CN105777472B - It is a kind of to separate pentane, hexane, heptane and the method for octane mixture system - Google Patents
It is a kind of to separate pentane, hexane, heptane and the method for octane mixture system Download PDFInfo
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Abstract
The present invention separates pentane, hexane, heptane and the method for octane mixture system to be a kind of.This method uses Sargent dividing wall columns, and three pieces of vertical clapboards are provided with tower, and rectifying column is divided into prefractionation section, interlude, public rectifying section, side take-off section and public stripping section totally five part；Mixture system is entered into Sargent dividing wall columns at the 20th block of column plate of prefractionation section, finally in the public rectifying section extraction pentane logistics of tower top, the side take-off hexane streams at the 16th block of column plate of side take-off section, the side take-off heptane logistics at the 44th block of column plate of side take-off section, in the public stripping section extraction octane of bottom of towe.The present invention product purity with densimeter more than 99%, it is identical with the product purity of the flow of conventional rectification direct sequence；The separation task of former flow can be not only completed, and compared with conventional rectification direct sequence, total load highest that exchanges heat can reduce by 42.5%.
Description
Technical field
The present invention relates to it is a kind of separate pentane, hexane, heptane, octane mixture system method.
Background technology
Rectifying is that use range is most wide in chemical industry, the operation of unit of high energy consumption.The energy consumption of distillation process is huge, changes
40~70% energy consumption is used to separate during work, and the energy consumption of rectifying accounts for the 95% of separating energy consumption.Energy prices continue
Go up and the research of distillation process power-saving technology is had great importance.Separation for ternary or ternary above component, is adopted
Multitower energy consumption of rectification with routine is big, and rectifying can greatly reduce energy consumption in partitioned column.
The whole world has more than the partitioned column of 300 and come into operation at present, and Koch-Glitsh companies are successfully by Algeciras
An isohexane solvent recovery tower of oil plant transform partitioned column as, compared to existing equipment, partitioned column saving energy 40%.
Kellogg and BP companies design the partitioned column suitable for alkyl reforming process, and rectifying, stripping and solvent are realized in a tower
Various procedures are reclaimed, it adds one times compared to the production capacity of original technique.I.J.Halvorsena et al. is in the literature
The specific structure for describing Sargent dividing wall columns, it is three pieces of vertical clapboards of installation in rectifying column, and rectifying column is divided into
Prefractionation section, interlude, public rectifying section, side take-off section and public stripping section totally five part；For four component mixtures
Feed side is prefractionation section, and the charging of interlude is two product stream stocks of prefractionation section, and side take-off side is referred to as side line and adopted
Go out section, three product stream stocks of middle tower section are public stripping section, side take-off section and public stripping section enter stream stock, through point
From obtaining meeting four set products of product purity requirement.Four component mixtures are separated into Sargent dividing wall columns pure
Product only needs a tower, a reboiler, a condenser and a reflux splitter, energy consumption and equipment investment all to be dropped
It is low.
Meanwhile Sargent tower structures are complicated.Because the component of mixed material is numerous and diverse, three pieces of vertical clapboards in different towers
Position is difficult to determine, simultaneously for different feed rate and composition, the number of plates and the overhead reflux ratio of each tower section, is slightly become
Change the efficiency for just substantially reducing Sargent dividing wall columns, seriously constrain its application in the separation of not jljl system.
In pentane, hexane, heptane, the component mixture system isolation technics route of octane four, traditional handicraft at least needs three
Individual rectifying column can be only achieved the separating effect of requirement, but this method technological process is grown, and investment is big, high energy consumption, and floor space is big.
The present invention separates pentane, hexane, heptane, the new technology of octane mixture system for Sargent dividing wall columns, obtains meeting separation
It is required that while product, process route is optimized, has reached the purpose for reducing energy consumption and reducing equipment investment.
