CN104027995B - The method of Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system - Google Patents
The method of Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system Download PDFInfo
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Abstract
The present invention relates to a kind of method of Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system, mainly solve the benzene, ethylbenzene, many ethylbenzene, the heavy constituent mixing system separation process complexity that exist in existing traditional Benzene Device, separation purity is not high, and investment is large, the problem that energy consumption is high.The present invention enters bilateral line rectifying tower with bulkhead by adopting the raw material containing benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system from the first bulkhead section side, through being separated, ethylbenzene stream is obtained at the first bulkhead section opposite side, the second bulkhead section side line many ethylbenzene stream, benzene logistics is obtained at the above rectifying section of the first bulkhead section, the technical scheme obtaining heavy constituent logistics at the following stripping section of the second bulkhead section solves this problem preferably, can be used in the industrial production of Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system.
Description
Technical field
The present invention relates to a kind of method of Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system.
Background technology
In traditional Benzene Device isolation technics route, the material containing benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system enters benzene tower and carries out initial gross separation, removed overhead benzene and light component, and tower reactor discharging forms primarily of ethylbenzene, many ethylbenzene and heavy constituent.Benzene tower tower reactor material out enters ethylbenzene tower and is further separated, ethylbenzene tower tower top isolate be by weight more than 99.95% ethylbenzene component, and tower reactor discharging is many ethylbenzene and heavy constituent.Ethylbenzene tower kettle material goes many ethylbenzene towers to carry out next step separation again.Many ethylbenzene towers tower top mainly isolates many ethylbenzene component, tower reactor discharging mainly heavy constituent.
Rectifying tower with bulkhead is by establishing a vertical wall in the middle part of rectifying column, tower is divided into the one of the integrated tower of complete heat of epimere, hypomere, the rectifying feed zone separated by dividing plate and the tetrameric new structure of rectifying extraction section.With rectifying tower with bulkhead, three mixture are separated into pure product and only need a tower, reboiler, a condenser and a reflux splitter, energy consumption and equipment investment can be minimized.Since 1985, BASF AG, Kellogg company, KyowaYuka company, Sumitomo heavy industry Deng Ji major company bring into use rectifying tower with bulkhead.Existing more than 40 rectifying tower with bulkheads have carried out comercial operation in the world, and major part belongs to BASF AG of Germany.
The research adopting rectifying tower with bulkhead to be separated all kinds of system is also deepening continuously.Kellogg company develops the technique that extractive distillation combines with bulkhead type tower technology, from reformed oil or hydropyrolysis gasoline recovery benzene.Which eliminate stripper, rectifying, stripping and solvent recovery are all carried out in a rectifying tower with bulkhead, and the conventional extraction distillation unit of output investment ratio reduces 20%.In addition, rectifying tower with bulkhead separating-purifying 1,3-butadiene from C 4 fraction can also be adopted, C6 ~ C8 component that content of purifying from the cut of more than C5 is higher.In addition, external rectifying tower with bulkhead is also separated with the material synthesis processes such as hexene, pentamethylene, cyclopentene with butylene, propylene with butanediol, propylene for oxolane, butanone.In US6540907, the people such as Towler also proposed the naphtha rectifying tower with bulkhead direct desulfurization technique of FCC.Through consulting: in 1976 ~ calendar year 2001, published rectifying tower with bulkhead United States Patent (USP) only has 33 sections; And the rectifying tower with bulkhead United States Patent (USP) applied in 2001 ~ 2004 years half just existing 31 sections; Wherein in nearly 1 year, the United States Patent (USP) of application just accounts for 21 sections.The growth momentum of rectifying tower with bulkhead is more and more violent, and application surface is more and more wider.Bilateral line rectifying tower with bulkhead establishes two sections of vertical partition plates in rectifying column inside, rectifying column is divided into from top to bottom successively the above rectifying section of the first bulkhead section, the first bulkhead section, interlude, the second bulkhead section and the following stripping section of the second bulkhead section totally five parts.The principle be separated due to rectifying tower with bulkhead and hot coupling rectifying and computational methods are consistent, rectifying tower with bulkhead thermodynamics is equal to a Petlyuk tower at present, there is not yet report bilateral line rectifying tower with bulkhead being used for benzene, ethylbenzene, many ethylbenzene, the separation of heavy constituent mixing system.
