CN111467828B - Binary distillation tower temperature control system and method - Google Patents
Binary distillation tower temperature control system and method Download PDFInfo
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- CN111467828B CN111467828B CN202010233682.6A CN202010233682A CN111467828B CN 111467828 B CN111467828 B CN 111467828B CN 202010233682 A CN202010233682 A CN 202010233682A CN 111467828 B CN111467828 B CN 111467828B
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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
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
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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
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
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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
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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Abstract
The invention discloses a binary distillation tower temperature control system and a binary distillation tower temperature control method, which have the problems of integration and design of a binary distillation tower temperature inference control system with low, medium and high product concentrations. For binary distillation columns with medium and high product concentrations, neither the method of minimizing sensitivity and steady state deviation gives a temperature inferential control system with superior performance. The invention provides a new method for compromising the sensitivity and the minimum steady state deviation in a rectification section and selecting the temperature difference as a controlled variable in a stripping section. The former helps to achieve a balance between steady-state and dynamic behavior of the controlled tray, and the latter is able to avoid the adverse effects of stripping section pressure variations. Is effective for neutralizing a binary distillation tower with high product concentration; it is also superior to the sensitivity and steady state deviation minimization method for binary distillation columns with low product concentrations. Not only is the steady state deviation reduced, but also the dynamic deviation of the concentration of the controlled product is reduced.
Description
Technical Field
The invention relates to a comprehensive and design technology of a distillation tower temperature control system, belonging to the operation and control of a chemical process.
Background
The characteristics of strong internal coupling, complex dynamic characteristics, long lag time and the like of the distillation tower lead to high complexity of the synthesis and design of a control system, and the control effect of product quality is seriously influenced, so the research on the operation and the optimized control of the distillation tower is always a research hotspot. Although concentration control can realize deviation-free control of the purity of a controlled product, the use of a concentration measuring device can cause the defects of high investment cost, high maintenance cost, long adjusting time and the like of a control system, thereby greatly limiting the industrial application of the control system. In contrast, temperature control is widely favored in the process industry due to the advantages of low investment, high reliability, and short delay times. The design of the distillation column temperature inferential control system is relatively much more complex than direct control of product concentration. The latter not only considers the problem of pairing between the controlled variable and the manipulated variable, but also ensures that the temperature of the controlled tray has a good correspondence with the product concentration, which requires a reasonably efficient determination of the position of the controlled tray. To date, numerous methods of selecting controlled trays have been proposed by academia and industry, including: (1) a slope method, (2) a sensitivity method, (3) a singular value decomposition method, (4) a constant temperature method, and (5) a steady state deviation minimization method. Luyben has performed systematic analysis and comparison of these methods. While these methods are generally effective in determining the position of the controlled trays, they also often make it difficult for a temperature inferential control system to give the best quality of control. These drawbacks not only limit the effective use of temperature inferential control systems but also hinder the development of new distillation systems. Although the determination of controlled trays has been a relatively old problem in the field of distillation operations, it remains an important problem worth intensive research.
Disclosure of Invention
The invention researches the integration and design problems of a temperature inference control system of a binary distillation tower with different product concentrations of low, medium and high. The controlled trays selected based on the sensitivity method generally have a faster dynamic response, but only when the product concentration is low, have a good correspondence between the temperature and the product concentration. The temperature of the controlled tray selected on the basis of the method of minimum deviation from steady state generally has a good correlation with the product concentration. However, at higher product concentrations, the selected controlled trays are too close to the ends of the column, resulting in degraded dynamic characteristics in the rectifying section and very sensitive pressure variations in the stripping section, both of which reduce the quality of the temperature inferential control system. The above results show that neither the method of minimizing sensitivity and steady-state deviation consistently gives an effective structure of a binary distillation column temperature estimation control system, and it is obviously necessary to develop a systematic method which can effectively compromise the steady-state characteristics and dynamic characteristics in the rectification section and can effectively avoid the influence of pressure changes in the stripping section.
In order to achieve the above purpose, the technical scheme of the invention comprises the following steps: :
step 1: controlled trays were selected based on the sensitivity method. The operating variables varied with an amplitude of + -1% and the tray with the largest temperature variation was selected as the sensitive plate.
