CN101890249A - Energy-saving process method for rectifying and separating three fractions - Google Patents
Energy-saving process method for rectifying and separating three fractions Download PDFInfo
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Abstract
The invention relates to an energy-saving process method for rectifying and separating three fractions, and a high-purity middle fraction B is prepared from a mixed material of a light fraction A, a middle fraction B and a heavy fraction C. The process method at least comprises a pre-distillation tower (T101) and a rectification tower (T102). The process method comprises the following steps of: making the mixed material enter the pre-distillation tower (T101); distilling out a part of the light fraction A on the top of the T101; making a distillate only comprising the heavy fraction C at the bottom of the T101 and the middle fraction B enter the middle-lower part of the T102; extracting a liquid phase stream comprising the A and the B on a side of the T101 and making the liquid phase stream enter the middle-upper part of the T102; distilling out the rest A on the top of the T102; distilling out the heavy fraction C at the bottom of the T102; and obtaining the high-purity middle fraction B from the side of the T102. In order to further reduce the operation energy consumption, heat integration operation is adopted between the T101 and the T102, namely, the tower top operation pressure of the T101 is properly increased and the tower top gaseous phase of the T101 is used as a heat source of a reboiler at the bottom of the T102. The energy-saving process method for rectifying and separating the three fractions overcomes the disadvantages of the prior art and has obvious practicability and extremely obvious energy-saving effect.
Description
Technical field
The present invention relates to the rectification process in the chemical separation engineering, the energy-saving process method that particularly a kind of three cut rectifying separate, but widespread usage is at the distillation process of various products.
Background technology
Rectifying is the product purification method that generally adopts in the chemical separation engineering.For the mixed material that contains light fraction A, midbarrel B and heavy distillat C, if expect highly purified midbarrel B, adopt common process, as shown in Figure 1, need a lightness-removing column (T1) and a rectifying column (T2).By lightness-removing column (T1) removed overhead light component, remove heavy ends by rectifying column (T2) tower still then, obtain high-purity midbarrel B by rectifying column (T2) cat head.Separating energy consumption is very high.
Fig. 2 is a kind of improved energy saving technique flow chart, utilize the differential pressure operation, lightness-removing column (T1) cat head operating pressure is higher than rectifying column (T2) cat head operating pressure, makes the T1 tower top temperature be higher than T2 tower still temperature, utilizes lightness-removing column (T1) cat head gas phase as T2 tower still heating thermal source.In the whole double tower separation process, only T1 needs external heat source that energy is provided, and T2 provides energy without external heat source, has reduced operation energy consumption.
Fig. 3 is another kind of improved energy saving technique flow chart, similar to Fig. 2, different is, rectifying column (T2) cat head operating pressure is higher than lightness-removing column (T1) cat head operating pressure, in the whole double tower separation process, only T2 needs external heat source that energy is provided, and T1 provides energy without external heat source, T1 tower still provides energy by T2 cat head gas phase, has reduced operation energy consumption.
Under the operating modes such as, temperature-sensitive system big for A, B, C three cut boiling-point differences, high vacuum operation, the application of Fig. 2, energy-saving process shown in Figure 3 is restricted.With flow process shown in Figure 2 is example, if A, B, C three cut boiling-point differences are bigger, if want to realize that T1 cat head gas phase heats to T2, the essential T1 cat head operating pressure that improves, can cause T1 tower still temperature too high like this, also can cause T1 tower still reboiler heating difficulty, perhaps T1 tower still material coking, polymerization losses strengthen.For operating modes such as temperature-sensitive system, high vacuum operations, in Fig. 2, the energy-saving process shown in Figure 3, the unfavorable situation that pressure raises than cat head/tower still operating temperature of high tower can appear equally.And, Fig. 2, energy-saving process shown in Figure 3 also be subjected between T1, the T2 can be flux matched restriction, if T1, the required separating energy consumption of T2 two towers differ more for a long time, still use Fig. 2, method shown in Figure 3, must cause the specification of equipment of a tower wherein bigger than normal, cause the waste of equipment investment.
