CN103360195A - Method for separation and purification of 1-octylene from hydrocarbon (oxygen) mixture - Google Patents
Method for separation and purification of 1-octylene from hydrocarbon (oxygen) mixture Download PDFInfo
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Abstract
The invention relates to a method for separation and purification of 1-octylene from a hydrocarbon (oxygen) mixture. The raw material is subjected to pre-separation, azeotropic distillation to remove oxides, fine distillation to remove light and heavy isomers, coarse product refining and other processing steps, and then the 1-octylene product can be obtained. Compared with the oligomerization method and wax cracking method for production of 1-octylene, the method provided in the invention has the advantages of simple process and low production cost.
Description
Technical field
The present invention relates to a kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, this technology be fit to hydrocarbon (oxygen) mixture stream passes that industry produces especially in the logistics that produces of Fischer-Tropsch synthesis method 1-octene product separation purify.
Background technology
The 1-octene is widely used in the production of aldehyde, brominated alkanes and the comonomer in the polymer production, it also is the important source material of making the fine chemical products such as senior softening agent, ucon oil, market requirement rapid development, so the 1-octene has very high economic worth.At present structural surplus and the shortage of China's synthetic resins and plastic prod is day by day serious, and the contradiction that many, the special-purpose trades mark of large universal product are few is very outstanding, and 1-butylene and external superseded propylene are also as comonomer, and product competitiveness is not high.Demand to high carbon number alpha-olefin (such as 1-hexene, 1-octene) relies on the high price import for a long time, has directly affected the exploitation of the new trade mark of domestic polyolefine, and this has become the bottleneck of restriction China polyolefine industry development.
The logistics that contains the 1-octene of many industrial preparations comprises the mixture of saturated alkane in the wide molecular weight scope very, alkene, aromatic hydrocarbons, cyclic hydrocarbon alkane (alkene) usually, in the industrial logistics that has even also comprise the oxide compounds such as alcohol, aldehyde, ketone, acid and ester, typical as produce the logistics that obtains with the Fischer-Tropsch synthesis method.All these compounds are isolated from above-mentioned logistics before particular composition all must commercially be provided, and comprise compound and the C of wide region carbon number in the logistics of the described 1-of containing octene
2～C
100Multiple normal paraffin, isoparaffin, linear alpha-olefins, branched-chain alkene, internal olefin, aromatic hydrocarbons and naphthenic hydrocarbon in the scope, wherein many have a close molecular weight, makes described lock out operation very complicated.Separate and the comparatively difficulty of alpha-olefin (such as the 1-octene) of emanating wherein, conventional distillation method is not enough to separate the close material of boiling point usually.
The method of separating alpha-olefin from hydrocarbon (oxygen) logistics that has proposed comprises utilizes molecular sieve (to be limited to average carbon number scope ratio at C
5～C
20The more effective raw material of composition of the wide average carbon number in the scope), the boiling point that utilizes exchange resin, utilizes oligomeric or etherificate conversion reaction to change the material in the described feed stream is realized separating.
Patent CN100400483C provide one from 1-hexene material the method for concentrate 1-hexene, described method by first with raw material with contain the complexing agent complexing of Ag ion, the gained complex liquid extracts through extraction agent again, then will distill in the extraction liquid, by repeatedly repeating said process with described material concentrate.The described 1-hexene of document material only comprises 1-hexene, anti--the 2-hexene, suitable-the 2-hexene, anti--3-hexene, suitable-several materials of 3-hexene.
Patent CN1738785A has described a kind of method of separating linear alpha-olefins from the raw material that contains linear alpha-olefins, stable hydrocarbon, internal olefin, branched olefin and alcohol, raw material is contacted with the line style polyaromatic compound, alkene in the logistics and line style polyaromatic compound form line style polyaromatic compound-olefin adducts under certain condition, remove the mixture of stable hydrocarbon, unreacting olefin, unreacted line style polyaromatic compound and alcohol after; Changing reaction conditions makes linear alpha-olefins percentage in line style polyaromatic compound-olefin adducts be higher than the percentage of line style polyaromatic compound-other olefin adducts, after separating other alkene that dissociates, the linear alpha-olefins adducts that dissociates again separates obtaining the alpha-olefin enriched products from polyaromatic compound.The method especially is fit to separate linear alpha-olefins from the synthetic logistics of Fischer-Tropsch, can be effectively with the alpha-olefin concentrate, but from give an actual example, gained linear alpha-olefins product is difficult to reach polymerization-grade, the method processing step is complicated in addition.
Patent US6483000B2 provides a kind of method of separating the 1-amylene from hydrocarbon mixture, and described logistics is isolated 1-amylene product after prefractionation, superfractionation, etherificate, washing, Methanol Recovery, drying and other steps are processed.
The method that above-mentioned document provides several alpha-olefins to separate, but raw material, separation method and products characteristics that each method is fit to have nothing in common with each other the invention provides the method for separating-purifying 1-octene in hydrocarbon (oxygen) mixture of a kind of leniently carbon number distribution.
Summary of the invention
Purpose of the present invention be exactly provide in order to overcome the defective that above-mentioned prior art exists a kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene.