The content of the invention
To be solved by this invention is pentane, hexane, heptane, octane mixture system present in traditional three tower process flows
Separation process is complicated, and separation purity is not high, and investment is big, the technical problem of high energy consumption, there is provided a kind of new separation pentane, hexane,
Heptane, the method for octane mixture system.This method uses Sargent dividing wall columns, and is directed to different feed rate and group
Into the number of plates of fixed prefractionation section, interlude and side take-off section, passing through the public rectifying section of design optimization and public stripping section
The number of plates and overhead reflux ratio, the product that meets separation requirement can be accessed and realize the purpose of energy-conservation.This method
Simple with flow, good separating effect, energy consumption is low, and investment reduces the advantages of notable.
The technical scheme is that：
It is a kind of to separate pentane, hexane, heptane and the method for octane mixture system, comprise the following steps：
Pentane, hexane, heptane and octane mixture system will be contained and enter Sargent dividing plates at the 20th block of column plate of prefractionation section
Rectifying column, after the separation by prefractionation section, the mixture of pentane, hexane and heptane enters interlude the at the top of prefractionation section
16 blocks of column plates, the mixture of hexane, heptane and octane enter at the 36th block of column plate of interlude from prefractionation section bottom；By centre
After the separation of section, pentane and hexanes mixtures enter the 1st block of column plate of side take-off section and public rectifying section from mid-section top
Bottom, hexane and heptane mixture enter the 35th block of column plate of side take-off section from the 31st block of column plate of interlude, heptane and octane
Mixture enters from mid-section bottom at the 64th block of column plate of side take-off section and at the top of public stripping section；Through each section of separation
Afterwards, finally in the extraction pentane logistics of tower top public rectifying section, the side take-off hexane streams at the 16th block of column plate of side take-off section,
The side take-off heptane logistics at the 44th block of column plate of side take-off section, in the public stripping section extraction octane of bottom of towe；
Wherein, three pieces of vertical clapboards are installed in described Sargent dividing wall columns, rectifying column is divided into prefractionation
Section, interlude, public rectifying section, side take-off section and public stripping section totally five part；
The prefractionation section of described Sargent dividing wall columns has 30 blocks of column plates；
The interlude and side take-off section of the Sargent dividing wall columns respectively have 64 blocks of column plates；
The extraction position of the hexane streams of the Sargent dividing wall columns is at the 16th block of column plate of side take-off section；Heptan
The extraction position of alkane logistics is at the 44th block of column plate of side take-off section；
1~30 block of column plate of prefractionation Duan Cong and the column plate of interlude the 16th~45 of described Sargent dividing wall columns
Between set first piece of vertical clapboard；Is set between the 1st~34 block of column plate of the 1st~30 block of column plate of interlude and side take-off section
Two pieces of vertical clapboards；Between the 32nd~64 block of column plate of interlude and the 36th~65 block of column plate of side take-off section set the 3rd piece every
Plate；
The public rectifying section of Sargent dividing wall columns has 5~50 blocks of column plates；
The public stripping section of Sargent dividing wall columns has 10~50 blocks of column plates；
The Sargent dividing wall columns tower top is using the reflux ratio of densimeter as 2~20；
The pentane, hexane, heptane, octane mixture system feed rate are 20~800kmol/h；
The content of pentane is 1~40% in described feed stream, and the content of hexane is 10~70%, and the content of heptane is
10~70%, the content of octane is 1~40%；Described percentage composition is in terms of molar content；
After being separated using Sargent dividing wall columns, pentane, hexane, heptane, the molar fraction of octane can reach 99%
More than.
The invention has the advantages that：
(1) present invention uses Sargent dividing plate rectification process.Have three in the Sargent dividing wall columns that the technique uses
Block vertical partition plate, rectifying column is divided into prefractionation section, interlude, public rectifying section, side take-off section and public stripping section totally five
Part.Light component pentane is produced respectively from overhead extraction, intermediate species hexane and heptane by side take-off section, heavy constituent octane by
Tower reactor produces, it is only necessary to which a set of Tower System can be achieved with the separation of four components.Compared with conventional rectification direct sequence, the present invention
Reduce two condensers and two reboilers and two sets of rectifying columns, equipment investment reduces about 20%.
