CN114247169A - Dynamic control scheme for process of bulkhead rectifying tower with middle and lower partitions - Google Patents
Dynamic control scheme for process of bulkhead rectifying tower with middle and lower partitions Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 43
- 230000008569 process Effects 0.000 title claims abstract description 33
- 238000005192 partition Methods 0.000 title claims description 15
- 239000000203 mixture Substances 0.000 claims abstract description 40
- 239000000047 product Substances 0.000 claims description 35
- 239000007788 liquid Substances 0.000 claims description 18
- 238000010992 reflux Methods 0.000 claims description 13
- 239000012071 phase Substances 0.000 claims description 12
- 239000007791 liquid phase Substances 0.000 claims description 10
- 239000006227 byproduct Substances 0.000 claims description 8
- 238000004821 distillation Methods 0.000 claims description 4
- 230000035945 sensitivity Effects 0.000 claims description 2
- 238000004886 process control Methods 0.000 claims 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 abstract description 18
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 abstract description 18
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 abstract description 18
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 abstract description 9
- 230000000694 effects Effects 0.000 abstract description 4
- 238000000926 separation method Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 230000008859 change Effects 0.000 description 4
- 230000008878 coupling Effects 0.000 description 4
- 238000010168 coupling process Methods 0.000 description 4
- 238000005859 coupling reaction Methods 0.000 description 4
- 239000012467 final product Substances 0.000 description 4
- 230000004044 response Effects 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 238000004540 process dynamic Methods 0.000 description 3
- 230000000087 stabilizing effect Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000009412 basement excavation Methods 0.000 description 1
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- 230000009467 reduction Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/141—Fractional distillation or use of a fractionation or rectification column where at least one distillation column contains at least one dividing wall
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4211—Regulation; Control of columns
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4211—Regulation; Control of columns
- B01D3/4294—Feed stream
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Abstract
The invention provides a dynamic control scheme of a process of a bulkhead rectifying tower for separating isopentane, n-pentane and n-hexane. This flow separates through next door rectifying column, and control circuit includes in this control scheme: the process can not only ensure that the product is thoroughly separated and the product purity reaches the aim of high purity, but also has good control effect under the disturbance of +/-10% of the feeding flow and the feeding composition, and the product purity can reach the original set value.
Description
Technical Field
The invention belongs to the field of chemical rectification process and automatic control, and relates to a dynamic control scheme of a process of a bulkhead rectifying tower with a partition plate at the middle lower part.
Background
Rectification technology is one of the most widely used separation technologies in the chemical and petrochemical industries. However, the energy consumption of the rectification process is up to 40% in the chemical industry. With the increasing reduction of non-renewable energy sources, in order to save energy consumption, deep excavation of energy-saving potential of the rectification process and improvement of thermodynamic efficiency become one of the problems which need to be solved urgently by modern process industries. The bulkhead rectifying tower is one of the most important ways of strengthening the process, and is widely researched by scholars at home and abroad.
Due to the high coupling between the coupled streams of the dividing wall tower, the interaction among all variables is more complicated, the number of manipulated variables and the number of controlled variables are increased, and the dynamic control of the method is always an important problem for preventing the rapid development of the industry. The manipulated variables in the dividing wall tower mainly comprise: condenser heat load, gas phase flow from the pre-dividing tower to the main tower, reboiler heat load, main tower top reflux, side draw flow, liquid phase flow from the pre-dividing tower to the main tower, gas phase flow from the pre-dividing tower to the main tower, main tower top draw flow, and main tower bottom draw flow. The control variables mainly include: the system comprises a pre-dividing tower top pressure, a main tower bottom product purity, a main tower top product purity, a main tower side product purity, a pre-dividing tower kettle liquid level, a main tower reflux tank liquid level, a main tower kettle liquid level, heavy component concentration from the pre-dividing tower to the main tower, a temperature sensitive tower plate in the pre-dividing tower and a temperature sensitive tower plate in the main tower. The control effect of the process can be effectively improved by controlling the gas ideal distribution ratio and the liquid phase distribution ratio among the coupled streams, and the process has a good energy-saving effect. In the design, a control loop for controlling coupling stream intervals and composition control of a main tower product are combined, and a tower bottom temperature-composition cascade control loop, when the feeding flow or the feeding composition is greatly disturbed, the control effect can still enable the product to return to the original set value in a short time and with small overshoot, and the product purity has no deviation value.
