CN107837552A - The operation of rectifying tower with bulkhead and control method - Google Patents
The operation of rectifying tower with bulkhead and control method Download PDFInfo
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- CN107837552A CN107837552A CN201610831227.XA CN201610831227A CN107837552A CN 107837552 A CN107837552 A CN 107837552A CN 201610831227 A CN201610831227 A CN 201610831227A CN 107837552 A CN107837552 A CN 107837552A
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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
- B01D3/14—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
-
- 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
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
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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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- 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
- B01D3/4205—Reflux ratio control splitter
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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
- B01D3/4211—Regulation; Control of columns
- B01D3/4255—Head-, side-, bottom- and feed stream
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of operation of rectifying tower with bulkhead and control method, mainly solve that conventional rectifying tower with bulkhead operational control is difficult, stability is bad and product quality and the uppity technical problem of yield.The present invention is by using to five control areas of rectifying tower with bulkhead：Feedstock control area, overhead reflux and extraction control area, liquid are collected and distribution control area, side take-off control area and tower reactor produce the technical scheme that temperature, flow and liquid level in control area are controlled and preferably solve above-mentioned technical problem, available in the industrial production of rectifying tower with bulkhead.
Description
Technical field
The present invention relates to a kind of operation of rectifying tower with bulkhead and control method, the industrial production available for rectifying tower with bulkhead
In.
Background technology
Rectifying is most ripe, most widely used a kind of isolation technics in petrochemical industry production, but distillation process energy consumption is huge
Greatly, it is estimated that, 40~70% energy consumption is used to separate in chemical process, and energy consumption of rectification accounts for therein 95%.In order to reduce essence
The energy consumption of process is evaporated, researcher both domestic and external conducts extensive research, and rectifying tower with bulkhead is as a kind of typical rectifying section
Energy equipment or process intensification power-saving technology are of great interest.
Rectifying tower with bulkhead is by installing the vertical partition plate of one or more certain length in a rectifying column or band inclines
The dividing plate of rake angle, using a set of vaporization and condensation system, while the product of isolated three kinds or more.Due to only having one
Vaporization and condensation system is covered, and avoids and is remixed using intermediate species during multitower rectifying, therefore bulkhead distillation technology is than passing
The distillation technology investment reduction 20~30% of system, energy consumption reduce by 20~40%.
In fact, most early in nineteen thirty, Eeic W.Luster (US1915681) are just because the separation of cracking gas proposes point
The concept of wall rectifying column, but until 1985 First rectifying tower with bulkhead (BASF) just put into industrial production, so far also only have 200
More rectifying tower with bulkhead are in commercial Application, it is difficult to are widely popularized, basic reason therein is except lacking reliable structure
Design is outer, and it is also the crucial point that can not be ignored that rectifying tower with bulkhead has larger difficulty in operation and control aspect.
By taking the rectifying tower with bulkhead for being most commonly used for three components separation as an example, dividing plate is axially placed along tower, by bulkhead rectifying
Tower is divided into public rectifying section more than dividing plate, the public stripping section below dividing plate, and the bulkhead section where dividing plate, according to charging
With the difference of intermediate species extraction, bulkhead section is divided into feed side and product side again.Therefore, compared with conventional rectification tower, bulkhead essence
Evaporate particularity of the tower due to its structure, the free degree is more, except with conventional rectification tower identical technological parameter, as operating pressure,
Cooling and heating load, reflux ratio, product produced quantity etc., rectifying tower with bulkhead also including sideline product extraction and dividing plate both sides gas phase and
The distribution condition of liquid phase, also, highly coupled between above-mentioned technological parameter, change it is therein any one can be to other specification
Operation brings direct influence, such as the change of overhead reflux liquid measure not only to influence overhead product quality, also directly changes public
Rectifying section bottom distillates the total amount of liquid, in the case of fixed both sides liquid phase distribution ratio, directly affects point of demarcation strip both sides
With liquid measure, and the change of both sides distribution liquid measure, and by the pre-separation effect for directly affecting bulkhead section feeding side and the side of product side
Line product quality；In the case that if in both sides, distribution liquid measure is fixed, then the change of overhead reflux liquid measure will be destroyed directly in tower
Material balance, influence mass transfer, heat transfer and vapor liquid equilibrium process, therefore, in rectifying tower with bulkhead between technological parameter height coupling
And chain reaction can significantly affect product quality and the stable operation control of rectifying tower with bulkhead, and this is also exactly that rectifying tower with bulkhead is difficult
It is the research emphasis and difficult point of rectifying tower with bulkhead development process to realize the immediate cause of stability contorting.