Step 2: and selecting the controlled tower plate based on the method of minimum steady state deviation. The basic principle of the steady state deviation minimum method is to search the controlled tower plate corresponding to the minimum steady state deviation under the condition of given disturbance combination. The objective function shown below is adopted in the present invention
J(L1,L2)＝Σi(|ΔXE|i+|ΔXB|i)
Wherein, i represents four disturbance conditions of the variation of plus or minus 20 percent of the feeding flow and the variation of plus or minus 20 percent of the feeding composition; l1 and L2 represent rectifying section and stripping section, respectivelyControlling the position of the tower plate; | Δ XE| and | Δ XBAnd | respectively represents the absolute values of steady state deviation of the discharge concentration of products at the top and the bottom of the tower. The optimization problem can be solved by a univariate search method.
Step 2.1: taking the tray obtained by the sensitivity analysis method as an initial value, only changing the position of the L1 tray, keeping the position of the L2 tray unchanged, and adjusting the positions of the controlled trays one by one to enable the tray with the minimum target function J to serve as a search plate of L1;
step 2.2: changing the position of the L2 tray, searching the tray which minimizes the target function J and using the tray as a search plate of L2;
step 2.3: after completing one round of search, a new round of search is performed from the beginning until the tray of the target function J reaching the minimum value is selected as the optimal search tray.
And step 3: the invention makes corresponding improvement on the method for minimizing the steady state deviation, compromises the controlled tower plates obtained based on the method for minimizing the sensitivity and the steady state deviation in the rectification section, and selects the temperature difference as the controlled variable in the stripping section.
Step 3.1: in the rectification section, in order to compromise and balance the steady-state and dynamic characteristics thereof, the controlled plates are selected between the sensitive plate (based on the sensitivity method) and the optimal search plate (based on the steady-state deviation minimum method);
step 3.2: in the stripping section, the controlled variable is selected as the temperature difference between the optimum search plate and its adjacent tray in order to effect an effective compensation of the pressure variations.
The method provided by the invention has the following advantages:
1. the method can provide a temperature inference control system with excellent performance for a binary distillation tower with three different product concentrations, namely low, medium and high.
2. The method can effectively compromise the steady-state characteristic and the dynamic characteristic in the rectifying section and can effectively avoid the influence of pressure change in the stripping section. Compared with the design method with the minimum sensitivity and steady-state deviation, the steady-state deviation is reduced more, and the dynamic deviation of the concentration of the controlled product is also reduced.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate an embodiment of the invention and, together with the description, serve to explain the invention and not to limit the invention.
FIG. 1 is a steady state configuration of an ethanol/butanol binary distillation column with low, medium, and high product concentrations.
FIG. 2 is a temperature inferential control system based on a sensitivity analysis method.
FIG. 3 is a temperature inferential control system based on a steady state deviation minimization method.
FIG. 4 is the closed loop response of example I after a step change of. + -. 20% in the composition of the ethanol feed.
FIG. 5 is the closed loop response of example I after a step change of the feed flow rate of + -20%.
FIG. 6 is the closed loop response of example II after a step change of. + -. 20% in the composition of the ethanol feed.
FIG. 7 is the closed loop response of example II after a step change of the feed flow rate by + -20%.
FIG. 8 is a graph of the closed loop response of example III after a step change of. + -. 20% in the composition of the ethanol feed.
FIG. 9 is a graph of the closed loop response of example III after a step change of + -20% in feed flow rate.
Fig. 10 shows a temperature estimation control system based on the new method.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention takes a simple distillation column for separating binary ethanol (E)/butanol (B) mixture as an example, and studies the integration and design problems of its temperature inference control system under steady state operating conditions with low, medium and high product concentrations, and further describes the present invention with reference to the accompanying drawings. Fig. 1 shows the steady state configuration of these three systems. The top product has the same purity as the bottom product, with low, medium and high concentration specifications of 95% mol (example I), 99% mol (example II) and 99.9% mol (example III), respectively.
The reflux ratio of the three distillation columns is about 1.0 and far less than 3.0, so the discharge flow (D) at the top of the column and the heat of the reboilerLoad (Q)reb) It is preferably selected as the system operating variable, and the liquid levels of the condenser and reboiler are controlled by reflux flow and bottom discharge flow, respectively. The resulting temperature inferential control system based on the sensitivity analysis method is shown in fig. 2, labeled CS1 in the present invention. For example I (FIG. 2a), the sensitive plates are the 3 rd and 28 th trays. For example II (FIG. 2b), the sensitive plates are the 5 th and 26 th trays. For example III (FIG. 2c), the sensitive plates are the 8 th and 22 nd trays.
The inferred temperature control system based on the steady state deviation minimization method is shown in fig. 3 and is labeled CS2 in the present invention. It can be seen that the best search boards for these three systems all appear on the 2 nd and 29 th trays, i.e., the topmost and bottommost trays.
