CN101612485B - Design method of process intensification reactive distillation column - Google Patents
Design method of process intensification reactive distillation column Download PDFInfo
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Abstract
The invention provides a design method of a process intensification reactive distillation column, belongs to the design and manufacture of chemical process, relates to a method for improving the efficiency of the reactive distillation column, and particularly provides a design method of a process intensification reactive distillation column as a solution to the effective treatment problem of intercoupling between reaction operation and distillation operation in the reactive distillation column. According to three situations of latent heat of vaporization ratio of reaction heat and reaction mixture, the method determines a corresponding intensification process to promote the coupling of internal substances and internal energy in the reaction operation and distillation operation in virtue of a progressive structure search method and a non-linear optimization method, greatly reduces the equipment investment cost and operation cost of a system to the maximum degree and has rather high thermodynamic efficiency. The design method can be applied to the integration and design of chemical process, effective utilization of energy sources and protection of the environment.
Description
Technical field
The present invention relates to the comprehensive and designing technique of reactive distillation column, belong to the design and the manufacturing of chemical process.
Background technology
Reactive distillation column has obtained application to a certain degree in chemical process.For example successfully be used in the production process of methyl tertiary butyl ether(MTBE) (methyl acetate and methyl tertiary butyl ether:MTBE) and methyl acetate, both improve the operating efficiency of production process significantly, reduced the cost of investment of equipment again significantly.Yet,,, how to handle both problems that intercouples reasonably and effectively well and but fail to be solved well always because reactive distillation column has comprised operation and distillation procedure for the comprehensive and design of system.The existence of this bottleneck problem has not only hindered the performance of reactive distillation column superiority, and has limited its range of application widely.At present, the comprehensive and method for designing of reactive distillation column may be summarized to be two kinds.
1. experience design method.Conversion zone is placed between rectifying section and the stripping section simply, carries out system's design according to certain economic indicator (for example all year consumption costs etc.) then.Because the coupling that can not fully excavate operation and distillation procedure has not only caused the waste of operating energy and has promoted equipment investment cost, and worsened operating flexibility, dynamic quality and the controllability of system.
2. non-linear mixed integer programming (Mixed-integer nonlinear programming:MINLP) method.It also is the comprehensive and design of carrying out system according to certain economic indicator (for example all year consumption costs etc.).Though the coupling that can more effectively excavate operation and distillation procedure than experience design method, because in the superstructure that needs tectonic system in advance, this becomes a very thorny difficult problem.For nonlinear optimal problem, for example non-protruding region of search or nonlinear restriction equation etc., its globally optimal solution also are difficult to obtain.Therefore, the application prospect of this method also has been subjected to strong restriction.
Summary of the invention
Be difficult to handle effectively the wherein problem that intercouples of operation and distillation procedure at the design of traditional reactive distillation column, the invention provides a kind of method for designing of novel process intensification reactive distillation column, it utilizes four kinds of process intensification strategies to promote inner material coupling and/or the internal energy coupling between the operation and distillation procedure in the reactive distillation columns, both avoided numerous and diverse Mathematical treatment, fully excavated the energy-saving potential of system again, guaranteed that the tower of reactive distillation column has very high thermodynamic efficiency.
For achieving the above object, the invention provides a kind of method for designing of process intensification reactive distillation column, it is characterized in that: according to the ratio H of the heat of vaporization of reaction heat and reactant mixture
R/ Δ H
V, Δ H wherein
VBe gasification latent heat, Δ H
RBe reaction heat, the method for designing of process intensification reactive distillation column is divided into three kinds of situations, utilize four kinds of process intensification strategies to promote inner material coupling and/or internal energy coupling between operation and the distillation procedure targetedly.These four kinds of process intensification strategies are that (1) is expanded conversion zone in rectifying section; (2) conversion zone is expanded in stripping section; (3) feed entrance point is done effectively move in conversion zone; (4) catalyst is effectively distributed in conversion zone.
Situation one: for containing heat-flash effect (Δ H
R/ Δ H
V＞1.0) reactive distillation column is divided into two kinds of situations:
1) for the endothermic reaction, (1) is expanded conversion zone in rectifying section, the top that spreading range can be from last piece column plate of rectifying section to tower, and particular location is determined by gradual search structure method; (2) feed entrance point is moved in conversion zone, moving range can move to the other end of conversion zone from an end of conversion zone, and particular location is determined by gradual search structure method; (3) keep the total amount of catalyst constant, catalyst is carried out the emphasis distribution at the lap of conversion zone and rectifying section, the concrete distribution determined by nonlinear optimization method.
