CN109627137A - A kind of separation method for coal base Fischer-Tropsch olefins - Google Patents
A kind of separation method for coal base Fischer-Tropsch olefins Download PDFInfo
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Abstract
The present invention relates to a kind of methods that alkene is separated from coal base F- T synthesis light fraction oil, comprising the following steps: (1) carries out depickling processing to Fischer-Tropsch light fraction oil raw material；(2) to depickling, treated that distillate adsorbs, and removes carbonyls.(3) treated that distillate enters lightness-removing column for depickling；Component by carbon number less than n is separated by lightness-removing column tower top, and tower bottom component enters weight-removing column；Component of the carbon number greater than n is isolated by weight-removing column tower bottom, and weight-removing column tower top separates the component that carbon number is n；(4) carbon number is that the component of n enters extractive distillation column, is inversely contacted with extractant, nonpolar alkane is separated by tower top, and extractant and target alkene are distillated by tower bottom into recovery tower；(5) target alkene is distillated by recycling tower top, and extractant is distillated by tower reactor, is recycled into extractive distillation column.Due to being the preparation of high carbon number holding, to prevent olefin cracking from all using vacuum distillation, the integrality of alkene structures ensure that.
Description
Technical field
The present invention relates to a kind of separation methods suitable for Fischer-Tropsch olefins, and in particular to one kind is divided from coal base Fischer-Tropsch alkane alkene
Method from alkene.
Background technique
Higher olefins are important and common organic petrochemical materials, can be used as detergent, oil dope, surfactant
And medicine intermediate etc., they are alternatively arranged as high-quality comonomer and produce high-grade polyolefin resin.
Existing alkene technology of preparing is divided into two classes: one is coal base routes, and one is petroleum path, (also known as ethylene is neat
Poly- method).Coal base route, which refers to, separates alkane from coal base light fraction oil, obtains alkene, common method has molecular sieve absorption
Technique and extraction rectification technique: petroleum path, which refers to, prepares alkene by ethylene oligomerization method.Existing preparation and separation method
In in place of Shortcomings, specific manifestation are as follows: (1) method that traditional coal base alkane, separation of olefins use molecular sieve absorption, by
The limitation of molecular sieve service life, need to periodically stop work and carry out regenerating molecular sieve, and the higher cost of equipment, continuous production is poor, production effect
Rate is low, while obtained alkene purity is lower.(2) extractant of the existing extraction rectification technique selected by it is low boiling point extraction
Agent can only separate C8 or less substance, and it is impossible to meet the requirements of C8 or more Fischer-Tropsch alkane, separation of olefins.(3) ethylene oligomerization method
Olefin carbon number obtained by route can only be from C4-C8, and can only produce even number carbon products, and product diversity is poor, and high production cost.
Patent CN102452888A discloses a kind of method that 1- hexene is separated from oil from Fischer-Tropsch synthesis.This method passes through
Cutting light oil fraction obtains C6 fraction, then removes organic oxygen-containing compound therein with the method for extracting rectifying；Then again
The alkane and alkene of this carbon number are separated with extraction fractional distillation；It is removed wherein with the method for reactive distillation under the effect of the catalyst again
Tertiary olefin；Finally 1- hexene is obtained with the method for precise distillation.Wherein separation of extractive distillation alkane and olefin process section
Extractant is the binary mixed solvent of one of ACN, NMP, DMF or CAN or NMP and water.Although this method can effectively from
Isolate 1- hexene in oil from Fischer-Tropsch synthesis, but related process energy consumption it is higher and there are equipment investment it is big etc. it is restricted because
Element, while its method can not obtain the alkene of high carbon number.
Patent CN102452886A elaborates a kind of method by purifying 1- octene in oil from Fischer-Tropsch synthesis.Its method
In using F- T synthesis light fraction oil as raw material, cut to obtain C8 fraction section by secondary fraction, then first use second alcohol and water group
At binary azeotropic agent using azeotropic distillation method removing it is therein acid and other oxygenatedchemicals；Pass through extracting rectifying again
Separation this fraction section alkane and alkene, obtain C8 alkene, this alkene be further purified by precise distillation, is met
The 1- octene product that polymer grade requires.The process equipment system complex and energy consumption is high, and the alkene of high carbon number can not be separated again.
