking carbon five fraction device Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 38
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims description 22
- 229910052799 carbon Inorganic materials 0.000 title claims description 22
- 238000005336 cracking Methods 0.000 title claims description 22
- 238000006243 chemical reaction Methods 0.000 claims abstract description 34
- 230000008569 process Effects 0.000 claims abstract description 20
- 238000004891 communication Methods 0.000 claims abstract description 13
- 230000001105 regulatory effect Effects 0.000 claims abstract description 9
- 230000001276 controlling effect Effects 0.000 claims abstract description 7
- 230000003828 downregulation Effects 0.000 claims abstract description 5
- 238000001816 cooling Methods 0.000 claims description 23
- 238000004321 preservation Methods 0.000 abstract description 7
- 238000013461 design Methods 0.000 abstract description 5
- 230000003827 upregulation Effects 0.000 abstract description 5
- 230000009467 reduction Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000005070 sampling Methods 0.000 description 4
- 239000002826 coolant Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000000197 pyrolysis Methods 0.000 description 3
- HECLRDQVFMWTQS-RGOKHQFPSA-N 1755-01-7 Chemical compound C1[C@H]2[C@@H]3CC=C[C@@H]3[C@@H]1C=C2 HECLRDQVFMWTQS-RGOKHQFPSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000011534 incubation Methods 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000036632 reaction speed Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 206010063385 Intellectualisation Diseases 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000004069 differentiation Effects 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000010583 slow cooling Methods 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05D—SYSTEMS FOR CONTROLLING OR REGULATING NON-ELECTRIC VARIABLES
- G05D23/00—Control of temperature
- G05D23/19—Control of temperature characterised by the use of electric means
- G05D23/20—Control of temperature characterised by the use of electric means with sensing elements having variation of electric or magnetic properties with change of temperature
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Abstract
The application provides a novel heat exchanger structural design and a temperature split control scheme based on the application of the heat exchanger, so as to meet the split control precision requirements of each stage of a reactor temperature preset curve, realize the process means of high-temperature rapid down-regulation and low-temperature rapid up-regulation, and further achieve the design purposes of stable heat preservation and high-efficiency compliance with the process preset temperature conditions. The reactor is provided with at least two groups of heat exchangers, the heat exchange areas of each group of heat exchangers are different, and each group of heat exchangers can be communicated with a cold medium with lower temperature or a heat medium with higher temperature; according to the difference value between the actual reaction temperature and the preset temperature in the reactor, a temperature regulating valve is used for controlling each group of heat exchangers to be communicated with different media or closing the heat exchangers so as to realize the temperature step control; the communication state of each group of heat exchangers is indirectly regulated by regulating the opening degree of the temperature regulating valve.
Description
Technical Field
The application provides a preset temperature control method of a reactor applied to a manufacturing process of cracking carbon five fractions, belonging to the petrochemical and computer informatization fields.
Background
The production process for preparing ethylene by cracking petroleum and heavy cracking raw materials at home and abroad generally needs to separate dicyclopentadiene from other components in the carbon five fraction. The cracking carbon five fraction process in the prior art is carried out in a reactor, the reaction process needs proper pressure and temperature, and particularly, the reaction temperature has very close relation to the reaction time and the product quality, so that the stability and the accuracy control of the reaction temperature have higher requirements.
In general, the temperature control process has the stages of temperature rise control, heat preservation control, temperature reduction control and the like, and only one group of heat exchangers of the existing reactor is provided, and the group of heat exchangers is used for introducing cold medium or heat medium at a certain moment, namely, the reactor is in a temperature rise or temperature reduction state. When the reaction temperature is raised to the heat preservation temperature, a heat medium is introduced into a heat exchanger of the reactor, and the temperature easily exceeds a preset control temperature under the action of temperature raising inertia. When the over-temperature state occurs, the temperature in the existing reactor is difficult to quickly adjust, the temperature adjustment is difficult to achieve by the adjustment means for reducing the flow of the heat medium, and the flow of the heat medium is reduced but the heating process is also carried out; in addition, the material consumption heat and the natural cooling heat consumption in the reactor are very small, and are uncontrollable from the viewpoint of preset temperature control. Conversely, when the internal temperature of the reactor is reduced from the temperature reduction to the heat preservation stage, the cold medium is introduced into the heat exchanger, the temperature is easily lower than the preset temperature under the action of the temperature reduction inertia, and once the temperature is lower than the preset temperature, the temperature is difficult to adjust, because the fact that the temperature reduction cannot be changed due to the reduction of the flow of the cold medium, and the internal temperature of the reactor is lower due to the factors such as the consumed heat of the reaction materials, the natural temperature reduction and the like, and the control of the preset temperature is also uncontrollable. The defects that the high temperature cannot be reduced and the low temperature cannot be up-regulated in the prior art form obvious obstruction and adverse conditions for realizing stable heat preservation and reaching the preset temperature index of the process.