Purpose of the present invention can be achieved through the following technical solutions: a kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, it is characterized in that, said method comprising the steps of:
(a) hydrocarbon (oxygen) mixture material logistics 1 is entered pre-separation unit A, purpose is to remove that most of carbon number is higher than C in the raw mix
8Component and most of carbon number be lower than C
8Component, this unit is by two (many) towers combine operationss, or adopts the method for a next door tower to finish, and after the pre-separation, obtains C
8-lighting end logistics 2, C
8Cut logistics 3 and C
8+ last running logistics 4; Gained C
8The cut logistics is except C
8Outside the hydrocarbon, also have hydrocarbon and the oxide compound of other carbon number of part;
(b) C
8Cut logistics 3 enters azeotropy rectification column B, removes C
8Oxygenatedchemicals in the logistics.Overhead vapours is through being divided into up and down two-phase in phase splitter after the condensation, the oil phase logistics of rich hydrocarbon is C
8Hydrocarbon and entrainer logistics 6 extraction, trim the top of column is returned in the logistics of entrainer phase, tower reactor extraction oxide-rich logistics 7;
(c) C
8Hydrocarbon and entrainer logistics 6 enter entrainer recovery tower C, and the phase splitter circulation of azeotropic distillation column overhead, the C of tower reactor extraction oxide-free are returned in the rich entrainer logistics 8 of overhead extraction, this logistics
8Hydrocarbon stream 9;
(d) C of oxide-free
8Hydrocarbon stream 9 enters essence minute tower D, and the cut logistics that the overhead extraction boiling point is lower than 1-octene is rectifying tower D overhead stream 10, and tower reactor obtains 1-octene and the cut logistics i.e. essence minute tower D tower reactor logistics 11 higher than 1-octene boiling point;
(e) an essence minute tower D tower reactor logistics 11 enters essence minute tower E, and the logistics of the rich 1-octene of overhead extraction i.e. essence minute tower E overhead stream 12, the i.e. essence minute tower E tower reactor logistics 13 of cut logistics that tower reactor extraction boiling point is higher than 1-octene;
(f) an essence minute tower E overhead stream 12 enters extractive distillation column F, and cat head obtains C
8Hydrocarbon stream is extracting rectifying cat head logistics 14, is rich in one or more components in positive structure, isoparaffin, internal olefin, cycloolefin, branched-chain alkene, the aromatic hydrocarbons in this logistics, and tower reactor extraction extraction agent and the logistics of 1-octene mixed solution are extracting rectifying tower reactor logistics 15;
(g) extracting rectifying tower reactor logistics 15 enters 1-octene knockout tower G, and cat head obtains 1-octene product stream 16, tower reactor extraction regenerating extracting agent logistics 17, and this logistics is returned extractive distillation column F top and is recycled.
Described hydrocarbon (oxygen) mixture material logistics 1 is C for the carbon number range that contains the 1-octene
2～C
100Hydrocarbon and carbon number range be C
2～C
20The mixture of oxygenatedchemicals, wherein same carbon number hydrocarbon compounds comprises positive structure and isoparaffin, linear alpha-olefin, branched-chain alkene, internal olefin, cycloolefin, aromatic hydrocarbons, naphthenic hydrocarbon; Same carbon number oxygenatedchemicals comprises one or more of alcohol, aldehyde, ketone, acid, ester compound.
Described hydrocarbon (oxygen) mixture material logistics 1 comprises the stream thigh that contains the 1-octene that different industrial processes obtain, the stream thigh that contains the 1-octene that preferred Fischer-Tropsch synthesis method obtains.
The described pre-separation of step (a) unit A is the above combined separation tower of two towers or two towers, or a kind of in the tower of single next door.
The described C of step (a)
8The 1-octene content is greater than 5wt% in the cut logistics 3.
Step (d) and (e) in essence divide tower D and essence minute tower E two towers also can be by following pattern serial operation: the C of oxide-free
8Hydrocarbon stream 9 enters essence minute tower D, from the cut logistics higher than 1-octene of tower reactor extraction boiling point, the cut logistics that overhead extraction 1-octene and boiling point are lower than 1-octene, overhead stream enters essence minute tower E, from the overhead extraction boiling point logistics cut lower than 1-octene, the logistics of the rich 1-octene of tower reactor extraction, the tower reactor logistics enters the extractive distillation column F of step (f).
The used entrainer of the described azeotropy rectification column B of step (b) is the aqueous solution of alcohol, ketone, ester, ethers organic oxygen-containing compound.
The preferred low carbon alcohol solution of entrainer that step (b) is used, alcohol comprises one or more in ethanol, Virahol, n-propyl alcohol, isopropylcarbinol, the trimethyl carbinol, the propyl carbinol.
The used extraction agent of step (f) is one or more in ethylene glycol, benzene hexanone, 1-Methyl-2-Pyrrolidone, methyl-sulphoxide, the hexyl acetate.
Described azeotropy rectification column B theoretical plate number is 10～50, feed entrance point be upper 3～45, reflux ratio is 0.5～10, control tower top temperature be 60～90 ℃, the tower reactor temperature is 110～150 ℃;
The theoretical plate number of described entrainer recovery tower C is 10～50, and reflux ratio is 0.5～10, feed entrance point be upper 3～45, control tower top temperature be 50～90 ℃, tower reactor is 100～150 ℃;
It is 80～250 that described essence is divided the theoretical plate number of tower D, and reflux ratio is 10～40, feed entrance point be upper 10～245, control tower top temperature be 80～120 ℃, the tower reactor temperature is 100～150 ℃;
It is 80～250 that described essence is divided the theoretical plate number of tower E, and reflux ratio is 10～40, feed entrance point be upper the 10th～245, control tower top temperature be 110～130 ℃, the tower reactor temperature is 110～150 ℃;
The theoretical plate number of described extractive distillation column F is 20～80, and reflux ratio is 1～20, feed entrance point be upper the 5th～75, the mass ratio of extraction agent and charging is 1～25, control tower top temperature be 110～130 ℃, the tower reactor temperature is 150～200 ℃;
The theoretical plate number of described 1-octene knockout tower G is 10～60, and reflux ratio is 1～10, feed entrance point be upper the 3rd～55, control cat head be 120～125 ℃, the tower reactor temperature is 200～210 ℃.
Compared with prior art, the present invention is intended to contain separating-purifying 1-octene carbon hydrocarbon (oxygen) mixture stream passes of 1-octene from industry, produce 1-octene product, produce the method such as 1-octene compares with oligomerisation and wax cracking, the method can contain hydrocarbon (oxygen) logistics of 1-octene directly separating-purifying from existing industry and realize, technical process is simple, has obvious production cost advantage.
Description of drawings
Fig. 1 be the present invention a kind of from carbon hydrocarbon oxygen mixture the process flow sheet of the method for purification 1-octene.
Wherein: A is that raw material pre-separation unit, B are that azeotropy rectification column, C are that entrainer recovery tower, D are that extractive distillation column, G are 1-octene knockout tower for essence minute tower 1, E for essence minute tower 2, F;
1 is that hydrocarbon (oxygen) mixture material logistics, 2 is C
8-lighting end logistics, 3 is C
8Cut logistics, 4 is C
8+ last running logistics, 5 is that entrainer logistics, 6 is C
8Hydrocarbon and entrainer logistics, 7 are that oxide-rich logistics, 8 is the C of oxide-free for rich entrainer logistics, 9
8Hydrocarbon stream, 10 is that rectifying tower D overhead stream, 11 is that the smart tower D tower reactor logistics, 12 that divides is that the smart tower E overhead stream, 13 that divides is that the smart tower E tower reactor logistics, 14 that divides is that extracting rectifying cat head logistics, 15 is that extracting rectifying tower reactor logistics, 16 is that 1-octene product stream, 17 is that regenerating extracting agent logistics, 18 is fresh extraction agent.