To test the effectiveness of the method of minimizing sensitivity and steady state deviation, the quality of the closed loop operation of the ethanol/butanol binary distillation column must be analyzed and compared. FIG. 4 shows the closed loop response of example I when the ethanol feed composition is varied in steps by. + -. 20%. Black indicates positive perturbations and grey indicates negative perturbations. Although CS2 has a slightly larger dynamic deviation than CS1, its steady state deviation is smaller. FIG. 5 shows the closed loop response of example I after a step change of. + -. 20% in the feed flow. It can be seen that CS2 and CS1 have very close steady state and dynamic qualities. Combining the two cases, it can be seen that although CS2 is slightly better than CS1, the two still have very close dynamic qualities. In other words, the sensitivity and steady state deviation minimization method has similar performance for ethanol/butanol binary distillation column control with low product concentration.
FIG. 6 shows the closed loop response of example II after a step change of. + -. 20% in the ethanol feed composition. Although CS2 still has smaller steady-state deviation than CS1, the dynamic quality of the tower top product is obviously deteriorated by the CS2, the dynamic deviation of the tower top product is obviously increased for positive disturbance, and a stronger oscillation phenomenon also occurs for negative disturbance. FIG. 7 shows the closed loop response of example II after a step change of. + -. 20% in the feed flow. Compared with CS1, CS2 significantly deteriorates the dynamic quality of the overhead product, resulting in not only greater dynamic deviation but also a more severe oscillation phenomenon. For the bottoms product, CS2 not only causes large dynamic deviations but also large steady state deviations. Combining the two cases, it can be seen that as the product concentration increases, although the dynamic quality of CS1 and CS2 decreases, CS2 is more sensitive to this change and is difficult to compare with CS 1.
FIG. 8 shows the closed loop response of example III after a step change of. + -. 20% in the ethanol feed composition. In this case, CS2 is not comparable to CS1, and the dynamic quality thereof is further deteriorated. For the overhead product, CS2 makes it subject to large deviations and severe hunting. For the bottom product composition, CS2 makes it appear very large dynamic and steady state deviations in the case of a positive disturbance. FIG. 9 shows the closed loop response of example III after a step change of + -20% in the feed flow. In this case, CS2 is also difficult to compare with CS1, and the dynamic quality thereof is further deteriorated. For the product at the top of the tower, not only large deviation exists, but also serious divergence oscillation phenomenon exists; for the bottoms product, very large dynamic and steady state deviations also occur at positive perturbations. Combining the two cases, it can be seen that as the product concentration is further increased, although the dynamic qualities of both CS1 and CS2 are reduced, CS2 is more sensitive to this change and it is already difficult in some cases to maintain stable operation.
Analysis and comparison of the temperature inferential control of three ethanol/butanol binary distillation columns with low, medium, and high product concentrations shows that the performance of the temperature inferential control system based on the method of sensitivity and steady state deviation minimization is closely related to product concentration. Since the sensitivity method mainly considers the dynamic characteristics of the system, CS1 generally has faster dynamic response, but can only keep the controlled tray temperature and the product concentration in good correspondence when the product concentration is lower. Since the steady state deviation minimization method only considers the steady state characteristics of the system, the controlled tray temperature of CS2 generally has a good correspondence with product concentration. However, when the product concentration is high, CS2 cannot make the composition of the product at the top and the bottom have small steady-state deviation. This phenomenon indicates that changes in feed flow and composition at higher product concentrations can significantly change the steady state and dynamic characteristics of the system, and therefore, to achieve a tight inferred control of product composition, changes in system characteristics must be compensated for as necessary.
In order to achieve a strict inferential control of the product composition, the proposed method based on the present invention results in a temperature inferential control system as shown in fig. 10, labeled as CS3 in the present invention. It can be seen that in the rectification section, the controlled plate is chosen between the top plate and the sensitive plate in order to compromise and balance the steady-state characteristics with the dynamic characteristics; in the stripping section, the controlled variable is selected as the temperature difference between the two bottom trays in order to effect an effective compensation of the pressure variations.
FIG. 4 also shows the closed loop response of example I to a step perturbation of. + -.20% ethanol feed composition under the action of CS 3. CS3 has slightly less dynamic and steady state deviations for the overhead product than CS 1; for the bottom product CS3, there is a greater plateau at negative perturbations than CS 1. FIG. 5 also shows the closed loop response of example I to a step disturbance of + -20% feed flow with CS 3. For the overhead product, both CS3 and CS1 have very similar qualities; for the bottoms product, CS3 has less dynamic and steady state deviations than CS 1. Combining the two above, it can be seen that CS3 has a better quality than CS1 for the overhead product. For the bottoms product, while CS3 was slightly inferior to CS1 in overcoming the negative perturbation in the feed composition, CS3 was significantly superior to CS1 for the other perturbations. Thus, in summary, CS3 is superior to CS 1.
