CN104027995A - Method for separating benzene, ethylbenzene, poly-ethylbenzene and heavy component mixture series - Google Patents
Method for separating benzene, ethylbenzene, poly-ethylbenzene and heavy component mixture series Download PDFInfo
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- CN104027995A CN104027995A CN201310210802.0A CN201310210802A CN104027995A CN 104027995 A CN104027995 A CN 104027995A CN 201310210802 A CN201310210802 A CN 201310210802A CN 104027995 A CN104027995 A CN 104027995A
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- ethylbenzene
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- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 title claims abstract description 315
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 203
- 238000000034 method Methods 0.000 title claims abstract description 52
- 239000000203 mixture Substances 0.000 title abstract description 13
- 239000002994 raw material Substances 0.000 claims abstract description 6
- 230000002146 bilateral effect Effects 0.000 claims description 48
- 239000000470 constituent Substances 0.000 claims description 45
- 238000000926 separation method Methods 0.000 claims description 23
- 238000010992 reflux Methods 0.000 claims description 17
- 238000002156 mixing Methods 0.000 claims description 9
- 239000000463 material Substances 0.000 abstract description 16
- 238000005265 energy consumption Methods 0.000 abstract description 11
- 238000009776 industrial production Methods 0.000 abstract 1
- 238000007599 discharging Methods 0.000 description 32
- 238000000605 extraction Methods 0.000 description 18
- 238000007600 charging Methods 0.000 description 10
- 230000000694 effects Effects 0.000 description 8
- 238000011084 recovery Methods 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 6
- 238000004821 distillation Methods 0.000 description 5
- VIDOPANCAUPXNH-UHFFFAOYSA-N 1,2,3-triethylbenzene Chemical compound CCC1=CC=CC(CC)=C1CC VIDOPANCAUPXNH-UHFFFAOYSA-N 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 2
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- LPIQUOYDBNQMRZ-UHFFFAOYSA-N cyclopentene Chemical compound C1CC=CC1 LPIQUOYDBNQMRZ-UHFFFAOYSA-N 0.000 description 2
- 238000000895 extractive distillation Methods 0.000 description 2
- RGSFGYAAUTVSQA-UHFFFAOYSA-N pentamethylene Natural products C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 description 2
- LIKMAJRDDDTEIG-UHFFFAOYSA-N 1-hexene Chemical compound CCCCC=C LIKMAJRDDDTEIG-UHFFFAOYSA-N 0.000 description 1
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 1
- 241000736911 Turritella communis Species 0.000 description 1
- CDQSJQSWAWPGKG-UHFFFAOYSA-N butane-1,1-diol Chemical compound CCCC(O)O CDQSJQSWAWPGKG-UHFFFAOYSA-N 0.000 description 1
- -1 butylene, propylene Chemical group 0.000 description 1
- 238000010835 comparative analysis Methods 0.000 description 1
- 238000000205 computational method Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 125000004817 pentamethylene group Chemical group [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a method for separating benzene, ethylbenzene, poly-ethylbenzene and a heavy component mixture series, which solves the problems of complex separating flow of benzene, ethylbenzene, poly-ethylbenzene and the heavy component mixture series, low separating purity, large investment, and high energy consumption. According to the invention, the raw materials containing benzene, ethylbenzene, poly-ethylbenzene and the heavy component mixture series are introduced in a double siding bulkhead rectification column from a first bulkhead part and then separated, ethylbenzene material flow is obtained at the other side of the first bulkhead part, poly-ethylbenzene material flow is obtained at the siding of a second bulkhead part, the benzene material flow is obtained at a rectifying section over the first bulkhead part, and the heavy component mixture series can be obtained at a stripping section below the second bulkhead part; the technical scheme better solves the problems. The separating method provided in the invention can be used for industrial production of benzene, ethylbenzene, poly-ethylbenzene and heavy component mixture series.