In view of this, the present patent application is specifically filed.
Disclosure of Invention
The application provides a preset temperature control method of a reactor of a cracking carbon five fraction device, which aims to solve the problems existing in the prior art and provides a novel heat exchanger structural design and a temperature split control scheme based on the application of the heat exchanger so as to meet the split control precision requirements of each stage of a preset temperature curve of the reactor, and realize the process means of rapid low-temperature down regulation and rapid low-temperature up regulation, thereby achieving the design purposes of stable heat preservation and high-efficiency compliance with preset temperature conditions of the process.
In order to achieve the above design objective, the preset temperature control method for the reactor of the cracking carbon five fraction device is provided with at least two groups of heat exchangers, wherein the heat exchange areas of each group of heat exchangers are different, and each group of heat exchangers can be communicated with a cold medium with lower temperature or a heat medium with higher temperature; according to the difference value between the actual reaction temperature and the preset temperature in the reactor, a temperature regulating valve is used for controlling each group of heat exchangers to be communicated with different media or closing the heat exchangers so as to realize the temperature step control; the split-control process comprises a lower control stage in which the actual reaction temperature is higher than the preset temperature and an upper control stage in which the actual reaction temperature is lower than the preset temperature; setting and adopting a digital A/D converter to sample the temperature, realizing the self-setting of parameters of the PID controller according to the temperature speed, and indirectly adjusting the communication state of each group of heat exchangers by adjusting the opening degree of a temperature regulating valve; the PID equation for incremental temperature control is as follows,
further, the split-phase control process includes an up-regulation control stage and a down-regulation control stage, the up-regulation control stage including a rapid temperature rise step when all heat exchangers are communicated with a heat medium, a medium speed temperature rise step when only a larger area of heat exchangers are communicated with the heat medium, and a low speed temperature rise step when only a smaller area of heat exchangers are communicated with the heat medium; the down-regulation control stage includes a rapid cooling step when all heat exchangers are connected to a cold medium, a medium speed cooling step when only a large area of heat exchangers are connected to a cold medium, and a low speed cooling step when only a small area of heat exchangers are connected to a cold medium.
Further, each group of heat exchangers are uniformly distributed along the outer wall of the reactor, and communication pipes among the heat exchangers are respectively and circularly closed and are independently arranged.
As described above, the preset temperature control method for the cracking carbon five fraction device reactor provided by the application has the following advantages: 1. based on the improved heat exchanger structure and medium introduction control means, the application realizes a brand new temperature split-control method, effectively solves the technical defects that the high temperature of the reactor in the prior art cannot be reduced and the low temperature cannot be adjusted upwards, can stably and rapidly reach the preset temperature condition of the process, and remarkably improves the reaction speed of cracking the carbon five fractions and the quality of cracked products. 2. The application can meet the process requirements of the chemical industry on temperature control precision and stability, realizes the high-precision temperature control effect by a temperature speed adjusting means, has smaller overshoot and has the characteristics of better intellectualization and controllability. Therefore, the method has the advantages of rapid reaction, good tracking performance and capability of eliminating temperature deviation in the cracking carbon five fraction device in real time, and is beneficial to improving the uniformity and stability of products.
3. The application can effectively maintain the temperature condition of the device for cracking the carbon five fractions according to the process requirements, thereby not only improving the reaction speed and ensuring the product quality, but also obviously improving the production efficiency and reducing the production cost.
4. The application integrates the intelligent solutions of comprehensive application of the reactor technology, the automatic control, the soft measurement technology, the computer monitoring technology and the like, and lays a solid foundation for the digital, intelligent and informationized development of the technology in the chemical industry.