(2) use technology of the present invention, the product purities of Sargent dividing wall columns with densimeter 99% with
On, it is identical with the product purity of conventional process flow；The separation of former flow can be not only completed using Sargent dividing wall columns
Task, and compared with conventional rectification direct sequence, total load highest that exchanges heat can reduce by 42.5%, have preferable technology effect
Fruit.
Brief description of the drawings
Fig. 1 is the process chart of the present invention；
Fig. 2 is the process chart of conventional rectification direct sequence.
In Fig. 1：The public stripping sections of 1-；2- prefractionation sections；3- interludes；First piece of vertical clapboard of 4-；The public stripping sections of 5-；
6- overhead condensers；Second piece of vertical clapboard of 7-；8- side take-off sections；The 3rd piece of vertical clapboard of 9-；10- tower reactor reboilers；F-
Pentane, hexane, heptane, octane mixture；D- light component pentanes；S1- intermediate species hexanes；S2- intermediate species heptane；W- is recombinated
Divide octane.
In Fig. 2：11- towers I；12- towers II；13- towers III；F- pentanes, hexane, heptane, octane mixture；D1- tower tops discharge
Pentane；D2- tower tops discharging hexane；D3- tower tops discharging heptane；W3- tower reactors discharging octane.
The present invention is described in more detail below.But following examples is only the simple example of the present invention, not generation
Table or limitation the scope of the present invention, protection scope of the present invention are defined by claims.
Embodiment
Further illustrate technical scheme below in conjunction with the accompanying drawings and by embodiment.
For the present invention is better described, technical scheme is readily appreciated, of the invention is typical but non-limiting
Embodiment is as follows：
As shown in figure 1, a kind of separation pentane, hexane, heptane, the method for octane mixture system, using Sargent dividing plates essence
Tower continuous rectification is evaporated, rectifying column is divided into five active sections by vertical clapboard 4,7 and 9：Prefractionation section 2, interlude 3, public rectifying
Section 1, side take-off section 8 and public stripping section 5；Prefractionation section 2 has 30 blocks of column plates, and interlude 3 and side take-off section 8 respectively have 64 pieces
Column plate.
The 1st~30 block of column plate of prefractionation section 2 and the column plate of interlude 3 the 16th~45 of described Sargent dividing wall columns
Between set first piece of vertical clapboard 4；Set between the 1st~30 block of column plate of interlude 3 and the 1st~34 block of column plate of side take-off section 8
Put second piece of vertical clapboard 7；Is set between the 36th~65 block of column plate of the 32nd~64 block of column plate of interlude 3 and side take-off section 8
Three pieces of dividing plates 9.
Raw material F containing pentane, hexane, heptane, octane mixture system enters Sargent from the 20th block of column plate of prefractionation section 2
Dividing wall column, the non-clear segmentation of pentane and octane is completed in prefractionation section 2, hexane and heptane exist according to relative volatility
Top and bottom are freely distributed, and the mixture of pentane, hexane and heptane enters the 16th piece of tower of interlude 3 from the top of prefractionation section 2
Plate, the mixture of hexane, heptane and octane enters the 36th block of column plate of interlude 3 from the bottom of prefractionation section 2, on the top of interlude 3
The non-clear segmentation of pentane and heptane is completed, the non-clear segmentation of hexane and octane is completed in bottom；Pentane and hexanes mixtures from
The top of interlude 3 enter side take-off section 8 top and public rectifying section 1, hexane and heptane mixture from the 31st piece of interlude 3
Column plate enters the 35th block of column plate of side take-off section 8, and the mixture of heptane and octane enters side take-off section 8 from the bottom of interlude 3
Bottom and public stripping section 5；After each section of separation, pentane logistics D finally is produced in the public rectifying section 1 of tower top, in side line
The 16th piece of column plate side take-off hexane streams S1 of section 8 is produced, in the 44th piece of column plate side take-off heptane logistics of side take-off section 8
S2, octane logistics W is produced in the public stripping section 5 of bottom of towe, so as to realize the separation of pentane, hexane, heptane, octane.