Fig. 4, Fig. 5 are the Petlyuk tower of two kinds of equivalent constructions, belong to the thermal coupling tower.As shown in Figure 4, the mixed material that contains A, B, C three cuts is introduced into secondary tower (T3), all light fraction A and all heavy distillat C respectively from secondary tower (frozen-free device and reboiler) (T3) cat head and tower stilling go out, midbarrel B has at T3 cat head, tower still.T3 cat head, tower still material are imported king-tower (condenser and reboiler are arranged) correct position (T4) respectively, in the T4 top portion from A and B, in the T4 lower part from B and C.The T4 cat head distillates light fraction A, and T4 tower stilling goes out heavy distillat C, and midbarrel B is by the side line extraction of T4 middle part.Because the overhead reflux liquid of T3 is provided by the top liquid phase side line of T4, the heating of T3 tower still is provided by T4 bottom gas phase side line, has only T4 that condenser and reboiler are arranged, and has therefore reduced operation energy consumption and equipment investment.
The greatest drawback of Fig. 4, Petlyuk tower shown in Figure 5 is that the position that T3 cat head, T3 tower still material are introduced the T4 tower is difficult to determine, and the amount of drawing of T4 top of tower liquid phase side line, T4 bottom gas phase side line is difficult to determine.And in the practical operation, the side line extraction of T4 tower bottom goes the gas phase flow of T3 tower bottom to be difficult to control, T4 bottom side line is extracted the tolerance size out directly influences T4 middle part rising gas phase flow (T4 bottom side line is extracted tolerance+T4 middle part rising gas phase flow=T4 bottom rising tolerance out), also directly can have influence on middle part side line---the purity of midbarrel B.Therefore though this Petlyuk thermal coupling tower proposed for three more than ten years, practical application seldom always, the actual problem of controlling is difficult to solve.
Summary of the invention
The present invention relates to the energy-saving process method that a kind of three cut rectifying separate, can overcome the defective of prior art, from the mixed material that contains light fraction A, midbarrel B and heavy distillat C, obtain the energy-saving process method of highly purified midbarrel B, have significant practicality and obvious energy-saving effect extremely, have a extensive future.
The step that the energy-saving process method that the three cut rectifying that remove the weight component provided by the invention separate comprises:
(1) comprises pre-distillation column (T101), rectifying column (T102) Liang Taita at least;
(2) mixed material enters pre-distillation column (T101), and the T101 top distillates part light fraction A, and T101 tower reactor distillate only contains heavy distillat C and midbarrel B goes to T102 tower middle and lower part.The T101 side line is extracted the liquid phase stream that contains A, B out and is gone to T102 tower middle and upper part;
(3) the T102 cat head distillates residue A, and T102 tower stilling goes out heavy distillat C, obtains midbarrel B by the T102 side line;
For further reduction operation energy consumption, can adopt hot integrated operation between T101 and the T102, promptly improve T101 cat head operating pressure, use T101 cat head gas phase as T102 tower still reboiler thermal source; Perhaps improve T102 cat head operating pressure, use T102 cat head gas phase as T101 tower still reboiler thermal source.
By process provided by the invention, the T101 side line is extracted the position out and generally is positioned at more than the T101 charging.
By process provided by the invention, the midbarrel B that T102 tower still extraction logistics can go recovery tower (T103) or the further recovery of other equipment (flash tank, superheater, evaporimeter etc.) wherein to contain.The midbarrel B that reclaims can return the T102 tower, also discharging separately, does not return the T102 tower.
Process provided by the invention only needs a condenser and two reboilers, compares with conventional two tower separating technologies, has saved a condenser.And, hot integrated operation between T101, T102 two towers, only a tower needs external heat source that energy is provided, and greatly reduces operation energy consumption.In addition, the rising quantity of steam is controlled respectively by the tower still reboiler of two towers in two Tatas, has effectively overcome the defective that the Petlyuk tower is difficult for controlling.
The energy-saving process method that removes the weight component provided by the invention can be widely used in various distillations, evaporation process in the chemical separating, operating mode that for example styrene product is refining, ethylene glycol product purification, acetic acid are carried dense retracting device, butene-1 is refining, n-hexane is purified or the like.
The present invention has overcome the shortcoming of prior art, has significant practicality and obvious energy-saving effect extremely, has a extensive future.
Description of drawings
Fig. 1 is that two towers that prior art adopts separate the process chart of weight component in proper order.