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 that contains 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 is mainly made up of ethylbenzene, many ethylbenzene and heavy constituent.Benzene tower tower reactor material out enters ethylbenzene tower and is further separated, and it is more than 99.95% ethylbenzene component by weight that ethylbenzene tower tower top is isolated, and tower reactor discharging is many ethylbenzene and heavy constituent.Ethylbenzene tower tower reactor material goes many ethylbenzene towers to carry out next step separation again.Many ethylbenzene towers tower top is mainly isolated many ethylbenzene component, and tower reactor discharging is mainly heavy constituent.
Rectifying tower with bulkhead is by establishing a vertical wall at rectifying column middle part, tower being divided into the one of the integrated tower of complete heat of epimere, hypomere, the rectifying feed zone being separated by dividing plate and the tetrameric new structure of rectifying extraction section.With rectifying tower with bulkhead, three mixture being separated into pure product only needs a tower, a reboiler, a condenser and a reflux splitter, and energy consumption and equipment investment can be minimized.Since 1985, BASF AG, Kellogg company, Kyowa Yuka company, Sumitomo heavy industry Deng Ji major company have brought into use rectifying tower with bulkhead.Existing more than 40 rectifying tower with bulkhead has carried out business operation in the world, and major part belongs to German BASF AG.
The research that adopts rectifying tower with bulkhead to separate all kinds of systems is also deepening continuously.Kellogg company has developed the technique that extractive distillation combines with bulkhead type tower technology, from reformed oil or hydropyrolysis gasoline recovery benzene.It has cancelled stripper, and rectifying, stripping and solvent recovery are all carried out in a rectifying tower with bulkhead, and the conventional extractive distillation device of output investment ratio reduces 20%.In addition, also can adopt rectifying tower with bulkhead separating-purifying 1,3-butadiene from C 4 fraction, C6～C8 component that the content of purifying the cut more than C5 is higher.In addition, external rectifying tower with bulkhead also separates with the material building-up processes such as hexene, pentamethylene, cyclopentene with butylene, propylene with butanediol, propylene for oxolane, butanone.In US6540907, the people such as Towler have 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) of having applied in 2001～2004 years half just has 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 is to establish two sections of vertical partition plates in rectifying column inside, and rectifying column is divided into 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 from top to bottom successively.Because rectifying tower with bulkhead is consistent with principle and the computational methods of hot coupling rectifying separation, rectifying tower with bulkhead is that on thermodynamics, to be equal to a Petlyuk tower current, there is not yet bilateral line rectifying tower with bulkhead is mixed to the report that system separates for benzene, ethylbenzene, many ethylbenzene, heavy constituent.
Summary of the invention
Technical problem to be solved by this invention is that the benzene, ethylbenzene, many ethylbenzene, the heavy constituent that in existing traditional Benzene Device, exist are mixed system separation process complexity, separation purity is not high, investment is large, the problem that energy consumption is high, a kind of method that provides new Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent to mix 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 that Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent are mixed system, comprises the following steps:
A) provide bilateral line rectifying tower with bulkhead; 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) enter bilateral line rectifying tower with bulkhead containing the raw material of benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system from the first bulkhead section one side, through separating, obtain ethylbenzene stream 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, below the second bulkhead section, stripping section obtains heavy constituent logistics.