The pentane, hexane, heptane, octane mixture F feed rate are 20~800kmol/h, pentane in logistics
Content is 1~40%, and the content of hexane is 10~70%, and the content of heptane is 10~70%, and the content of octane is 1~40%.
The public rectifying section of Sargent dividing wall columns has 5~50 blocks of column plates, and the public stripping section of rectifying column has 10~50
Block column plate, tower top is using the reflux ratio of densimeter as 2~20.
The operating pressure of the Sargent dividing wall columns is normal pressure.
After being separated using Sargent dividing wall columns, pentane, hexane, heptane, the molar fraction of octane can reach 99%
More than.
Fig. 2 shows the process chart of conventional rectification direct sequence.Pentane, hexane, heptane, the mixture F of octane enter
Enter tower I, the separation of pentane is mainly completed in tower I, D1 is tower top discharging pentane.Enter tower II from the mixture of bottom of towe extraction,
The separation of hexane is completed in tower II, D2 is tower top discharging hexane.Enter tower III from the mixture of bottom of towe extraction, it is complete in tower III
Into the separation of heptane and octane, D3 is tower top discharging heptane, and W3 is tower reactor discharging octane.
Embodiment 1
Using the flow shown in Fig. 1, pentane to be separated, hexane, heptane, the inlet amount of octane mixture are 40kmol/
H, pentane, hexane, heptane, the mol ratio of octane are 1:1:1:1.The Sargent dividing wall column prefractionation sections of use have 30 pieces
Column plate, interlude and side take-off section respectively have 64 blocks of column plates, and public rectifying section has 10 blocks of column plates, public 20 blocks of column plates of stripping section,
Produced quantity is 10kmol/h；The extraction position of hexane streams is produced quantity 10kmol/h at the 16th block of column plate of side take-off section；
The extraction position of heptane logistics is produced quantity 10kmol/h at the 44th block of column plate of side take-off section；Overhead reflux is than 11, operation
Pressure is normal pressure, tower diameter 3m.Sargent dividing wall column component separating effects are shown in Table 1, and energy consumption result is listed in table 2.
Using the flow shown in Fig. 2, inlet amount and charging mole composition are constant, and tower I shares 20 blocks of column plates, and the 10th block of plate enters
Material, reflux ratio 3；Tower II shares 20 blocks of column plates, the 10th piece of plate charging, reflux ratio 4；Tower III shares 20 blocks of column plates, the 10th piece
Plate is fed, reflux ratio 4；The operating pressure of three towers is normal pressure.For ease of comparing, energy consumption result is also found in table 2.
Table 1 lists the separating effect using Sargent dividing wall columns
| Product purity (concentration %) | Pentane | Hexane | Heptane | Octane |
| Public rectifying section D | 0.999 | 0.001 | — | — |
| Side take-off section S1 | 0.001 | 0.999 | — | — |
| Side take-off section S2 | — | — | 0.999 | 0.001 |
| Public stripping section W | — | — | 0.001 | 0.999 |
Table 2 lists the energy consumption comparative result using Sargent dividing wall columns and conventional rectification direct sequence
Embodiment 2
Using the flow shown in Fig. 1, in the case that inlet amount is constant, pentane, hexane, heptane, the mol ratio of octane are changed into
1:2:2:1.The Sargent dividing wall column prefractionation sections of use have 30 blocks of column plates, and interlude and side take-off section respectively have 64 pieces
Column plate, public rectifying section have 40 blocks of column plates, public 30 blocks of column plates of stripping section, produced quantity 6.67kmol/h；Hexane streams are adopted
Out position is produced quantity 13.33kmol/h at the 16th block of column plate of side take-off section；Adopted for side line the extraction position of heptane logistics
Go out at the 44th block of column plate of section, produced quantity 13.33kmol/h；For overhead reflux than 17.2, operating pressure is normal pressure, and tower diameter is
2.73m.Sargent dividing wall column component separating effects are shown in Table 3, and energy consumption result is listed in table 4.