FIG. 6 also shows the closed loop response of example II to a step perturbation of. + -. 20% ethanol feed composition under the action of CS 3. For the overhead product CS3, the overhead product CS1 has slightly larger overhead dynamic deviation, but the steady state deviation is smaller; for the bottoms product, CS3 has less dynamic and steady state deviations than CS 1. FIG. 7 also shows the closed loop response of example II to a ± 20% step disturbance in feed flow with CS 3. For the overhead product, CS3 and CS1 have very close dynamic and steady state performance; the former has smaller steady state and dynamic deviations than the latter for the bottoms product. Combining the two cases, it can be seen that the dynamic quality of CS3 is slightly inferior to that of CS1, but the steady-state quality is significantly better than that of CS1 for the overhead product. For the bottoms product, CS3 is significantly better than CS1, both in dynamic and steady state performance. Thus, for example II, CS3 outperformed CS 1.
FIG. 8 also shows the closed loop response of example III in the face of a step disturbance of. + -. 20% ethanol feed composition under the action of CS 3. For the overhead product, although the dynamic deviation of CS3 is slightly larger than that of CS1, the steady-state deviation is obviously reduced; for the bottoms product, both the dynamic deviation and the steady state deviation are significantly reduced for CS3 compared to CS 1. FIG. 9 also shows the closed loop response of example III to a step disturbance of + -20% feed flow with CS 3. For the overhead product, CS3 and CS1 have very similar qualities; for the bottom product, CS3 has better dynamic and steady state performance than CS 1. Combining the two cases, it can be seen that the superiority of CS3 becomes more obvious as the product concentration is further increased. Thus, for example III, CS3 also outperformed CS 1.
It should be noted that the above description is only a specific embodiment of the invention, and they are not intended to limit the invention, but also to apply to a binary distillation column for separating other mixtures. Various changes or modifications may be made by those skilled in the art within the scope of the claims provided they are within the spirit and scope of the invention as defined and defined by the appended claims.
Claims (1)
1. A binary distillation tower temperature control method is characterized in that: the method comprises the following steps of,
step 1: selecting a controlled column plate based on a sensitivity method; the operating variable is changed in the range of +/-1%, and the tower plate with the largest temperature change is selected as a sensitive plate;
step 2: selecting a controlled tower plate based on a steady state deviation minimum method; the basic principle of the steady state deviation minimum method is to search the controlled tower plate corresponding to the minimum steady state deviation under the condition of given disturbance combination; using an objective function as shown below
J(L1,L2)＝Σi(|ΔXE|i+|ΔXB|i)
Wherein i represents a feed flow variation of + -20% and a feed composition variationPlus or minus 20% of four disturbance conditions; l1 and L2 represent the positions of the controlled trays of the rectifying section and the stripping section respectively; | Δ XE| and | Δ XBI respectively represents the absolute values of steady state deviation of the discharge concentration of products at the top and the bottom of the tower; solving by a univariate search method;
and step 3: correspondingly improving the steady state deviation minimum method, compromising the controlled tower plate obtained based on the sensitivity and steady state deviation minimum method in the rectification section, and selecting the temperature difference as a controlled variable in the stripping section;
the specific implementation in step 2 is as follows, step 2.1: taking the tray obtained by the sensitivity analysis method as an initial value, only changing the position of the L1 tray, keeping the position of the L2 tray unchanged, and adjusting the positions of the controlled trays one by one to enable the tray with the minimum target function J to serve as a search plate of L1;
step 2.2: changing the position of the L2 tray, searching the tray which minimizes the target function J and using the tray as a search plate of L2;
step 2.3: after one round of search is finished, carrying out a new round of search from the beginning until the tower plate of which the target function J reaches the minimum value is selected as a search plate;
the specific implementation process of the step 3 is as follows, and the step 3.1: in the rectification section, the steady-state characteristic and the dynamic characteristic are compromised and balanced, and a controlled tower plate is selected between a sensitive plate and a search plate;
step 3.2: in the stripping section, effective compensation for pressure variations is implemented, the controlled variable being selected as the temperature difference between the search plate and its adjacent tray.
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