CN102719270A - Method and system for separating saturated alkane in liquid hydrocarbon material flow from mixed primary alcohol - Google Patents
Method and system for separating saturated alkane in liquid hydrocarbon material flow from mixed primary alcohol Download PDFInfo
- Publication number
- CN102719270A CN102719270A CN2012101856405A CN201210185640A CN102719270A CN 102719270 A CN102719270 A CN 102719270A CN 2012101856405 A CN2012101856405 A CN 2012101856405A CN 201210185640 A CN201210185640 A CN 201210185640A CN 102719270 A CN102719270 A CN 102719270A
- Authority
- CN
- China
- Prior art keywords
- extraction
- tower
- section
- fraction
- agent
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a method and a system for separating saturated alkane in liquid hydrocarbon material flow from mixed primary alcohol. The liquid hydrocarbon material flow is a mixture of saturated straight-chain alkane and straight-chain primary alcohol. The method comprises the following steps of: I, pretreating raw materials with a fraction cutting method; II, extracting each section of fraction with an extracting agent; and III, purifying mixed primary alcohol and recovering the extracting agent. The raw materials are pretreated with the fraction cutting method, and the temperature range of each section fraction extracted from a tower top is 0-90 DEG C, 90-140 DEG C and 140-190 DEG C respectively. Through azeotropic distillation, the extracting agent is separated from mixed primary alcohol, and while high-purity mixed primary alcohol is obtained, the extracting agent is recovered. The recovered extracting agent can be recycled after treatment.
Description
Technical field
The present invention provide a kind of with the saturated alkane in the liquid hydrocarbon stream with mix the isolating method and system of primary alconol.Said liquid hydrocarbonaceous streams is a Fischer-Tropsch synthetic.
Background technology
In have a large amount of associated gas in the process of extra large oil oil and natural gas exploitation at sea; Because the engineering and the envrionment conditions of offshore oilfield; The method of handling associated gas at present is to the atmosphere dispensing, discharges behind oil reservoir re-injection or the torch burning, has not only wasted the energy; And containing a large amount of greenhouse gases methane in the associated gas, methane makes the coefficient of global warming be about 21 times of carbonic acid gas.The scale that these torches are dropped a hint less (treatment capacity is 20～300,000 side/skies), output and reserves are difficult to accurate prediction, and output descends comparatively fast in time, adopts conventional means to be difficult to reach the level of economic utilization.
Last century, the nineties rose, and the natural gas via synthetic gas is produced liquid fuel, and the research of especially high-quality diesel oil causes people's attention again.Sweet natural gas system synthetic oil (GTL) process is produced high-quality diesel oil; This combined diesel oil has cetane value height, advantages such as sulfur-bearing, nitrogen and aromatic hydrocarbons not; Can be directly as the automobile-used diesel oil of ultra cleaning minimum discharge; Also can be used as blending component and add in the existing a large amount of low-quality diesel oil, improve its quality, satisfy strict day by day environmental requirement.
Chinese patent CN1764619 introduced a kind of from hydrocarbon stream extraction of oxygenates (be mainly mix primary alconol) kept the commercial feasible method of the olefin(e) centent of condensate product simultaneously, said hydrocarbon stream is the fraction of typical Fischer-Tropsch reaction condensate.It is solvent that the oxygenate extracting process is to use the mixture of first alcohol and water; The method of extraction of oxygenates in the liquid-liquid extraction method; Wherein the extraction liquid of liquid-liquid extraction is delivered to solvent recovery tower; The overhead product that in regenerating column, will comprise methyl alcohol, alkene and paraffins is recycled to extraction tower, thereby improves the total yield of alkene and paraffins.In this method, the water cut that requires solvent is 5% ~ 15% (massfraction).Utilization this method, after reclaiming extraction agent, bottom product only comprises the oxygenate less than 0.02% (massfraction), and the recovery of alkene and paraffins is higher than 80%.This method is limited to the synthetic condensate of Fischer-Tropsch in C10 ~ C13 scope, and purpose is to improve the purity and the recovery of alkene and alkane.Extract in the hydrocarbon stream outside the not mentioned scope from then on and mix primary alconol, and this method does not focus on the recovery that mixes primary alconol.
Chinese patent CN1468292A has introduced the method for alkene and alkane and oxide compound in a kind of separating liquid hydrocarbon stream, contains a high proportion of alkene, alkane, oxide compound (being mainly alcohol) in the said liquid hydrocarbon stream.Described hydrocarbon stream is obtained by Fischer-Tropsch reaction.In the method, introduce the boiling point used a kind of counter solvent, its boiling point to be lower than in the hydrocarbon stream the volatile alcohol of tool.The raffinate that from the liquid-liquid extraction tower, obtains is through a distillation tower, and bottom product contains alkene and alkane, contains the then recycling of overhead product of solvent.The come together extraction phase of surplus tower gained of liquid-liquid is delivered to stripping column, can obtain containing the bottom product of the said institute extraction tower of purified alcohol, contains the then recycling of overhead product of counter solvent.In this method, carbonatoms is that the hydro carbons of C1～C7 and the alcohols of C1～C3 are left in the basket in the logistics, otherwise, can't select reverse-extraction agent.In the separate hydrocarbons logistics of this method institute, higher alcohols content is very little, and the above oxide compound of C12 is trace, in calculating, is left in the basket.