Patent CN106966852A discloses the side of a kind of continuous extraction rectifying separation high-carbon n-alkane and normal olefine
Method high-carbon n-alkane and normal olefine mixture is added from the middle part of extractive distillation column, extractant phthalate
Compound is added from the top of extractive distillation column, extractive distillation column overhead extraction high-carbon n-alkane；From extractive distillation column tower bottom
The high-carbon normal olefine of extraction and the mixture of extractant are fed in the middle part of solvent recovery tower, solvent recovery tower overhead extraction high-carbon
Normal olefine, solvent recovery tower tower bottom produce extractant, and extractant is reused.Raw material used by its method is laboratory mould
Quasi- cooperation raw material, ingredient is only the mixture of alkene and alkane, and olefin(e) centent is no more than 50%, is a kind of ideal original
Material, this method are suitable only for obtaining high purity olefin under the ideal conditions.And material composition in actual production is much more complex,
And containing plurality of impurities, the raw material difficulty that obtain meeting this method requirement is very high, and this method can not be applied to coal base Fischer-Tropsch
In the olefin separation process for synthesizing light fraction oil, because the oxygenatedchemicals in alkene will affect the separation of alkane alkene, and meanwhile it is oxygen-containing
The presence of compound will affect the quality of product, and catalyst used in the synthesis process for downstream product has extremely strong
Toxicity, therefore more harsh requirement is just proposed for the technique of actual separation.
To solve problems of the prior art, it needs to propose a kind of with production cost is low, product purity is high, can give birth to
Produce the separation production method of the strong higher olefins of odd number carbon olefin, product diversity.
Summary of the invention
To solve the problems, such as that above method exists, the present invention provides a kind of separation method suitable for Fischer-Tropsch olefins, specifically
It is related to a kind of method that higher olefins are separated from coal base Fischer-Tropsch alkane alkene, it is specific as follows.
A method of alkene is separated from coal base F- T synthesis light fraction oil, which is characterized in that the carbon of target alkene
Counting is n, 8≤n≤18, specifically includes the following steps:
(1) depickling processing is carried out to Fischer-Tropsch light fraction oil raw material, alkane and alkene in depickling treated distillate
Content is not less than 98wt%, and oxygenates level is not higher than 2wt%, and acid value is not higher than 0.1；Alcohols material in oxygenatedchemicals
Content 40-60wt%, remaining is the impurity such as aldehyde, ketone, esters；
(2) the Fischer-Tropsch light fraction oil after depickling carries out the absorption of carbonyls, adsorbing medium 5A by chromatographic column
Molecular sieve, alkane and alkene contains 99wt% or more, oxygenates level 1wt% or less after adsorbing；In oxygenatedchemicals
Most oxygenatedchemicals are alcohol, and the content of carbonyls drops to 1ppm or less；It is preferred that alkane and alkene gross mass hundred
Divide than being 99.7wt%, oxygenatedchemicals mass percent is 0.3wt%, and wherein the oxygenatedchemicals overwhelming majority is alcohol, carbonyl
Compound is less than 1ppm through detection level.
(3) distillate after adsorption treatment enters lightness-removing column, and the component by carbon number less than n is separated by lightness-removing column tower top, tower
Bottom component enters weight-removing column；Component of the carbon number greater than n is isolated by weight-removing column tower bottom, and weight-removing column tower top separates the group that carbon number is n
Point, wherein hydrocarbon content is not less than 99.7wt%, remaining is oxygenatedchemicals；The oxygenatedchemicals overwhelming majority is alcohol, carbonyl compound
Object is less than 1ppm through detection level；
(4) carbon number is that the component of n enters extractive distillation column, is inversely contacted with extractant, nonpolar alkane is by tower top point
Out, extractant and target alkene are distillated by tower bottom into recovery tower, and target alkene is distillated by recycling tower top, and extractant is evaporated by tower reactor
Out, it is recycled into extractive distillation column；
Wherein, the alkene that extracting rectifying obtains is polymer grade product；Fischer-Tropsch light fraction oil be it is a kind of with carbon number distribution from
Light dydrocarbon is to the alkane alkene mixture as main component of carbon 18, and wherein alkene and alkane mass ratio are 2.5: 1~3.5: 1；Extraction
Agent is phthalate compound.Olefin product purity is lower than 1ppm, contains in 99.7wt% or more, carbonyl compound content
Oxygen compound total amount is lower than 10ppm.
Specifically,
N=8, extractant are repefral；Lightness-removing column operating parameter are as follows: 58 DEG C of bottom temperature, operating pressure
21.3kpa, the number of plates 65, feed entrance point 45, reflux ratio 4: 1；Weight-removing column operating parameter are as follows: 80 DEG C of bottom temperature, operation pressure
Power 21.3kpa, the number of plates 55, feed entrance point 35, reflux ratio 5: 1；Extractive distillation column operating parameter are as follows: 85 DEG C of bottom temperature,
Operating pressure 21.3kpa, the number of plates 40, feed entrance point 18, reflux ratio 5.5: 1；Extractant and material quality ratio are 5: 1；It returns
Receive tower operating parameter are as follows: 87 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 45, feed entrance point 23, reflux ratio 4.5:
1.For olefin product purity in 99.7wt% or more, oxygenates level is lower than 10ppm, and carbonyls is lower than 1ppm.