Fig. 2 is the process chart of the integrated separation weight of a kind of heat component, and the T1 gas phase provides thermal source for T2 tower still.
Fig. 3 is the process chart of the integrated separation weight of a kind of heat component, and T2 cat head gas phase provides thermal source for T1 tower still.
Fig. 4 is a kind of typical Petlyuk tower, and material is introduced into secondary tower, extracts product out by the king-tower side line.
Fig. 5 is another kind of typical Petlyuk tower, and material is introduced into king-tower, extracts product out by the secondary tower side line.
Fig. 6 is the energy saving technique figure that a kind of three cut rectifying provided by the invention separate.
Fig. 7 is the distressed structure of equal value of Fig. 6.T101 top rectifying section and condenser move to the T102 top.
Fig. 8 is the distressed structure of process shown in Figure 6.
Fig. 9 is a kind of energy saving technique flow chart that typically removes the weight component provided by the invention, and hot integrated operation between T101, T102 two towers uses T101 cat head gas phase as T102 tower still thermal source.
Figure 10 is the energy saving technique flow chart that another kind provided by the invention typically removes the weight component, and hot integrated operation between T101, T102 two towers uses T102 cat head gas phase as T101 tower still thermal source.
Figure 11 is that a kind of typical case of contained midbarrel in the T102 tower still reclaims process chart, the midbarrel B that T102 tower still extraction logistics can go the further recovery of recovery tower (T103) wherein to contain.The midbarrel B that reclaims can return the T102 tower, also discharging separately, does not return the T102 tower.
The specific embodiment
Specific embodiments of the present invention is described in detail as follows with reference to accompanying drawing, but for illustrative purposes only rather than the restriction the present invention.
As shown in Figure 9, the invention provides a kind of energy-saving process method that typically removes the weight component, the mixed material 1 that contains light fraction A, midbarrel B and heavy distillat C is introduced into the middle part of pre-distillation column (T101), T101 cat head gas phase 2 becomes self lime set 3 after giving the heating of T102 tower still reboiler, lime set 3 parts are returned the T101 cat head as T101 backflow 4, and another part is as T101 cat head discharging 5 extraction.Key component is light fraction A in the logistics 5.7 of T101 tower reactor distillates contain heavy distillat C and midbarrel B goes to T102 tower middle and lower part.Extract the liquid phase stream that contains A, B out by T101 top side line 6 and go to rectifying column (T102) tower middle and upper part.Lime set 9 parts of T102 cat head gas phase 8 after condenser condenses reflux as T102 and 10 return the T102 cat head, and another part is as T102 cat head discharging 11 extraction (key component is the T101 residue light fraction A of extraction not in the charging).T102 tower stilling goes out 13 heavy distillat C, obtains midbarrel B by T102 bottom side line 12.
Adopt hot integrated operation between T101 and the T102, promptly suitably improve T101 cat head operating pressure, use T101 cat head gas phase as T102 tower still reboiler thermal source.Perhaps as shown in figure 10, suitably improve T102 cat head operating pressure, use T102 cat head gas phase as T101 tower still reboiler thermal source.A whole separation process only tower still reboiler needs the outside that thermal source is provided, and only a condenser needs the outside that cold is provided simultaneously, and operation energy consumption reduces greatly.
Under some operation operating mode, boiling-point difference is bigger between A, B, C three cuts, problems such as the too low or tower still reboiler temperature of overhead condensation temperature is too high may appear by the process that Fig. 9 or Figure 10 provided, can cancel hot integrated operation between T101 and the T102 this moment, T101, T102 two column overhead are provided with condenser respectively, and a kind of energy-saving process method that typically removes the weight component that then Fig. 9 provided develops into technological process shown in Figure 8.For large-scale plant, adopt shown in Figure 8 distillating can effectively reduce the single device scale, reduce and make, transport, install difficulty.Only T101 is provided with condenser, T102 condenser is not set; Perhaps only T102 is provided with condenser, T101 condenser is not set.Technological process then shown in Figure 8 further develops into Fig. 6, technological process shown in Figure 7, is about to that the top rectifying section of T101 and T102 merges among Fig. 8.The merging of two tower rectifying sections is placed on T101 top flow process then shown in Figure 8 and develops into flow process shown in Figure 6: the merging of two tower rectifying sections is placed on T102 top flow process then shown in Figure 8 and develops into flow process shown in Figure 7.
