CN101759520A - Method for extracting, rectifying and separating phenylethylene from hydrocarbon mixture - Google Patents
Method for extracting, rectifying and separating phenylethylene from hydrocarbon mixture Download PDFInfo
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- CN101759520A CN101759520A CN 200810246518 CN200810246518A CN101759520A CN 101759520 A CN101759520 A CN 101759520A CN 200810246518 CN200810246518 CN 200810246518 CN 200810246518 A CN200810246518 A CN 200810246518A CN 101759520 A CN101759520 A CN 101759520A
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Abstract
The invention relates to a method for extracting, rectifying and separating phenylethylene from a hydrocarbon mixture, comprising the following steps of: introducing the hydrocarbon mixture to an extracting and rectifying tower from the middle and supplying an extracting and rectifying solvent to the extracting and rectifying tower from the top; discharging raffinate from the top of the extracting and rectifying tower and discharging a rich solvent abundant in the phenylethylene from the bottom of the extracting and rectifying tower through extraction and rectification; supplying the extracting and rectifying solvent to a solvent recovering tower using water as a steam stripping medium, returning the extracting and rectifying solvent discharged from the bottom of the solvent recovering tower to the extracting and rectifying tower for recycling, and then enabling the water to flow back to the solvent recovering tower after separating the phenylethylene and the water discharged from the top of the solvent recovering tower. The method can effectively reduce the temperature of the solvent recovering tower and the concentration of the phenylethylene, greatly relieve the polymerization of the phenylethylene, and enhance the running time of a device.
Description
Technical field
The present invention relates to a kind of method that extracting rectifying separates unsaturated hydrocarbons from hydrocarbon mixture, specifically, be a kind of from hydrocarbon mixture the method for extracting, rectifying and separating phenylethylene.
Background technology
Styrene monomer is important basic Organic Chemicals, at aspects such as coating, agricultural chemicals, medicine extensive use is arranged also.According to statistics, contain 3～5% vinylbenzene in the steam cracking gasoline of ethylene cracker by-product, the ethylene unit that a cover is 1,000,000 tons/year contains vinylbenzene and is about 2～30,000 tons/year because of the difference of raw material in the pyrolysis gasoline.In the technological process of existing processing pyrolysis gasoline, this part vinylbenzene is that ethylbenzene is stored in C by hydrocracking
8In the cut, this C that is rich in ethylbenzene
8Cut, it is very undesirable as raw material to supply with downstream p-Xylol device.Dehydrogenation changes vinylbenzene into if adopt superfractionation to separate after the ethylbenzene again, and then technical process is long, energy consumption is high, and is also unreasonable.
By contrast, direct separating phenylethylene is a very attractive technology from pyrolysis gasoline.Yet pyrolysis gasoline C
8Fractions consisting is very complicated, and boiling point is very approaching between the component, is o-Xylol and phenylacetylene with the most difficult isolating component of vinylbenzene wherein.O-Xylol and cinnamic boiling-point difference only are 0.8 ℃, and the relative volatility of the two has only 1.04, need thousands of theoretical stages with conventional distillation, therefore are actually to realize.
From without separating phenylethylene the pyrolysis gasoline of hydrogenation, feasible method is to adopt extracting rectifying, and its ultimate principle is the effect by selective solvent, changes the relative volatility between o-Xylol and the vinylbenzene, thereby reaches the purpose of separating purifying styrene.Therefore, the performance of extraction distillation solvent plays a part crucial to the technico-economical comparison of sepn process, wherein most important performance comprises that selectivity, boiling point, thermo-chemical stability and solvent self is to cinnamic polymerization inhibition performance etc., in addition, the operational condition of extracting rectifying miscellaneous equipment and method also directly influence the cinnamic effect of extracting rectifying.