N=9, extractant are repefral.Lightness-removing column operating parameter are as follows: 85 DEG C of bottom temperature, operating pressure
21.3kpa, the number of plates 65, feed entrance point 45, reflux ratio 4: 1；Weight-removing column operating parameter are as follows: 104 DEG C of bottom temperature, operation pressure
Power 21.3kpa, the number of plates 55, feed entrance point 35, reflux ratio 5: 1；Extractive distillation column operating parameter are as follows: 109 DEG C of bottom temperature,
Operating pressure 21.3kpa, the number of plates 40, feed entrance point 18, reflux ratio 5.5: 1；Extractant and material quality ratio are 5: 1；It returns
Receive tower operating parameter are as follows: 101 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 45, feed entrance point 23, reflux ratio 4.5:
1 olefin product purity 99.7wt%, oxygenates level are lower than 10ppm.Wherein carbonyl compound content is lower than 1ppm.
N=10, extractant are repefral.Lightness-removing column operating parameter are as follows: 105 DEG C of bottom temperature, operation pressure
Power 21.3kpa, the number of plates 65, feed entrance point 45, reflux ratio 4: 1；Weight-removing column operating parameter are as follows: 125 DEG C of bottom temperature, operation
Pressure 21.3kpa, the number of plates 55, feed entrance point 35, reflux ratio 5: 1；Extractive distillation column operating parameter are as follows: bottom temperature 129
DEG C, operating pressure 21.3kpa, the number of plates 40, feed entrance point 18, reflux ratio 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 131 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 45, feed entrance point 23, reflux ratio is
4.5: 1 olefin product purity 99.7wt%, oxygenates level are lower than 10ppm.Wherein carbonyl compound content is lower than 1ppm.
N=11, extractant are the mixture of repefral and diethyl phthalate, molar ratio 1: 1.
Lightness-removing column operating parameter are as follows: 126 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 65, feed entrance point 45, reflux ratio 4:
1；Weight-removing column operating parameter are as follows: 146 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 55, feed entrance point 35, reflux ratio is
5:1；Extractive distillation column operating parameter are as follows: 151 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 40, feed entrance point 18 returns
Stream is than being 5.5: 1；Extractant and material quality ratio are 5: 1；Recovery tower operating parameter are as follows: 153 DEG C of bottom temperature, operating pressure
21.3kpa, the number of plates 45, feed entrance point 23, reflux ratio 4.5: 1.Olefin product purity 99.7wt%, oxygenates level
Lower than 10ppm.Wherein carbonyl compound content is lower than 1ppm.
N=12, extractant are diethyl phthalate, molar ratio 1: 1.Lightness-removing column operating parameter are as follows: bottom temperature
145 DEG C, operating pressure 21.3kpa, the number of plates 65, feed entrance point 45, reflux ratio 4: 1；Weight-removing column operating parameter are as follows: tower reactor temperature
166 DEG C, operating pressure 21.3kpa of degree, the number of plates 55, feed entrance point 35, reflux ratio 5: 1；Extractive distillation column operating parameter are as follows:
172 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 40, feed entrance point 18, reflux ratio 5.5: 1；Extractant and raw material
Mass ratio is 5: 1；Recovery tower operating parameter are as follows: 174 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 45, feed entrance point
23,4.5: 1 olefin product purity 99.7wt% of reflux ratio, oxygenates level are lower than 10ppm.Wherein carbonyls contains
Amount is lower than 1ppm.
N=13, extractant are diethyl phthalate.Lightness-removing column operating parameter are as follows: 96 DEG C of bottom temperature, operating pressure
1.33kpa, the number of plates 65, feed entrance point 45, reflux ratio 4: 1；Weight-removing column operating parameter are as follows: 115 DEG C of bottom temperature, operation pressure
Power 1.33kpa, the number of plates 55, feed entrance point 35, reflux ratio 5: 1；Extractive distillation column operating parameter are as follows: 118 DEG C of bottom temperature,
Operating pressure 1.33kpa, the number of plates 40, feed entrance point 18, reflux ratio 5.5: 1；Extractant and material quality ratio are 5: 1；It returns
Receive tower operating parameter are as follows: 120 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 45, feed entrance point 23, reflux ratio 4.5:
1.Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm.Wherein carbonyl compound content is lower than 1ppm.