Summary of the invention
The present invention provides a kind of System and method for that from liquid hydrocarbon stream, separates primary alconol.Said liquid hydrocarbon stream is the Fischer-Tropsch synthesis product, is the mixture of saturated straight chain alkane and straight chain primary alcohol, and both ratios are very high, and are more or less the same.
Technical scheme of the present invention is following:
A kind of with the saturated alkane in the liquid hydrocarbon stream with mix the isolating method of primary alconol, liquid hydrocarbon stream is the mixture of saturated straight chain alkane and straight chain primary alcohol; This method comprises three parts: the one, and adopt the method for cut cutting that raw material is carried out pre-treatment; The 2nd, adopt extraction agent to carry out extracting operation to each section cut; The 3rd, mix the purification of primary alconol and the recovery of extraction agent.
Adopt the method for cut cutting that raw material is carried out pre-treatment, each section cut TR of cat head institute extraction is respectively: 0～90 ℃, 90 ℃～140 ℃, 140 ℃～190 ℃.
First section fraction introduced extraction tower, adopts water as extraction agent, and the extraction agent consumption is no less than the half the of first section fraction volume.
Second section fraction introduced extraction tower, adopts acetonitrile-water as extraction agent, and the extraction agent water cut is 40%, and consumption is 4 times of second section fraction volume, and extraction temperature is 20 ℃.
The 3rd section fraction introduced extraction tower, adopts acetonitrile-water as extraction agent, and the extraction agent water cut is 40%, and consumption is 4 times of the 3rd section fraction volume, and extraction temperature is 20 ℃.
The 4th section fraction introduced extraction tower, adopts acetonitrile-methyl alcohol as extraction agent, adds entry as the layering agent, and it is 20% that extraction agent contains quantity of methyl alcohol, and consumption is 4 times of the 3rd section fraction volume, and extraction temperature is 50 ℃.
Realize in the liquid hydrocarbon stream saturated alkane with mix the primary alconol separation system, comprise the pre-treatment rectifying tower, extraction tower and extraction phase rectifying tower; Pre-treatment rectifying tower cat head has three bursts of cut extraction according to the different temperature interval, is connected with three extraction towers respectively and carries out extracting operation; Bottom product also is connected with extraction tower as a plume thigh and carries out extracting operation; Extraction phase after the process extraction is connected with the extraction phase rectifying tower respectively and carries out distillation operation, thereby makes the mixing primary alconol obtain separating purification with saturated alkane.
Adopt different extraction agents to name section fraction, be aided with different extracting operation conditions, so that saturated alkane reaches maximum with primary alconol and separates in each section fraction.Mix primary alconol in first section fraction of cat head institute extraction and mainly form, only contain a small amount of butanols, do not contain other primary alconol by methyl alcohol, ethanol, propyl alcohol; Mix primary alconol in second section fraction and mainly form, only contain a small amount of propyl alcohol and hexanol, do not contain other primary alconol by butanols, amylalcohol; Mix primary alconol in the 3rd section fraction and mainly form, only contain a small amount of amylalcohol and decyl alcohol, do not contain other primary alconol by hexanol, enanthol, octanol; The 4th section fraction is tower bottoms, wherein mixes primary alconol and mainly is higher than ten primary alconol by carbon number and forms, and only contains a small amount of octanol.
Liquid hydrocarbon stream is introduced rectifying tower, and pretreating scheme be that fraction is cut, according to the height of the boiling point of each component, from cat head extraction successively.The foundation of cat head extraction is following:
1. in the said liquid hydrocarbon stream, polar changes main in being present in primary alconol, is index with the primary alconol therefore, only considers the enrichment of primary alconol, does not consider the enrichment of saturated alkane;
2. methyl alcohol, ethanol, three of propyl alcohol can be belonged to first section fraction with the miscible component of water at normal temperatures;
3. tower bottoms is preferably liquid, so must contain the component that condensation point is lower than normal temperature at the bottom of the tower.Preferred decyl alcohol is as this component in present method.That is to say that boiling point is higher than the component of decyl alcohol and all will at the bottom of tower, collects;
4. after cutting apart through above-mentioned 2,3; Remaining five primary alconols are divided into two groups; According to the polar phase approximately principle, preferred butanols of present method and amylalcohol are formed as the primary alconol of second section fraction of cat head, and preferred hexanol, enanthol, octanol are formed as the primary alconol of the 3rd section fraction of cat head.