Disclosure of Invention
The invention aims to solve the problems of difficult control of the bulkhead rectifying tower, poor stability, product quality requirement and the like. The method aims to provide a partition wall rectifying tower process dynamic control scheme with a partition plate at the middle lower part, and after the feeding flow or the feeding composition is greatly disturbed (plus or minus 10 percent), the product purity returns to the original set value through a short time and a small overshoot, so that the purity of three products reaches 98 percent, 96 percent and 98 percent. In addition, the invention has simple control structure, easy operation and great application prospect.
In order to achieve the purpose of the invention, the invention adopts the following technical scheme:
the dynamic control scheme of the process of the bulkhead rectifying tower based on the middle lower part of the bulkhead mainly comprises the following control loops: the control method of the feed flow control, the tower top pressure control, the liquid level control, the control of the gas phase distribution ratio and the liquid phase distribution ratio, the composition control and the tower bottom temperature-composition cascade control loop comprises the following steps:
(1) the feed flow control loop comprises a flow controller used for controlling the feed flow entering the pre-dividing tower;
(2) the top pressure control loop comprises a pressure controller which is used for controlling the flow of the top of the pre-dividing tower entering the main tower and controlling the heat load of the condenser at the top of the main tower. The pressure controller controls the top pressure of the pre-dividing tower and the top pressure of the main tower, and automatically adjusts the flow entering the main tower from the top of the pre-dividing tower and the heat load of a condenser at the top of the main tower according to the pressure;
(3) the liquid level control loop comprises a flow controller, a liquid level control unit and a liquid level control unit, wherein the flow controller is used for controlling the flow entering the main tower from the bottom of the pre-dividing tower, the flow controller is used for controlling the top output quantity of the main tower, and the flow controller is used for controlling the bottom output quantity of the main tower;
(4) the control loop of the gas phase distribution ratio and the liquid phase distribution ratio comprises a flow controller for controlling the liquid phase flow from the main tower to the pre-dividing tower and a temperature controller for controlling the temperature in the pre-dividing tower. The temperature controller automatically adjusts the gas phase flow entering the pre-dividing tower according to the temperature of the sensitive plate of the pre-dividing tower;
(5) the composition control loop comprises a flow controller used for controlling the flow of a side product and a composition controller used for controlling the reflux quantity of the top of the main tower, wherein the composition controller is used for controlling the purity of the top product and responding to the reflux quantity of the top of the main tower;
(6) the temperature-composition cascade control loop comprises a temperature controller for controlling the heat load of a reboiler at the bottom of the main tower and a composition controller for controlling a set temperature value. The temperature controller automatically adjusts the heat load of the reboiler at the bottom of the tower according to the temperature of the sensitive plate of the main tower, and the composition controller adjusts the purity of the product at the bottom of the tower according to the set temperature value of the temperature controller.
In the technical scheme, the feeding flow control loop controls the feeding flow entering the tower by controlling the opening degree of the valve.
In the technical scheme, the top pressure of the pre-dividing tower is controlled by controlling the flow from the top of the pre-dividing tower to the main tower through the pressure control loop at the top of the pre-dividing tower and the main tower, and the top pressure of the main tower is controlled by controlling the heat load of the condenser at the top of the main tower.
In the technical scheme, the liquid levels of the reflux tanks at the bottom and the top of the main tower of the pre-dividing tower and the liquid level control loops at the bottom of the tower are controlled by controlling the flow from the bottom of the pre-dividing tower to the main tower, the liquid level of the reflux tank at the top of the main tower is controlled by controlling the product yield at the top of the main tower, and the liquid level at the bottom of the main tower is controlled by controlling the product yield at the bottom of the main tower. The basic control loop of the process is controlled to ensure the conservation of the quality and materials in the tower.
In the technical scheme, the control loop of the gas phase distribution ratio and the liquid phase distribution ratio controls the concentration of heavy components from the top of the pre-dividing tower to the main tower by controlling the flow from the top of the pre-dividing tower to the main tower, and controls the temperature in the pre-dividing tower by controlling the flow from the main tower to the pre-dividing tower.