N=14, extractant are dibutyl phthalate.Lightness-removing column operating parameter are as follows: 113 DEG C of bottom temperature, operation pressure
Power 1.33kpa, the number of plates 65, feed entrance point 45, reflux ratio 4: 1；Weight-removing column operating parameter are as follows: 128 DEG C of bottom temperature, operation
Pressure 1.33kpa, the number of plates 55, feed entrance point 35, reflux ratio 5: 1；Extractive distillation column operating parameter are as follows: bottom temperature 130
DEG C, operating pressure 1.33kpa, the number of plates 40, feed entrance point 18, reflux ratio 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 132 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 45, feed entrance point 23, reflux ratio is
4.5:1.Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm.Wherein carbonyl compound content is lower than
1ppm。
N=15, extractant are dioctyl phthalate.Lightness-removing column operating parameter are as follows: 131 DEG C of bottom temperature, operation pressure
Power 1.33kpa, the number of plates 65, feed entrance point 45, reflux ratio 4: 1；Weight-removing column operating parameter are as follows: 141 DEG C of bottom temperature, operation
Pressure 1.33kpa, the number of plates 55, feed entrance point 35, reflux ratio 5: 1；Extractive distillation column operating parameter are as follows: bottom temperature 144
DEG C, operating pressure 1.33kpa, the number of plates 40, feed entrance point 18, reflux ratio 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 146 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 45, feed entrance point 23, reflux ratio is
4.5:1.Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm.Wherein carbonyl compound content is lower than
1ppm。
N=16, extractant are dioctyl phthalate.Lightness-removing column operating parameter are as follows: 143 DEG C of bottom temperature, operation pressure
Power 1.33kpa, the number of plates 65, feed entrance point 45, reflux ratio 4: 1；Weight-removing column operating parameter are as follows: 153 DEG C of bottom temperature, operation
Pressure 1.33kpa, the number of plates 55, feed entrance point 35, reflux ratio 5: 1；Extractive distillation column operating parameter are as follows: bottom temperature 155
DEG C, operating pressure 1.33kpa, the number of plates 40, feed entrance point 18, reflux ratio 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 157 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 45, feed entrance point 23, reflux ratio is
4.5:1.Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm.Wherein carbonyl compound content is lower than
1ppm。
N=17, extractant are dioctyl phthalate.Lightness-removing column operating parameter are as follows: 156 DEG C of bottom temperature, operation pressure
Power 1.33kpa, the number of plates 65, feed entrance point 45, reflux ratio 4: 1；Weight-removing column operating parameter are as follows: 165 DEG C of bottom temperature, operation
Pressure 1.33kpa, the number of plates 55, feed entrance point 35, reflux ratio 5: 1；Extractive distillation column operating parameter are as follows: bottom temperature 167
DEG C, operating pressure 1.33kpa, the number of plates 40, feed entrance point 18, reflux ratio 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 169 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 45, feed entrance point 23, reflux ratio is
4.5:1.Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm.Wherein carbonyl compound content is lower than
1ppm。
N=18, extractant are dioctyl phthalate.Lightness-removing column operating parameter are as follows: 153 DEG C of bottom temperature, operation pressure
Power 0.67kpa, the number of plates 65, feed entrance point 45, reflux ratio 4: 1；Weight-removing column operating parameter are as follows: 170 DEG C of bottom temperature, operation
Pressure 0.67kpa, the number of plates 55, feed entrance point 35, reflux ratio 5: 1；Extractive distillation column operating parameter are as follows: bottom temperature 172
DEG C, operating pressure 0.67kpa, the number of plates 40, feed entrance point 18, reflux ratio 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 174 DEG C of bottom temperature, operating pressure 0.67kpa, the number of plates 45, feed entrance point 23, reflux ratio is
4.5:1.Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm.Wherein carbonyl compound content is lower than
1ppm。
In addition, this method further includes the steps that the product obtained to extracting rectifying carries out oxide removal processing.
Beneficial effect
1. method of the invention is particularly suitable for the separation process of coal base Fischer-Tropsch olefins, the combination of various process parameters with
The composition of raw material is closely related, is the mistake of adjustment by analysis, parameter to raw material, lab scale to the continuous adjustment and improvement of pilot scale
Journey, wherein distillate feedstock source is 1,200,000 tons/year of coal oil devices of chemical industry Co., Ltd, Inner Mongol gouy Thailand, at present should
Method has passed through 10 tonnes of pilot scales, will be used to be mass produced in next step.