2) for exothermic reaction, (1) is expanded conversion zone in stripping section, the bottom that spreading range can be from first block of column plate of stripping section to tower, and particular location is determined by gradual search structure method; (2) feed entrance point is moved in conversion zone, moving range can move to the other end of conversion zone from an end of conversion zone, and particular location is determined by gradual search structure method; (3) keep the total amount of catalyst constant, catalyst is carried out the emphasis distribution at the lap of conversion zone and stripping section, the concrete distribution determined by nonlinear optimization method.
Situation two: for containing moderate fever effect (0.05≤Δ H
R/ Δ H
V≤ 1.0) reactive distillation column, (1) is expanded conversion zone in rectifying section, the top that spreading range can be from last piece column plate of rectifying section to tower, and particular location is determined by gradual search structure method; (2) conversion zone is expanded in stripping section, the bottom that spreading range can be from first block of column plate of stripping section to tower, and particular location is determined by gradual search structure method; (3) feed entrance point is moved in conversion zone, moving range can move to the other end of conversion zone from an end of conversion zone, and particular location is determined by gradual search structure method; (4) keep the total amount of catalyst constant, catalyst is carried out the emphasis distribution at the lap of conversion zone and stripping section and conversion zone and rectifying section, the concrete distribution determined by nonlinear optimization method.
Situation three: for containing on a small quantity or do not contain fully fuel factor (0≤Δ H
R/ Δ H
V＜0.05) reactive distillation column, (1) is expanded conversion zone in rectifying section, the top that spreading range can be from last piece column plate of rectifying section to tower, and particular location is determined by gradual search structure method; (2) conversion zone is expanded in stripping section, the bottom that spreading range can be from first block of column plate of stripping section to tower, and particular location is determined by gradual search structure method; (3) feed entrance point is moved in conversion zone, moving range can move to the other end of conversion zone from an end of conversion zone, and particular location is determined by gradual search structure method; (4) keep the total amount of catalyst constant, catalyst is carried out the emphasis distribution at the lap of conversion zone and stripping section and conversion zone and rectifying section, the concrete distribution determined by nonlinear optimization method.
When reactive distillation column contains heat-flash effect (Δ H
R/ Δ H
V＞1.0) time, process intensification only need be coupled by the internal energy of operation and distillation procedure and realize, this moment, the inner material coupling of operation and distillation procedure can be ignored.When reactive distillation column contains moderate fever effect (0.05≤Δ H
R/ Δ H
V≤ 1.0) time, process intensification not only needs the internal energy coupling by operation and distillation procedure, also will be coupled by the inner material of operation and distillation procedure and realize that this just need carry out the mutual compromise of the two.When reactive distillation column contains on a small quantity or do not contain fully fuel factor (0≤Δ H
R/ Δ H
V＜0.05) time, process intensification only need be coupled by the inner material of operation and distillation procedure and realize, this moment, the internal energy coupling of operation and distillation procedure can be ignored.For dissimilar reactive distillation columns, utilize four kinds of process intensification strategies to promote coupling of the inner material between the operation and distillation procedure and/or internal energy coupling in the reactive distillation column targetedly, these four kinds of process intensification strategies are that (1) is expanded conversion zone in rectifying section, the top that the scope of expansion can be from last piece column plate of rectifying section to tower; (2) conversion zone is expanded the bottom that the scope of expansion can be from first block of column plate of stripping section to tower in stripping section; (3) feed entrance point is done effectively move in conversion zone, the scope that moves can move to the other end of conversion zone from an end of conversion zone; (4) keep the total amount of catalyst constant, and catalyst is carried out the emphasis distribution at the lap of conversion zone and stripping section and conversion zone and rectifying section.
From technique scheme as can be seen, the present invention has following beneficial effect.
(1) utilize the present invention, owing to strengthened the inner material coupling of operation and distillation procedure and the effect of internal energy coupling to greatest extent, thereby can improve the thermodynamic efficiency of reactive distillation column greatly.
(2) utilize the present invention, owing to strengthened the inner material coupling of operation and distillation procedure and the effect of internal energy coupling to greatest extent, thereby can improve the conversion ratio and the selectivity of reaction.