In the technical scheme, the side product extraction of the main tower and the extraction of the tower top product form a control loop, the purity of the side product is controlled by controlling the extraction amount of the side product, and the purity of the tower bottom product is controlled by controlling the reflux amount of the tower top of the main tower.
In the technical scheme, the temperature extracted from the product at the bottom of the main tower forms a cascade control loop, the temperature sensitive plate in the main tower is controlled by operating the heat load of the reboiler, and the purity of the product at the bottom of the main tower is controlled.
In the above technical solution, the control loop adopts a PID control signal and a controller.
In the above technical solution, the position of the sensitive plate in the temperature control loop is determined by a sensitivity criterion method. The method is to make a small change (e.g. 0.1% of the set value) in a certain manipulated variable (e.g. reboiler heat load), examine the temperature change of each tray and find the tray with the largest temperature change. For other manipulated variables (e.g., coupled stream gas phase flow), the process can be repeated.
In the technical scheme, the temperature and the tuning parameters of the controller in the composition control loop are carried out by adopting a Tyreus-Luyben method.
In the technical scheme, after the feeding flow or the feeding composition is changed, the control loops act together, so that the product purity returns to the original set value in a short time with small overshoot, and the product purity has no deviation value with the set value.
Drawings
FIG. 1 is a schematic process flow diagram of a bulkhead rectifying tower with a middle and lower partition according to the present invention.
Fig. 1 is an equivalent flow diagram of a process flow of a bulkhead rectifying tower, which is divided into a PRE-dividing tower and a MAIN tower, PRE is the PRE-dividing tower, MAIN is the MAIN, M1 is the condenser at the top of the MAIN tower, M2 is the reflux drum at the top of the MAIN tower, and M3 is the reboiler at the bottom of the MAIN tower. The fresh stream F is fed from 18 trays of the pre-dividing tower, the coupling positions of the pre-dividing tower and the main tower are at 41 th and 95 th blocks, the coupling streams are L1, V1, L2 and V2, the main tower comprises 98 trays in total, saturated gas at the top of the tower completely condenses through a condenser and then enters a reflux tank M2, one part of condensate R enters from the top of the main tower, the other part of condensate R is taken out as a light component product D, a side product S is taken out from the 86 th tray of the main tower, and a heavy component product is taken out from a bottom stream B.
FIG. 2 is a schematic diagram of a process dynamics control scheme for a bulkhead distillation column with a middle lower portion as described in example 1.
In fig. 2, FC is a feed flow controller, PC1 and PC2 are pressure controllers, LC1, LC2 and LC3 are liquid level controllers, CC2 and CC3 are component controllers, TC is a temperature controller, and TC 3-CC 3 are temperature-component cascade controllers.
FIG. 3 is a graph of the dynamic response of three product purities after a + -10% perturbation in feed flow as described in example 1.
FIG. 4 is a graph of the dynamic response of three product purities after. + -. 10% perturbation of isopentane feed composition as described in example 2.
FIG. 5 is a graph of the dynamic response of three product purities after n-pentane. + -. 10% perturbation of the feed composition as described in example 3.
FIG. 6 is a graph of the dynamic response of three product purities after n-hexane. + -. 10% perturbation of the feed composition as described in example 4.
Detailed Description
The dynamic control scheme of the dividing wall rectifying tower process with the dividing wall at the middle lower part is further described in the following by combining the drawings and specific examples in the specification, and the invention is not limited to the scope of the invention.