Summary of the invention
Technical problem to be solved by this invention is the benzene, ethylbenzene, many ethylbenzene, the heavy constituent mixing system separation process complexity that exist in existing traditional Benzene Device, separation purity is not high, investment is large, the problem that energy consumption is high, provides a kind of new Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent to mix the method for system.It is simple that the method has flow process, good separating effect, and energy consumption is low, and investment reduces significant advantage.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method of Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system, comprises the following steps:
A) bilateral line rectifying tower with bulkhead is provided; Described bilateral line rectifying tower with bulkhead is followed successively by the above rectifying section of the first bulkhead section, the first bulkhead section, interlude, the second bulkhead section and the following stripping section of the second bulkhead section from top to bottom;
B) raw material containing benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system enters bilateral line rectifying tower with bulkhead from the first bulkhead section side, through being separated, ethylbenzene stream is obtained at the first bulkhead section opposite side, the second bulkhead section side line many ethylbenzene stream, obtain benzene logistics at the above rectifying section of the first bulkhead section, obtain heavy constituent logistics at the following stripping section of the second bulkhead section.
In technique scheme, preferably, by weight percentage, in feed stream, the content of benzene is 50 ~ 90%, and the content of ethylbenzene is 10 ~ 40%, and the content of many ethylbenzene is 1 ~ 10%, and the content of heavy component is 0.1 ~ 1%.
In technique scheme, preferably, described bilateral line rectifying tower with bulkhead has 90 ~ 130 pieces of theoretical plates; Wherein, the above rectifying section of the first bulkhead section has 15 ~ 35 pieces of theoretical plates, and the first bulkhead section has 20 ~ 50 pieces of theoretical plates, and interlude has 5 ~ 20 pieces of theoretical plates, and the second bulkhead section has 15 ~ 40 pieces of theoretical plates, and the following stripping section of the second bulkhead section has 5 ~ 15 pieces of theoretical plates.More preferably, described bilateral line rectifying tower with bulkhead has 95 ~ 125 pieces of theoretical plates; Wherein, the above rectifying section of the first bulkhead section has 20 ~ 30 pieces of theoretical plates, and the first bulkhead section has 25 ~ 45 pieces of theoretical plates, and interlude has 10 ~ 15 pieces of theoretical plates, and the second bulkhead section has 20 ~ 35 pieces of theoretical plates, and the following stripping section of the second bulkhead section has 7 ~ 13 pieces of theoretical plates.
In technique scheme, preferably, described bilateral line rectifying tower with bulkhead tower top operating pressure is 430 ~ 550kPa.More preferably, described bilateral line rectifying tower with bulkhead tower top operating pressure is 480 ~ 500kPa.
In technique scheme, preferably, described bilateral line rectifying tower with bulkhead tower top reflux ratio is by weight 0.8 ~ 1.1.More preferably, described bilateral line rectifying tower with bulkhead tower top reflux ratio is by weight 0.85 ~ 1.05.
In technique scheme, preferably, the side line exit position of ethylbenzene stream is top several 35th ~ 45 blocks of column plates downwards from bilateral line rectifying tower with bulkhead.
In technique scheme, preferably, the side line exit position of many ethylbenzene stream is top several 85th ~ 95 blocks of column plates downwards from bilateral line rectifying tower with bulkhead.
Pressure described in the inventive method refers to gauge pressure.
In the inventive method, described heavy component mainly comprises triethylbenzene (TEB), ethylbenzene tar.Wherein, by weight percentage, triethylbenzene (TEB) is 50 ~ 80% of heavy component, and ethylbenzene tar is heavy component 20 ~ 50%.
The bilateral line rectifying tower with bulkhead that the inventive method is used, is followed successively by the above rectifying section of the first bulkhead section, the first bulkhead section, interlude, the second bulkhead section and the following stripping section of the second bulkhead section from top to bottom.First bulkhead section and the second bulkhead section respectively arrange one piece of dividing plate, vertically respective bulkhead section are divided at least Liang Ge district, and this inside, Liang Ge district is all provided with column plate.Dividing plate can be installed along tower center line, also can eccentricly install.Material inlet is positioned at the first bulkhead section side, and the first bulkhead section opposite side establishes ethylbenzene component material outlet, and many ethylbenzene component material outlet established by the second bulkhead section side line; The above rectifying section of first bulkhead section is provided with the material outlet of benzene component, and the following stripping section of the second bulkhead section is provided with the material outlet of heavy component.