At present, the publication in terms of rectifying tower with bulkhead operational control is less, and one is disclosed in CN102631791A
The control method of kind rectifying tower with bulkhead, mainly in 3 control methods (Operation of of E.A.Wolff et al.
integrated three-product (Petlyuk)distillation columns,E.A.Wolff,S.Skogestad,
Ind.Eng.Chem.Res.,1995,34(6):2094-2103) on the basis of, a control loop has been increased newly, i.e., in adjusting tower
Push up capacity of returns control tower top product purity, regulation side take-off amount control sideline product purity, regulation tower reactor quantity of steam control tower
On the basis of kettle product purity, add and control feed side top by adjusting the liquid phase distribution ratio of rectifying tower with bulkhead dividing plate both sides
Heavy constituent content in portion's ascending vapor.Although it has all carried out corresponding control, tower top and tower reactor product to product quality
Load do not control, each product yield including sideline product can not ensure, meanwhile, the liquid in multiple regions in tower
Position, such as overhead reflux region, public rectifying section bottom liquid is collected and distribution region, and tower reactor region is not done control and said
It is bright, it is difficult to ensure the material balance and stability contorting of rectifying tower with bulkhead.
Obviously, control method of the prior art can not ensure to ensure product yield while product quality, can not realize
Stable operation, therefore, it is necessary to more efficiently operation and control method are developed, to numerous technological parameters of rectifying tower with bulkhead or behaviour
Make variable comprehensively to be controlled, realize the stable operation of divided wall column, while ensure the quality and yield of each product.
The content of the invention
To be solved by this invention is that rectifying tower with bulkhead operational control in the prior art is difficult, stability is bad and product matter
Amount and the uppity technical problem of yield.The invention provides a kind of operation of rectifying tower with bulkhead and control method, by right
The temperature of different zones, flow and Liquid level in rectifying tower with bulkhead, comprehensive control of rectifying tower with bulkhead is realized, both ensure that
Product quality, product yield, also achieve stability contorting, available in the industrial production of rectifying tower with bulkhead.
In order to solve the above-mentioned technical problem, the technical solution adopted by the present invention is as follows：Rectifying tower with bulkhead includes 5 control zones
Domain, it is respectively：Feedstock control area, overhead reflux and extraction control area, liquid are collected and distribution control area, side line
Control area is produced, and tower reactor produces control area, the control method of each control area is as follows：
(1) feedstock control area：Controlled using flow controller control feedstock amount, using temperature controller former
Expect feeding temperature；
(2) overhead reflux and extraction control area：Controlled using temperature controller control tower top backflow volume, using flow
Device controls overhead product produced quantity, controls tower reactor reboiler heat using fluid level controller；
(3) control area is collected and distributed to liquid：Public rectifying section bottom is controlled to distillate liquid using fluid level controller
Flow, the distribution liquid measure using temperature controller control bulkhead section feeding side；
(4) side take-off control area：Sideline product produced quantity is controlled using flow controller；
(5) tower reactor extraction control area：Tower reactor product produced quantity is controlled using fluid level controller.
In above-mentioned technical proposal, what the flow controller in feedstock control area controlled is feedstock amount, according to
The feedstock amount of setting automatically adjusts actual feedstock amount.
In above-mentioned technical proposal, what the temperature controller in feedstock control area controlled is rectifying tower with bulkhead bulkhead section
The temperature of product side sensitive plate, according to this sensitive plate temperature automatic adjustment feedstock temperature.Because temperature is corresponding with composition
Relation, the sensitive plate temperature in bulkhead section product side directly affect sideline product quality, therefore, carry out temperature control to product side, protect
Sideline product quality is demonstrate,proved；Usual rectifying tower with bulkhead bulkhead section product side sensitive plate is located at the bottom or middle and lower part of product side.