2. method and process process of the invention is simple, low energy consumption, can obtain high carbon number holding, and the alkene obtained is poly-
Close grade, can directly as polymerized monomer, for country's high quality higher olefins production provide a kind of low energy consumption, low cost,
The strong production method of product diversity.
3. oxygenatedchemicals mainly influences sorbent life, if oxygenatedchemicals in oil product can be reduced to 0.5%wt with
Under, then sorbent life will increase by 70% (compared with the oil product of 2%wt oxygenatedchemicals).Polymer grade olefin product requirement is oxygen-containing
Compound amount is lower than 1ppm, and polymerization reaction does not otherwise occur.In method of the invention, adsorbing and removing carbonyl compound is carried out after depickling
Object is effectively guaranteed the continuity of absorbing process and the performance of subsequent olefin product.
4. the product that pair extracting rectifying obtains carries out the step of oxide removal processing, oxygenatedchemicals can be effectively reduced
Content, improve extracting rectifying extractant in process recovery utilization rate, avoid the excessive consumption of extractant, reduce production at
This, further increases the purity of product.
Detailed description of the invention
Fig. 1 alkene separation method schematic diagram of the present invention；
Specific embodiment
Fig. 1 is one schematic diagram of alkene separation method of the present invention, Fischer-Tropsch light fraction oil raw material (C8-C18 alkane alkene
Mixture) carry out depickling: first by distillate and suitable solution of potassium carbonate, (additional amount of potassium carbonate is 200mgK2CO3/100ml
Distillate；Mass fraction is that neutralization reactor 20%) is added under solution of potassium carbonate room temperature, is sufficiently stirred, after complete reaction, quiet
Set layering, by it is newborn mutually and water phase is transferred to standing phase separation tank, washed that (water filling volume ratio is, oily: water=3: 1), to go
Except extra lye, after washing, neutral distillate is sent into subsequent workshop section by stratification.Adsorption treatment is carried out after depickling.
Neutral distillate enters preheating furnace, enters back into the adsorption tower equipped with molecular sieve, carries out adsorbing separation to oxycompound
(adsorbent is 13x molecular sieve, and adsorbent and oily mass ratio are 1: 3).Operation temperature is 40 DEG C, pressure 0.5Mpa.
Distillate after adsorption treatment enters lightness-removing column, and Cn-1 and more light component are separated by tower top (assuming that target carbon number
Group is divided into Cn), tower bottom component (Cn, Cn+1 and more heavy constituent) enters weight-removing column；Cn+1 and more heavy constituent are separated by weight-removing column bottom
Out, weight-removing column top separates Cn component (target carbon number alkane alkene mixture)；Cn component enters extraction tower, inversely connects with polarity extracting agent
Touching, nonpolar alkane are separated by tower top, and extractant and alkene are distillated by tower bottom into recovery tower；Cn alkene is evaporated by recycling tower top
Out, extractant is distillated by tower reactor, is recycled into extraction tower.
The present invention uses distillate feedstock source for 1,200,000 tons/year of coal oils of Inner Mongol chemical industry Co., Ltd, gouy Thailand
Device, ingredient such as table 1.
1 distillate feedstock ingredient of table
Material composition such as table 2 in the distillate obtained after depickling.
2 depickling tails oil of table composition
| Number | Substance classes | Content/wt% |
| 1 | Alkane (positive structure/isoparaffin) | 23.9 |
| 2 | Alkene (positive structure/isomeric olefine) | 74.1 |
| 3 | Acids | -- |
| 4 | Other oxygenatedchemicals | 2 |
The distillate feedstock ingredient obtained after absorption such as table 3.
Table 3 adsorbs tails oil composition
| Number | Substance classes | Content/wt% |
| 1 | Alkane (positive structure/isoparaffin) | 24.3 |
| 2 | Alkene (positive structure/isomeric olefine) | 75.4 |
| 3 | Acids | -- |
| 4 | Other oxygenatedchemicals | 0.3 |
Comparative example 1-3
Raw material sources are the distillate of 1,200,000 tons/year of coal oil devices of chemical industry Co., Ltd, Inner Mongol gouy Thailand, are passed through
It is handled after depickling, fraction cutting using the method for embodiment 1 in patent CN106966852A, due to oxygenatedchemicals pair
The influence of extracting rectifying process, obtained 1- decene purity 99%, the not up to requirement of polymer grade, therefore just need in extraction essence
Deoxy compound is set before evaporating.
Likewise, being evaporated using corresponding carbon number in the method processing present invention of embodiment 4 and 7 in patent CN106966852A
Point, the purity of obtained 1-13 alkene, 1-16 alkene is 99.5%, the requirement of same not up to polymer grade.
