CN102631791B - A kind of control method of rectifying tower with bulkhead - Google Patents
A kind of control method of rectifying tower with bulkhead Download PDFInfo
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Abstract
The invention discloses a kind of control method of rectifying tower with bulkhead, adopt four control loops, be respectively: overhead composition control loop, control tower top capacity of returns by overhead concentration of component; Side stream composition control loop, controls side line flow by side stream concentration of component; Tower reactor distillate composition control loop, controls tower reactor thermic load by tower reactor distillate concentration of component; Prefractionation section top gas phase composition control loop, controls point liquor ratio of rectifying tower with bulkhead inside by prefractionation section top gas phase heavy constituent concentration.Described control loop is all preferably pid control circuit.Control method of the present invention, when feed rate or feed component content change, can realize the steady control of full tower, ensures product quality, and guarantees that full tower energy consumption is in optimized scope.
Description
Technical field
The invention belongs to chemical industry distillation process and automation control area, relate to the control method that rectifying tower with bulkhead is separated multicomponent mixture.
Background technology
Along with being becoming tight energy day and market competition day by day fierce, save energy and reduce the cost more and more comes into one's own in the operational management of chemical industry.Rectifying tower with bulkhead receives the common concern of people in the industry and researcher as typical process intensification technology.
Rectifying tower with bulkhead can realize the clear segmentation of three components, Four composition and more multicomponent mixture in a tower.Rectifying tower with bulkhead arranges a vertical partition wall in rectifying column inside, rectifying column is divided into four parts: the upper and lower two parts of partition wall are upper rectifying section and bottom stripping section, and partition wall both sides are respectively prefractionation section (or feed zone) and lateral line discharging section.Compared with two traditional tower distillation processes, rectifying tower with bulkhead have energy-conservation, invest low, take up an area the advantages such as few.
Different from traditional rectifying column, rectifying tower with bulkhead inside is more complicated, highly be coupled between adjacent block and multi-tiling, between the different free degree and between multivariable in tower, change any one performance variable and all can bring chain reaction to vapor liquid equilibrium state, heat transfer and mass transport process in tower and target product purity, the steady control realizing rectifying tower with bulkhead is a difficult problem always.
At present the research of divided-wall distillation column is also mainly concentrated on and the comparing of the efficiency aspect of traditional rectifying column, for the control aspect report of rectifying tower with bulkhead and patent less.The pioneering document of rectifying tower with bulkhead stable state research delivers (Operationofintegratedthree-product (Petlyuk) distillationcolumns by Wolff and Skogestad in nineteen ninety-five, Wolff, E.A., Skogestad, S, Ind.Eng.Chem.Res, 1995,34:2094 – 2103), they utilize rectifying tower with bulkhead to have studied ethanol/propanol/butanols three-component system.This tower king-tower is made up of 40 blocks of column plates, and prefractionation part has 20 blocks of column plates.They have studied three point control and four point control simultaneously.In three point control models, regulate reflux ratio to change overhead product purity, regulate side line flow rate to change sideline product purity, quantity of steam at the bottom of adjusting tower changes bottom product purity.Four point control models add the impurity content utilizing the purity of tower top bottom product to regulate sideline product, and this model can not guarantee that rectifying tower with bulkhead operates near optimum energy consumption, and can not realize steady control when feed rate and feed composition fluctuation.
Within 1998, AbdulMutalib and Smith is studied (OperationandcontrolofdividingwallcolumnsPart1:Degreeoffr eedomanddynamicsimulation to methyl alcohol/2-propyl alcohol/butanols system in containing the rectifying tower with bulkhead of 23 blocks of column plates, AbdulMutalib, M.I., Smith, R., Trans.Inst.Chem.Eng., PartA1998,76:308-318), product purity can reach 98.5%.Different from the result that Wolff and Skogestad draws, they find in three components Controlling model, utilize pair relationhip V-XS2 and the S-XB3 after changing and change capacity of returns in conjunction with R-XD1 or D-XD1() regulating loop, extraordinary result can be obtained.They do not use liquid phase to distribute variable.AbdulMutalib, Zeglam utilize temperature instead of composition to carry out research (the OperationandcontrolofdividingwallcolumnsPart2:Simulation andpilotplantstudiesusingtemperaturecontrol of simulation and experiment as control variables with Smith to identical system, AbdulMutalib, M.I., Zeglam, A.O., Smith, R., Trans.Inst.Chem.Eng., PartA1998,76:319-334).These scholars attempt two temperature in a control system.They keep the constant of side-stream flow rate simultaneously.These two features are two main defects in mentioned model, cause steady-state simulation result and Steady Experimental result to have obvious difference.The overhead product purity such as, obtained in experimentation is 98.1%, instead of 98.5% in the middle of simulation.In addition, even if there is very little disturbance in feed composition, the control effects of expecting also cannot be realized.Such as when feed composition becomes 36.3% methyl alcohol, 28.4%2-propyl alcohol, 35.3% butanols from 33.3% methyl alcohol, 33.3%2-propyl alcohol, 33.4% butanols, the methanol rectification purity obtained has dropped to 96.5% by 98.5%.These results show, only controlling two temperature fixation side line material flow rate cannot effectively control.