In above-mentioned technical proposal, what the temperature controller in overhead reflux and extraction control area controlled is rectifying tower with bulkhead
The temperature of public rectifying section sensitive plate, according to this sensitive plate temperature automatic adjustment top reflux flow rate.Due to temperature and composition
Corresponding relation, the temperature control of public rectifying section sensitive plate is realized by adjusting tower top backflow volume, it is ensured that tower top
Product quality.Usual public rectifying section sensitive plate is located at the top or middle and upper part of public rectifying section.
In above-mentioned technical proposal, what the flow controller in overhead reflux and extraction control area controlled is that overhead product is adopted
Output, its flow are set according to percentage composition in feed composition of feedstock amount and corresponding light component, root
Actual overhead product produced quantity is automatically adjusted according to the product produced quantity of above-mentioned setting, so as to ensure that the yield of overhead product.
In above-mentioned technical proposal, what the fluid level controller in overhead reflux and extraction control area controlled is return tank of top of the tower
Liquid level, tower reactor reboiler heat is automatically adjusted according to the liquid level, ensures the rising vapor volume of tower reactor.Due to overhead reflux and adopt
Go out and carried out corresponding control, therefore, realize the stabilization of return tank of top of the tower liquid level, being equal to realizes overhead reflux and extraction
The stable operation in region, while ensure that the material balance of light component in rectifying tower with bulkhead.
In above-mentioned technical proposal, what the fluid level controller in liquid collection and distribution control area controlled is rectifying tower with bulkhead
The liquid level of public rectifying section bottom liquid collecting zone, the total flow that bottom distillates liquid is automatically adjusted according to the liquid level.Due to
The liquid distribution of demarcation strip both sides directly affects the separating resulting of rectifying tower with bulkhead, and above-mentioned distribution liquid comes from public essence
Evaporate the liquid of the liquid collection regions of section bottom, therefore, to the region carry out Liquid level, help avoid gas phase race material or
The overflow of liquid phase, while ensure liquid distribution effects and the stable operation of rectifying tower with bulkhead of bulkhead sides.
In above-mentioned technical proposal, what the temperature controller in liquid collection and distribution control area controlled is rectifying tower with bulkhead
The temperature of bulkhead section feeding side sensitive plate, according to the distribution liquid measure of this sensitive plate temperature automatic adjustment feed side.Due to feed side
Main function be the pre-separation for realizing raw material, i.e., part intermediate species with light component enter public rectifying section, remaining middle groups
Divide and enter public stripping section with heavy constituent, therefore, liquid measure is distributed to realize bulkhead section feeding side sensitive plate by adjusting feed side
Temperature control, it is ensured that above-mentioned pre-separation effect, effectively avoid heavy constituent from entering public rectifying section from the top of demarcation strip,
And then enter product side in a manner of liquid phase, influence sideline product quality.Usual rectifying tower with bulkhead bulkhead section feeding side sensitive plate position
In the top of feed side or middle and upper part.
In above-mentioned technical proposal, what the flow controller in side take-off control area controlled is sideline product produced quantity,
Its flow is according to feedstock amount and corresponds to percentage composition of the intermediate species in feed composition to be set, according to upper
The product produced quantity for stating setting automatically adjusts actual sideline product produced quantity, so as to ensure that the yield of sideline product.
In above-mentioned technical proposal, what the fluid level controller in tower reactor extraction control area controlled is rectifying tower with bulkhead tower reactor
Liquid level, tower reactor product produced quantity is automatically adjusted according to the liquid level.Obviously, tower reactor liquid level is controlled, advantageously ensured that in tower
Rising vapor volume, realize the stable operation of rectifying tower with bulkhead；Meanwhile had to tower top and sideline product produced quantity
On the basis of effect control, the yield of tower reactor product is in turn ensure that, realizes the material balance of whole tower.