Embodiment
The present invention is described in detail below in conjunction with the drawings and specific embodiments.
Embodiment 1
Obtain C after hydrocarbon (oxygen) mixture material logistics 1 process pre-separation unit A double tower pre-separation
8Cut logistics 3 (composition sees Table 1), C
8-lighting end logistics 2, C
8+ last running logistics 4, wherein C
8Cut logistics 3 enters azeotropy rectification column B, and theoretical plate number is 20, feed entrance point be upper 10, reflux ratio is 2.6, control tower top temperature be 73～75 ℃, the tower reactor temperature is 121～123 ℃, overhead extraction entrainer and C
8Hydrocarbon stream 6 enters entrainer recovery tower C, theoretical plate number is 25, reflux ratio is 1, feed entrance point be upper 11, the control tower top temperature is 61～64 ℃, and tower reactor is 113～117 ℃, the rich entrainer logistics 8 of overhead extraction, the phase splitter circulation of azeotropic distillation column overhead, the C of tower reactor extraction oxide-free are returned in this logistics
8Hydrocarbon stream 9 enters essence minute tower D, theoretical plate number is 150, reflux ratio is 30, feed entrance point be upper 75, control tower top temperature be 105～108 ℃, the tower reactor temperature is 122～125 ℃, the cut logistics 10 that the overhead extraction boiling point is lower than 1-octene, minute tower D tower reactor logistics 11 of tower reactor extraction essence enters essence minute tower E, and theoretical plate number is 150, and reflux ratio is 25, feed entrance point be upper the 75th, the control tower top temperature is 119～122 ℃, and the tower reactor temperature is 126～127 ℃, the cut logistics 13 that tower reactor extraction boiling point is higher than 1-octene, an overhead extraction essence minute tower E overhead stream 12 enters extractive distillation column F, theoretical plate number is 50, and reflux ratio is 8, feed entrance point be upper the 25th, the mass ratio of extraction agent and charging is 15, the control tower top temperature is 120～121 ℃, and the tower reactor temperature is 174～177 ℃, and cat head obtains C
8Hydrocarbon stream 14, be rich in one or more components in positive structure, isoparaffin, internal olefin, cycloolefin, branched-chain alkene, the aromatic hydrocarbons in this logistics, tower reactor extraction extracting rectifying tower reactor logistics 15 enters 1-octene knockout tower G, theoretical plate number is 30, reflux ratio is 3, feed entrance point be upper the 15th, the control cat head is 120～120.5 ℃, the tower reactor temperature is 203.5～204.5 ℃, overhead extraction 1-octene logistics 16, the extractant stream 17 of tower reactor extraction regeneration is returned extractive distillation column F top with fresh extraction agent 18 and is recycled.Separating resulting table 1 under the aforesaid operations condition.
Each logistics analysis data among table 1 embodiment 1
| Logistics | The 1-octene | Fat alkane | Branched-chain alkene | Internal olefin | Virtue/cyclic hydrocarbon | Oxide compound | Other |
| 3 | 33.79 | 11.74 | 22.28 | 3.58 | 11.27 | 5.42 | 11.92 |
| 5 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 88.00 | 0.00 |
| 6 | 32.10 | 10.31 | 23.21 | 3.43 | 10.16 | 8.68 | 11.84 |
| 7 | 0.04 | 18.81 | 0.01 | 0.01 | 7.71 | 71.27 | 2.16 |
| 8 | 1.61 | 2.22 | 20.76 | 0.47 | 0.21 | 64.06 | 8.36 |
| 9 | 36.13 | 11.38 | 23.54 | 3.82 | 11.48 | 1.36 | 12.30 |
| 10 | 4.00 | 10.19 | 48.81 | 1.04 | 19.46 | 1.16 | 15.34 |
| 11 | 62.61 | 12.36 | 2.71 | 6.11 | 4.90 | 1.52 | 9.80 |
| 12 | 92.73 | 0.38 | 4.02 | 1.88 | 0.01 | 0.95 | 0.03 |
| 13 | 0.50 | 37.07 | 0.00 | 14.82 | 14.98 | 2.70 | 29.93 |
| 14 | 80.44 | 1.58 | 14.20 | 2.53 | 0.02 | 0.05 | 0.00 |
| 15 | 4.28 | 0.00 | 0.04 | 0.07 | 0.00 | 0.09 | 0.00 |
| 16 | 97.88 | 0.00 | 0.84 | 1.09 | 0.00 | 0.17 | 0.02 |
| 17 | 0.01 | 0.00 | 0.00 | 0.00 | 0.00 | 0.09 | 0.00 |
| 18 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 |
。
Embodiment 2
Obtain C after hydrocarbon (oxygen) mixture material logistics 1 process double tower pre-separation
8Cut logistics 3 (composition sees Table 2), C
8Cut logistics 3 enters azeotropy rectification column B, and theoretical plate number is 10, feed entrance point be upper 5, reflux ratio is 4, control tower top temperature be 73～76 ℃, the tower reactor temperature is 125～127 ℃, overhead extraction C
8Hydrocarbon and entrainer logistics 6 enter entrainer recovery tower C, theoretical plate number is 10, reflux ratio is 10, feed entrance point be upper 5, the control tower top temperature is 60～62 ℃, and tower reactor is 114～116 ℃, the rich entrainer logistics 8 of overhead extraction, the phase splitter circulation of azeotropic distillation column overhead, the C of tower reactor extraction oxide-free are returned in this logistics
8Hydrocarbon stream 9 enters essence minute tower D, theoretical plate number is 80, reflux ratio is 40, feed entrance point be upper 40, the control tower top temperature is 107～109 ℃, the tower reactor temperature is 121～124 ℃, the cut logistics that the overhead extraction boiling point is lower than 1-octene is rectifying tower D overhead stream 10, minute tower D tower reactor logistics 11 of tower reactor extraction essence enters essence minute tower E, and theoretical plate number is 80, and reflux ratio is 40, feed entrance point be upper the 40th, the control tower top temperature is 119～121 ℃, and the tower reactor temperature is 124～126 ℃, the i.e. essence minute tower E tower reactor logistics 13 of cut logistics that tower reactor extraction boiling point is higher than 1-octene, an overhead extraction essence minute tower E overhead stream 12 enters extractive distillation column F, theoretical plate number is 20, and reflux ratio is 15, feed entrance point be upper the 10th, the mass ratio of extraction agent and charging is 15, the control tower top temperature is 120～122 ℃, and the tower reactor temperature is 185～188 ℃, and cat head obtains C
8Hydrocarbon stream is extracting rectifying cat head logistics 14, be rich in one or more components in positive structure, isoparaffin, internal olefin, cycloolefin, branched-chain alkene, the aromatic hydrocarbons in this logistics, tower reactor extraction extracting rectifying tower reactor logistics 15 enters 1-octene knockout tower G, theoretical plate number is 10, reflux ratio is 15, feed entrance point be upper the 6th, the control cat head is 119.5～120.5 ℃, the tower reactor temperature is 203.5～204.5 ℃, overhead extraction 1-octene logistics 16, tower reactor extraction regenerating extracting agent logistics 17 is returned extractive distillation column F top with fresh extraction agent 18 and is recycled.Separating resulting sees Table 2 under these conditions.