(3) utilize the present invention, owing to strengthened the inner material coupling of operation and distillation procedure and the effect of internal energy coupling to greatest extent, thereby can further reduce the equipment investment cost of reactive distillation column.
(4) utilize the present invention,, thereby can improve operating flexibility, dynamic characteristic and the controllability of reactive distillation column because the inner material coupling has been coordinated the interaction of operation and distillation procedure with the reinforcement of internal energy coupling.
Description of drawings
Fig. 1 is the comprehensive and design procedure of the process intensification of reactive distillation column provided by the invention;
Fig. 2 is the tower (situation I) of traditional reactive distillation column;
Fig. 3 is the tower (situation I) of the process intensification reactive distillation column that obtains after the invention process;
Fig. 4 is the tower (situation II) of traditional reactive distillation column;
Fig. 5 is the tower (situation II) of the process intensification reactive distillation column that obtains after the invention process;
Fig. 6 is the tower (situation III) of traditional reactive distillation column;
Fig. 7 is the tower (situation III) of the process intensification reactive distillation column that obtains after the invention process;
Contrast schematic diagram (situation I) when Fig. 8 overcomes the treating capacity disturbance for traditional reactive distillation column and process intensification reactive distillation column;
Fig. 9 is the tower of traditional MTBE decomposition reaction destilling tower;
Figure 10 is the tower of the process intensification type MTBE decomposition reaction destilling tower that obtains after the invention process;
Dynamic response contrast schematic diagram when Figure 11 is traditional MTBE decomposition reaction destilling tower and the fluctuation of process intensification type MTBE decomposition reaction destilling tower setting value;
Figure 12 is the tower of traditional ethylene glycol synthetic reaction destilling tower;
Figure 13 is the tower of the process intensification type ethylene glycol synthetic reaction destilling tower that obtains after the invention process;
Dynamic response when Figure 14 overcomes the treating capacity disturbance for traditional ethylene glycol synthetic reaction destilling tower and process intensification type ethylene glycol synthetic reaction destilling tower contrasts schematic diagram.
E among Fig. 1
IMinimal energy consumption for employing method I gained; E
IIMinimal energy consumption for employing method II gained; E
IIIMinimal energy consumption for employing method III; E
MMinimal energy consumption for comprehensive employing method I, II and III gained;
F among Fig. 2,3,4,5,6,7
AFeed flow rates for material A; F
BFeed flow rates for material B; Q
CONLoad for condenser; Q
REBLoad for reboiler; RR is a capacity of returns; Holdup is a catalytic amount; D is the cat head load; x
CMolar fraction for component C; B is a load at the bottom of the tower; x
DMolar fraction for component D;
F among Fig. 9,10
MTBEFeed flow rates for material MTBE; Q
CONLoad for condenser; Q
REBLoad for reboiler; RR is a capacity of returns; D is the cat head load; x
IBUTMolar fraction for component I BUT; B is a load at the bottom of the tower; x
MEOHMolar fraction for component MEOH;
F among Figure 12,13
H2OBe material H
2The feed flow rates of O; F
EOFeed flow rates for material EO; L
1Be the overhead liquid capacity of returns; V
nBe the tower bottom steam capacity of returns; B is a load at the bottom of the tower; x
EOMolar fraction for component EO; x
WBe component H
2The molar fraction of O; x
EGMolar fraction for component EG; x
DEGMolar fraction for component DEG;
The specific embodiment
At first, use the comprehensive and method for designing of tradition and provide the traditional reactive distillation column of a conversion zone strictness between rectifying section and stripping section, wherein reaction-ure feeding all places the two ends of conversion zone.Comprehensive and the design procedure according to process intensification type shown in Figure 1 uses four kinds of process intensification strategies (1) proposed by the invention that conversion zone is expanded in rectifying section targetedly then; (2) conversion zone is expanded in stripping section; (3) feed entrance point is done effectively move in conversion zone; (4) catalyst is effectively distributed in conversion zone, strengthen the inner material coupling of operation and distillation procedure and the effect of internal energy coupling.The tower of the reactive distillation column that obtains thus will have higher thermodynamic efficiency, conversion ratio and selectivity than traditional reactive distillation column, lower equipment investment cost and the operating flexibility of improvement, dynamic characteristic and controllability.A kind of in the corresponding separately following three kinds of methods of method I among Fig. 1, method II and method III, but its corresponding relation is done certain adjustment with what order difference of energy consumption in the middle of design: and (1) is expanded conversion zone in rectifying section; (2) conversion zone is expanded in stripping section; (3) feed entrance point is done effectively move in conversion zone.At different reaction situations,, can determine to improve the design of reactive distillation column thermodynamic efficiency effectively according to step application method I, method II and method III shown in Figure 1.