As shown in Figure 6, the invention provides the energy-saving process method that a kind of three cut rectifying separate, the mixed material 1 that contains light fraction A, midbarrel B and heavy distillat C is introduced into the middle part of pre-distillation column T101, T101 cat head gas phase 2 becomes self lime set 3 after condensation, a part is returned the T101 cat head as T101 backflow 4, and another part is as T101 cat head discharging 5 extraction.Key component is light fraction A in the logistics 5.7 of T101 tower reactor distillates contain heavy distillat C and midbarrel B.Extract the liquid phase stream that contains A, B (not containing C) out by T101 top side line 6 and remove the T102 tower.T102 cat head gas phase 8 is returned T101 top.T102 tower stilling goes out 13 heavy distillat C, obtains midbarrel B by T102 side line 12.
Because pre-distillation column T101 has also realized the initial gross separation of B and C when removing light fraction A, promptly T101 side line liquid phase 6 is mainly A and B (not containing C), and T101 tower still material 7 is mainly C and B (not containing A). Logistics 6,7 imports T102 top and bottom respectively then, continues to separate in T102.Therefore, though the differentiation technological process energy-saving effect that Fig. 6 provided organically combines between T101 and the T102 be not as remarkable as the process that Fig. 9 provided, more conventional separation method (as shown in Figure 1) still has significant advantage.Process energy-saving effect shown in Figure 6 and Fig. 4, Petlyuk tower shown in Figure 5 are suitable, but the rising quantity of steam is controlled respectively by the tower still reboiler of two towers in T101, T102 two Tatas, solved that Petlyuk tower gas phase is drawn and the difficult problem of flow-control, effectively overcome the defective that the Petlyuk tower is difficult for controlling.
Application Example 1:
A kind of energy-saving process method that typically removes the weight component that adopts Fig. 9 to provide carries out cinnamic refining, the mixed material that contains light fraction A (benzene/methylbenzene/ethylbenzene etc.), midbarrel B (styrene) and heavy distillat C (heavy ends such as AMS, tar) in the crude styrene raw material is introduced into the T101 middle part, T101 cat head ethylbenzene gas phase 2 is used to heat T102 tower still reboiler, lime set 3 parts of logistics 2 reflux 4 as the T101 tower, another part 5 extraction.Logistics 5 is mainly light fractions such as ethylbenzene, accounts for 50% of light fraction in the T101 charging.Ethylbenzene extracted out by T101 top side line 6 and cinnamic mixture (not containing benzene/methylbenzene substantially) enters T102 tower middle and upper part.T101 tower still discharging 7 is mainly styrene and T102 tower bottom is gone in heavy ends (not containing light components such as ethylbenzene substantially).Lime set 9 parts of T102 cat head ethylbenzene gas phase 8 after condenser condenses reflux 10 as the T102 tower, and another part 11 is as the discharging of T102 cat head.Logistics 11 is mainly in the raw material the not ethylbenzene of extraction of T101 cat head, does not contain light components such as benzene/methylbenzene in the logistics 11 substantially, can directly return leading portion ethyl benzene dehydrogenation preparation of styrene reaction process.Obtain the styrene product of purity more than 99.8% by T102 tower side line 12.T102 tower still discharging 13 is heavy ends such as styrene and tar.As Figure 11, logistics 13 can be removed further recovery styrene wherein of subsequent recovery tower (T103) (or styrene evaporimeter), the styrene 15 that reclaims can return T102 tower (perhaps discharging separately, do not return the T102 tower), and T103 tower still material 16 is for containing the very low heavy ends such as tar of concentration of styrene.
Calculate by 500,000 tons of/year styrene product (operation hour was by 8000 hours/year) production scale, per hour refining benzene ethylene product output is 62.5Ton/h.The crude styrene raw material is formed calculating by following typical styrene material.