When the mixture that the material adopting the method for rectifying to be separated more than three kinds forms and the concentration of middle distillate is larger time, no matter adopt conventional order separation process or backward separation process, all inevitable middle distillate axially produces along tower and mixes, this is thermodynamically disadvantageous, is equivalent to the waste of a part of work of separation.Rectifying tower with bulkhead is thermodynamically equivalent to a rectifying column that completely heat is integrated, only uses a tower shell unlike rectifying tower with bulkhead, and arranging thermal baffle by centre, to realize the complete heat of distillation process integrated.Charging is in the side of separator segment, a middle distillate part in charging is entered the opposite side of dividing plate by the upper end of dividing plate with Light ends, another part is then entered the opposite side of dividing plate by the lower end of dividing plate with heavy constituent, thus make middle distillate obtain enrichment at the opposite side of dividing plate, avoid middle distillate mixing again in tower, thus realize effect that is energy-conservation and raising intermediate products purity.Meanwhile, realize the function of three conventional distillations because bilateral line rectifying tower with bulkhead only adopts a tower, fixed investment cost reduces significantly.
The component that mixture in the present invention has four kinds of need to be separated, a bilateral line rectifying tower with bulkhead is adopted to be separated this mixture, in rectifying tower with bulkhead overhead extraction benzene component, in the first bulkhead section side take-off ethylbenzene component, in second bulkhead section side take-off many ethylbenzene component, in tower reactor extraction heavy constituent.Adopt the inventive method, the benzene concentration of component in the extraction of rectifying tower with bulkhead top can reach 99.18% by weight, higher than the overhead components second concentration of component (99.16%) of former flow process benzene tower; The ethylbenzene concentration of component of rectifying tower with bulkhead first bulkhead section side take-off can reach 99.95% by weight, and the concentration (99.95%) of the overhead ethylbenzene component discharging of former flow process ethylbenzene tower maintains an equal level; Many ethylbenzene concentration of component of rectifying tower with bulkhead second bulkhead section side take-off can reach 92.33% by weight, higher than the concentration (92.21%) of tower top many ethylbenzene component discharging of the many ethylbenzene towers of former flow process; The heavy constituent concentration of rectifying tower with bulkhead tower reactor extraction can reach 99.59% by weight, higher than the concentration of component (99.21%) of the tower reactor discharging of the many ethylbenzene towers of former flow process.As can be seen here, bilateral line bulkhead distillation technology is adopted better can to complete the separation task of benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system.Particularly this bilateral line rectifying tower with bulkhead only just can replace original San Taita with a tower, significantly reduces the cost of equipment investment; Meanwhile, adopt bulkhead distillation technology compared with former distillation process, total heat exchange load can reduce by 8 ~ 15%.Therefore, technology of the present invention is adopted to have significant economic effect.
Accompanying drawing explanation
Fig. 1 is benzene, ethylbenzene, many ethylbenzene, the heavy constituent mixing system rectification process typical process example of existing Benzene Device.
Fig. 2 is the inventive method schematic flow sheet.
In Fig. 1,1 is the charging of mixing system containing benzene, ethylbenzene, many ethylbenzene, heavy constituent; 2 is the tower top discharging of benzene tower, mainly consists of benzene component; 3 is the tower reactor discharging of benzene tower, is mainly ethylbenzene, many ethylbenzene and heavy constituent; 4 is the tower top discharging of ethylbenzene tower, is mainly ethylbenzene component; 5 is the tower reactor discharging of ethylbenzene tower, is mainly many ethylbenzene and heavy constituent; 6 is the tower top discharging of many ethylbenzene, is mainly many ethylbenzene component; 7 is heavy constituent discharging; 8 is benzene tower; 9 is ethylbenzene tower; 10 is many ethylbenzene towers.
In Fig. 2,11 is the charging of mixing system containing benzene, ethylbenzene, many ethylbenzene, heavy constituent, identical with logistics 1 component in Fig. 1; 12 is the discharging of bilateral line rectifying tower with bulkhead overhead benzene component; 13 is the first bulkhead section side line ethylbenzene component discharging; 14 is second bulkhead section side line many ethylbenzene component discharging; 15 is the discharging of tower reactor heavy constituent, and 16 is bilateral line rectifying tower with bulkhead; A is the above rectifying section of the first bulkhead section; B is the first bulkhead section; C is interlude; D is the second bulkhead section; E is the following stripping section of the second bulkhead section.
Below in conjunction with accompanying drawing, the present invention is elaborated.