GB1,038,606 proposed a kind of from hydrocarbon mixture the method for separating phenylethylene, this method is handled hydrocarbon raw material with Fuller's earth earlier, uses the solvent of the aqueous solution of silver salt as extracting rectifying again, and described silver salt is a Silver Nitrate, but the cost of this solvent is higher, and industrial utility value is lower.
USP3,763,015 discloses a kind of method by use polymerization retarder and extracting rectifying separating phenylethylene from pyrolysis gasoline, this method is carried out extracting rectifying to pyrolysis gasoline in the presence of polar solvent and nitrogenous polymerization retarder, from solvent, reclaim vinylbenzene then, the nitric acid reaction of vinylbenzene that recovery is obtained and capacity is removed the impurity in the vinylbenzene again, and the vinylbenzene cut of removing behind the impurity from new distillation obtains colourless and pure substantially vinylbenzene again.Described polar solvent is selected from N,N-DIMETHYLACETAMIDE, dimethyl formamide, N-Methyl pyrrolidone and methyl-sulphoxide etc., and the polymerization retarder that uses is sulphur, Resorcinol, p-ten.-butylcatechol.
USP4,596,655 disclose a kind of from hydrocarbon mixture the method for unsaturated hydrocarbon such as separating phenylethylene, adopt aminoethylpiperazine as the solvent of the extracting rectifying stopper of holding concurrently, be also to need 115～125 theoretical stages under 8 the condition in solvent ratio.
The method of the disclosed extracting rectifying of CN1077560C separating phenylethylene from pyrolysis gasoline proposes the solvent of extracting rectifying is divided into two portions, solvent is mainly by being selected from propylene carbonate, tetramethylene sulfone, methyl carbitol, 1-Methyl-2-Pyrrolidone, 2-Pyrrolidone or their mixture but do not comprise the first part of water and be made up of the second section that water constitutes, first part's solvent enters from extractive distillation column top, and the second section solvent adds at the bottom of extractive distillation column.
CN1962013A discloses from steam cracking C
8The solvent of recycling vinyl benzene with abstraction distillation in the cut; comprise 55～60% sulfone compound and 40～45% nitrogenous compound; described sulfone compound is selected from dimethyl sulfoxide (DMSO) or tetramethylene sulfone; nitrogenous compound is selected from least a in succinonitrile, N,N-dimethylacetamide, N-N-methyl-2-2-pyrrolidone N-, 2-Pyrrolidone, aminoethyl piperazine or the N-formyl morpholine.This solvent can make the pH value of solvent be about 7, and improves o-Xylol to cinnamic relative volatility.
CN1541988A discloses a kind of method of extracting rectifying aromatics separation, and this method is isolated C by prefractionation earlier from hydrocarbon mixture
6～C
7Cut and C
8Cut is with C
6～C
7Cut is introduced extractive distillation column and is carried out extracting rectifying, cat head is isolated non-aromatics and water, water is injected lean solvent, non-aromatics is discharged system, the rich solvent that is rich in aromatic hydrocarbons that obtains at the bottom of the tower separates in solvent recovery tower, overhead stream isolated water after condensation is introduced solvent recovery tower again as water stripping, and lean solvent returns extractive distillation column.This method can increase the water-content in the lean solvent, improves solvent selectivity, the isolated water of extracting rectifying cat head is directly introduced lean solvent, and do not introduce solvent recovery tower as water stripping, also can avoid in the water dissolved non-aromatics to the pollution of aromatic hydrocarbon product.
Summary of the invention
The purpose of this invention is to provide a kind of from hydrocarbon mixture the cinnamic method of extracting rectifying, this method can reduce concentration of styrene and the service temperature in the solvent recovery tower to greatest extent, reduces styrene polymerization, the implement device long-period stable operation.