The purpose, technical solutions and advantages of the present invention are more clear understands that below in conjunction with three specific embodiment, and with reference to accompanying drawing 2-14, the present invention is described in further detail in order to make.
Example 1: suppose in a reactive distillation column, to take place following desirable reversible heterogeneous reaction.
Wherein, A and B are reactants, and C and D are product and extract out at the bottom of cat head and tower respectively.The relative volatility of supposing this reactant mixture is α
A: α
B: α
C: α
D=4: 2: 8: 1, gasification latent heat was Δ H
V=29053.7kJ kmol
-1For the reaction heat of above-mentioned reversible reaction, consider three kinds of different situations, that is: situation I: Δ H
R=41840kJ kmol
-1Situation II: Δ H
R=14527kJ kmol
-1With situation III: Δ H
R=0kJ kmol
-1
Situation I: because Δ H
R/ Δ H
V=1.44＞1.0, so only need being coupled by means of the internal energy of operation and distillation procedure, realizes process intensification.Carry out the exploitation of reactive distillation column by three kinds of process intensification strategies.They are: (i) conversion zone is expanded in stripping section; (ii) feed entrance point is done effectively to move in conversion zone; (iii) catalyst is effectively distributed in conversion zone.According to system synthesis shown in Figure 1 and design procedure, and can obtain process intensification type shown in Figure 3 design from traditional design shown in Figure 2.Relatively these two designs can find that process intensification reactive distillation column: (i) conversion zone has been expanded 3 blocks of column plates in stripping section, and this determines by gradual search structure method.Its concrete principle is at first to expand the energy consumption of 1 block of column plate and checking system in stripping section.In stripping section, expand the energy consumption of 2 blocks of column plates and checking system and then, until searching the pairing expansion plate number of least energy consumption; (ii) the feed entrance point of material A has moved 1 block of column plate in conversion zone, and this also determines by gradual search structure method.Its concrete principle is at first the feed entrance point of material A to be moved the energy consumption of 1 block of column plate and checking system in conversion zone.And then the feed entrance point of material A is moved the energy consumption of 2 blocks of column plates and checking system in conversion zone, until the feed entrance point that searches the pairing material A of least energy consumption; (iii) catalyst has carried out effective distribution in conversion zone.The feed tray that is specially material A is divided into two parts with conversion zone, and each part has different catalyst concns, but the total amount of catalyst remains unchanged.It can pass through constrained nonlinear optimization method, as steepest gradient method etc., and is that the least energy consumption of decision variable search system is achieved with the catalyst concn of above-mentioned two parts.Through this kind design, the load of the reboiler of process intensification reactive distillation column has reduced by 13.08%.Because the influence of factors such as the minimizing of condenser and reboiler heat transfer area and tower diameter reduce, equipment investment cost also can significantly reduce.
Situation II: because 0.05＜Δ H
R/ Δ H
V=0.72＜1.0, so process intensification not only needs the internal energy coupling by operation and distillation procedure, also to be coupled and realize that this just need carry out the mutual compromise of the two by the inner material of operation and distillation procedure.In the comprehensive and design of system, can carry out the exploitation of reactive distillation column by four kinds of process intensification strategies.They are: (i) conversion zone is expanded in rectifying section; (ii) conversion zone is expanded in stripping section; (iii) feed entrance point is done effectively to move in conversion zone; (iv) catalyst is effectively distributed in conversion zone.According to system synthesis shown in Figure 1 and design procedure, and the process intensification type that can obtain as shown in Figure 5 from traditional design shown in Figure 4 designs.Relatively these two reactive distillation columns are not difficult to find that process intensification reactive distillation column: (i) conversion zone has been expanded 1 block of column plate in rectifying section, and this can determine by above-mentioned gradual search structure method; (ii) conversion zone has been expanded 3 blocks of column plates in stripping section, and this also can determine by above-mentioned gradual search structure method; (iii) the feed entrance point of material A and material B has moved 1 and 2 blocks of column plates respectively in conversion zone, and this also can determine by above-mentioned gradual search structure method respectively; (iv) catalyst has carried out effective distribution in conversion zone, and this can determine by above-mentioned constrained nonlinear optimization method.The feed tray that is specially two kinds of materials is divided into three parts with conversion zone, and various piece has different catalyst concns, but the total amount of catalyst remains unchanged.Through this kind design, the load of the reboiler of process intensification reactive distillation column has reduced by 15.35%.Because the influence of the factor such as reduce of the minimizing of condenser and reboiler heat transfer area and tower diameter, equipment investment cost also can significantly reduce.