Using the flow shown in Fig. 2, inlet amount and charging mole composition are constant, and tower I shares 34 blocks of column plates, and the 21st block of plate enters
Material, reflux ratio 11.7；Tower II shares 30 blocks of column plates, the 17th piece of plate charging, reflux ratio 2.2；Tower III shares 20 blocks of column plates,
7th piece of plate charging, reflux ratio 2.7；The operating pressure of three towers is normal pressure.For ease of comparing, energy consumption result is also found in table 4.
Table 3 lists the separating effect using Sargent dividing wall columns
| Product purity (concentration %) | Pentane | Hexane | Heptane | Octane |
| Public rectifying section D | 0.999 | 0.001 | — | — |
| Side take-off section S1 | 0.001 | 0.99 | 0.009 | — |
| Side take-off section S2 | — | 0.009 | 0.99 | 0.001 |
| Public stripping section W | — | — | 0.001 | 0.999 |
Table 4 lists the energy consumption comparative result using Sargent dividing wall columns and conventional rectification direct sequence
Embodiment 3
Using the flow shown in Fig. 1, in the case that inlet amount is constant, pentane, hexane, heptane, the mol ratio of octane are changed into
2:1:1:1.The Sargent dividing wall column prefractionation sections of use have 30 blocks of column plates, and interlude and side take-off section respectively have 64 pieces
Column plate, public rectifying section have 30 blocks of column plates, public 30 blocks of column plates of stripping section, produced quantity 8kmol/h；The extraction position of hexane streams
It is set at the 16th block of column plate of side take-off section, produced quantity 8kmol/h；The extraction position of heptane logistics is side take-off section the 44th
At block column plate, produced quantity 8kmol/h；For overhead reflux than 6.4, operating pressure is normal pressure.Tower diameter is 2.76m.Sargent dividing plates
Rectifying column component separating effect is shown in Table 5, and energy consumption result is listed in table 6.
Using the flow shown in Fig. 2, inlet amount and charging mole composition are constant, and tower I shares 27 blocks of column plates, and the 13rd block of plate enters
Material, reflux ratio 3.4；Tower II shares 36 blocks of column plates, the 23rd piece of plate charging, reflux ratio 4；Tower III shares 20 blocks of column plates, the 7th piece
Plate is fed, reflux ratio 4.3；The operating pressure of three towers is normal pressure.For ease of comparing, energy consumption result is also found in table 6.
Table 5 lists the separating effect using Sargent dividing wall columns
| Product purity (concentration %) | Pentane | Hexane | Heptane | Octane |
| Public rectifying section D | 0.998 | 0.002 | — | — |
| Side take-off section S1 | — | 0.999 | 0.001 | — |
| Side take-off section S2 | — | 0.01 | 0.99 | 0.001 |
| Public stripping section W | — | — | 0.008 | 0.992 |
Table 6 lists the energy consumption comparative result using Sargent dividing wall columns and conventional rectification direct sequence
Embodiment 4
Using the flow shown in Fig. 1, pentane to be separated, hexane, heptane, the inlet amount of octane mixture are 600kmol/
H, pentane, hexane, heptane, the mol ratio of octane are 1:2:1:2.The Sargent dividing wall column prefractionation sections of use have 30 pieces
Column plate, interlude and side take-off section respectively have 64 blocks of column plates, and public rectifying section has 10 blocks of column plates, public 20 blocks of column plates of stripping section,
Produced quantity is 200kmol/h；The extraction position of hexane streams is produced quantity 200kmol/ at the 16th block of column plate of side take-off section
h；The extraction position of heptane logistics is produced quantity 100kmol/h at the 44th block of column plate of side take-off section；Overhead reflux ratio
11.7, operating pressure is normal pressure, tower diameter 9.77m.Sargent dividing wall column component separating effects are shown in Table 7, energy consumption result row
In table 8.