Provided by the invention from hydrocarbon mixture the method for extracting, rectifying and separating phenylethylene, comprise hydrocarbon mixture is introduced extractive distillation column from the middle part, extraction distillation solvent is introduced extractive distillation column from the top, through extracting rectifying, not containing cinnamic raffinate discharges from the top of extractive distillation column, the rich solvent of rich in styrene is discharged by the extracting rectifying tower bottom, enter with water is the solvent recovery tower of stripping medium, the extraction distillation solvent of discharging at the bottom of the solvent recovery tower returns the extractive distillation column recycle, the vinylbenzene that the solvent recuperation cat head is discharged separates with the water process, and water is gone into solvent recovery tower from trim the top of column.
The present invention is in the extracting rectifying separation of C
8In the cinnamic process, the solvent recuperation cat head employing water backflow at separating phenylethylene and extraction distillation solvent makes the interior temperature of tower reduce by 20～30 ℃ in the aromatic hydrocarbons, significantly reduction of styrene polymerization loss, and solvent nature is stablized, and installs to prolong greatly running period.
Description of drawings
Fig. 1 is the schematic flow sheet of extracting and separating vinylbenzene of the present invention.
Embodiment
The present invention is in the extracting rectifying separation of C
8In the cinnamic process in the aromatic hydrocarbons, at the solvent recovery tower of extracting rectifying with water as the stripping medium, and adopt water to reflux and the vinylbenzene that replaces available technology adopting refluxes at the solvent recuperation cat head.Adopt the reflux materials of water as the solvent recuperation cat head, can reduce the concentration of styrene of solvent recovery tower rectifying section, reduce the residence time of vinylbenzene in tower, can significantly reduce the temperature in the solvent recovery tower simultaneously, thereby alleviate cinnamic polymerization, improve the working time of extracting rectifying device.
The vinylbenzene that described extraction distillation solvent reclaims the cat head discharge separates with the water process, isolated water can all pass back into solvent recovery tower as required, preferably with the isolated water of solvent recuperation cat head, a part is as the backflow of solvent recuperation column overhead, and all the other then enter at the bottom of the solvent recovery tower as water stripping.
Of the present inventionly go into the recirculation water of solvent recovery tower and the mass ratio of cat head recovered water is 1～4: 1, preferred 1～2.5: 1 from trim the top of column.
The reflux ratio of solvent recuperation cat head of the present invention, i.e. the vinylbenzene mass ratio of recirculation water and extraction are 0.1～1.5, preferred 0.4～0.8.Enter the water stripping of solvent recovery tower and the mass ratio of solvent, promptly the water stripping ratio is 0.01～0.10, preferred 0.03～0.08.
Extraction distillation solvent of the present invention is tetramethylene sulfone, glycol ether, triglycol, Tetraglycol 99, N; at least a or several mixture in N-N,N-DIMETHYLACETAMIDE and the N-formyl morpholine; be preferably tetramethylene sulfone, triglycol or Tetraglycol 99 and N; the mixture of N-N,N-DIMETHYLACETAMIDE; the content of N,N-dimethylacetamide is 10～40 quality %, preferred 15～30 quality % in the mixture.
The C of the preferred pyrolysis gasoline of hydrocarbon mixture of the present invention
8Cut, wherein styrene content is 20～70 quality %, C
8Aromatic hydrocarbons and non-aromatics content are 30～80 quality %.
The theoretical plate number of described extractive distillation column preferred 60～90, the trim the top of column ratio, be the trim the top of column thing and the ratio of cat head production is 1～5, the mass ratio of used extraction solvent and hydrocarbon mixture, be that solvent ratio is 3～10: 1, preferred 5～8: 1, preferred 120～150 ℃ of column bottom temperature, the preferred 8～20kPa of tower top pressure.
The theoretical plate number of described solvent recovery tower is preferred 20～50, preferred 130～150 ℃ of column bottom temperature, the preferred 8～20kPa of tower top pressure.
The inventive method is applicable to extracting, rectifying and separating phenylethylene from hydrocarbon mixture, is specially adapted to from C
8Extracting, rectifying and separating phenylethylene in the aromatic hydrocarbons.