Adrian etc. report achievement in research (the Modelpredictivecontrolofintegratedunitoperations:Control ofadividedwallcolumn of butanols/amylalcohol/hexanol ternary system in Bath not small test device, Adrian, T., Schoenmakers, H., Boll, M, Chem.Eng.Process., 2004,43:347-355).The tower total height that they use is 11.5 meters.Need control three temperature, one of them is the temperature of prefractionation part, and the Main Function of prefractionation part prevents heavy constituent from entering side take-off part from the top of partition wall.This control method is more reasonable than only controlling two temperature or not controlling the method for prefractionation portion temperature.PID controls to compare with Model Predictive Control (MPC) to draw and utilize MPC to control to improve control effects by they.PID Controlling model mainly comprises three aspects: regulate reflux ratio to control the temperature of prefractionation part, regulator solution phase partitioning to control temperature on side take-off position and by regulating the temperature at the bottom of side line flow rate control tower.In MPC Controlling model, except above three temperature control variables, also use the heat flow of reboiler as variable.Although their conclusion shows the better effects if of MPC, it supposes that in PID Controlling model input heat is fixing, and this hypothesis allows people create query to their correctness of conclusion.In addition, the selection of other set of variables and the control and regulation of improvement are not evaluated in their paper.
Research few in number above, although carried out the control research for raw material composition and raw material flow fluctuation, but the generation of raw material composition is when fluctuating on a large scale, how to realize the problem that rectifying tower with bulkhead steadily controlled, kept the purity of product and not yet solves.
Summary of the invention
For solving the problems of the technologies described above, the invention provides a kind of control method of rectifying tower with bulkhead, can when feed rate or feed component content change, the steady control that four concentration of component control loops realize full tower is amounted to by the bottom of tower top, side line, tower and prefractionation section top, ensure product quality, and guarantee that full tower energy consumption is in optimized scope.Solve the control problem of rectifying tower with bulkhead when feed rate and feed component content fluctuation, there is important practical and be worth, have a extensive future.
The present invention adopts following technical scheme:
A control method for rectifying tower with bulkhead, adopts four control loops, is respectively:
(1) overhead composition control loop, controls tower top capacity of returns by overhead concentration of component;
(2) side stream composition control loop, controls side line flow by side stream concentration of component;
(3) tower reactor distillate composition control loop, controls tower reactor thermic load by tower reactor distillate concentration of component;
(4) prefractionation section top gas phase composition control loop, controls point liquor ratio of rectifying tower with bulkhead inside by prefractionation section top gas phase heavy constituent concentration.
Described overhead concentration of component refers to the concentration of object product or impurity in overhead; Side stream concentration of component refers to the concentration of object product or impurity in side stream; Tower reactor distillate concentration of component refers to the concentration of object product or impurity in tower reactor distillate; Prefractionation section top gas phase heavy constituent concentration refer to raw material mid-boiling point higher than or volatility lower than a kind of concentration of material of tower top and side line object product or the concentration summation of several material.
Preferably, described overhead concentration of component, side stream concentration of component, tower reactor distillate concentration of component or prefractionation section top gas phase heavy constituent concentration are measured by online concentration analyzer.
Control loop of the present invention is all preferably pid control circuit.