Table 1:
| Title | Form wt% |
| Benzene | 0.3076 |
| Toluene | 1.2668 |
| Non-aromatic | 0.1276 |
| Ethylbenzene | 37.3898 |
| Styrene | 57.8824 |
| Paraxylene | 0.0048 |
| Meta-xylene | 0.0057 |
| Ortho-xylene | 0.0006 |
| Isopropylbenzene | 0.0002 |
| AMS | 0.0114 |
| Water | 0.0909 |
| Other | 2.9122 |
| Add up to | 100.0000 |
| Temperature | 55℃ |
Carried out the operation energy consumption contrast by the energy-saving process method (process that Fig. 9 provides) that removes the weight component provided by the invention with the process (shown in Figure 1) that the routine that extensively adopts at present removes the weight component, contrast operation's condition and energy-saving effect are listed in the table 2.
Application Example 2:
As shown in Figure 6, the energy-saving process method that a kind of three cut rectifying of adopting Fig. 6 to provide separate carries out cinnamic refining, the mixed material that contains light component, styrene and heavy ends such as benzene/methylbenzene/ethylbenzene (AMS, tar etc.) is introduced into T101 top, distillated in the raw material light components such as benzene/methylbenzene/ethylbenzene by the T101 cat head, ethylbenzene extracted out by T101 middle part side line 6 and cinnamic mixture (not containing benzene/methylbenzene substantially) advances the T102 cat head.T101 tower still discharging 7 is mainly styrene and T102 tower bottom is gone in heavy ends (not containing light components such as ethylbenzene substantially).T102 cat head ethylbenzene gas phase 8 is the ethyl benzene/styrene mixture, goes the T101 side line to extract the position out.Obtain the styrene product of purity more than 99.8% by T102 tower side line 12.T102 tower still discharging 13 is heavy ends such as styrene and tar.Logistics 13 can go subsequent recovery tower or styrene evaporimeter to reclaim wherein styrene, and the styrene of recovery can return the T102 tower, perhaps discharging separately, does not return the T102 tower.
Calculate by 500,000 tons of/year styrene product (operation hour was by 8000 hours/year) production scale, per hour refining benzene ethylene product output is 62.5Ton/h.The crude styrene raw material is with table 1.
Carried out the operation energy consumption contrast by the energy-saving process method (process that Fig. 6 provides) that removes the weight component provided by the invention with the process (shown in Figure 1) that the routine that extensively adopts at present removes the weight component, contrast operation's condition and energy-saving effect are also listed in the table 2.
Table 2:
By above-mentioned correction data, adopt the energy-saving process method (as shown in Figure 6) that removes the weight component provided by the invention to carry out with adopting common process method (as shown in Figure 1) that styrene is refining to be compared operation energy consumption and reduced:
(1.344-1.030)/1.344×100％≈23％
Per hour can save steam 84-64.4=19.6 ton.
Can save steam 19.6 * 8000=156800 ton (15.68 ten thousand tons) every year.
By 150 yuan of calculating of steam per ton, can save the steam expense every year:
15.68 ten thousand tons/year * 150 yuan/ton=2,352 ten thousand yuan/year.
By above-mentioned correction data, adopt the energy-saving process method (as shown in Figure 9) that removes the weight component provided by the invention to carry out with adopting common process method (as shown in Figure 1) that styrene is refining to be compared operation energy consumption and reduced:
(1.344-0.589)/1.344×100％≈56％
Per hour can save steam 84-36.8=47.2 ton.
Can save steam 47.2 * 8000=377600 ton (37.76 ten thousand tons) every year.
By 150 yuan of calculating of steam per ton, can save the steam expense every year:
37.76 ten thousand tons/year * 150 yuan/ton=5,664 ten thousand yuan/year.
The energy-saving process method that a kind of three cut rectifying provided by the invention separate has extremely distinct economic.Specified in conjunction with the embodiments, the personnel of association area can suitably change or change and make up fully according to method provided by the invention, realize this technology.Of particular note, all these are by technological process provided by the invention being carried out similar change or change and being reconfigured, and are apparent to those skilled in the art, all are regarded as in spirit of the present invention, scope and content.