Drawings
FIG. 1 is a graph of preset variations in reactor temperature;
FIG. 2 is a schematic illustration of a reactor cross-sectional structure and medium line communication;
FIG. 3 is a block diagram of a preset temperature rate real-time control;
in FIG. 2, the solid arrows are medium conduits, the dashed arrows are control signal paths, 1-reactor; 11-stirring device; 21-a first heat exchanger; 22-a second heat exchanger; 3-a temperature sensor; 31-a first temperature controller; 32-a second temperature controller; 4-material inlet; 51-a first solenoid valve; 52-a second solenoid valve; 53-a third solenoid valve; 54-a fourth solenoid valve; 55-a fifth solenoid valve; 56-a sixth solenoid valve; a 6-temperature transmitter; 71-a first pneumatic control valve; 72-a second pneumatic control valve;
Detailed Description
The application is further described below with reference to the drawings and examples.
Example 1 the application provides a preset temperature control method of a cracking carbon five fraction device reactor, which is applied to the technical process of preparing ethylene by steam cracking petroleum and heavy cracking raw materials, and the dicyclopentadiene is separated from other components in the carbon five fraction.
As shown in FIG. 1, the temperature preset curve of the pyrolysis carbon five fraction device requires a certain range of pressure and temperature conditions in the pyrolysis carbon five fraction reaction process in the reactor, the temperature is particularly important for the quality of the pyrolysis product, and the temperature control process comprises a temperature rising stage V u A heat preservation stage (temperature is respectively stabilized at T) 2 And T 3 ) And a cooling stage V d In this example, T1 is set to 60 ℃, T2 is set to 90 ℃, and T3 is set to 70 ℃.
As shown in fig. 2, the cracking carbon five fraction device provided by the application has at least two groups of heat exchangers (such as a first heat exchanger 21 and a second heat exchanger 22 provided by the embodiment), the heat exchange area of each group of heat exchangers is different (such as the heat exchange area of the first heat exchanger 21 is larger than that of the second heat exchanger 22), and each group of heat exchangers can be communicated with a cold medium (such as cooling water) with lower temperature or a heat medium (such as hot water or steam) with higher temperature;
in the process of cracking the carbon five fraction, according to the difference (delta T) between the actual reaction temperature and the preset temperature in the reactor 1, the on-off valve (such as the first pneumatic adjusting valve 71 and/or the second pneumatic adjusting valve 72) is adjusted to control each group of heat exchangers to be communicated with different media (namely, to be communicated with a cold medium or a hot medium) or to close the heat exchangers, so as to realize the process control of the reaction temperature in the reactor 1; the split-control process comprises a lower control stage in which the actual reaction temperature is higher than the preset temperature and an upper control stage in which the actual reaction temperature is lower than the preset temperature.
Specifically, the up-regulation control stage (i.e., the temperature-raising stage V u ) Comprising the following steps: a rapid temperature rise step when all the heat exchangers are communicated with the heat medium; a medium speed warm-up step when a larger area heat exchanger (e.g., first heat exchanger 21) is in communication with the thermal medium, wherein second heat exchanger 22 may be closed or in communication with the cold medium; a low-rate warm-up step when a smaller area heat exchanger (e.g., the second heat exchanger 22) is in communication with the heat medium, wherein the first heat exchanger 21 is turned off.
Lower control stage (i.e. cooling stage V) d ) Comprising the following steps: a rapid cooling step when all heat exchangers are communicated with the cold medium; a medium speed cooling step when a larger area heat exchanger (such as the first heat exchanger 21) is in communication with a cold medium, wherein the second heat exchanger 22 can be closed or in communication with a hot medium; a low-speed cooling step when a smaller area heat exchanger (such as the second heat exchanger 22) is in communication with the cold medium, wherein the first heat exchanger 21 is turned off.
Furthermore, in order to improve the control efficiency and uniformity of the reaction temperature inside the reactor 1, each group of heat exchangers are uniformly distributed along the outer wall of the reactor, and the communicating pipes are respectively and circularly closed and are independently arranged.