Embodiment 1
Target alkene carbon number is 8, and extractant is phthalic acid ester dimethyl ester, lightness-removing column operating parameter are as follows: bottom temperature
58 DEG C, operating pressure 21.3kpa, the number of plates 65, feed entrance point 45, reflux ratio 4: 1；Weight-removing column operating parameter are as follows: tower reactor temperature
80 DEG C, operating pressure 21.3kpa of degree, the number of plates 55, feed entrance point 35, reflux ratio 5: 1；Extractive distillation column operating parameter are as follows:
85 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 40, feed entrance point 18, reflux ratio 5.5: 1；Extractant and raw material matter
Amount is than being 5: 1；Recovery tower operating parameter are as follows: 87 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 45, feed entrance point 23,
Reflux ratio is 4.5: 1 olefin product purity in 99.7wt% or more, and oxygenates level is lower than 10ppm, and carbonyls is low
In 1ppm.
Embodiment 2-11
For basic handling method with embodiment 1, concrete operations parameter is different, is specifically shown in Table 4- table 8.
Embodiment 12
Adsorption tower equipped with molecular sieve is passed through to the product that embodiment 2-11 extracting rectifying obtains, is carried out at oxide removal
Reason, to the further adsorbing separation of oxycompound progress, (adsorbent is 5A molecular sieve, and adsorbent and oily mass ratio are 1: 1), grasping
Making temperature is 40 DEG C, and pressure 0.5Mpa obtains product purity and is above 99.7wt%, and oxygenates level is lower than 1ppm.
4 embodiment 2-3 target alkene carbon number of table and technological parameter
5 embodiment 4-5 target alkene carbon number of table and technological parameter
6 embodiment 6-7 target alkene carbon number of table and technological parameter
7 embodiment 8-9 target alkene carbon number of table and technological parameter
8 embodiment 10-11 target alkene carbon number of table and technological parameter
Claims (15)
1. a kind of method for separating alkene from coal base F- T synthesis light fraction oil, which is characterized in that the carbon number of target alkene
For n, 8≤n≤18, specifically includes the following steps:
(1) depickling processing is carried out to Fischer-Tropsch light fraction oil raw material, the content of alkane and alkene in depickling treated distillate
Not less than 98wt%, oxygenates level is not higher than 2wt%, and acid value is not higher than 0.1mgKOH/100ml；In oxygenatedchemicals
Alcohols material content 40-60wt%, remaining is the impurity such as aldehyde, ketone, esters；
(2) the Fischer-Tropsch light fraction oil after depickling carries out the absorption of carbonyls by chromatographic column, and adsorbing medium is 5A molecule
Sieve, alkane and alkene contains 99wt% or more, oxygenates level 1wt% or less after adsorbing；It is big absolutely in oxygenatedchemicals
Oxygenates are alcohol, and the content of carbonyls drops to 1ppm or less；
(3) distillate after adsorption treatment enters lightness-removing column, and the component by carbon number less than n is separated by lightness-removing column tower top, tower bottom group
Divide and enters weight-removing column；Component of the carbon number greater than n is isolated by weight-removing column tower bottom, and weight-removing column tower top separates the component that carbon number is n,
Middle hydrocarbon content is not less than 99.7wt%, remaining is oxygenatedchemicals；The oxygenatedchemicals overwhelming majority is alcohol, and carbonyls is through examining
It surveys content and is less than 1ppm；
(4) carbon number is that the component of n enters extractive distillation column, is inversely contacted with extractant, and nonpolar alkane is separated by tower top, extraction
Agent and target alkene is taken to be distillated by tower bottom into recovery tower, target alkene is distillated by recycling tower top, and extractant is distillated by tower reactor, is followed
Ring enters extractive distillation column；
Wherein, the alkene that extracting rectifying obtains is polymer grade product；Fischer-Tropsch light fraction oil be it is a kind of with carbon number distribution from light dydrocarbon
To the alkane alkene mixture as main component of carbon 18, wherein alkene and alkane mass ratio are 2.5: 1~3.5: 1；Extractant is
Phthalate compound.
Olefin product purity is lower than 1ppm in 99.7wt% or more, carbonyl compound content, and oxygenatedchemicals total amount is lower than
10ppm。
2. a kind of method for separating alkene from coal base F- T synthesis light fraction oil according to claim 1, feature
It is, the depickling treated distillate composition are as follows: alkane and alkene gross mass percentage are not less than 99.7wt%, containing oxidation
It closes amount of substance percentage and is not higher than 0.3wt%, wherein the oxygenatedchemicals overwhelming majority is alcohol, and carbonyls is small through detection level
In 1ppm.