In above-mentioned pid control circuit, preferably, by mathematical formulae (I), set up overhead reflux amount and overhead concentration of component, side line flow and side stream concentration of component, tower reactor thermic load and tower reactor distillate concentration of component, point liquor ratio of rectifying tower with bulkhead inside and the contact of prefractionation section top gas phase heavy constituent concentration respectively
I
Wherein, U (t) represent inlet amount or feed component change after overhead reflux amount, side line flow, tower reactor thermic load or rectifying tower with bulkhead inside point liquor ratio;
e (t)the signal errors of PID controller after expression inlet amount or feed component change,
e (t)=
r (t)-y (t), wherein
r (t)represent the setting value of overhead concentration of component, side stream concentration of component, tower reactor distillate concentration of component or prefractionation section top gas phase concentration of component,
y (t)the practical measurement value of the overhead concentration of component represented, side stream concentration of component, tower reactor distillate concentration of component or prefractionation section top gas phase concentration of component;
K
p, T
iand T
dfor the tuner parameters of described PID controller.
Preferably, the tuner parameters of described PID controller is obtained by Tyreus-Luyben method.
As a kind of preferred embodiment of the present invention, described control method provided by the invention, concrete steps comprise:
(1) be separately positioned on line concentration analyzer at tower top discharging place of rectifying tower with bulkhead, lateral line discharging place, tower reactor discharging place and prefractionation section top, and set up the pid control circuit of overhead reflux amount control device, pump-around stream amount control device, tower reactor reboiler control device and prefractionation section top portion liquor ratio control device respectively;
(2) each PID controller adopts Tyreus-Luyben method, and carry out parameter tuning respectively, method is as follows:
First, change PID controller into proportional action, be placed on initial proportion degree, change automatic operation into by manual operation; After steadily, change the performance variable of the control device in pid control circuit, after concentration of component measured value is stable, utilizes the performance variable of record and described concentration of component measured value to draw the nyquist diagram of this process, from figure, read cross-over frequency ω
cwith amplification coefficient K
u, utilize T
u=2 π/ω
ccalculate T
u, then the tuner parameters of described PID controller is drawn by following formulae discovery: K
p, T
iand T
d,
K
p=K
u/2.2
T
i=2.2T
U
T
d=T
U/6.3；
(3), after inlet amount or feed component change, after concentration of component measured value is stable, the setting value of described concentration of component is calculated
r (t)and measured value
y (t)difference
e (t), will
e (t), K
p, T
iand T
dsubstitute into the new performance variable that described formula I calculates control device described in each.
Another object of the present invention is to provide described control method and is realizing rectifying tower with bulkhead separation multicomponent mixture, the application in stability contorting when inlet amount or feed component change.
Described multicomponent mixture is three components, Four composition or five component mixtures.
As one embodiment of the present of invention, described multicomponent mixture is based on the mixture of benzene-toluene-xylene.The prefractionation section of described rectifying tower with bulkhead has 46 blocks of column plates, rectifying section has 17 blocks of column plates, and lateral line discharging section has 46 blocks of column plates, and stripping section has 25 blocks of column plates, wherein feedboard is on the 16th block of column plate of described prefractionation section, and lateral line discharging position is described lateral line discharging section the 11st block of plate.
As shown in Figure 2, have one piece of partition wall in rectifying tower with bulkhead, divided by rectifying tower with bulkhead in order to four parts, A is the prefractionation section of rectifying tower with bulkhead, and B is the rectifying section of rectifying tower with bulkhead, and C is the lateral line discharging section of rectifying tower with bulkhead, and D is the stripping section of rectifying tower with bulkhead.Five performance variables are had: overhead reflux amount, side line flow, tower reactor reboiler heat duty, point liquor ratio and point gas ratio in this rectifying tower with bulkhead.But the position of partition wall is fixed in practical operation, a point gas ratio cannot change, and can only be fixed on the design load of stable state.Historical facts or anecdotes border performance variable only has four: overhead reflux amount, side line flow, tower reactor reboiler heat duty and point liquor ratio.In rectifying tower with bulkhead, if the heavy constituent at prefractionation section top enters side line discharging section from partition wall top, then finally can flow into side line with the form of liquid phase, sideline product will be caused defective.Point liquor ratio is the performance variable realizing the soonest, the most accurately control prefractionation section top-heavy constituent content, therefore in practical operation, is used for realization by point liquor ratio controls the heavy constituent content at prefractionation section top.Due to the restriction by response speed and control effects, overhead purity is controlled by overhead reflux amount, and side stream purity is controlled by side line flow, and the purity of the bottomsstream is controlled by reboiler heat duty.