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 theoretical plates; Wherein, the above rectifying section of the first bulkhead section has 15～35 theoretical plates, and the first bulkhead section has 20～50 theoretical plates, and interlude has 5～20 theoretical plates, and the second bulkhead section has 15～40 theoretical plates, and the following stripping section of the second bulkhead section has 5～15 theoretical plates.More preferably, described bilateral line rectifying tower with bulkhead has 95～125 theoretical plates; Wherein, the above rectifying section of the first bulkhead section has 20～30 theoretical plates, and the first bulkhead section has 25～45 theoretical plates, and interlude has 10～15 theoretical plates, and the second bulkhead section has 20～35 theoretical plates, and the following stripping section of the second bulkhead section has 7～13 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 heavy component 50～80%, 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.The first bulkhead section and the second bulkhead section respectively arrange a dividing plate, vertically bulkhead section are separately divided into at least Liang Ge district, and inside, Zhe Liangge 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 one side, and the first bulkhead section opposite side is established ethylbenzene component material outlet, and the second bulkhead section side line is established many ethylbenzene component material outlet; The above rectifying section of the 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 adopting the method for rectifying to separate the concentration of mixture that more than three kinds materials forms and middle distillate when larger, no matter adopt conventional order separation process or backward separation process, all inevitable middle distillate is mixed along the axial generation of tower again, this is disadvantageous on thermodynamics, is equivalent to the waste of a part of work of separation.Rectifying tower with bulkhead is equivalent to a completely integrated rectifying column of heat on thermodynamics, and different is that rectifying tower with bulkhead is only used a tower shell, and by centre, thermal baffle being set, to realize the complete heat of distillation process integrated.Charging is in a 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 component, another part is entered the opposite side of dividing plate by the lower end of dividing plate with heavy constituent, thereby make middle distillate obtain enrichment at the opposite side of dividing plate, avoid middle distillate mixing again in tower, thereby realized effect 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 is remarkable.
The component that mixture in the present invention has four kinds of need to separate, adopt a bilateral line rectifying tower with bulkhead to separate this mixture, in rectifying tower with bulkhead overhead extraction benzene component, in the first bulkhead section side line extraction ethylbenzene component, in second many ethylbenzene of bulkhead section side line extraction 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 tower top component second concentration of component (99.16%) of former flow process benzene tower; The ethylbenzene concentration of component of rectifying tower with bulkhead the first bulkhead section side line extraction can reach 99.95% by weight, and the concentration (99.95%) of the tower top ethylbenzene component discharging of former flow process ethylbenzene tower maintains an equal level; Many ethylbenzene concentration of component of rectifying tower with bulkhead the second bulkhead section side line extraction can reach 92.33% by weight, higher than the concentration (92.21%) of many ethylbenzene of tower top 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, adopt bilateral line bulkhead distillation technology can better 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, adopt technology of the present invention to there is significant economic effect.
Brief description of the drawings
Fig. 1 is that benzene, ethylbenzene, many ethylbenzene, the heavy constituent of existing Benzene Device mixed system rectification process typical process example.
Fig. 2 is the inventive method schematic flow sheet.
In Fig. 1,1 charging that is the mixing system that contains benzene, ethylbenzene, many ethylbenzene, heavy constituent; 2 is the tower top discharging of benzene tower, and chief component is 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 chargings that are the mixing system that contains 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 many ethylbenzene of bulkhead section side line 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, the logistics 1 that contains benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system enters benzene tower from the 17th theoretical plate, the theoretical cam curve of benzene tower is 43, tower top pressure is 490 kPas, reflux ratio is 0.29 by weight, tower top is isolated logistics 2 benzene components, and tower reactor obtains logistics 3(ethylbenzene, many ethylbenzene and heavy constituent).Ethylbenzene tower has 54 theoretical plates, and reflux ratio is 0.98 by weight, and tower top pressure is 147 kPas.The 42nd 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 further separates many ethylbenzene, and many ethylbenzene towers theoretical cam curve is 20, and tower top pressure is 27 kPas of gauge pressures, reflux ratio is 0.15 by weight, feed tray is the 11st theoretical plate, many ethylbenzene stream 6 that top extraction is reclaimed, and bottom is heavy constituent logistics 7 dischargings.