Example 1
Dynamic control scheme for process of bulkhead rectifying tower with middle and lower partitions
FIG. 2 is a schematic diagram of a process dynamics control scheme for a dividing wall distillation column with a dividing wall in the middle and lower parts. Taking separation of a ternary mixture of isopentane, n-pentane and n-hexane as an example, the light component isopentane is extracted from the top of the main tower, the middle component n-pentane is extracted from the lateral line, and the heavy component n-hexane is extracted from the bottom of the main tower. The process flow diagram is shown in figure 1. The control loop of the invention is as follows:
(1) the feed flow control loop comprises a flow controller used for controlling the feed flow entering the pre-dividing tower;
(2) the top pressure control loop comprises a pressure controller which is used for controlling the flow of the top of the pre-dividing tower entering the main tower and controlling the heat load of the condenser at the top of the main tower. The pressure controller controls the top pressure of the pre-dividing tower and the top pressure of the main tower, and automatically adjusts the flow entering the main tower from the top of the pre-dividing tower and the heat load of a condenser at the top of the main tower according to the pressure;
(3) the liquid level control loop comprises a flow controller, a liquid level control unit and a liquid level control unit, wherein the flow controller is used for controlling the flow entering the main tower from the bottom of the pre-dividing tower, the flow controller is used for controlling the top output quantity of the main tower, and the flow controller is used for controlling the bottom output quantity of the main tower;
(4) the control loop of the gas phase distribution ratio and the liquid phase distribution ratio comprises a flow controller for controlling the liquid phase flow from the main tower to the pre-dividing tower and a temperature controller for controlling the temperature in the pre-dividing tower. The temperature controller automatically adjusts the gas phase flow entering the pre-dividing tower according to the temperature of the sensitive plate of the pre-dividing tower;
(5) the composition control loop comprises a flow controller used for controlling the flow of a side product and a composition controller used for controlling the reflux quantity of the top of the main tower, wherein the composition controller is used for controlling the purity of the top product and responding to the reflux quantity of the top of the main tower;
(6) the temperature-composition cascade control loop comprises a temperature controller for controlling the heat load of a reboiler at the bottom of the main tower and a composition controller for controlling a set temperature value. The temperature controller automatically adjusts the heat load of the reboiler at the bottom of the tower according to the temperature of the sensitive plate of the main tower, and the composition controller adjusts the purity of the product at the bottom of the tower according to the set temperature value of the temperature controller.
Example 2
The dynamic control scheme of the process of the bulkhead rectifying tower with the partition plate of the control structure in the middle lower part in the embodiment 1 is adopted, and the separation of isopentane, n-pentane and n-hexane is taken as an example. After the process runs smoothly for 1h, the feed flow rate changes by + -10% from the original 300kmol/h to 330kmol/h or 270kmol/h, and as can be seen from fig. 3, the product purity returns to the original set value under the disturbance of flow rate + -10% in a short time and with small overshoot by the action of the control loop. The maximum overshoot is not more than 0.005, the maximum time is not more than 7h, and the final product purity returns to the set value, which shows that the control loop can well cope with the disturbance within +/-10%, and has better robustness and stability.
Example 3
The dynamic control scheme of the process of the bulkhead rectifying tower with the partition plate of the control structure in the middle lower part in the embodiment 1 is adopted, and the separation of isopentane, n-pentane and n-hexane is taken as an example. After the process had run smoothly for 1 hour, the feed composition isopentane was changed by 10% with mole fraction from 0.33 to 0.363 or 0.297 as shown in fig. 4. by the control loop, the product purity returned to the original set value with a short time and small overshoot at a composition of 10% upset. The maximum overshoot is not more than 0.002, the stabilizing time is 7h at most, and the final product purity returns to a set value, so that the control loop can well cope with disturbance within +/-10%, and has better robustness and stability.
Example 4
The dynamic control scheme of the process of the bulkhead rectifying tower with the partition plate of the control structure in the middle lower part in the embodiment 1 is adopted, and the separation of isopentane, n-pentane and n-hexane is taken as an example. After the process had run smoothly for 1h, the feed composition n-pentane had changed by 10% and the mole fraction changed from 0.33 to 0.363 or 0.297, as can be seen from fig. 5, by the action of the control loop, the product purity returned to the original set point with a short time and small overshoot at a composition of 10% disturbance. The maximum overshoot is not more than 0.003, the stabilizing time is about 7h, and the final product purity returns to a set value, which shows that the control loop can well cope with disturbance within +/-10%, and has better robustness and stability.