At tower top discharging place of rectifying tower with bulkhead, lateral line discharging place, tower reactor discharging place and prefractionation section top, concentration of component measuring point is set respectively.Preferably, the mensuration of concentration of component is carried out with online concentration analyzer, the output signal of online concentration analyzer, enter PID controller, and then set up the pid control circuit of overhead reflux amount control device, pump-around stream amount control device, tower reactor reboiler control device and prefractionation section top portion liquor ratio control device, as shown in Figure 3.During measurement, with the object product content in the object product content in overhead, the object product content in side stream, the bottomsstream and the heavy constituent content in prefractionation section top gas phase for measuring object.Or using impurity content in distillate as measuring object.
When carrying out the parameter tuning of PID controller, the changes values of performance variable is generally 5%.
On determining concentration of component measurement point and completing basis that PID controller parameter adjusts, feed rate or feed composition can be obtained when changing, the measured value of four measurement points concentration of component separately
y (t),relative to its setting value
r (t)variable quantity
e (t), will
e (t)and the parameter K of corresponding PID controller
p, T
i, T
d, substitute into formula (I), can draw feed rate or feed composition change after new performance variable value, thus after feed state changes, obtain qualified products of separated rapidly, realize the steady control of rectifying tower with bulkhead,
Rectifying tower with bulkhead concentration of component control method provided by the invention is not limited to the separation of three components, and it can be widely used in the high purity separation process of Four composition, five components and more multicomponent mixture.
Accompanying drawing explanation
Fig. 1 is nyquist diagram.
Fig. 2 is rectifying tower with bulkhead structural representation.
Fig. 3 is the example process schematic diagram of concentration control method provided by the invention.
Detailed description of the invention
Below in conjunction with embodiment and accompanying drawing, the present invention is further illustrated; But those skilled in the art should understand that, this embodiment does not limit the inventive method use other Controlling model except PID, and the change of other scope occurs or other feed component content changes at feed rate, or be separated the application in other multicomponent mixture.
The rectifying tower with bulkhead with 4 pid control circuits as shown in Figure 3, is main mixture for separating of benzene/methylbenzene/dimethylbenzene, reduces 10%, the application of concrete control method of the present invention for toluene in charging.
Described rectifying tower with bulkhead, A is prefractionation section, and have 46 blocks of column plates, B is rectifying section, and have 17 blocks of column plates, C is lateral line discharging section, and have 46 blocks of column plates, D is stripping section, has 25 blocks of column plates.Wherein feedboard is on prefractionation section the 16th block of column plate, and lateral line discharging position is lateral line discharging section the 11st block of plate.Divide gas ratio to be 0.437, feeding temperature 85 DEG C, feed pressure 0.8MPag, feed rate 8.5 tons/hour, feed composition is as shown in table 1.
Table 1 feed composition
| Sequence number | Composition | Mass fraction (W) % |
| 1 | Water | 0.0001 |
| 2 | Pentane | 1.00E-05 |
| 3 | Benzene | 12.683 |
| 4 | Toluene | 44.185 |
| 5 | Face dimethylbenzene | 5.947 |
| 6 | Meta-xylene | 23.443 |
| 7 | Paraxylene | 5.409 |
| 8 | Ethylo benzene | 8.162 |
| 9 | 1 methyl 3 ethylo benzene | 0.038 |
| 10 | Isopropylbenzene | 0.104 |
| 11 | N-nonane | 0.018 |
When feed rate and each concentration of component do not change, the load of overhead condenser is 1.35MW; At the concentration of component measurement point of setting, measure the tested concentration of component at discharging place and prefractionation section top at the bottom of discharging place of rectifying tower with bulkhead tower top, lateral line discharging place, tower.Performance variable corresponding in measurement result and 4 pid control circuits, as shown in table 2.
The tested concentration of component of pid control circuit and the performance variable of correspondence before table 2 feed variation
| Pid control circuit position | Tested component/concentration (%) | Respective operations variable | |
| 1 | Prefractionation section top | Gas phase heavy constituent/5.47e-05 | Divide liquor ratio/0.232 |
| 2 | Tower top discharging place | Benzene/0.9996 | Overhead reflux amount/1.08 ton/hour |
| 3 | Lateral line discharging place | Toluene/0.9997 | Side line flow/3.76 ton/hour |
| 4 | Tower reactor discharging place | Liquid phase heavy constituent a/0.99996 | Reboiler heat duty/1.58MW |
a: the liquid phase restructuring of described tower reactor discharging place is divided into other components except benzene, toluene, water and pentane.