Situation III: because 0=Δ H
R/ Δ H
V＜0.05, process intensification only need be coupled by means of the inner material of operation and distillation procedure and realize because this moment operation and distillation procedure the internal energy coupling can ignore.In the comprehensive and design of system, can carry out the exploitation of reactive distillation column by four kinds of process intensification strategies.They are: (i) conversion zone is expanded in rectifying section; (ii) conversion zone is expanded in stripping section; (iii) feed entrance point is done effectively to move in conversion zone; (iv) catalyst is effectively distributed in conversion zone.According to system synthesis shown in Figure 1 and design procedure, and the process intensification type that can obtain as shown in Figure 7 from traditional design shown in Figure 6 designs.Relatively these two reactive distillation columns are not difficult to find that process intensification reactive distillation column: (i) conversion zone has been expanded 1 block of column plate in rectifying section, and this can determine by above-mentioned gradual search structure method; (ii) conversion zone has been expanded 3 blocks of column plates in stripping section, and this also can determine by above-mentioned gradual search structure method; (iii) the feed entrance point of material B has moved 3 blocks of column plates in conversion zone, and this also can determine by above-mentioned gradual search structure method; (iv) catalyst effectively distributes in conversion zone, and this can determine by above-mentioned constrained nonlinear optimization method.The feed tray that is specially two kinds of materials is divided into three parts with conversion zone, and various piece has different catalyst concns, but the total amount of catalyst is constant substantially.Through this kind design, the load of the reboiler of process intensification reactive distillation column has reduced by 13.89%.Because the influence of the factor such as reduce of the minimizing of condenser and reboiler heat transfer area and tower diameter, equipment investment cost also can significantly reduce.
Fig. 8 has provided the contrast schematic diagram when traditional reactive distillation column and process intensification reactive distillation column overcome the treating capacity disturbance among the situation I.As can be seen, the tower of process intensification reactive distillation column also makes operating flexibility, dynamic characteristic and the controllability of system obtain improvement to a certain degree.
The decomposition reaction of example 2:MTBE is a reversible strong endothermic reaction, and it can carry out in a reactive distillation column.
Because Δ H
R/ Δ H
V＞1.0, so process intensification only need be coupled by means of the internal energy of operation and distillation procedure and realizes.In the comprehensive and design of system, can realize by following three kinds of modes.They are: (i) conversion zone is expanded in rectifying section; (ii) feed entrance point is done effectively to move in conversion zone; (iii) catalyst is effectively distributed in conversion zone.According to system synthesis shown in Figure 1 and design procedure, and the process intensification type that can obtain as shown in figure 10 from traditional design shown in Figure 9 designs.Relatively these two reactive distillation columns are not difficult to find that process intensification reactive distillation column: (i) conversion zone has been expanded 2 blocks of column plates in rectifying section, and this can determine by above-mentioned gradual search structure method; (ii) the feed entrance point of material MTBE has moved 7 blocks of column plates in conversion zone, and this also can determine by above-mentioned gradual search structure method; (iii) catalyst has carried out effective distribution in conversion zone, but the total amount of catalyst remains unchanged, and this can determine by above-mentioned constrained nonlinear optimization method.Through this kind design, the load of the reboiler of process intensification reactive distillation column has reduced by 94.46%.Because the influence of the factor such as reduce of the minimizing of condenser and reboiler heat transfer area and tower diameter, equipment investment cost also can significantly reduce.Dynamic response contrast schematic diagram when Figure 11 has provided traditional reactive distillation column and process intensification reactive distillation column and overcomes external disturbance.As can be seen, the design of process intensification type also makes operating flexibility, dynamic characteristic and the controllability of system produce improvement to a certain degree.
Example 3: the synthetic reaction of ethylene glycol is an irreversible strong exothermal reaction, and it also can carry out in a reactive distillation column.