Example 5
The dynamic control scheme of the process of the bulkhead rectifying tower with the partition plate of the control structure in the middle lower part in the embodiment 1 is adopted, and the separation of isopentane, n-pentane and n-hexane is taken as an example. After the process runs stably for 1h, the n-hexane composition of the feed is changed by +/-10%, the mole fraction is changed from the original 0.34 to 0.374 or 0.306, and as can be seen from figure 6, the product purity returns to the original set value under the disturbance of +/-10% of the composition in a short time and with small overshoot by the action of a control loop. The maximum overshoot is not more than 0.003, the stabilizing time is about 7h, and the final product purity returns to a set value, which shows that the control loop can well cope with disturbance within +/-10%, and has better robustness and stability.
It should be understood by those skilled in the art that the dynamic control scheme of the dividing wall rectifying tower process with the dividing wall at the middle lower part can be realized by using the control structure and the control method based on the control structure. Under the disturbance of the feeding flow and the feeding composition, the product purity can be returned to the original set value, and the method is also suitable for the stable control of other ternary mixing systems.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not intended to limit the present invention in any way, so that any person skilled in the art can modify or change the technical content of the above disclosure into an equivalent embodiment with equivalent changes. Any modification, equivalent replacement, improvement and the like of the present invention without departing from the spirit and scope of the present invention shall be included in the protection scope of the present invention.
Claims (6)
1. The dynamic control scheme of the process of the bulkhead rectifying tower with the bulkhead at the middle lower part comprises the following control loops:
(1) a feed flow control loop for controlling the feed flow into the column using a flow controller;
(2) the top pressure control loop comprises a pressure controller which is used for controlling the flow of the top of the pre-dividing tower entering the main tower and controlling the heat load of the condenser at the top of the main tower. The pressure controller controls the top pressure of the pre-dividing tower and the top pressure of the main tower, and automatically adjusts the flow entering the main tower from the top of the pre-dividing tower and the heat load of a condenser at the top of the main tower according to the pressure;
(3) the liquid level control loop comprises a flow controller, a liquid level control unit and a liquid level control unit, wherein the flow controller is used for controlling the flow entering the main tower from the bottom of the pre-dividing tower, the flow controller is used for controlling the top output quantity of the main tower, and the flow controller is used for controlling the bottom output quantity of the main tower;
(4) the control loop of the gas phase distribution ratio and the liquid phase distribution ratio comprises a flow controller for controlling the liquid phase flow from the main tower to the pre-dividing tower and a temperature controller for controlling the temperature in the pre-dividing tower. The temperature controller automatically adjusts the gas phase flow entering the pre-dividing tower according to the temperature of the sensitive plate of the pre-dividing tower, so that the gas phase distribution ratio is changed;
(5) the composition control loop comprises a flow controller used for controlling the flow of a side product and a composition controller used for controlling the reflux quantity of the top of the main tower, wherein the composition controller is used for controlling the purity of the top product and responding to the reflux quantity of the top of the main tower;
(6) the temperature-composition cascade control loop comprises a temperature controller for controlling the heat load of a reboiler at the bottom of the main tower and a composition controller for controlling a set temperature value. The temperature controller automatically adjusts the heat load of the reboiler at the bottom of the tower according to the temperature of the sensitive plate of the main tower, and the composition controller adjusts the purity of the product at the bottom of the tower according to the set temperature value of the temperature controller.
2. The dynamic control scheme of the process of the dividing wall rectifying tower with the middle and lower partition plates as claimed in claim 1, wherein PID control signals and a controller are adopted in the control loop.
3. The dynamic control scheme for the process of the dividing wall rectifying tower with the middle and lower part being provided with the partition plates as claimed in claim 1, wherein the purity of the separated products is 98%, 96% and 98% respectively.
4. The dynamic control scheme for a process in a dividing wall distillation column with a middle-lower partition wall as claimed in claim 1, wherein the position of the sensitive plate in the temperature control loop is determined by a sensitivity criterion method.
5. The dynamic process control scheme for a divided wall distillation column with middle and lower partition walls as claimed in claim 1, wherein the tuning parameters of the temperature and composition controllers in the control loop are carried out by the Tyreus-Luyben method, and the tuning sequence is bottom, top and side.
6. The dynamic control scheme of claim 1, wherein the control loops work together to return the product purity to the original set value after the feed flow rate and feed composition are changed.
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2022
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| US20060137967A1 (en) * | 2002-12-04 | 2006-06-29 | Henry Kister | Distillation systems |
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