In Fig. 2, form the 49th 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, tower top pressure is 490 kPas of gauge pressures, reflux ratio is 0.9, and tower top is isolated logistics 12 benzene components, and logistics 13 is first bulkhead section side line ethylbenzene component dischargings, logistics 14 is first many ethylbenzene of bulkhead section side line component dischargings, and logistics 15 is the dischargings of tower reactor heavy constituent.Because potential temperature in logistics 13 and logistics 14 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 theoretical plates, preferably there are 95～125 theoretical plates, the above rectifying section of the first bulkhead section has 15～35 theoretical plates, preferably there are 20～30 theoretical plates, the first bulkhead section has 20～50 theoretical plates, preferably there are 25～45 theoretical plates, interlude has 5～20 theoretical plates, preferably there are 10～15 theoretical plates, the second bulkhead section has 15～40 theoretical plates, preferably have 20～35 theoretical plates, the following stripping section of the second bulkhead section has 5～15 theoretical plates, preferably has 7～13 theoretical plates.Bilateral line rectifying tower with bulkhead operating pressure is set as 430～550 kPas of tower tops, 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; The first bulkhead section side line extraction ethylbenzene component, its concentration can reach 99.95% by weight; Second many ethylbenzene of bulkhead section side line extraction 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, taking 320,000 tons/year of Benzene Devices as benchmark, the material as shown in table 1 to raw material weight percentage composition separates, 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% | ? | ? |
| Tower top ethylbenzene concentration of component, wt% | ? | 99.95% | ? |
| Many ethylbenzene of tower top concentration of component, wt% | ? | ? | 92.21% |
| Tower reactor heavy constituent concentration, wt% | ? | ? | 99.21% |
Corresponding detailed component separating 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, taking 320,000 tons/year of Benzene Devices as benchmark, the material as shown in table 1 to raw material weight percentage composition separates.The bilateral line rectifying tower with bulkhead adopting has 110 theoretical plates, the above rectifying section of the first bulkhead section has 25 theoretical plates, respectively there are 35 theoretical plates the first bulkhead section dividing plate both sides, interlude has 15 theoretical plates, respectively there are 25 theoretical plates the second bulkhead section dividing plate both sides, operating pressure is 490 kPas of gauge pressures of tower top, and reflux ratio is 0.9 by weight; Charging 11 is from tower top several the 49th tower tray chargings downwards, and the withdrawn position of side line ethylbenzene be from tower top several the 39th theoretical plates downwards, and the withdrawn position of the many ethylbenzene of side line is from downward several the 90th theoretical plates of tower top.There is respectively 0.4MPaG low-pressure steam in ethylbenzene discharging and the discharging of many ethylbenzene, obtains logistics 13 and logistics 14 after reclaiming after heat.
For the ease of comparing, operating condition and separating resulting are listed in table 11.
The detailed component separating 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, with [embodiment 1], change total number of theoretical plate of bilateral line rectifying tower with bulkhead, number of theoretical plate, feed entrance point, lateral line withdrawal function position and the reflux ratio of dividing plate both sides.
The bilateral line rectifying tower with bulkhead adopting has 100 theoretical plates, respectively there are 30 theoretical plates the first bulkhead section dividing plate both sides, and interlude has 10 theoretical plates, and respectively there are 25 theoretical plates the second bulkhead section dividing plate both sides, the following stripping section of the second bulkhead section has 10 theoretical plates, and reflux ratio is 1 by weight; Charging 11 is the 44th tower tray charging, and the withdrawn position of side line ethylbenzene is from tower top several the 38th theoretical plates downwards, and the withdrawn position of the many ethylbenzene of side line is from tower top several the 80th theoretical plates downwards.There is respectively 0.4MPaG low-pressure steam in ethylbenzene discharging and the discharging of many ethylbenzene, obtains logistics 13 and logistics 14 after reclaiming after heat.
For the ease of comparing, operating condition and separating resulting are listed in table 11.
The detailed component separating 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, with [embodiment 1], change total number of theoretical plate of bilateral line rectifying tower with bulkhead, number of theoretical plate, feed entrance point, lateral line withdrawal function position and the reflux ratio of dividing plate both sides.