Each PID controller adopts Tyreus-Luyben method, carries out parameter tuning respectively:
For overhead benzene concentration-overhead reflux amount pid control circuit.First, change PID controller into proportional action, be placed on initial proportion degree, that is: the time of integration in PID controller is set as infinity, derivative time is set as 0; Automatic operation is changed into by manual operation; After steadily, overhead reflux amount is changed into 1.03 tons/hour (this performance variable reduces about 5%) by 1.08 tons/hour, after overhead benzene concentration measured value is stable, the overhead reflux amount of record and described benzene concentration measured value is utilized to draw the nyquist diagram of this process, as shown in Figure 1, from figure, cross-over frequency ω is read
cwith amplification coefficient K
u, utilize T
u=2 π/ω
ccalculate T
u, then the tuner parameters of described PID controller is drawn by following formulae discovery: K
p, T
iand T
d,
K
p=K
u/2.2
T
i=2.2T
U
T
d=T
U/6.3；
In the same way, obtain the PID controller tuner parameters of four control loops, as shown in table 3.
The tuner parameters of table 3 four PID controller
| Position, control point | Proportional coefficient K p(%/%) | Integration time constant T i (min) | |
| 1 | Prefractionation section top | 0.185673 | 48.84 |
| 2 | Tower top discharging place | 114.57695 | 46.200001 |
| 3 | Lateral line discharging place | 791.180359 | 55.440002 |
| 4 | Discharging place at the bottom of tower | 145.994247 | 56.759998 |
After in charging, toluene reduces 10%, each concentration of component is as shown in table 4.
Table 4 toluene reduces the feed composition after 10%
| Sequence number | Composition | Mass fraction (W) % |
| 1 | Water | 0.011 |
| 2 | Pentane | 1.07916E-05 |
| 3 | Benzene | 13.687 |
| 4 | Toluene | 39.767 |
| 5 | Face dimethylbenzene | 6.418 |
| 6 | Meta-xylene | 25.299 |
| 7 | Paraxylene | 5.837 |
| 8 | Ethylo benzene | 8.808 |
| 9 | 1 methyl 3 ethylo benzene | 0.041 |
| 10 | Isopropylbenzene | 0.112 |
| 11 | N-nonane | 0.019 |
After each measuring point measured value is stable, before fed toluene changes of contents, the concentration of each component is concentration set point
r (t),the concentration of component of each measurement point after 10% is reduced for concentration measurement with toluene in charging
y (t), the difference of both calculating, obtains the signal errors of PID controller
e (t), recycle the tuner parameters that obtained, by formula (I), calculate when can make that in charging, toluene reduces 10%, each performance variable value that tower top, side line and bottom product purity are qualified, as shown in table 5.
I
Table 5
| Position, control point | Respective operations variable | Performance variable value | |
| 1 | Prefractionation section top | Divide liquor ratio | 0.226 |
| 2 | Tower top discharging place | Benzaldehyde product load | 1.164 ton/hour |
| 3 | Lateral line discharging place | Toluene product discharge amount | 3.380 ton/hour |
| 4 | Discharging place at the bottom of tower | Reboiler | 1.551MW |
Utilize control method of the present invention, reduce in 16 hours after 10% at toluene, just again achieve plateau, now at the bottom of tower top, side line, tower and the concentration of the tested component at prefractionation section top as shown in table 6.
Table 6
| The phase of sampling | Measure component | Concentration | |
| Prefractionation section top | Gas phase | Heavy constituent | 5.47e-05 |
| Tower top discharging place | Liquid phase | Benzene | 0.9996 |
| Lateral line discharging place | Liquid phase | Toluene | 0.9997 |
| Discharging place at the bottom of tower | Liquid phase | Heavy constituent | 0.99996 |
As can be seen from Table 6, utilize concentration control method of the present invention, when toluene reduces 10% in charging, keep always before the purity of distillate and feed variation, thus realize multi-component high purity separation.