Claims (5)
1. the energy-saving process method that separates of a cut rectifying, this process is to obtain highly purified midbarrel B from the mixed material that contains light fraction A, midbarrel B and heavy distillat C, it is characterized in that this process comprises:
(1) comprises two towers of pre-distillation column T101, rectifying column T102 at least;
(2) mixed material enters pre-distillation column T101, and the T101 top distillates part light fraction A, and T101 tower reactor distillate only contains heavy distillat C and midbarrel B goes to T102 tower middle and lower part; The T101 side line is extracted the liquid phase stream that contains light fraction A, midbarrel B out and is gone to T102 tower middle and upper part;
(3) rectifying column T102 cat head distillates residue light fraction A, and T102 tower stilling goes out heavy distillat C, obtains midbarrel B by the T102 side line.
2. according to the said process of claim 1, it is characterized in that adopting hot integrated operation between said pre-distillation column T101 and the rectifying column T102, use pre-distillation column T101 cat head gas phase as rectifying column T102 tower still reboiler thermal source; Perhaps use rectifying column T102 cat head gas phase as pre-distillation column T101 tower still reboiler thermal source.
3. according to the said process of claim 1, it is characterized in that said pre-distillation column T101 side line extraction position is positioned at more than the pre-distillation column T101 charging.
4. according to claim 1 or 2 said processes, it is characterized in that when boiling-point difference is big between light fraction A, midbarrel B, heavy distillat C three components in the raw material, the hot integrated operation of cancellation between pre-distillation column T101 and the rectifying column T102, pre-distillation column T101, rectifying column T102 two column overhead are provided with condenser respectively; Perhaps only pre-distillation column T101 is provided with condenser, rectifying column T102 is not provided with condenser; Perhaps only rectifying column T102 is provided with condenser, pre-distillation column T101 is not provided with condenser.
5. according to the said process of claim 1, it is characterized in that said rectifying column T102 tower still extraction logistics can remove recovery tower T103, or the midbarrel B that wherein contains of the further recovery of other equipment, the midbarrel B of recovery can return rectifying column T102 tower, or does not return rectifying column T102 tower.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102641604A (en) * | 2012-04-01 | 2012-08-22 | 中国石油化工股份有限公司 | Multiple-component lateral line thermal coupling rectification method |
| CN104203909A (en) * | 2012-03-26 | 2014-12-10 | 旭化成化学株式会社 | Method for purifying acetonitrile |
| CN108794350A (en) * | 2017-04-26 | 2018-11-13 | 福建省东南电化股份有限公司 | A method of it improving the utilization rate of two-wire TDI process units distillation systems and reduces stop frequency |
| CN109745723A (en) * | 2018-12-29 | 2019-05-14 | 恒天纤维集团有限公司 | A kind of double tower continuous feeding distillation system and control method |
| CN111111248A (en) * | 2018-10-30 | 2020-05-08 | 中国石油化工股份有限公司 | Device and method for recovering toluene from organic solvent for preparing polyolefin catalyst |
| CN112791435A (en) * | 2019-11-13 | 2021-05-14 | 中国石油化工股份有限公司 | Thermal coupling rectification device and thermal coupling rectification process |
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| CN1736961A (en) * | 2005-04-26 | 2006-02-22 | 蓝仁水 | Styrene separation process |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104203909A (en) * | 2012-03-26 | 2014-12-10 | 旭化成化学株式会社 | Method for purifying acetonitrile |
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| CN108794350A (en) * | 2017-04-26 | 2018-11-13 | 福建省东南电化股份有限公司 | A method of it improving the utilization rate of two-wire TDI process units distillation systems and reduces stop frequency |
| CN111111248A (en) * | 2018-10-30 | 2020-05-08 | 中国石油化工股份有限公司 | Device and method for recovering toluene from organic solvent for preparing polyolefin catalyst |
| CN111111248B (en) * | 2018-10-30 | 2021-10-15 | 中国石油化工股份有限公司 | Device and method for recovering toluene from organic solvent for preparing polyolefin catalyst |
| CN109745723A (en) * | 2018-12-29 | 2019-05-14 | 恒天纤维集团有限公司 | A kind of double tower continuous feeding distillation system and control method |
| CN109745723B (en) * | 2018-12-29 | 2021-07-06 | 恒天纤维集团有限公司 | Double-tower continuous feed rectification system and control method |
| CN112791435A (en) * | 2019-11-13 | 2021-05-14 | 中国石油化工股份有限公司 | Thermal coupling rectification device and thermal coupling rectification process |
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Application publication date: 20101124 |