Each logistics analysis data among table 2 embodiment 2
| Logistics | The 1-octene | Fat alkane | Branched-chain alkene | Internal olefin | Virtue/cyclic hydrocarbon | Oxide compound | Other |
| 3 | 33.79 | 11.74 | 22.28 | 3.58 | 11.27 | 5.42 | 11.92 |
| 5 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 88.00 | 0.00 |
| 6 | 30.70 | 9.95 | 24.73 | 3.30 | 10.08 | 8.56 | 12.42 |
| 7 | 0.12 | 18.23 | 0.04 | 0.02 | 1.87 | 76.71 | 2.48 |
| 8 | 0.43 | 1.97 | 31.73 | 0.39 | 0.23 | 50.10 | 13.37 |
| 9 | 36.07 | 11.36 | 23.49 | 3.81 | 11.82 | 1.19 | 12.25 |
| 10 | 17.60 | 8.66 | 41.79 | 0.92 | 17.15 | 0.89 | 13.00 |
| 11 | 57.00 | 14.43 | 2.76 | 7.09 | 5.79 | 1.54 | 11.40 |
| 12 | 91.47 | 0.75 | 5.81 | 0.81 | 0.05 | 0.97 | 0.15 |
| 13 | 26.78 | 26.42 | 0.09 | 12.59 | 10.82 | 2.03 | 21.26 |
| 14 | 83.91 | 1.86 | 12.30 | 0.88 | 0.04 | 0.03 | 0.00 |
| 15 | 2.08 | 0.00 | 0.03 | 0.02 | 0.00 | 0.06 | 0.01 |
| 16 | 97.27 | 0.01 | 1.40 | 0.67 | 0.03 | 0.42 | 0.20 |
| 17 | 0.05 | 0.00 | 0.00 | 0.00 | 0.00 | 0.05 | 0.00 |
| 18 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 |
。
Embodiment 3
Hydrocarbon (oxygen) mixture material logistics 1 obtains C after separating through single next door tower
8Logistics 3 (composition sees Table 3), C
8Cut logistics 3 enters azeotropy rectification column B, and theoretical plate number is 50, feed entrance point be upper 25, reflux ratio is 2.6, control tower top temperature be 73～75 ℃, the tower reactor temperature is 108～111 ℃, tower reactor extraction oxide-rich logistics 7, overhead extraction C
8Hydrocarbon and entrainer logistics 6 enter entrainer recovery tower C, theoretical plate number is 50, reflux ratio is 0.5, feed entrance point be upper 25, the control tower top temperature is 58～59 ℃, and tower reactor is 113～115 ℃, the rich entrainer logistics 8 of overhead extraction, the phase splitter circulation of azeotropic distillation column overhead, the C of tower reactor extraction oxide-free are returned in this logistics
8Hydrocarbon stream 9 enters essence minute tower D, theoretical plate number is 250, reflux ratio is 15, feed entrance point be upper 125, the control tower top temperature is 104～106 ℃, the tower reactor temperature is 123～125 ℃, the cut logistics that the overhead extraction boiling point is lower than 1-octene is rectifying tower D overhead stream 10, tower reactor obtains the 1-octene and a cut logistics i.e. essence minute tower D tower reactor logistics 11 higher than 1-octene boiling point enters essence minute tower E, and theoretical plate number is 250, and reflux ratio is 15, feed entrance point be upper the 125th, the control tower top temperature is 119～121 ℃, and the tower reactor temperature is 126～127 ℃, the i.e. essence minute tower E tower reactor logistics 13 of cut logistics that tower reactor extraction boiling point is higher than 1-octene, the rich 1-octene of an overhead extraction logistics i.e. essence minute tower E overhead stream 12 enters extractive distillation column F, theoretical plate number is 80, and reflux ratio is 1, feed entrance point be upper the 30th, the mass ratio of extraction agent and charging is 15, the control tower top temperature is 120～122 ℃, and the tower reactor temperature is 177～180 ℃, and cat head obtains C
8Hydrocarbon stream is extracting rectifying cat head logistics 14, be rich in one or more components in positive structure, isoparaffin, internal olefin, cycloolefin, branched-chain alkene, the aromatic hydrocarbons in this logistics, tower reactor extraction extraction agent and the logistics of 1-octene mixed solution are that extracting rectifying tower reactor logistics 15 enters 1-octene knockout tower G, theoretical plate number is 60, reflux ratio is 2, feed entrance point be upper the 30th, control cat head be 120～121 ℃, the tower reactor temperature is 203.5～204.5 ℃, overhead extraction 1-octene logistics 16.Tower reactor extraction regenerating extracting agent logistics 17 is returned extractive distillation column F top with fresh extraction agent 18 and is recycled.Separating resulting sees Table 3 under these conditions.