C
2H
4O(EO)+H
2O(W)→C
2H
6O
2(EG) (3)
C
2H
4O(EO)+C
2H
6O
2(EG)→C
4H
10O
3(DEG) (4)
Because Δ H
R/ Δ H
V＞1.0, so process intensification only need be coupled by means of the internal energy of operation and distillation procedure and realizes.In the comprehensive and design of system, can realize by following three kinds of modes.They are: (i) conversion zone is expanded in stripping section; (ii) feed entrance point is done effectively to move in conversion zone; (iii) catalyst is effectively distributed in conversion zone.According to system synthesis shown in Figure 1 and design procedure, and can obtain the tower of process intensification reactive distillation column as shown in figure 13 from traditional design shown in Figure 12.Relatively these two reactive distillation columns are not difficult to find that process intensification reactive distillation column: (i) conversion zone has been expanded 4 blocks of column plates in stripping section, and this can determine by above-mentioned gradual search structure method; (ii) the feed entrance point of material EO has moved 2 blocks of column plates in conversion zone, and this also can determine by above-mentioned gradual search structure method; (iii) catalyst has carried out effective distribution in conversion zone, and the total amount of catalyst remains unchanged, and this can determine by above-mentioned constrained nonlinear optimization method.Through this kind design, the load of the reboiler of process intensification reactive distillation column has reduced by 10.43%.Because the influence of the factor such as reduce of the minimizing of condenser and reboiler heat transfer area and tower diameter, equipment investment cost also can significantly reduce.Dynamic response contrast schematic diagram when Figure 14 has provided traditional reactive distillation column and process intensification reactive distillation column and overcomes the treating capacity disturbance.As can be seen, the tower of process intensification reactive distillation column also makes operating flexibility, dynamic characteristic and the controllability of system produce improvement to a certain degree.
By above-described three specific embodiment, purpose of the present invention, technical scheme and beneficial effect have been made further instruction.Should be pointed out that the above only is specific embodiments of the invention, they are not limited to the present invention.Within the spirit and principles in the present invention all, any modification of being done, be equal to and replace and improvement etc., all should be included within protection scope of the present invention.
Claims (1)
1. the method for designing of process intensification reactive distillation column comprises that the ratio of the latent heat of vaporization of reaction heat and reactant mixture is Δ H according to three kinds of situations of the ratio of the latent heat of vaporization of reaction heat and reactant mixture
R/ Δ H
V, Δ H wherein
VBe gasification latent heat, Δ H
RBe reaction heat, it is characterized in that:
Situation one: for containing the heat-flash effect is Δ H
R/ Δ H
V＞1.0 reactive distillation column is divided into two kinds of situations:
1) for the endothermic reaction, (1) conversion zone is expanded in rectifying section, the top of spreading range from last piece column plate of rectifying section to tower, and particular location is determined by the following method, at first in rectifying section, expand the energy consumption of 1 block of column plate and checking system, in rectifying section, expand the energy consumption of 2 blocks of column plates and checking system and then, until searching the pairing expansion plate number of least energy consumption; (2) feed entrance point is moved in conversion zone, moving range moves to the other end of conversion zone from an end of conversion zone, and particular location is determined by the following method, at first the feed entrance point of material is moved the energy consumption of 1 block of column plate and checking system in conversion zone, and then the feed entrance point of material is moved the energy consumption of 2 blocks of column plates and checking system in conversion zone, until the feed entrance point that searches the pairing material of least energy consumption; (3) keep the total amount of catalyst constant, catalyst is carried out the emphasis distribution at the lap of conversion zone and rectifying section, the concrete distribution determined by nonlinear optimization method;
2) for exothermic reaction, (1) conversion zone is expanded in stripping section, the bottom of spreading range from first block of column plate of stripping section to tower, and particular location is determined by the following method, at first in stripping section, expand the energy consumption of 1 block of column plate and checking system, in stripping section, expand the energy consumption of 2 blocks of column plates and checking system and then, until searching the pairing expansion plate number of least energy consumption; (2) feed entrance point is moved in conversion zone, moving range moves to the other end of conversion zone from an end of conversion zone, and particular location is determined by the following method, at first the feed entrance point of material is moved the energy consumption of 1 block of column plate and checking system in conversion zone, and then the feed entrance point of material is moved the energy consumption of 2 blocks of column plates and checking system in conversion zone, until the feed entrance point that searches the pairing material of least energy consumption; (3) keep the total amount of catalyst constant, catalyst is carried out the emphasis distribution at the lap of conversion zone and stripping section, the concrete distribution determined by nonlinear optimization method;