Below in conjunction with description of drawings the present invention, among Fig. 1, contain cinnamic hydrocarbon mixture and enter interchanger 101 by pipeline 1, enter extractive distillation column 102 from the middle part by pipeline 4 after the heat exchange, extraction distillation solvent enters extractive distillation column 102 by pipeline 15 from the top, through extracting rectifying, not containing cinnamic raffinate is discharged by the overhead line 5 of extractive distillation column, enter return tank 103 and carry out oily water separation, the effusive oil phase part of return tank passes back into the top of extractive distillation column 102 by pipeline 16, another part then as raffinate by pipeline 6 discharge systems.The rich solvent of rich in styrene is discharged by the extracting rectifying tower bottom, enter solvent recovery tower 104 from the middle part through pipeline 7, vinylbenzene and water are discharged by overhead line 9, enter lime set jar 105 and carry out oily water separation, the vinylbenzene that lime set jar 105 is discharged is by pipeline 10 discharge systems, 105 jars of water of telling of lime set jar, a part passes back into the solvent recuperation cat head through pipeline 17, the remaining water of discharging through pipeline 11 and extractive distillation column return tank of top of the tower 103 pipelines 8 is mixed into interchanger 106 and lean solvent heat exchange, the water vapour that is vaporized enters solvent recovery tower 104 bottoms as the stripping medium through pipeline 12, the lean solvent at 104 ends of solvent recovery tower is derived by pipeline 13, after interchanger 106 heat exchange, return the top of extractive distillation column 102 through pipeline 14.
Further describe the present invention below by example, but the present invention is not limited to this.
Example 1
To consist of the pyrolysis gasoline C shown in the table 1
8Cut is a raw material, by the flow process of Fig. 1 described raw material is carried out extracting rectifying, reclaims vinylbenzene wherein.Used extraction distillation solvent contains the tetramethylene sulfone of 80 quality %, the N,N-DIMETHYLACETAMIDE of 20 quality %, and solvent recuperation cat head employing isolated water from the cat head material is phegma, and is the stripping medium with water.The theoretical plate number of described extractive distillation column is 75, and trim the top of column is than 3, tower top pressure 15kPa, 138 ℃ of column bottom temperatures.The theoretical plate number 45 of recovery tower, tower top pressure 15kPa, tower bottom pressure 20kPa.Under the condition of not carrying out solvent reclamation, see Table 2 the working time of the operational condition of solvent recovery tower and separating resulting and device.
Comparative Examples 1
Press the method extracting rectifying pyrolysis gasoline C of example 1
8Vinylbenzene in the cut, different is that solvent recovery tower adopts the isolated vinylbenzene of cat head as backflow, the operational condition of solvent recovery tower and separating resulting and device see Table 2 working time.
Table 1
Table 2
As shown in Table 2, be in vinylbenzene purity under 99.5% the situation, adopt the inventive method, the head temperature of solvent recovery tower has only 51 ℃, rectifying section and stripping section middle part temperature are respectively 60 ℃ and 108 ℃, adopt vinylbenzene to reduce by 23 ℃, 30 ℃ and 6 ℃ respectively as the Comparative Examples 2 of trim the top of column.Particularly rectifying section is because concentration of styrene is very high, and 20～30 ℃ cooling can be alleviated cinnamic polymerization significantly.In addition, solvent also is reduced to 1mg/kg by original 10mg/kg in the vinylbenzene of the present invention.Under the condition of not carrying out solvent reclamation, the device parallel-adder settle-out time improves 40% than Comparative Examples 1.
Example 2
The method of pressing example 1 is from pyrolysis gasoline C
8Separating phenylethylene in the cut, the different extraction distillation solvents that is to use contain the triglycol of 70 quality %, the N,N-DIMETHYLACETAMIDE of 30 quality %, and see Table 3 the working time of the operational condition of solvent recovery tower and separating resulting and device.