Each logistics analysis data among table 3 embodiment 3
| Logistics | The 1-octene | Fat alkane | Branched-chain alkene | Internal olefin | Virtue/cyclic hydrocarbon | Oxide compound | Other |
| 3 | 33.79 | 11.74 | 22.28 | 3.58 | 11.27 | 5.42 | 11.92 |
| 5 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 88.00 | 0.00 |
| 6 | 32.20 | 9.53 | 24.06 | 2.74 | 9.17 | 10.79 | 11.21 |
| 7 | 2.87 | 20.58 | 0.11 | 13.40 | 34.76 | 11.16 | 17.12 |
| 8 | 1.25 | 2.47 | 24.95 | 0.49 | 3.28 | 55.92 | 9.16 |
| 9 | 36.64 | 10.54 | 23.93 | 3.06 | 10.01 | 4.31 | 11.51 |
| 10 | 11.48 | 9.68 | 43.67 | 0.96 | 18.89 | 1.12 | 14.20 |
| 11 | 61.04 | 11.37 | 4.78 | 5.10 | 1.40 | 7.41 | 8.90 |
| 12 | 89.57 | 0.92 | 7.56 | 1.02 | 0.01 | 0.91 | 0.02 |
| 13 | 12.12 | 29.29 | 0.00 | 12.10 | 3.80 | 18.55 | 24.14 |
| 14 | 66.96 | 3.23 | 22.90 | 1.25 | 0.02 | 0.02 | 0.00 |
| 15 | 3.47 | 0.00 | 0.05 | 0.03 | 0.00 | 0.08 | 0.00 |
| 16 | 97.78 | 0.00 | 1.31 | 0.71 | 0.00 | 0.17 | 0.01 |
| 17 | 0.03 | 0.00 | 0.00 | 0.00 | 0.00 | 0.07 | 0.00 |
| 18 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 |
。
Embodiment 4
According to flow process as shown in Figure 1, change the composition of hydrocarbon (oxygen) mixture material logistics 1, feed stream 1 obtains C after the next door tower separates
8Cut logistics 3 (composition sees Table 4), C
8Cut logistics 3 enters azeotropy rectification column B, and theoretical plate number is 20, feed entrance point be upper 10, reflux ratio is 2.6, and the control tower top temperature is 73～75 ℃, and the tower reactor temperature is 115～117 ℃, tower reactor extraction oxide-rich logistics 7, the C of overhead extraction oxide-free
8Hydrocarbon stream 6 enters entrainer recovery tower C, theoretical plate number is 25, reflux ratio is 1, feed entrance point be upper 11, the control tower top temperature is 54～55 ℃, tower reactor is 112～113 ℃, the rich entrainer logistics 8 of overhead extraction, the phase splitter circulation of azeotropic distillation column overhead is returned in this logistics, tower reactor extraction logistics 9 enters essence minute tower D, theoretical plate number is 200, reflux ratio is 30, feed entrance point be upper 100, the control tower top temperature is 103～105 ℃, the tower reactor temperature is 121～123 ℃, the cut logistics that the overhead extraction boiling point is lower than 1-octene is rectifying tower D overhead stream 10, tower reactor obtains the 1-octene and a cut logistics i.e. essence minute tower D tower reactor logistics 11 higher than 1-octene boiling point enters essence minute tower E, theoretical plate number is 200, reflux ratio is 30, feed entrance point be upper the 100th, the control tower top temperature is 119～121 ℃, and the tower reactor temperature is 122～123 ℃, the i.e. essence minute tower E tower reactor logistics 13 of cut logistics that tower reactor extraction boiling point is higher than 1-octene, the rich 1-octene of an overhead extraction logistics i.e. essence minute tower E overhead stream 12 enters extractive distillation column F, theoretical plate number is 50, and reflux ratio is 3, feed entrance point be upper the 25th, the mass ratio of extraction agent and charging is 15, the control tower top temperature is 120～121 ℃, and the tower reactor temperature is 155～160 ℃, and cat head obtains C
8Hydrocarbon stream is extracting rectifying cat head logistics 14, be rich in positive structure in this logistics, isoparaffin, internal olefin, cycloolefin, branched-chain alkene, one or more components in the aromatic hydrocarbons, tower reactor extraction extraction agent and the logistics of 1-octene mixed solution are that extracting rectifying tower reactor logistics 15 enters 1-octene knockout tower G, theoretical plate number is 30, reflux ratio is 3, feed entrance point be upper the 15th, the control cat head is 120.～121 ℃, the tower reactor temperature is 203～204 ℃, overhead extraction 1-octene logistics 16, tower reactor extraction regenerating extracting agent logistics 17 is returned extractive distillation column F top with fresh extraction agent 18 and is recycled.Separating resulting sees Table 4 under these conditions.
Each logistics analysis data among table 4 embodiment 4
| Logistics | The 1-octene | Fat alkane | Branched-chain alkene | Internal olefin | Virtue/cyclic hydrocarbon | Oxide compound | Other |
| 3 | 6.89 | 16.61 | 31.51 | 5.06 | 15.94 | 7.14 | 16.85 |
| 5 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 88.00 | 0.00 |
| 6 | 6.62 | 14.68 | 34.86 | 4.89 | 15.15 | 6.71 | 16.87 |
| 7 | 0.00 | 17.87 | 0.00 | 0.00 | 0.20 | 80.97 | 0.22 |
| 8 | 0.09 | 2.05 | 38.72 | 0.42 | 0.15 | 48.01 | 8.88 |
| 9 | 7.59 | 16.56 | 34.28 | 5.56 | 17.38 | 0.58 | 18.05 |
| 10 | 0.10 | 10.52 | 51.90 | 1.04 | 20.38 | 0.66 | 15.41 |
| 11 | 21.75 | 27.97 | 1.01 | 14.08 | 11.71 | 0.43 | 23.04 |
| 12 | 93.01 | 0.33 | 5.13 | 1.53 | 0.00 | 0.00 | 0.00 |
| 13 | 4.26 | 34.75 | 0.00 | 17.16 | 14.58 | 0.54 | 28.70 |
| 14 | 67.47 | 1.99 | 27.67 | 2.33 | 0.01 | 0.00 | 0.00 |
| 15 | 3.41 | 0.00 | 0.02 | 0.05 | 0.00 | 0.00 | 0.00 |
| 16 | 98.00 | 0.00 | 0.62 | 1.37 | 0.00 | 0.00 | 0.00 |
| 17 | 0.10 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 |
| 18 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 |
。
Embodiment 5
According to flow process as shown in Figure 1, change the composition of hydrocarbon (oxygen) mixture material logistics 1, feed stream 1 obtains C after the next door tower separates
8Cut logistics 3 (composition sees Table 5), each tower operational condition is identical with example 4, and separating resulting sees Table 5.