The preset temperature control method of the cracking carbon five fraction device reactor aims at the time critical point (such as t in figure 1) of the temperature control process 2 、t 3 And t 4 ) According to the difference delta T between the actual reaction temperature and the preset temperature inside the reactor 1 detected by the temperature sensor 3, the opening degree of the first pneumatic adjusting valve 71 and the opening degree of the second pneumatic adjusting valve 72 are respectively adjusted by the first temperature controller 31 and the second temperature controller 32 to indirectly control the opening and closing states of the first heat exchanger 2 and the second heat exchanger 22 and the property of the communication medium so as to realize a constant temperature control scheme based on the reaction process. The scheme comprises the following steps:
when the reaction temperature reaches the incubation period from the heating period (t in FIG. 1 2 Moment), at this time, the first heat exchanger 21 is communicated with the heat medium, and the second heat exchanger 22 is closed; if the difference DeltaT between the actual reaction temperature and the preset temperature does not exceed the set range, the first step is adjustedThe opening degree of the pneumatic control valve 71 is controlled to control the internal temperature of the reactor 1 through the first heat exchanger 21, i.e., to maintain the internal temperature without overshoot; if the difference Δt between the actual reaction temperature and the preset temperature exceeds the set range, the second heat exchanger 22 is connected to the cooling medium to perform the slow cooling inside the reactor 1 (because the heat exchange area of the second heat exchanger 22 is smaller than that of the first heat exchanger 21), so that the reaction temperature inside the reactor 1 is more accurately reduced to the preset temperature.
When the reaction temperature reaches the incubation period from the cooling period (t in FIG. 1) 4 Moment), at the moment, the first heat exchanger 21 is communicated with the cooling medium, and the second heat exchanger 22 is closed; if the difference deltat between the actual reaction temperature and the preset temperature does not exceed the set range, the opening of the first pneumatic control valve 71 is adjusted to control the internal temperature of the reactor 1 through the first heat exchanger 21, i.e. to maintain the internal temperature without overshoot; if the difference Δt between the actual reaction temperature and the preset temperature exceeds the set range, the second heat exchanger 22 communicates with the heat medium to perform a slow temperature rise inside the reactor 1, so that the reaction temperature inside the reactor 1 rises to the preset temperature more accurately.
As shown in FIG. 3, in order to realize the preset temperature control process, the preset temperature speed is set as V in the heating stage according to the requirements of the reaction process of the cracking carbon five fraction device on the temperature and the temperature speed index su Setting the preset temperature speed to be V in the cooling stage sd All heat exchangers work in combination in the following manner:
when the first heat exchanger 21 is connected to the heat medium to perform the temperature raising operation, the maximum temperature raising speed thereof is V 1maxu The method comprises the steps of carrying out a first treatment on the surface of the When the second heat exchanger 22 is connected to the heat medium to perform the temperature raising operation, the maximum temperature raising speed thereof is V 2maxu The method comprises the steps of carrying out a first treatment on the surface of the When the first heat exchanger 21 and the second heat exchanger 22 are simultaneously connected with the heat medium to perform the temperature raising operation, the maximum temperature raising speed is V 1maxu +V 2maxu ；
When the first heat exchanger 21 is communicated with the cooling medium to perform the cooling operation, the maximum cooling speed is V 1maxd The method comprises the steps of carrying out a first treatment on the surface of the When the second heat exchanger 22 is communicated with the cold medium to perform the cooling operation, the maximum cooling speed is V 2maxd The method comprises the steps of carrying out a first treatment on the surface of the When the first heat exchanger 21 and the second heat exchanger 22 are simultaneously communicated with the cold medium to realizeWhen the cooling operation is performed, the maximum cooling speed is V 1maxd +V 2maxd ；
When the first heat exchanger 21 is communicated with the heat medium to perform the temperature raising operation and the second heat exchanger 22 is communicated with the cold medium to perform the temperature lowering operation, the maximum temperature raising speed is V 1maxu -V 2maxd ；
When the first heat exchanger 21 is communicated with the cold medium to perform the cooling operation and the second heat exchanger 22 is communicated with the heat medium to perform the heating operation, the maximum cooling speed is V 1maxd -V 2maxu 。
Setting a digital A/D converter to sample the temperature, wherein the temperature sampling value is T (k) at the time T (k), and the temperature sampling value is T (k-1) at the time T (k-1); the time interval between two samplings, i.e. the time difference deltat (k), is
Δt(k)＝t(k)-t(k-1) k＝0，1，2，3，……(1)
The difference DeltaT between the actual reaction temperature and the preset temperature in the reactor 1 is
ΔT(k)＝T(k)-T(k-1)k＝0，1，2，3，……(2)
At time k, the rate of change of temperature, i.e., the temperature rate, is
The digital A/D converter repeatedly samples the actual reaction temperature in the reactor 1, and the time interval of each sampling is consistent, i.e. the time difference deltat (k) is a constant, and is set to ts, then the formula (3) can be changed to
In the temperature rising stage, the set value of the temperature speed is V su A representation; in the cooling stage, the set value of the temperature speed is V sd A representation; the set value of the temperature rate is expressed by Vset (k) in both the temperature increasing and decreasing stages. In actual operation, the set value of the temperature speed is not higher than the temperature by Vset (k) according to the working condition of the heat exchanger80% of the maximum speed.