Situation two: for containing the i.e. 0.05≤Δ H of moderate fever effect
R/ Δ H
V≤ 1.0 reactive distillation column, (1) conversion zone is expanded in rectifying section, the top of spreading range from last piece column plate of rectifying section to tower, and particular location is determined by the following method, at first in stripping section, expand the energy consumption of 1 block of column plate and checking system, in stripping section, expand the energy consumption of 2 blocks of column plates and checking system and then, until searching the pairing expansion plate number of least energy consumption; (2) conversion zone is expanded in stripping section, the bottom of spreading range from first block of column plate of stripping section to tower, and particular location is determined by the following method, at first in stripping section, expand the energy consumption of 1 block of column plate and checking system, in stripping section, expand the energy consumption of 2 blocks of column plates and checking system and then, until searching the pairing expansion plate number of least energy consumption; (3) feed entrance point is moved in conversion zone, moving range moves to the other end of conversion zone from an end of conversion zone, and particular location is determined by the following method, at first the feed entrance point of material is moved the energy consumption of 1 block of column plate and checking system in conversion zone, and then the feed entrance point of material is moved the energy consumption of 2 blocks of column plates and checking system in conversion zone, until the feed entrance point that searches the pairing material of least energy consumption; (4) keep the total amount of catalyst constant, catalyst is carried out the emphasis distribution at the lap of conversion zone and stripping section and conversion zone and rectifying section, the concrete distribution determined by nonlinear optimization method;
Situation three: for containing on a small quantity or do not contain fully the i.e. 0≤Δ H of fuel factor
R/ Δ H
V＜0.05 reactive distillation column, (1) conversion zone is expanded in rectifying section, the top of spreading range from last piece column plate of rectifying section to tower, and particular location is determined by the following method, at first in stripping section, expand the energy consumption of 1 block of column plate and checking system, in stripping section, expand the energy consumption of 2 blocks of column plates and checking system and then, until searching the pairing expansion plate number of least energy consumption; (2) conversion zone is expanded in stripping section, the bottom of spreading range from first block of column plate of stripping section to tower, and particular location is determined by the following method, at first in stripping section, expand the energy consumption of 1 block of column plate and checking system, in stripping section, expand the energy consumption of 2 blocks of column plates and checking system and then, until searching the pairing expansion plate number of least energy consumption; (3) feed entrance point is moved in conversion zone, moving range moves to the other end of conversion zone from an end of conversion zone, and particular location is determined by the following method, at first the feed entrance point of material is moved the energy consumption of 1 block of column plate and checking system in conversion zone, and then the feed entrance point of material is moved the energy consumption of 2 blocks of column plates and checking system in conversion zone, until the feed entrance point that searches the pairing material of least energy consumption; (4) keep the total amount of catalyst constant, catalyst is carried out the emphasis distribution at the lap of conversion zone and stripping section and conversion zone and rectifying section, the concrete distribution determined by nonlinear optimization method.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1356301A (en) * | 2001-10-23 | 2002-07-03 | 中国石油化工股份有限公司 | External coupler of rectifying reaction for preparing cyclohexane by catalyst hydrogenation of benzene and its synthesizing process |
| CN1368897A (en) * | 1999-12-11 | 2002-09-11 | 伊丽沙白·童 | New design of reactive distillation technology |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1368897A (en) * | 1999-12-11 | 2002-09-11 | 伊丽沙白·童 | New design of reactive distillation technology |
| CN1356301A (en) * | 2001-10-23 | 2002-07-03 | 中国石油化工股份有限公司 | External coupler of rectifying reaction for preparing cyclohexane by catalyst hydrogenation of benzene and its synthesizing process |
Non-Patent Citations (3)
| Title |
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| F. Zhuetal..Towards furtherinternalheatintegrationindesignofreactivedistillationcolumns—Part IV:Applicationtoahigh-purityethyleneglycolreactivedistillationcolumn.《ChemicalEngineeringScience》.2009,第64卷3498--3509. * |
| K. Iwakabe et al..Energy saving in multicomponent separation using an internally heat-integrated distillation column (HIDiC).《Applied Thermal Engineering》.2005,第26卷1362–1368. * |
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