It will be appreciated by those skilled in the art that and use control method of the present invention, steady control when fluctuation occurs other constituent contents in the feed rate of described benzene/methylbenzene/dimethylbenzene mixed system or charging can be realized; And be applicable to the stability contorting that rectifying tower with bulkhead is separated other multicomponent mixtures too.
Rectifying tower with bulkhead control method provided by the invention, has economic benefit and wide application prospect extremely significantly.The personnel of association area completely can suitably change according to method provided by the invention or change, and are applied to the rectifying separation process of all three components, Four composition and multicomponent mixture.It should be noted that, all these are by carrying out similar change or changing and reconfigure to control method provided by the invention, apparent to those skilled in the art, are all regarded as in spirit of the present invention, scope and content.
Claims (5)
1. a control method for rectifying tower with bulkhead, is characterized in that: adopt four control loops, be respectively:
(1) overhead composition control loop, controls tower top capacity of returns by overhead concentration of component;
(2) side stream composition control loop, controls side line flow by side stream concentration of component;
(3) tower reactor distillate composition control loop, controls tower reactor thermic load by tower reactor distillate concentration of component;
(4) prefractionation section top gas phase composition control loop, controls point liquor ratio of rectifying tower with bulkhead inside by prefractionation section top gas phase heavy constituent concentration;
Described overhead concentration of component, side stream concentration of component, tower reactor distillate concentration of component or prefractionation section top gas phase heavy constituent concentration are measured by online concentration analyzer; Described control loop is pid control circuit;
Concrete steps comprise:
(1) be separately positioned on line concentration analyzer at tower top discharging place of rectifying tower with bulkhead, lateral line discharging place, tower reactor discharging place and prefractionation section top, and set up the pid control circuit of overhead reflux amount control device, pump-around stream amount control device, tower reactor reboiler control device and prefractionation section top portion liquor ratio control device respectively;
(2) each PID controller adopts Tyreus-Luyben method, and carry out parameter tuning respectively, method is as follows:
First, change PID controller into proportional action, be placed on initial proportion degree, change automatic operation into by manual operation; After steadily, change the performance variable of the control device in pid control circuit, after concentration of component measured value is stable, utilizes the performance variable of record and described concentration of component measured value to draw the nyquist diagram of this process, from figure, read cross-over frequency ω
cwith amplification coefficient K
u, utilize T
u=2 π/ω
ccalculate T
u, then the tuner parameters of described PID controller is drawn by following formulae discovery: K
p, T
iand T
d,
K
p＝K
u/2.2
T
i＝2.2T
U
T
d＝T
U/6.3；
(3) after inlet amount or feed component change, after concentration of component measured value is stable, the setting value r (t) of described concentration of component and the difference e (t) of measured value y (t) is calculated, by e (t), K
p, T
iand T
dsubstitute into the new performance variable that described formula I calculates control device described in each;
Wherein, U (t) represent inlet amount or feed component change after overhead reflux amount, side line flow, tower reactor thermic load or rectifying tower with bulkhead inside point liquor ratio;
E (t) represent inlet amount or feed component change after the signal errors of PID controller, e (t)=r (t)-y (t), wherein r (t) represents the setting value of overhead concentration of component, side stream concentration of component, tower reactor distillate concentration of component or prefractionation section top gas phase concentration of component, the practical measurement value of the overhead concentration of component that y (t) represents, side stream concentration of component, tower reactor distillate concentration of component or prefractionation section top gas phase concentration of component;
K
p, T
iand T
dfor the tuner parameters of described PID controller.
2. according to the said control method of claim 1, it is characterized in that: described overhead concentration of component refers to the concentration of object product or impurity in overhead; Side stream concentration of component refers to the concentration of object product or impurity in side stream; Tower reactor distillate concentration of component refers to the concentration of object product or impurity in tower reactor distillate; Prefractionation section top gas phase heavy constituent concentration refer to raw material mid-boiling point higher than or volatility lower than a kind of concentration of material of tower top and side line object product or the concentration summation of several material.
3. the control method described in claim 1 or 2 is realizing rectifying tower with bulkhead separation multicomponent mixture, the application in stability contorting when inlet amount or feed component change.
4. application according to claim 3, is characterized in that, described multicomponent mixture is three components, Four composition or five component mixtures.
5. application according to claim 4, is characterized in that: described multicomponent mixture is based on the mixture of benzene-toluene-xylene.
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