Sum it up, the corresponding relation based on temperature in rectifying column with composition, the sensitive plate temperature of public rectifying section are straight
Quality, feed side and the sensitive plate temperature of product side for connecing influence overhead product then directly affect product side roof part decline heavy constituent
Rise the content of heavy constituent with product side bottom, namely directly affect the quality of sideline product, therefore, by controlling suitable spirit
Quick plate temperature can ensure the quality of tower top and sideline product.By adjusting in overhead reflux and extraction control area in the present invention
Phegma flow realize control to the sensitive plate temperature of public rectifying section, so as to ensure that overhead product quality；Pass through tune
The feedstock temperature that liquid is collected and distributed in feed side distribution liquid measure and feedstock control area in control area is saved,
The temperature control to feed side and product side sensitive plate is realized respectively, it is achieved thereby that to product side impurity, is especially recombinated
Divide the control of content, ensure that sideline product quality；Meanwhile on the premise of the said goods quality is ensured, the present invention passes through original
Three flow controllers difference in material charging control area, overhead reflux and extraction control area and side take-off control area
The control to feedstock amount, tower top and sideline product produced quantity is realized, so as to ensure that the yield of tower top and sideline product；
In addition, stable operation and product produced quantity based on rectifying tower with bulkhead are influenceed by tower inner vapor amount or gas-liquid flow, the present invention
By adjust tower reactor produce control area in tower reactor produced quantity and reboiler heat realize respectively to tower reactor liquid level and tower top
The control of drainer liquid level, and collected by adjusting liquid and the bottom of distribution control area distillates total amount of liquid and realized pair
The Liquid level in the region, so as on the one hand ensure that the material balance of gas-liquid flow and whole tower in tower, now, in tower top and
In the case that sideline product quality and yield have achieved effective control, the product quality and yield of tower reactor also further obtain
Ensure, on the other hand then ensure that the stable operation of full tower regional, realize the stable operation of whole rectifying tower with bulkhead；Cause
This, to above-mentioned five control areas, i.e. feedstock control area, overhead reflux and extraction control area, liquid is collected and divided
Enter the control of trip temperature, flow and liquid level respectively with control area, side take-off control area and tower reactor extraction control area,
The quality and yield of tower top, side line and tower reactor product can not only be ensured, moreover it is possible to ensure to include tower top, tower in rectifying tower with bulkhead
The stable operation of the regionals such as kettle, public rectifying section bottom, finally realizes the stable operation of whole tower.Therefore, using the present invention
Disclosed technology can preferably solve that conventional rectifying tower with bulkhead operational control is difficult, stability is bad and product quality and yield
Uppity technical problem.
Brief description of the drawings
Fig. 1 is rectifying tower with bulkhead operation involved in the present invention and control method schematic diagram；
Fig. 2 is the rectifying tower with bulkhead control method schematic diagram described in comparative example 1；
Fig. 3 is the rectifying tower with bulkhead control method schematic diagram described in comparative example 2.
In Fig. 1, C101 is rectifying tower with bulkhead, E101 is overhead condenser, E102 is tower reactor reboiler, E102 is that raw material is pre-
Hot device；TIC is temperature controller, FIC is flow controller, LIC is fluid level controller；Middle part of the demarcation strip along tower is placed, will
Rectifying tower with bulkhead is divided into 4 parts, and I is public rectifying section, II is public stripping section, III is bulkhead section feeding side, IV is bulkhead
Section product side；N1 is public rectifying section sensitive plate, N2 is bulkhead section feeding side sensitive plate, N3 is bulkhead section product side sensitive plate；
Logistics (101) is raw material, logistics (102) is overhead product, logistics (103) is sideline product, logistics (104) be tower reactor product,
Logistics (105) is overhead reflux liquid, logistics (106) is public rectifying section bottom distillate, logistics (107) is bulkhead section feeding side
Distribution liquid, logistics (108) be bulkhead section product side distribution liquid.
In Fig. 1, feedstock region controls feedstock valve opening, using the spirit of bulkhead section product side using flow controller
Quick plate N3 temperature control feedstock temperature；Overhead reflux and the temperature control that public rectifying section sensitive plate N1 is used using region
Overhead reflux liquid measure processed, using flow controller control overhead product extraction control valve opening, using return tank of top of the tower liquid level control
Tower reactor reboiler E102 processed heating power or flow rate of heat medium；Liquid is collected and distribution region uses public rectifying section bottom liquid
The Liquid level bottom of collecting region distillates the total flow of liquid, distributes liquid using feed side sensitive plate N2 temperature control feed side
The control valve opening of body；Side take-off region is using flow controller control sideline product extraction control valve opening；Tower reactor produces
Region is using tower reactor liquid level control tower kettle product extraction control valve opening.