Each logistics analysis data among table 5 embodiment 5
| Logistics | The 1-octene | Fat alkane | Branched-chain alkene | Internal olefin | Virtue/cyclic hydrocarbon | Oxide compound | Other |
| 3 | 89.69 | 1.83 | 3.47 | 0.56 | 1.76 | 0.84 | 1.86 |
| 5 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 88.00 | 0.00 |
| 6 | 77.39 | 1.47 | 5.01 | 0.49 | 1.49 | 11.99 | 1.76 |
| 7 | 0.00 | 27.54 | 0.00 | 0.00 | 0.00 | 68.65 | 0.00 |
| 8 | 7.43 | 0.39 | 13.50 | 0.09 | 0.04 | 74.64 | 1.32 |
| 9 | 90.19 | 1.67 | 3.46 | 0.56 | 1.75 | 0.53 | 1.84 |
| 10 | 40.22 | 5.64 | 18.51 | 0.97 | 18.33 | 1.90 | 14.43 |
| 11 | 94.03 | 1.36 | 2.30 | 0.53 | 0.48 | 0.43 | 0.88 |
| 12 | 96.87 | 0.36 | 2.62 | 0.01 | 0.04 | 0.10 | 0.00 |
| 13 | 73.52 | 8.63 | 0.00 | 4.28 | 3.62 | 2.76 | 7.18 |
| 14 | 88.67 | 1.87 | 7.98 | 0.01 | 0.18 | 0.02 | 0.00 |
| 15 | 9.69 | 0.00 | 0.13 | 0.00 | 0.00 | 0.02 | 0.00 |
| 16 | 98.55 | 0.01 | 1.38 | 0.01 | 0.01 | 0.04 | 0.00 |
| 17 | 0.08 | 0.00 | 0.00 | 0.00 | 0.00 | 0.02 | 0.00 |
| 18 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 |
。
Embodiment 6
A kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, described hydrocarbon (oxygen) mixture material is that the carbon number range that contains the 1-octene is C
5～C
20Hydrocarbon and carbon number range be C
2～C
20The mixture of oxygenatedchemicals, wherein same carbon number hydrocarbon compounds comprises positive isoparaffin, positive isomeric olefine, internal olefin, cycloolefin, aromatic ring hydrocarbon, same carbon number oxygenatedchemicals comprises one or more of alcohol, aldehyde, ketone, acid, ester compound.Described method may further comprise the steps:
(a) raw material pre-separation A
Hydrocarbon (oxygen) mixture material logistics 1 that contains the 1-octene enters the pre-separation unit, and purpose is to remove that most of carbon number is higher than C in the raw mix
8Component and most of carbon number be lower than C
8Component, this unit is by two (many) towers combine operationss, or adopts the method for a next door tower to finish, and after the pre-separation, feed stream 1 is divided into C
8-lighting end logistics 2, C
8Cut logistics 3 and C
8+ last running logistics 4, gained C
8The cut logistics is except C
8Outside the hydrocarbon, also have hydrocarbon and the oxide compound of other carbon number of part;
(b) azeotropy rectification column B
C
8Cut logistics 3 enters azeotropy rectification column B, removes C
8Oxygenatedchemicals in the logistics.The used entrainer of this tower is aqueous ethanolic solution.Be 10 in theoretical stage number, feed entrance point be upper 3, reflux ratio is 0.5, tower top temperature is 60～65 ℃, and the tower reactor temperature is that hydrocarbon and entrainer are steamed cat head with the azeotrope form under 110～115 ℃ of conditions, in the cat head phase splitter, be divided into the profit two-phase, the oil phase flow C of rich hydrocarbon
8Hydrocarbon and entrainer logistics 6 are as the extraction of overhead extraction liquid, and lower floor's water returns the rectifying tower top circulation; Tower reactor obtains being rich in oxygen compound logistics 7;
(c) entrainer recovery tower C
C
8Hydrocarbon and entrainer logistics 6 enter entrainer recovery tower C, a small amount of entrainer of carrying secretly in the returned logistics.Be 10 in theoretical stage number, reflux ratio is 0.5, feed entrance point be upper 3, the control tower top temperature is 50～55 ℃, and tower reactor is under 100～110 ℃ of conditions, and cat head obtains rich entrainer logistics 8, the circulation of azeotropic distillation column overhead phase splitter is returned in this logistics, and the tower reactor extraction does not contain the C of oxygenatedchemicals
8Hydrocarbon stream 9;
(d) essence minute tower D
The C that does not contain oxygenatedchemicals
8Hydrocarbon stream 9 enters essence minute tower D, and this tower is the operation of high tray-number high reflux ratio, and purpose is that the logistics mid-boiling point component lower than 1-octene removed in maximization.It is 80 in theoretical stage number, reflux ratio is 10, feed entrance point be upper 10, the control tower top temperature is 80～90 ℃, the tower reactor temperature is under 100～110 ℃ of conditions, the cut logistics 10 lower than 1-octene of cat head maximization extraction boiling point, tower reactor obtains 1-octene and the cut logistics 11 higher than 1-octene boiling point.
(e) essence minute tower E
Logistics 11 enters essence minute tower E, and this tower is the operation of high tray-number high reflux ratio, is used for maximization and removes the logistics mid-boiling point component higher than 1-octene.It is 80 in theoretical stage number, reflux ratio is 10, feed entrance point be upper the 10th, tower top temperature is 110～115 ℃, the tower reactor temperature is under 110～115 ℃ of conditions, the rich 1-octene of overhead extraction logistics 12,1-octene concentration reaches about 90% in the logistics, except the 1-octene, and the component that also has a small amount of boiling point and 1-octene very to approach, even these components still can't be removed under high critical operation condition, the cut logistics 13 that tower reactor extraction boiling point is higher than 1-octene.