In Fig. 1, logistics 1 containing benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system enters benzene tower from the 17th piece of theoretical plate, the theoretical cam curve of benzene tower is 43 pieces, tower top pressure is 490 kPas, reflux ratio is 0.29 by weight, tower top isolates logistics 2 benzene component, and tower reactor obtains logistics 3(ethylbenzene, many ethylbenzene and heavy constituent).Ethylbenzene tower has 54 pieces of theoretical plates, and reflux ratio is 0.98 by weight, and tower top pressure is 147 kPas.The 42nd piece of theoretical plate that logistics 3 enters ethylbenzene tower is further separated, by overhead extraction logistics 4(ethylbenzene component), the many ethylbenzene of tower reactor extraction logistics 5(and heavy constituent).Logistics 5 enters many ethylbenzene towers and is separated many ethylbenzene further, and many ethylbenzene towers theoretical cam curve is 20 pieces, and tower top pressure is 27 kPas of gauge pressures, reflux ratio is 0.15 by weight, feed tray is the 11st piece of theoretical plate, many ethylbenzene stream 6 that top extraction is reclaimed, and attaches most importance to component streams 7 discharging in bottom.
In Fig. 2, form the 49th piece of theoretical plate that the material liquid 11 identical with logistics in Fig. 11 enters bilateral line rectifying tower with bulkhead, the theoretical cam curve of rectifying tower with bulkhead is 110 pieces, tower top pressure is 490 kPas of gauge pressures, reflux ratio is 0.9, and tower top isolates logistics 12 benzene component, and logistics 13 is first bulkhead section side line ethylbenzene component dischargings, logistics 14 is first bulkhead section side line many ethylbenzene component dischargings, and logistics 15 is the dischargings of tower reactor heavy constituent.Because in logistics 13 and logistics 14, potential temperature is very high, be respectively 220 DEG C and 270 DEG C, therefore reclaim heat wherein by heat exchanger generation low-pressure steam.
Bilateral line rectifying tower with bulkhead is totally 90 ~ 130 pieces of theoretical plates, preferably there are 95 ~ 125 pieces of theoretical plates, the above rectifying section of first bulkhead section has 15 ~ 35 pieces of theoretical plates, preferably there are 20 ~ 30 pieces of theoretical plates, first bulkhead section has 20 ~ 50 pieces of theoretical plates, preferably there are 25 ~ 45 pieces of theoretical plates, interlude has 5 ~ 20 pieces of theoretical plates, preferably there are 10 ~ 15 pieces of theoretical plates, second bulkhead section has 15 ~ 40 pieces of theoretical plates, preferably have 20 ~ 35 pieces of theoretical plates, the following stripping section of the second bulkhead section has 5 ~ 15 pieces of theoretical plates, preferably has 7 ~ 13 pieces of theoretical plates.Bilateral line rectifying tower with bulkhead operating pressure is set as tower top 430 ~ 550 kPas, and preferred operating pressure is 480 ~ 500 kPas.The backflow of rectifying tower with bulkhead is 0.8 ~ 1.1, and preferred operating reflux ratio is 0.85 ~ 1.05.Rectifying tower with bulkhead top extraction benzene component, its concentration of component can reach 99.18% by weight; First bulkhead section side take-off ethylbenzene component, its concentration can reach 99.95% by weight; Second bulkhead section side take-off many ethylbenzene component, its concentration can reach 92.33% by weight; Tower reactor extraction heavy constituent, wherein concentration of component can reach 99.59% by weight.
Below by embodiment, the invention will be further elaborated.Raw material composition used in all comparative examples and embodiment is as shown in table 1.
Table 1
| Sequence number | Component | Logistics 1(% by weight) |
| 1 | Non-aromatics light component | 0.21% |
| 2 | Benzene | 68.55% |
| 3 | Ethylbenzene | 26.86% |
| 4 | Many ethylbenzene | 4.05% |
| 5 | Heavy constituent | 0.33% |
| Add up to | 100% |
Detailed description of the invention
[comparative example]
Adopt the flow process shown in Fig. 1, with 320,000 tons/year of Benzene Devices for benchmark, the material as shown in table 1 to raw material weight percentage composition is separated, and the operating condition of each tower and separating resulting are all listed in table 2.In table, tower top thermic load is the refrigeration duty of overhead condenser, and tower reactor thermic load is the thermic load of tower reactor reboiler.