In Fig. 2, in addition to feed preheater, the equipment and logistics of rectifying tower with bulkhead are consistent with Fig. 1, and its control program is：It is logical
Cross overhead product composition control overhead reflux liquid measure, produced by sideline product composition control sideline product produced quantity, by tower reactor
Product composition control tower reactor reboiler thermic load, and controlled and separated by the heavy constituent content in bulkhead section feeding side roof part gas phase
The ratio of liquid is distributed in plate both sides.
In Fig. 3, the equipment and logistics of rectifying tower with bulkhead are consistent with Fig. 1, and its control program is：Pushed up by bulkhead section product side
Portion's sensitive plate temperature control tower top backflow volume, by overhead condenser Liquid level overhead product produced quantity, pass through public essence
Evaporate a section bottom liquid collecting region Liquid level bulkhead section feeding side distribution liquid measure, the both sides distribution of passing ratio controller control dividing plate
Ratio between liquid measure, by bulkhead section product side bottom sensitive plate temperature control sideline product produced quantity, and pass through tower bottoms
Position control tower reactor product produced quantity.
Below by embodiment, the invention will be further elaborated.
Embodiment
【Embodiment 1】
Using benzene/methylbenzene/mixed xylenes material as raw material, its composition by weight percentage for 12.80% benzene+
The mixed xylenes of 70.69% toluene+16.51%.On the basis of feed rate 80g/min, rectifying tower with bulkhead behaviour as shown in Figure 1
Separated as control method, tower top obtains benzaldehyde product, and side line obtains toluene product, and tower reactor obtains mixed xylenes product.Its
Total number of theoretical plate of middle rectifying tower with bulkhead is 70, the number of theoretical plate of public rectifying section is 15, bulkhead section feeding side and product side
Number of theoretical plate is 35, and from bulkhead section feeding side I, the 23rd piece of theoretical plate entrance of number, toluene produce raw material from bulkhead section from top to bottom
The 17th piece of theoretical plate extraction that product side III is counted from top to bottom, operating pressure are normal pressure, and sensitive plate N1, N2, N3 control temperature are divided
Not Wei 79.8 DEG C, 108.4 DEG C, 110.8 DEG C, tower top, the produced quantity of side line be controlled as 10.2g/min, 56.5g/min, tower
Top drainer, the liquid level of liquid collection region and tower reactor control 50%, 60%, 80% respectively, and control result is as shown in table 1.Can
To find out, the purity of benzene, toluene and mixed xylenes product reaches more than 99.9%, and the yield of benzene and toluene also reaches
More than 99.9%, while the stabilization time of whole tower is shorter, about 4hr, separating effect and stabilization time are significantly better than that comparative example,
Illustrate that operation involved in the present invention and control method realize the preferable control effect of rectifying tower with bulkhead.
【Embodiment 2】
Using benzene/methylbenzene/mixed xylenes material as raw material, its composition by weight percentage for 33.85% benzene+
The mixed xylenes of 54.61% toluene+11.54%.On the basis of feed rate 80g/min, rectifying tower with bulkhead behaviour as shown in Figure 1
Separated as control method, total number of theoretical plate of wherein rectifying tower with bulkhead is 70, the number of theoretical plate of public rectifying section is 20, point
The number of theoretical plate of wall section feeding side and product side is 30, the 17th piece of theory that raw material counts from top to bottom from bulkhead section feeding side I
The 15th piece of theoretical plate extraction that plate enters, toluene counts from top to bottom from bulkhead section product side III, operating pressure is normal pressure, sensitive
Plate N1, N2, N3 control temperature are respectively 79.9 DEG C, 108.5 DEG C, 111.2 DEG C, tower top, the produced quantity of side line be controlled as
27.1g/min, 43.6g/min, the liquid level of overhead condensation tank, liquid collection region and tower reactor controls 60% respectively, 60%,
75%, control result is as shown in table 1.As can be seen that after the structural parameters of replacing raw material composition and rectifying tower with bulkhead, institute of the present invention
The operation being related to and control method have equally reached preferable control effect.
【Embodiment 3】
Using ethanol/isobutanol/n-amyl alcohol mixed material as raw material, its composition by weight percentage is 12.80% second
The n-amyl alcohol of the isobutanol of alcohol+70.69%+16.51%.On the basis of feed rate 80g/min, rectifying tower with bulkhead as shown in Figure 1
Method of controlling operation thereof is separated, and tower top obtains alcohol product, and side line obtains isobutanol product, and tower reactor obtains n-amyl alcohol product.