3. -2 described in any item a kind of sides for separating alkene from coal base F- T synthesis light fraction oil according to claim 1
Method, which is characterized in that n=8, extractant are repefral；
Lightness-removing column operating parameter are as follows: 58 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 65, feed entrance point 45, reflux ratio
It is 4: 1；
Weight-removing column operating parameter are as follows: 80 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 55, feed entrance point 35, reflux ratio
It is 5: 1；
Extractive distillation column operating parameter are as follows: 85 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 40, feed entrance point 18 returns
Stream is than being 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 87 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 45, feed entrance point 23, reflux ratio
It is 4.5: 1；
For olefin product purity in 99.7wt% or more, oxygenates level is lower than 10ppm, and carbonyls is lower than 1ppm.
4. -2 described in any item a kind of sides for separating alkene from coal base F- T synthesis light fraction oil according to claim 1
Method, which is characterized in that n=9, extractant are repefral,
Lightness-removing column operating parameter are as follows: 85 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 65, feed entrance point 45, reflux ratio
It is 4: 1；
Weight-removing column operating parameter are as follows: 104 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 55, feed entrance point 35, reflux ratio
It is 5: 1；
Extractive distillation column operating parameter are as follows: 109 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 40, feed entrance point 18 returns
Stream is than being 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 101 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 45, feed entrance point 23, reflux ratio
It is 4.5: 1；
Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm, and carbonyl compound content is lower than 1ppm.
5. -2 described in any item a kind of sides for separating alkene from coal base F- T synthesis light fraction oil according to claim 1
Method, which is characterized in that n=10, extractant are repefral；
Lightness-removing column operating parameter are as follows: 105 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 65, feed entrance point 45, reflux ratio
It is 4: 1；
Weight-removing column operating parameter are as follows: 125 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 55, feed entrance point 35, reflux ratio
It is 5: 1；
Extractive distillation column operating parameter are as follows: 129 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 40, feed entrance point 18 returns
Stream is than being 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 131 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 45, feed entrance point 23, reflux ratio
It is 4.5: 1；
Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm, and carbonyl compound content is lower than 1ppm.
6. -2 described in any item a kind of sides for separating alkene from coal base F- T synthesis light fraction oil according to claim 1
Method, which is characterized in that n=11, extractant are the mixture of repefral and diethyl phthalate, molar ratio
It is 1: 1；
Lightness-removing column operating parameter are as follows: 126 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 65, feed entrance point 45, reflux ratio
It is 4: 1；
Weight-removing column operating parameter are as follows: 146 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 55, feed entrance point 35, reflux ratio
It is 5: 1；
Extractive distillation column operating parameter are as follows: 151 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 40, feed entrance point 18 returns
Stream is than being 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 153 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 45, feed entrance point 23, reflux ratio
It is 4.5: 1；
Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm, and carbonyl compound content is lower than 1ppm.
7. -2 described in any item a kind of sides for separating alkene from coal base F- T synthesis light fraction oil according to claim 1
Method, which is characterized in that n=12, extractant are diethyl phthalate, molar ratio 1: 1；
Lightness-removing column operating parameter are as follows: 145 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 65, feed entrance point 45, reflux ratio
It is 4: 1；
Weight-removing column operating parameter are as follows: 166 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 55, feed entrance point 35, reflux ratio
It is 5: 1；
Extractive distillation column operating parameter are as follows: 172 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 40, feed entrance point 18 returns
Stream is than being 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 174 DEG C of bottom temperature, operating pressure 21.3kpa, the number of plates 45, feed entrance point 23, reflux ratio
It is 4.5: 1；
Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm, and carbonyl compound content is lower than 1ppm.
8. -2 described in any item a kind of sides for separating alkene from coal base F- T synthesis light fraction oil according to claim 1
Method, which is characterized in that n=13, extractant are diethyl phthalate；
Lightness-removing column operating parameter are as follows: 96 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 65, feed entrance point 45, reflux ratio
It is 4: 1；
Weight-removing column operating parameter are as follows: 115 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 55, feed entrance point 35, reflux ratio
It is 5: 1；
Extractive distillation column operating parameter are as follows: 118 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 40, feed entrance point 18 returns
Stream is than being 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 120 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 45, feed entrance point 23, reflux ratio
It is 4.5: 1；
Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm, and carbonyl compound content is lower than 1ppm.