The former benzene tower of table 2, ethylbenzene tower and many ethylbenzene towers operating condition/separating resulting gather
| Equipment in Fig. 1 | Benzene tower | Ethylbenzene tower | Many ethylbenzene towers |
| Tower top operating pressure, kPa | 490 | 147 | 27 |
| Theoretical tray sum | 43 | 54 | 20 |
| Feed entrance point (plate number) | 17 | 42 | 11 |
| Reflux ratio, wt% | 0.29 | 0.98 | 0.15 |
| Overhead benzene concentration of component, wt% | 99.16% | ||
| Overhead ethylbenzene concentration of component, wt% | 99.95% | ||
| Tower top many ethylbenzene concentration of component, wt% | 92.21% | ||
| Tower reactor heavy constituent concentration, wt% | 99.21% |
Corresponding detailed Component seperation effect is in table 3.
The former benzene tower of table 3, ethylbenzene tower and many ethylbenzene towers separating resulting are shown (comparative example) in detail
The former benzene tower of table 4, ethylbenzene tower and many ethylbenzene towers flow process energy consumption analysis table (comparative example)
| Sequence number | Equipment | Thermic load, kilowatt |
| 1 | Benzene column overhead condenser | 13460 |
| 2 | Benzene tower tower reactor reboiler | 9370 |
| 3 | Ethylbenzene tower overhead condenser | 7820 |
| 4 | Ethylbenzene tower tower reactor reboiler | 6240 |
| 5 | Many ethylbenzene towers overhead condenser | 759 |
| 6 | Many ethylbenzene towers tower reactor reboiler | 302 |
| Amount to | 37951 |
[embodiment 1]
Adopt flow process shown in Fig. 2, with 320,000 tons/year of Benzene Devices for benchmark, the material as shown in table 1 to raw material weight percentage composition is separated.The bilateral line rectifying tower with bulkhead adopted has 110 pieces of theoretical plates, the above rectifying section of first bulkhead section has 25 pieces of theoretical plates, respectively there are 35 pieces of theoretical plates first bulkhead section dividing plate both sides, interlude has 15 pieces of theoretical plates, respectively there are 25 pieces of theoretical plates second bulkhead section dividing plate both sides, operating pressure is tower top 490 kPas of gauge pressures, and reflux ratio is 0.9 by weight; Charging 11 is from tower top several 49th piece of tower tray charging downwards, and the withdrawn position of side line ethylbenzene is from tower top several 39th piece of theoretical plate downwards, and the withdrawn position of the many ethylbenzene of side line is from tower top several 90th piece of theoretical plate downwards.There is 0.4MPaG low-pressure steam respectively in ethylbenzene discharging and the discharging of many ethylbenzene, reclaims after after heat and obtain logistics 13 and logistics 14.
For the ease of comparing, operating condition and separating resulting are listed in table 11.
The detailed Component seperation effect of bilateral line rectifying tower with bulkhead is in table 5.
Table 5 bilateral line rectifying tower with bulkhead separating resulting is shown (embodiment 1) in detail
The present embodiment energy consumption is in table 6.
Table 6 bilateral line rectifying tower with bulkhead flow process energy consumption analysis table (embodiment 1)
| Sequence number | Equipment | Thermic load, kilowatt | Remarks |
| 1 | Overhead condenser | 19763 | |
| 2 | Tower reactor reboiler | 15537 | |
| 3 | Ethylbenzene discharging heat recovery | -1866 | There is 0.4MPaG low-pressure steam |
| 4 | Many ethylbenzene discharging heat recovery | -596 | There is 0.4MPaG low-pressure steam |
| Amount to | 32838 |
[embodiment 2]
Adopt flow process shown in Fig. 2, other conditions same [embodiment 1], total number of theoretical plate of change bilateral line rectifying tower with bulkhead, the number of theoretical plate of dividing plate both sides, feed entrance point, lateral line withdrawal function position and reflux ratio.
The bilateral line rectifying tower with bulkhead adopted has 100 pieces of theoretical plates, respectively there are 30 pieces of theoretical plates first bulkhead section dividing plate both sides, and interlude has 10 pieces of theoretical plates, and respectively there are 25 pieces of theoretical plates the second bulkhead section dividing plate both sides, the following stripping section of second bulkhead section has 10 pieces of theoretical plates, and reflux ratio is 1 by weight; Charging 11 is the 44th piece of tower tray charging, and the withdrawn position of side line ethylbenzene is from tower top several 38th piece of theoretical plate downwards, and the withdrawn position of the many ethylbenzene of side line is from tower top several 80th piece of theoretical plate downwards.There is 0.4MPaG low-pressure steam respectively in ethylbenzene discharging and the discharging of many ethylbenzene, reclaims after after heat and obtain logistics 13 and logistics 14.