For wherein rectifying tower with bulkhead structural parameters with embodiment 1, operating pressure is normal pressure, and sensitive plate N1, N2, N3 control temperature are respectively
77.5 DEG C, 105.8 DEG C, 108.2 DEG C, tower top, the produced quantity of side line be controlled as 10.2g/min, 56.5g/min, tower top is cold
The liquid level of solidifying tank, liquid collection region and tower reactor controls 60%, 60%, 80% respectively, and control result is as shown in table 1.It can see
Go out, after changing separation mixture, operation involved in the present invention and control method still can realize preferable control effect.
The control effect of table 1
【Comparative example 1】
Being formed using rectifying tower with bulkhead same as Example 1 and raw material, control method as shown in Figure 2 is separated,
Control result is shown in Table 2.As can be seen that under the control method, in order to ensure that the product purity of benzene and toluene is not less than
99.9%, the purity and yield of tower reactor mixed xylenes are difficult to ensure that, only 99.78%, while the stabilization time of whole tower is longer,
More than 10hr；If further increasing the thermic load of tower reactor reboiler, the purity of tower reactor mixed xylenes can be improved to 99.9%, but
Now the pressure difference below public stripping section and dividing plate is significantly increased, and 3KPa, the stable operation of rectifying tower with bulkhead are risen to by 0.5KPa
It is destroyed.
【Comparative example 2】
Being formed using rectifying tower with bulkhead same as Example 1 and raw material, control method as shown in Figure 3 is separated,
Control result is shown in Table 2.As can be seen that under the control method, the purity of benzene and toluene product is substantially relatively low, especially benzene,
Reason is, only controls the temperature of product side roof part column plate and the liquid phase distribution of bulkhead section both sides, effectively side line can only be controlled to produce
The content of impurity benzene and dimethylbenzene in product, that is, control the product quality of side line toluene, but can not ensure overhead benzene and tower reactor diformazan
The product quality of benzene；Meanwhile in the control program, because the evaporation capacity in tower or gas-liquid flow are not controlled accordingly, cause
Product yield can not be effectively controlled, and the yield such as tower reactor mixed xylenes is significant lower, while the stabilization of rectifying tower with bulkhead
Time is also relatively long.
The control effect of 2 different control programs of table
Claims (10)
1. operation and the control method of a kind of rectifying tower with bulkhead, including following five control areas：
(1) feedstock control area：Enter using flow controller control feedstock amount, using temperature controller control raw material
Material temperature degree；
(2) overhead reflux and extraction control area：Using temperature controller control tower top backflow volume, using flow controller control
Overhead product produced quantity processed, tower reactor reboiler heat controlled using fluid level controller；
(3) control area is collected and distributed to liquid：Using fluid level controller control public rectifying section bottom distillate liquid flow,
Using the distribution liquid measure of temperature controller control bulkhead section feeding side；
(4) side take-off control area：Sideline product produced quantity is controlled using flow controller；
(5) tower reactor extraction control area：Tower reactor product produced quantity is controlled using fluid level controller.
2. operation and the control method of rectifying tower with bulkhead according to claim 1, it is characterised in that feedstock control zone
What the flow controller in domain controlled is feedstock amount, and actual feedstock is automatically adjusted according to the feedstock amount of setting
Amount.
3. operation and the control method of rectifying tower with bulkhead according to claim 1, it is characterised in that feedstock control zone
What the temperature controller in domain controlled is the temperature of rectifying tower with bulkhead bulkhead section product side sensitive plate, according to this sensitive plate temperature certainly
Dynamic regulation feedstock temperature.
4. operation and the control method of rectifying tower with bulkhead according to claim 1, it is characterised in that overhead reflux and extraction
What the temperature controller in control area controlled is the temperature of the public rectifying section sensitive plate of rectifying tower with bulkhead, according to this sensitive plate temperature
Degree automatically adjusts top reflux flow rate.