Comparative Examples 2
Press the method extracting rectifying pyrolysis gasoline C of example 1
8Vinylbenzene in the cut, different is that solvent recovery tower adopts the isolated vinylbenzene of cat head as backflow, and the extraction distillation solvent of use is identical with example 2, and the operational condition of solvent recovery tower and separating resulting and device see Table 3 working time.
Table 3
As shown in Table 3, be in vinylbenzene purity under the situation of 99.5 quality %, the inventive method solvent recovery tower head temperature is 51 ℃, and rectifying section and stripping section middle part temperature are respectively 58 ℃ and 105 ℃, adopt vinylbenzene to reduce by 23 ℃, 31 ℃ and 8 ℃ respectively as the Comparative Examples 2 that refluxes.Particularly rectifying section is because concentration of styrene is very high, and 20～30 ℃ cooling can be alleviated cinnamic polymerization significantly.In addition, solvent also is reduced to below the 1mg/kg by original 10mg/kg in the vinylbenzene of the present invention.Under the condition of not carrying out solvent reclamation, the device parallel-adder settle-out time improves 60% than Comparative Examples 2.
Claims (10)
1. the method for an extracting, rectifying and separating phenylethylene from hydrocarbon mixture, comprise hydrocarbon mixture is introduced extractive distillation column from the middle part, extraction distillation solvent is introduced extractive distillation column from the top, through extracting rectifying, not containing cinnamic raffinate discharges from the top of extractive distillation column, the rich solvent of rich in styrene is discharged by the extracting rectifying tower bottom, enter with water is the solvent recovery tower of stripping medium, the extraction distillation solvent of discharging at the bottom of the solvent recovery tower returns the extractive distillation column recycle, the vinylbenzene that the solvent recuperation cat head is discharged separates with the water process, and water is gone into solvent recovery tower from trim the top of column.
2. in accordance with the method for claim 1, it is characterized in that vinylbenzene that described solvent recuperation cat head discharges and water through separating, an isolated water part is as the backflow of solvent recuperation column overhead, and all the other then enter at the bottom of the solvent recovery tower as water stripping.
3. in accordance with the method for claim 2, it is characterized in that describedly going into the recirculation water of solvent recovery tower and the mass ratio of cat head recovered water is 1～4: 1 from trim the top of column.
4. in accordance with the method for claim 1, it is characterized in that the recirculation water of solvent recuperation cat head and the vinylbenzene mass ratio of extraction are 0.1～1.5.
5. in accordance with the method for claim 1, it is characterized in that entering the water stripping of solvent recovery tower and the mass ratio of solvent is 0.01～0.10.
6. in accordance with the method for claim 1, it is characterized in that described extraction distillation solvent is at least a or several mixture in tetramethylene sulfone, glycol ether, triglycol, Tetraglycol 99, N,N-dimethylacetamide and the N-formyl morpholine.
7. in accordance with the method for claim 1, it is characterized in that extraction distillation solvent is the mixture of tetramethylene sulfone, triglycol or Tetraglycol 99 and N,N-dimethylacetamide, the content of N,N-dimethylacetamide is 10～40 quality % in the mixture.
8. in accordance with the method for claim 1, it is characterized in that described hydrocarbon mixture is the C of pyrolysis gasoline
8Cut, wherein styrene content is 20～70 quality %.
9. in accordance with the method for claim 1, the theoretical plate number that it is characterized in that described extractive distillation column is 60～90, and the trim the top of column ratio is 1～5, and column bottom temperature is 120～150 ℃, and tower top pressure is 8～20kPa.
10. in accordance with the method for claim 1, the theoretical plate number that it is characterized in that described solvent recovery tower is 20～50, and column bottom temperature is 130～150 ℃, and tower top pressure is 8～20kPa.