For the ease of comparing, operating condition and separating resulting are listed in table 11.
The detailed Component seperation effect of bilateral line rectifying tower with bulkhead is in table 7.
Table 7 bilateral line rectifying tower with bulkhead separating resulting is shown (embodiment 2) in detail
In the present embodiment, energy consumption is in table 8.
Table 8 bilateral line rectifying tower with bulkhead flow process energy consumption analysis table (embodiment 2)
| Sequence number | Equipment | Thermic load, kilowatt | Remarks |
| 1 | Overhead condenser | 20803 | |
| 2 | Tower reactor reboiler | 16577 | |
| 3 | Ethylbenzene discharging heat recovery | -1867 | There is 0.4MPaG low-pressure steam |
| 4 | Many ethylbenzene discharging heat recovery | -596 | There is 0.4MPaG low-pressure steam |
| Amount to | 34917 |
[embodiment 3]
Adopt flow process shown in Fig. 2, other conditions same [embodiment 1], total number of theoretical plate of change bilateral line rectifying tower with bulkhead, the number of theoretical plate of dividing plate both sides, feed entrance point, lateral line withdrawal function position and reflux ratio.
The bilateral line rectifying tower with bulkhead adopted has 120 pieces of theoretical plates, respectively there are 40 pieces of theoretical plates first bulkhead section dividing plate both sides, and interlude has 15 pieces of theoretical plates, and respectively there are 30 pieces of theoretical plates the second bulkhead section dividing plate both sides, the following stripping section of second bulkhead section has 10 pieces of theoretical plates, and reflux ratio is 0.95 by weight; Charging 11 is the 53rd piece of tower tray charging, and the withdrawn position of side line ethylbenzene is from tower top several 39th piece of theoretical plate downwards, and the withdrawn position of the many ethylbenzene of side line is from tower top several 95th piece of theoretical plate downwards.There is 0.4MPaG low-pressure steam respectively in ethylbenzene discharging and the discharging of many ethylbenzene, reclaims after after heat and obtain logistics 13 and logistics 14.For the ease of comparing, operating condition and separating resulting are also listed in table 11.
The final separating effect of the present embodiment flow process is in table 9.
Table 9 bilateral line rectifying tower with bulkhead separating resulting is shown to gather (embodiment 3) in detail
The energy consumption of the present embodiment flow process is in table 10.
Table 10 bilateral line rectifying tower with bulkhead flow process energy consumption analysis table (embodiment 3)
| Sequence number | Equipment | Thermic load, kilowatt | Remarks |
| 1 | Overhead condenser | 20282 | |
| 2 | Tower reactor reboiler | 16055 | |
| 3 | Ethylbenzene discharging heat recovery | -1865 | There is 0.4MPaG low-pressure steam |
| 4 | Many ethylbenzene discharging heat recovery | -596 | There is 0.4MPaG low-pressure steam |
| Amount to | 33876 |
The operating condition of [embodiment 1 ~ 3] and separating resulting are summarised in table 11 is convenient to comparative analysis.