5. operation and the control method of rectifying tower with bulkhead according to claim 1, it is characterised in that overhead reflux and extraction
What the flow controller in control area controlled is overhead product produced quantity, and its flow is according to feedstock amount and light group of correspondence
The percentage composition divided in feed composition automatically adjusts actual tower come what is set according to the product produced quantity of above-mentioned setting
Push up product produced quantity.
6. operation and the control method of rectifying tower with bulkhead according to claim 1, it is characterised in that overhead reflux and extraction
What the fluid level controller in control area controlled is the liquid level of return tank of top of the tower, and tower reactor reboiler heat is automatically adjusted according to the liquid level
Amount.
7. operation and the control method of rectifying tower with bulkhead according to claim 1, it is characterised in that liquid is collected and distribution
What the fluid level controller in control area controlled is the liquid level of the public rectifying section bottom liquid collecting zone of rectifying tower with bulkhead, according to
The liquid level automatically adjusts the total flow that bottom distillates liquid.
8. operation and the control method of rectifying tower with bulkhead according to claim 1, it is characterised in that liquid is collected and distribution
What the temperature controller in control area controlled is the temperature of rectifying tower with bulkhead bulkhead section feeding side sensitive plate, according to this sensitive plate
The distribution liquid measure of temperature automatic adjustment feed side.
9. operation and the control method of rectifying tower with bulkhead according to claim 1, it is characterised in that side take-off control zone
What the flow controller in domain controlled is sideline product produced quantity, and its flow is existed according to feedstock amount and corresponding intermediate species
Percentage composition in feed composition automatically adjusts actual side line according to the product produced quantity of above-mentioned setting and produced come what is set
Product produced quantity.
10. operation and the control method of rectifying tower with bulkhead according to claim 1, it is characterised in that tower reactor produces control zone
What the fluid level controller in domain controlled is the liquid level of rectifying tower with bulkhead tower reactor, and the extraction of tower reactor product is automatically adjusted according to the liquid level
Amount.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610831227.XA CN107837552B (en) | 2016-09-19 | 2016-09-19 | Operation and control method of dividing wall rectifying tower |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110052051A (en) * | 2019-04-29 | 2019-07-26 | 中国石油大学(华东) | Distillation process overall situation concentration online observation device and method based on column plate temperature |
| WO2019191582A1 (en) * | 2018-03-29 | 2019-10-03 | Uop Llc | Controlling the split of liquid reflux in a dividing wall column |
| CN110960881A (en) * | 2018-09-28 | 2020-04-07 | 中国石油化工股份有限公司 | Control structure and control method of Kaibel bulkhead rectifying tower |
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| US4230533A (en) * | 1978-06-19 | 1980-10-28 | Phillips Petroleum Company | Fractionation method and apparatus |
| AU2003210987A1 (en) * | 2003-02-12 | 2004-09-06 | Uop Llc | Dividing wall column control system |
| US7444193B2 (en) * | 2005-06-15 | 2008-10-28 | Cutler Technology Corporation San Antonio Texas (Us) | On-line dynamic advisor from MPC models |
| CN102872609B (en) * | 2011-07-11 | 2015-04-15 | 中国石油化工股份有限公司 | Dividing wall rectifying tower |
| CN102631791B (en) * | 2012-03-31 | 2016-03-09 | 中国石油化工股份有限公司 | A kind of control method of rectifying tower with bulkhead |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019191582A1 (en) * | 2018-03-29 | 2019-10-03 | Uop Llc | Controlling the split of liquid reflux in a dividing wall column |
| US10792583B2 (en) | 2018-03-29 | 2020-10-06 | Uop Llc | Process and apparatus for controlling the split of liquid reflux in a divided wall column |
| CN110960881A (en) * | 2018-09-28 | 2020-04-07 | 中国石油化工股份有限公司 | Control structure and control method of Kaibel bulkhead rectifying tower |
| CN110960881B (en) * | 2018-09-28 | 2022-09-27 | 中国石油化工股份有限公司 | Control structure and control method of Kaibel bulkhead rectifying tower |
| CN110052051A (en) * | 2019-04-29 | 2019-07-26 | 中国石油大学(华东) | Distillation process overall situation concentration online observation device and method based on column plate temperature |
| CN110052051B (en) * | 2019-04-29 | 2021-03-16 | 中国石油大学(华东) | Rectifying process global concentration on-line observer and method based on tower plate temperature |
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