The control law of the temperature controller adopts an increment PID (proportion integration differentiation) formula, and at the moment k, the temperature deviation Ve of the controller is as follows:
Ve(k)＝Vset(k)-V(k) (5)
at time k, the PID position discrete equation is:
wherein u is the output value of the controller;
K P amplifying the amplification factor of the PID controller;
T I the integral time of the PID controller is in min;
T D the unit is min, which is the differential time of the PID controller;
ts is the differential time of the PID controller, and the unit is min;
from equation (6) above, at time k-1, the PID position dispersion equation is:
let the temperature control increment be Deltau, there are:
Δu(k)＝u(k)-u(k-1) (8)
in the formula, deltau is the output increment of the PID controller;
at time k, equations (6) and (7) are substituted into equation (8), respectively, and there are
The above formula (9) is a differential PID increment formula.
Is convertible by formula (8):
u(k)＝u(k-1)+Δu(k)
or (10)
u(k)＝u(0)+Δu(k)
The above formulas (9) and (10) are iterative incremental temperature control formulas.
To better eliminate temperature deviation, the stability of the system is enhanced when the temperature speed is set to V set At a speed of less than 0.2 ℃/min, the proportion is reduced, and the integral is increased, i.e. the
K P ′＝K P /α (11)
T I ′＝T I /β (12)
In the above formula, α is a reduced magnification; beta is a multiple that increases the integral effect;
substituting the above formulas (11) and (12) into formula (9) respectively yields:
the self-tuning of the parameters of the PID controller can be realized according to the temperature, so that the control precision of the temperature is ensured, the accurate control of the temperature in the reaction process of the cracking carbon five fraction device is indirectly realized, and the accurate and rapid control of the reaction temperature in the reactor 1 is realized.
Similar technical solutions can be derived from the solution content presented in connection with the figures and description, as described above. But all the solutions without departing from the structure of the present application still fall within the scope of the claims of the technical solution of the present application.
Claims (3)
1. A method for controlling the preset temperature of a reactor of a cracking carbon five fraction device is characterized by comprising the following steps: the reactor is provided with at least two groups of heat exchangers, the heat exchange areas of each group of heat exchangers are different, and each group of heat exchangers can be communicated with a cold medium with lower temperature or a heat medium with higher temperature;
according to the difference value between the actual reaction temperature and the preset temperature in the reactor, a temperature regulating valve is used for controlling each group of heat exchangers to be communicated with different media or closing the heat exchangers so as to realize the temperature step control;
the split-control process comprises a lower control stage in which the actual reaction temperature is higher than the preset temperature and an upper control stage in which the actual reaction temperature is lower than the preset temperature;
setting and adopting a digital A/D converter to sample the temperature, realizing the self-setting of parameters of the PID controller according to the temperature speed, and indirectly adjusting the communication state of each group of heat exchangers by adjusting the opening degree of a temperature regulating valve;
the PID equation for incremental temperature control is as follows,
2. the method for controlling the preset temperature of a reactor of a five-fraction cracking device according to claim 1, wherein the method comprises the following steps: the separate control process comprises an upper control stage and a lower control stage,
the upper control stage comprises a rapid temperature rise step when all heat exchangers are communicated with a heat medium, a medium speed temperature rise step when only a large area of heat exchangers are communicated with the heat medium, and a low speed temperature rise step when only a small area of heat exchangers are communicated with the heat medium;
the down-regulation control stage includes a rapid cooling step when all heat exchangers are connected to a cold medium, a medium speed cooling step when only a large area of heat exchangers are connected to a cold medium, and a low speed cooling step when only a small area of heat exchangers are connected to a cold medium.
3. The method for controlling the preset temperature of a reactor of a five-fraction cracking carbon device according to claim 1 or 2, wherein: each group of heat exchangers are uniformly distributed along the outer wall of the reactor, and communication pipelines among the heat exchangers are respectively and circularly closed and are independently arranged.
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2023
- 2023-09-20 CN CN202311213701.9A patent/CN117130406A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103775186A (en) * | 2012-10-17 | 2014-05-07 | 重庆长安汽车股份有限公司 | Automotive double-fan three-level speed control circuit and control method |
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