Using the flow shown in Fig. 2, inlet amount and charging mole composition are constant, and tower I shares 20 blocks of column plates, and the 10th block of plate enters
Material, reflux ratio 3；Tower II shares 20 blocks of column plates, the 10th piece of plate charging, reflux ratio 4；Tower III shares 20 blocks of column plates, the 10th piece
Plate is fed, reflux ratio 4；The operating pressure of three towers is normal pressure.For ease of comparing, energy consumption result is also found in table 8.
Table 7 lists the separating effect using Sargent dividing wall columns
| Product purity (concentration %) | Pentane | Hexane | Heptane | Octane |
| Public rectifying section D | 0.999 | 0.001 | — | — |
| Side take-off section S1 | — | 0.995 | 0.005 | — |
| Side take-off section S2 | — | 0.009 | 0.99 | 0.001 |
| Public stripping section W | — | — | 0.001 | 0.999 |
Table 8 is listed using Sargent dividing wall columns and conventional rectification direct sequence energy consumption result of the comparison
The not described matters of the present invention are known technology.
Claims (3)
1. a kind of separate pentane, hexane, heptane and the method for octane mixture system, it is characterized in that comprising the following steps：
Pentane, hexane, heptane and octane mixture system will be contained and enter Sargent dividing plate rectifying at the 20th block of column plate of prefractionation section
Tower, after the separation by prefractionation section, the mixture of pentane, hexane and heptane enters the 16th piece of interlude at the top of prefractionation section
Column plate, the mixture of hexane, heptane and octane enter at the 36th block of column plate of interlude from prefractionation section bottom；By interlude
After separation, pentane and hexanes mixtures enter the 1st block of column plate of side take-off section and public rectifying section bottom from mid-section top,
Hexane and heptane mixture enter the mixture of the 35th block of column plate of side take-off section, heptane and octane from the 31st block of column plate of interlude
Enter from mid-section bottom at the 64th block of column plate of side take-off section and at the top of public stripping section；After each section of separation, finally
In the public rectifying section extraction pentane logistics of tower top, the side take-off hexane streams at the 16th block of column plate of side take-off section, in side line
Side take-off heptane logistics at the 44th block of column plate of section is produced, in the public stripping section extraction octane of bottom of towe；
Wherein, three pieces of vertical clapboards are installed in described Sargent dividing wall columns, by rectifying column be divided into prefractionation section, in
Between section, public rectifying section, side take-off section and public stripping section totally five part；
The prefractionation section of described Sargent dividing wall columns has 30 blocks of column plates；
The interlude and side take-off section of the Sargent dividing wall columns respectively have 64 blocks of column plates；
The extraction position of the hexane streams of the Sargent dividing wall columns is at the 16th block of column plate of side take-off section；Heptane thing
The extraction position of stream is at the 44th block of column plate of side take-off section；
Between 1~30 block of column plate of prefractionation Duan Cong and the column plate of interlude the 16th~45 of described Sargent dividing wall columns
First piece of vertical clapboard is set；Second piece is set between the 1st~30 block of column plate of interlude and the 1st~34 block of column plate of side take-off section
Vertical clapboard；3rd piece of dividing plate is set between the 32nd~64 block of column plate of interlude and the 36th~64 block of column plate of side take-off section；
The public rectifying section of Sargent dividing wall columns has 5~50 blocks of column plates；
The public stripping section of Sargent dividing wall columns has 10~50 blocks of column plates；
The Sargent dividing wall columns tower top is using the reflux ratio of densimeter as 2~20.
2. separation pentane, hexane, heptane and the method for octane mixture system as claimed in claim 1, it is characterized in that described penta
Alkane, hexane, heptane, octane mixture system feed rate are 20~800kmol/h.
3. separation pentane, hexane, heptane and the method for octane mixture system as claimed in claim 1, it is characterized in that raw material thing
The content of pentane is 1~40% in stream, and the content of hexane is 10~70%, and the content of heptane is 10~70%, and the content of octane is 1
~40%；Described percentage composition is in terms of molar content.
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