9. -2 described in any item a kind of sides for separating alkene from coal base F- T synthesis light fraction oil according to claim 1
Method, which is characterized in that n=14, extractant are dibutyl phthalate；
Lightness-removing column operating parameter are as follows: 113 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 65, feed entrance point 45, reflux ratio
It is 4: 1；
Weight-removing column operating parameter are as follows: 128 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 55, feed entrance point 35, reflux ratio
It is 5: 1；
Extractive distillation column operating parameter are as follows: 130 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 40, feed entrance point 18 returns
Stream is than being 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 132 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 45, feed entrance point 23, reflux ratio
It is 4.5: 1；
Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm, and carbonyl compound content is lower than 1ppm.
10. -2 described in any item a kind of sides for separating alkene from coal base F- T synthesis light fraction oil according to claim 1
Method, which is characterized in that n=15, extractant are dioctyl phthalate；
Lightness-removing column operating parameter are as follows: 131 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 65, feed entrance point 45, reflux ratio
It is 4: 1；
Weight-removing column operating parameter are as follows: 141 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 55, feed entrance point 35, reflux ratio
It is 5: 1；
Extractive distillation column operating parameter are as follows: 144 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 40, feed entrance point 18 returns
Stream is than being 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 146 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 45, feed entrance point 23, reflux ratio
It is 4.5: 1；
Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm, and carbonyl compound content is lower than 1ppm.
11. -2 described in any item a kind of sides for separating alkene from coal base F- T synthesis light fraction oil according to claim 1
Method, which is characterized in that n=16, extractant are dioctyl phthalate；
Lightness-removing column operating parameter are as follows: 143 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 65, feed entrance point 45, reflux ratio
It is 4: 1；
Weight-removing column operating parameter are as follows: 153 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 55, feed entrance point 35, reflux ratio
It is 5: 1；
Extractive distillation column operating parameter are as follows: 155 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 40, feed entrance point 18 returns
Stream is than being 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 157 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 45, feed entrance point 23, reflux ratio
It is 4.5: 1；
Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm, and carbonyl compound content is lower than 1ppm.
12. -2 described in any item a kind of sides for separating alkene from coal base F- T synthesis light fraction oil according to claim 1
Method, which is characterized in that n=17, extractant are dioctyl phthalate；
Lightness-removing column operating parameter are as follows: 156 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 65, feed entrance point 45, reflux ratio
It is 4: 1；
Weight-removing column operating parameter are as follows: 165 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 55, feed entrance point 35, reflux ratio
It is 5: 1；
Extractive distillation column operating parameter are as follows: 167 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 40, feed entrance point 18 returns
Stream is than being 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 169 DEG C of bottom temperature, operating pressure 1.33kpa, the number of plates 45, feed entrance point 23, reflux ratio
It is 4.5: 1；
Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm, and carbonyl compound content is lower than 1ppm.
13. -2 described in any item a kind of sides for separating alkene from coal base F- T synthesis light fraction oil according to claim 1
Method, which is characterized in that n=18, extractant are dioctyl phthalate；
Lightness-removing column operating parameter are as follows: 153 DEG C of bottom temperature, operating pressure 0.67kpa, the number of plates 65, feed entrance point 45, reflux ratio
It is 4: 1；
Weight-removing column operating parameter are as follows: 170 DEG C of bottom temperature, operating pressure 0.67kpa, the number of plates 55, feed entrance point 35, reflux ratio
It is 5: 1；
Extractive distillation column operating parameter are as follows: 172 DEG C of bottom temperature, operating pressure 0.67kpa, the number of plates 40, feed entrance point 18 returns
Stream is than being 5.5: 1；Extractant and material quality ratio are 5: 1；
Recovery tower operating parameter are as follows: 174 DEG C of bottom temperature, operating pressure 0.67kpa, the number of plates 45, feed entrance point 23, reflux ratio
It is 4.5: 1；
Olefin product purity 99.7wt%, oxygenates level are lower than 10ppm, and carbonyl compound content is lower than 1ppm.
14. -2 described in any item a kind of sides for separating alkene from coal base F- T synthesis light fraction oil according to claim 1
Method, which is characterized in that further include the steps that the product obtained to extracting rectifying carries out oxide removal processing.
15. using the described in any item method systems for separating alkene from coal base F- T synthesis light fraction oil of claim 1-14
The olefin product obtained.
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| CN113636592A (en) * | 2020-04-27 | 2021-11-12 | 中国石油化工股份有限公司 | Resourceful treatment equipment and method for polyolefin catalyst mother liquor |
| CN115612521A (en) * | 2021-07-14 | 2023-01-17 | 国家能源投资集团有限责任公司 | Process for removing oxygenates from a hydrocarbon-containing stream |
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