The bilateral line rectifying tower with bulkhead adopting has 120 theoretical plates, respectively there are 40 theoretical plates the first bulkhead section dividing plate both sides, and interlude has 15 theoretical plates, and respectively there are 30 theoretical plates the second bulkhead section dividing plate both sides, the following stripping section of the second bulkhead section has 10 theoretical plates, and reflux ratio is 0.95 by weight; Charging 11 is the 53rd tower tray charging, and the withdrawn position of side line ethylbenzene is from tower top several the 39th theoretical plates downwards, and the withdrawn position of the many ethylbenzene of side line is from tower top several the 95th theoretical plates downwards.There is respectively 0.4MPaG low-pressure steam in ethylbenzene discharging and the discharging of many ethylbenzene, obtains logistics 13 and logistics 14 after reclaiming after heat.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 in detail table gathers (embodiment 3)
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 is convenient to comparative analysis in table 11.
Table 11
| Embodiment | 1 | 2 | 3 |
| Total number of theoretical plate | 110 | 100 | 120 |
| The first bulkhead section number of theoretical plate | 35 | 30 | 40 |
| The second bulkhead section number of theoretical plate | 25 | 25 | 30 |
| The above theoretical number of plates of rectifying section of the 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 |
| Many ethylbenzene of side line 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, the many ethylbenzene towers in former flow process, reduce investment outlay; The in the situation that of 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 many ethylbenzene of tower side line 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 (10)
1. the method that Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent are mixed system, comprises the following steps:
A) provide bilateral line rectifying tower with bulkhead; 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) enter bilateral line rectifying tower with bulkhead containing the raw material of benzene, ethylbenzene, many ethylbenzene, heavy constituent mixing system from the first bulkhead section one side, through separating, obtain ethylbenzene stream 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, below the second bulkhead section, stripping section obtains heavy constituent logistics.
2. the method that Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent are mixed system according to claim 1, it is characterized in that by weight percentage, in feed stream, the content of benzene is 50～90%, and the content of ethylbenzene is 10～40%, the content of many ethylbenzene is 1～10%, and the content of heavy component is 0.1～1%.
3. the method that Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent are mixed system according to claim 1, is characterized in that described bilateral line rectifying tower with bulkhead has 90～130 theoretical plates; Wherein, the above rectifying section of the first bulkhead section has 15～35 theoretical plates, and the first bulkhead section has 20～50 theoretical plates, and interlude has 5～20 theoretical plates, and the second bulkhead section has 15～40 theoretical plates, and the following stripping section of the second bulkhead section has 5～15 theoretical plates.
4. the method that Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent are mixed system according to claim 3, is characterized in that described bilateral line rectifying tower with bulkhead has 95～125 theoretical plates; Wherein, the above rectifying section of the first bulkhead section has 20～30 theoretical plates, and the first bulkhead section has 25～45 theoretical plates, and interlude has 10～15 theoretical plates, and the second bulkhead section has 20～35 theoretical plates, and the following stripping section of the second bulkhead section has 7～13 theoretical plates.
5. the method that Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent are mixed system according to claim 1, is characterized in that described bilateral line rectifying tower with bulkhead tower top operating pressure is 430～550kPa.
6. the method that Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent are mixed system according to claim 5, is characterized in that described bilateral line rectifying tower with bulkhead tower top operating pressure is 480～500kPa.
7. the method that Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent are mixed system according to claim 1, is characterized in that described bilateral line rectifying tower with bulkhead tower top reflux ratio is by weight 0.8～1.1.
8. the method that Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent are mixed system according to claim 7, is characterized in that described bilateral line rectifying tower with bulkhead tower top reflux ratio is by weight 0.85～1.05.
9. the method that Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent are mixed system according to claim 1, the side line exit position that it is characterized in that ethylbenzene stream is top several 35th～45 blocks of column plates downwards from bilateral line rectifying tower with bulkhead.
10. the method that Separation of Benzene, ethylbenzene, many ethylbenzene, heavy constituent are mixed system according to claim 1, the side line exit position that it is characterized in that many ethylbenzene stream is top several 85th～95 blocks of column plates downwards from bilateral line rectifying tower with bulkhead.
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| CN113979828A (en) * | 2021-11-18 | 2022-01-28 | 万华化学集团股份有限公司 | Method for recovering byproduct ethylbenzene in production of epoxypropane by using co-oxidation method |
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