(f) extractive distillation column F
Logistics 12 enters extractive distillation column F, and used extraction agent is ethylene glycol.Be 20 in theoretical stage number, reflux ratio is 1, feed entrance point be upper the 5th, the mass ratio of extraction agent and charging is 1, tower top temperature is 110～115 ℃, the tower reactor temperature is that cat head obtains C under 150～160 ℃ of conditions
8Hydrocarbon stream 14 is rich at least a or various ingredients in positive isoparaffin, internal olefin, cycloolefin, branched-chain alkene, the aromatic hydrocarbons in this logistics, tower reactor extraction extraction agent and 1-octene mixed solution logistics 15;
(g) 1-octene knockout tower
Logistics 15 enters 1-octene knockout tower G, and the purpose of this tower is for separating 1-octene product, simultaneously with extractant regeneration.Be 10 in theoretical stage number, reflux ratio is 1, feed entrance point be upper the 3rd, cat head is 120～125 ℃, the tower reactor temperature is under 200～210 ℃ of conditions.Cat head obtains 1-octene logistics 16, and the extractant stream 17 of tower reactor extraction regeneration is returned the circulation of extractive distillation column top.
Embodiment 7
A kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, described hydrocarbon (oxygen) mixture material is the feed stream that Fischer-Tropsch synthesis method obtains.Described method may further comprise the steps:
(a) raw material pre-separation A
Hydrocarbon (oxygen) mixture material logistics 1 that contains the 1-octene enters the pre-separation unit, and purpose is to remove that most of carbon number is higher than C in the raw mix
8Component and most of carbon number be lower than C
8Component, this unit is by two (many) towers combine operationss, or adopts the method for a next door tower to finish, and after the pre-separation, feed stream 1 is divided into C
8-lighting end logistics 2, C
8Cut logistics 3 and C
8+ last running logistics 4, gained C
8The cut logistics is except C
8Outside the hydrocarbon, also have hydrocarbon and the oxide compound of other carbon number of part;
(b) azeotropy rectification column B
C
8Cut logistics 3 enters azeotropy rectification column B, removes C
8Oxygenatedchemicals in the logistics.The used entrainer of this tower is the aqueous solution of alcohol, ketone, ester, ethers organic oxygen compound, one or more in the low carbon alcohol solutions such as preferred alcohol, Virahol, n-propyl alcohol, isopropylcarbinol, the trimethyl carbinol, propyl carbinol.It is 50 in theoretical stage number, feed entrance point be upper 45, reflux ratio is 10, tower top temperature is 90 ℃, the tower reactor temperature is that hydrocarbon and entrainer are steamed cat head with the azeotrope form under 140～150 ℃ of conditions, is divided into the profit two-phase in the cat head phase splitter, the oil phase logistics 6 of rich hydrocarbon is as the extraction of overhead extraction liquid, and lower floor's water returns the rectifying tower top circulation; Tower reactor obtains being rich in oxygen compound logistics 7;
(c) entrainer recovery tower C
Logistics 6 enters entrainer recovery tower C, a small amount of entrainer of carrying secretly in the returned logistics.Be 50 in theoretical stage number, reflux ratio is 10, feed entrance point be upper 45, the control tower top temperature is 90 ℃, and tower reactor is under 140～150 ℃ of conditions, and cat head obtains rich entrainer logistics 8, the circulation of azeotropic distillation column overhead phase splitter is returned in this logistics, and the tower reactor extraction does not contain the C of oxygenatedchemicals
8Hydrocarbon stream 9;
(d) essence minute tower D
Logistics 9 enters essence minute tower D, and this tower is the operation of high tray-number high reflux ratio, and purpose is that the logistics mid-boiling point component lower than 1-octene removed in maximization.It is 250 in theoretical stage number, reflux ratio is 40, feed entrance point be upper 245, control tower top temperature be 120 ℃, the tower reactor temperature is under 140～150 ℃ of conditions, from the cut logistics higher than 1-octene of tower reactor extraction boiling point, the cut logistics that overhead extraction 1-octene and boiling point are lower than 1-octene, overhead stream enter essence minute tower E, from the overhead extraction boiling point logistics cut lower than 1-octene, the logistics of the rich 1-octene of tower reactor extraction, the tower reactor logistics enters the extractive distillation column F of step (f).
(e) essence minute tower E
An essence minute tower D tower reactor logistics 11 enters essence minute tower E, and this tower is the operation of high tray-number high reflux ratio, is used for maximization and removes the logistics mid-boiling point component higher than 1-octene.It is 250 in theoretical stage number, reflux ratio is 40, feed entrance point be upper the 245th, tower top temperature is 120～130 ℃, the tower reactor temperature is under 140～150 ℃ of conditions, the rich 1-octene of overhead extraction logistics 12,1-octene concentration reaches about 90% in the logistics, except the 1-octene, and the component that also has a small amount of boiling point and 1-octene very to approach, even these components still can't be removed under high critical operation condition, the cut logistics 13 that tower reactor extraction boiling point is higher than 1-octene.
(f) extractive distillation column F
Logistics 12 enters extractive distillation column F, and used extraction agent is the mixture of ethylene glycol, benzene hexanone, 1-Methyl-2-Pyrrolidone, methyl-sulphoxide, hexyl acetate.Be 80 in theoretical stage number, reflux ratio is 20, feed entrance point be upper the 75th, the mass ratio of extraction agent and charging is 25, tower top temperature is 120～130 ℃, the tower reactor temperature is that cat head obtains C under 190～200 ℃ of conditions
8Hydrocarbon stream 14 is rich at least a or various ingredients in positive isoparaffin, internal olefin, cycloolefin, branched-chain alkene, the aromatic hydrocarbons in this logistics, tower reactor extraction extraction agent and 1-octene mixed solution logistics 15;
(g) 1-octene knockout tower
Logistics 15 enters 1-octene knockout tower G, and the purpose of this tower is for separating 1-octene product, simultaneously with extractant regeneration.Be 60 in theoretical stage number, reflux ratio is 10, feed entrance point be upper the 55th, cat head is 120～125 ℃, the tower reactor temperature is under 200～210 ℃ of conditions.Cat head obtains 1-octene logistics 16, and the extractant stream 17 of tower reactor extraction regeneration is returned the circulation of extractive distillation column top.