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| CN102452891A (en) * | 2010-10-25 | 2012-05-16 | 中国石油化工股份有限公司 | Method for separating styrene through extractive distillation |
| CN103044793A (en) * | 2011-10-17 | 2013-04-17 | 金发科技股份有限公司 | Low-odor low-VOC (volatile organic compound)-content styrene polymer composition and preparation method thereof |
| CN103360200A (en) * | 2012-03-30 | 2013-10-23 | 中国石油化工股份有限公司 | Composite solvent and method for extracting, rectifying and recovering styrene from hydrocarbon mixture |
| CN104829413A (en) * | 2015-03-26 | 2015-08-12 | 南京师范大学 | A single-side-draw vacuum extraction method for styrene in light cracked C9 aromatic hydrocarbons |
| CN106316769A (en) * | 2015-06-19 | 2017-01-11 | 中国石油化工股份有限公司 | Apparatus and method for separating styrene from hydrocarbons mixture |
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| CN110028376A (en) * | 2018-01-12 | 2019-07-19 | 中国石油化工股份有限公司 | The purification of extracting, rectifying and separating phenylethylene solvent for use and styrene separation process |
| CN117776847A (en) * | 2023-12-27 | 2024-03-29 | 南京长江江宇环保科技股份有限公司 | Process method for separating ethylbenzene and styrene by extractive distillation |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4781820A (en) * | 1985-07-05 | 1988-11-01 | Union Carbide Corporation | Aromatic extraction process using mixed polyalkylene glycols/glycol ether solvents |
| US5073669A (en) * | 1989-03-09 | 1991-12-17 | Uop | Method for aromatic hydrocarbon recovery |
| ZA972966B (en) * | 1996-05-21 | 1997-11-21 | Glitsch Int Inc | Recovery of styrene from purolysis gasoline by extractive distillation. |
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| CN100522305C (en) * | 2005-11-11 | 2009-08-05 | 中国石油化工股份有限公司 | Extraction distillation solvent |
-
2008
- 2008-12-25 CN CN 200810246518 patent/CN101759520B/en active Active
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| CN102452891B (en) * | 2010-10-25 | 2014-07-02 | 中国石油化工股份有限公司 | Method for separating styrene through extractive distillation |
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| CN103360200A (en) * | 2012-03-30 | 2013-10-23 | 中国石油化工股份有限公司 | Composite solvent and method for extracting, rectifying and recovering styrene from hydrocarbon mixture |
| CN104829413A (en) * | 2015-03-26 | 2015-08-12 | 南京师范大学 | A single-side-draw vacuum extraction method for styrene in light cracked C9 aromatic hydrocarbons |
| CN104829413B (en) * | 2015-03-26 | 2017-01-18 | 南京师范大学 | A single-side-draw vacuum extraction method for styrene in light cracked C9 aromatic hydrocarbons |
| CN106316769A (en) * | 2015-06-19 | 2017-01-11 | 中国石油化工股份有限公司 | Apparatus and method for separating styrene from hydrocarbons mixture |
| CN107814680A (en) * | 2016-09-14 | 2018-03-20 | 中国石油化工股份有限公司 | From the full gear method and refined styrene method of crude styrene obtained by drippolene |
| CN107814680B (en) * | 2016-09-14 | 2021-01-08 | 中国石油化工股份有限公司 | Method for removing aldehyde from crude styrene obtained from pyrolysis gasoline and method for refining styrene |
| CN110028376A (en) * | 2018-01-12 | 2019-07-19 | 中国石油化工股份有限公司 | The purification of extracting, rectifying and separating phenylethylene solvent for use and styrene separation process |
| CN109847396A (en) * | 2018-12-28 | 2019-06-07 | 广东新华粤华德科技有限公司 | A kind of device for hydrocarbon mixture extracting, rectifying and separating phenylethylene |
| CN117776847A (en) * | 2023-12-27 | 2024-03-29 | 南京长江江宇环保科技股份有限公司 | Process method for separating ethylbenzene and styrene by extractive distillation |
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