Table 11
| Embodiment | 1 | 2 | 3 |
| Total number of theoretical plate | 110 | 100 | 120 |
| First bulkhead section number of theoretical plate | 35 | 30 | 40 |
| Second bulkhead section number of theoretical plate | 25 | 25 | 30 |
| The above theoretical number of plates of rectifying section of first bulkhead section | 25 | 25 | 25 |
| Interlude number of theoretical plate | 15 | 10 | 15 |
| Operating pressure, kPa | 490 | 490 | 490 |
| Feed entrance point | 49 | 44 | 53 |
| Ethylbenzene component extraction position | 39 | 38 | 39 |
| Many ethylbenzene component extraction position | 90 | 80 | 95 |
| Reflux ratio, wt% | 0.9 | 1 | 0.95 |
| Overhead benzene concentration of component, wt% | 99.18% | 99.19% | 99.19% |
| Side line ethylbenzene concentration of component, wt% | 99.95% | 99.96% | 99.97% |
| Embodiment | 1 | 2 | 3 |
| Side line many ethylbenzene concentration of component, wt% | 92.33% | 92.35% | 92.36% |
| Tower reactor heavy constituent concentration, wt% | 99.59% | 99.62% | 99.61% |
| Tower top thermic load, kilowatt | 19763 | 20803 | 20282 |
| Tower reactor thermic load, kilowatt | 15537 | 16577 | 16055 |
| Reclaim thermic load, kilowatt | -2462 | -2463 | -2461 |
| Total heat duties, kilowatt | 32838 | 34917 | 33876 |
| Total fractional energy savings | 13% | 8% | 11% |
[embodiment 1] is preferred operating mode.Adopt a bilateral line rectifying tower with bulkhead to replace benzene tower, ethylbenzene tower, many ethylbenzene towers in former flow process, reduce investment outlay; When operation conditions optimization, total fractional energy savings reaches 13%; Simultaneously, under the arbitrary operating condition shown in embodiment, the purity of overhead benzene component is all higher than 99.16%, the purity of tower side line ethylbenzene component is all not less than 99.95%, the purity of tower side line many ethylbenzene component is all higher than 92.21%, the purity of tower reactor heavy constituent is all higher than 99.21%, and separating effect is all better than former technological process.
Claims (6)
1. a method for Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system, comprises the following steps:
A) bilateral line rectifying tower with bulkhead is provided; Described bilateral line rectifying tower with bulkhead is followed successively by the above rectifying section of the first bulkhead section, the first bulkhead section, interlude, the second bulkhead section and the following stripping section of the second bulkhead section from top to bottom;
B) raw material containing benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system enters bilateral line rectifying tower with bulkhead from the first bulkhead section side, through being separated, ethylbenzene stream is obtained at the first bulkhead section opposite side, the second bulkhead section side line many ethylbenzene stream, obtain benzene logistics at the above rectifying section of the first bulkhead section, obtain heavy constituent logistics at the following stripping section of the second bulkhead section;
By weight percentage, in feed stream, the content of benzene is 50 ~ 90%, and the content of ethylbenzene is 10 ~ 40%, and the content of many ethylbenzene is 1 ~ 10%, and the content of heavy component is 0.1 ~ 1%;
Described bilateral line rectifying tower with bulkhead has 90 ~ 130 pieces of theoretical plates; Wherein, the above rectifying section of the first bulkhead section has 15 ~ 35 pieces of theoretical plates, and the first bulkhead section has 20 ~ 50 pieces of theoretical plates, and interlude has 5 ~ 20 pieces of theoretical plates, and the second bulkhead section has 15 ~ 40 pieces of theoretical plates, and the following stripping section of the second bulkhead section has 5 ~ 15 pieces of theoretical plates;
Described bilateral line rectifying tower with bulkhead tower top operating pressure is 430 ~ 550kPa;
Described bilateral line rectifying tower with bulkhead tower top reflux ratio is by weight 0.8 ~ 1.1.
2. according to claim 1 Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system method, it is characterized in that described bilateral line rectifying tower with bulkhead has 95 ~ 125 pieces of theoretical plates; Wherein, the above rectifying section of the first bulkhead section has 20 ~ 30 pieces of theoretical plates, and the first bulkhead section has 25 ~ 45 pieces of theoretical plates, and interlude has 10 ~ 15 pieces of theoretical plates, and the second bulkhead section has 20 ~ 35 pieces of theoretical plates, and the following stripping section of the second bulkhead section has 7 ~ 13 pieces of theoretical plates.
3. according to claim 1 Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system method, it is characterized in that described bilateral line rectifying tower with bulkhead tower top operating pressure is 480 ~ 500kPa.
4. according to claim 1 Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system method, it is characterized in that described bilateral line rectifying tower with bulkhead tower top reflux ratio is by weight 0.85 ~ 1.05.
5. according to claim 1 Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system method, it is characterized in that the side line exit position of ethylbenzene stream is top several 35th ~ 45 blocks of column plates downwards from bilateral line rectifying tower with bulkhead.
6. according to claim 1 Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system method, it is characterized in that the side line exit position of many ethylbenzene stream is top several 85th ~ 95 blocks of column plates downwards from bilateral line rectifying tower with bulkhead.
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| CN106631668A (en) * | 2015-10-28 | 2017-05-10 | 中国石油化工股份有限公司 | Ethylbenzene separation method, ethylbenzene production method, apparatus used for ethylbenzene production and method for ethylbenzene production by using apparatus |
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