Claims (10)
1. the method for a separating-purifying 1-octene from hydrocarbon (oxygen) mixture is characterized in that, said method comprising the steps of:
(a) hydrocarbon (oxygen) mixture material logistics (1) is entered pre-separation unit (A), obtain C
8-lighting end logistics (2), C
8Cut logistics (3) and C
8+ last running logistics (4);
(b) C
8Cut logistics (3) enters azeotropy rectification column (B), and overhead vapours is through being divided into up and down two-phase in phase splitter after the condensation, and the oil phase logistics of rich hydrocarbon is C
8Hydrocarbon and entrainer logistics (6) extraction, trim the top of column is returned in the logistics of entrainer phase, tower reactor extraction oxide-rich logistics (7);
(c) C
8Hydrocarbon and entrainer logistics (6) enter entrainer recovery tower (C), and the phase splitter circulation of azeotropic distillation column overhead, the C of tower reactor extraction oxide-free are returned in the rich entrainer logistics (8) of overhead extraction, this logistics
8Hydrocarbon stream (9);
(d) C of oxide-free
8Hydrocarbon stream (9) enters essence minute tower (D), the cut logistics that the overhead extraction boiling point is lower than 1-octene is rectifying tower D overhead stream (10), and tower reactor obtains 1-octene and the cut logistics i.e. essence minute tower D tower reactor logistics (11) higher than 1-octene boiling point;
(e) an essence minute tower D tower reactor logistics (11) enters essence minute tower (E), and the logistics of the rich 1-octene of overhead extraction i.e. essence minute tower E overhead stream (12), the i.e. essence minute tower E tower reactor logistics (13) of cut logistics that tower reactor extraction boiling point is higher than 1-octene;
(f) an essence minute tower E overhead stream (12) enters extractive distillation column (F), and cat head obtains C
8Hydrocarbon stream is extracting rectifying cat head logistics (14), be rich in one or more components in positive structure, isoparaffin, internal olefin, cycloolefin, branched-chain alkene, the aromatic hydrocarbons in this logistics, tower reactor extraction extraction agent and the logistics of 1-octene mixed solution are extracting rectifying tower reactor logistics (15);
(g) extracting rectifying tower reactor logistics (15) enters 1-octene knockout tower (G), cat head obtains 1-octene product stream (16), tower reactor extraction regenerating extracting agent logistics (17), this logistics are returned extractive distillation column (F) top and are recycled.
According to claim 1 a kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, it is characterized in that, described hydrocarbon (oxygen) mixture material logistics (1) is C for the carbon number range that contains the 1-octene
2～C
100Hydrocarbon and carbon number range be C
2～C
20The mixture of oxygenatedchemicals, wherein same carbon number hydrocarbon compounds comprises positive structure and isoparaffin, linear alpha-olefin, branched-chain alkene, internal olefin, cycloolefin, aromatic hydrocarbons, naphthenic hydrocarbon; Same carbon number oxygenatedchemicals comprises one or more of alcohol, aldehyde, ketone, acid, ester compound.
According to claim 1 a kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, it is characterized in that, described hydrocarbon (oxygen) mixture material logistics (1) comprises the stream thigh that contains the 1-octene that different industrial processes obtain, the stream thigh that contains the 1-octene that preferred Fischer-Tropsch synthesis method obtains.
According to claim 1 a kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, it is characterized in that, step (a) described pre-separation unit (A) is the above combined separation tower of two towers or two towers, or a kind of in the tower of single next door.
According to claim 1 a kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, it is characterized in that the described C of step (a)
8The 1-octene content is greater than 5wt% in the cut logistics (3).
According to claim 1 a kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, it is characterized in that, step (d) and (e) in essence divide tower (D) and essence minute tower (E) two towers also can be by following pattern serial operation: the C of oxide-free
8Hydrocarbon stream (9) enters essence minute tower (D), from the cut logistics higher than 1-octene of tower reactor extraction boiling point, the cut logistics that overhead extraction 1-octene and boiling point are lower than 1-octene, overhead stream enters essence minute tower (E), from the overhead extraction boiling point logistics cut lower than 1-octene, the logistics of the rich 1-octene of tower reactor extraction, the tower reactor logistics enters the extractive distillation column (F) of step (f).
According to claim 1 a kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, it is characterized in that, the used entrainer of the described azeotropy rectification column of step (b) (B) is the aqueous solution of alcohol, ketone, ester, ethers organic oxygen-containing compound.
According to claim 7 a kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, it is characterized in that, the preferred low carbon alcohol solution of entrainer that step (b) is used, alcohol comprises one or more in ethanol, Virahol, n-propyl alcohol, isopropylcarbinol, the trimethyl carbinol, the propyl carbinol.
According to claim 1 a kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, it is characterized in that, the used extraction agent of step (f) is one or more in ethylene glycol, benzene hexanone, 1-Methyl-2-Pyrrolidone, methyl-sulphoxide, the hexyl acetate.
According to claim 1 a kind of from hydrocarbon (oxygen) mixture the method for separating-purifying 1-octene, it is characterized in that, described azeotropy rectification column (B) theoretical plate number is 10～50, feed entrance point be upper 3～45, reflux ratio is 0.5～10, the control tower top temperature is 60～90 ℃, and the tower reactor temperature is 110～150 ℃;
The theoretical plate number of described entrainer recovery tower (C) is 10～50, and reflux ratio is 0.5～10, feed entrance point be upper 3～45, control tower top temperature be 50～90 ℃, tower reactor is 100～150 ℃;
It is 80～250 that described essence is divided the theoretical plate number of tower (D), and reflux ratio is 10～40, feed entrance point be upper 10～245, control tower top temperature be 80～120 ℃, the tower reactor temperature is 100～150 ℃;
It is 80～250 that described essence is divided the theoretical plate number of tower (E), and reflux ratio is 10～40, feed entrance point be upper the 10th～245, control tower top temperature be 110～130 ℃, the tower reactor temperature is 110～150 ℃;
The theoretical plate number of described extractive distillation column (F) is 20～80, reflux ratio is 1～20, feed entrance point be upper the 5th～75, the mass ratio of extraction agent and charging is 1～25, the control tower top temperature is 110～130 ℃, and the tower reactor temperature is 150～200 ℃;
The theoretical plate number of described 1-octene knockout tower (G) is 10～60, and reflux ratio is 1～10, feed entrance point be upper the 3rd～55, control cat head be 120～125 ℃, the tower reactor temperature is 200～210 ℃.
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