After the fraction cutting, each section fraction is introduced extraction tower respectively, adopts the lightweight polar solvent to extract.
After above-mentioned first section fraction introduced extraction tower, preferably water was as extraction agent.The cat head extracting phase is highly purified saturated alkane, and extraction phase is the aqueous solution of methyl alcohol, ethanol, propyl alcohol at the bottom of the tower.
After above-mentioned second section and the 3rd section fraction were introduced extraction tower, preferred acetonitrile-water was as extraction agent.The cat head extracting phase is highly purified saturated alkane, and extraction phase is the mixing primary alconol solution that contains extraction agent at the bottom of the tower.
After above-mentioned the 4th section fraction introduced extraction tower, preferred acetonitrile-methyl alcohol was as extraction agent, and preferably water promotes layering.The cat head extracting phase is highly purified saturated alkane, and extraction phase is the mixing primary alconol solution that contains extraction agent at the bottom of the tower.
Second and third, four sections extraction phase introduces rectifying tower, adds excessive acetonitrile, adopts the method for azeotropic distillation to reclaim each section extraction agent.
Present method is to first section extraction phase, that is the aqueous solution of methyl alcohol, ethanol, propyl alcohol, and wherein the purification of primary alconol is not introduced.
Present method is made up of three parts.At first, adopt the method for rectifying that said Fischer-Tropsch synthetic is carried out pre-treatment,, at the bottom of cat head and tower, obtain the fraction of different compositions, character respectively by the boiling range cutting; Then, to each fraction character, select different extraction agent to realize separating of saturated alkane and primary alconol, extracting phase is highly purified saturated alkane; At last, extraction phase is introduced rectifying tower, through azeotropic distillation, extraction agent is separated with the mixing primary alconol, obtains highly purified mixing primary alconol and reclaims extraction agent simultaneously.The extraction agent that reclaims can be recycled after treatment.
Present method is characterised in that and adopts the method for fraction cutting that raw material is carried out pre-treatment, obtains four sections fractions that component is different.The polarity of primary alconol is close in each section fraction, because of then the solubleness in extraction agent is close, helps taking unified extraction conditions.Through azeotropic distillation, extraction agent is separated with the mixing primary alconol, obtain highly purified mixing primary alconol and reclaim extraction agent simultaneously.The extraction agent that reclaims can be recycled after treatment.
Description of drawings
Fig. 1: be process flow sheet of the present invention.
Wherein: T1-pre-treatment rectifying tower; E1-one section cut extraction tower; E2-two section cut extraction tower;
E3-three section cut extraction tower; E4-four section cut extraction tower; T2-two section cut extraction phase rectifying tower;
T3-three section cut extraction phase rectifying tower; T4-four section cut extraction phase rectifying tower;
1-liquid stock; 2-overhead fraction; 3-one section cut; 4-two sections cuts; 5-three sections cuts;
6-four sections cuts; 7-one section cut extraction agent; 8-one section cut extracting phase; 9-one section cut extraction phase;
10-two sections cut extracting phases; 11-two sections cut extraction phases; 12-two sections cut extraction agents reflux;
13-two sections separating obtained high-purity primary alconols of cut; 14-three sections cut extracting phases; 15-three sections cut extraction phases;
16-three sections cut extraction agents reflux; 17-three sections cut extraction agents;
18-three sections separating obtained high-purity primary alconols of cut; 19-four sections cut extracting phases; 20-four sections cut extraction phases;
21-four sections cut extraction agents reflux; 22-four sections separating obtained high-purity primary alconols of cut;
Embodiment
The present invention provides a kind of method of from liquid hydrocarbon stream, separating primary alconol.Said liquid hydrocarbon stream is the Fischer-Tropsch synthesis product, comprises C5～C21 saturated straight chain alkane and C1～C18 straight chain primary alcohol.
Reference flowchart: 1, liquid hydrocarbon stream is introduced T1, under normal pressure, carry out the fraction cutting.Collecting boiling range respectively at cat head is 0～90 ℃, 90 ℃～140 ℃, 140 ℃～190 ℃ fraction, at the bottom of tower, collects raffinate.In each section fraction of cat head extraction, the polarity of primary alconol is all more close.
The boiling range of T1 cat head extraction is that 0～90 ℃ fraction is introduced among the extraction tower E1, adopts water as extraction agent.Fraction gets into extraction agent at the bottom of tower, extraction agent gets into extraction tower from cat head, and the consumption of water is the half the of fraction volume.After passing through liquid-liquid extraction at normal temperatures, obtain highly purified saturated alkane, at the bottom of tower, obtain methyl alcohol, ethanol, propyl alcohol and the aqueous solution at cat head.For the separation of alcohol-water system, present method is not discussed.
The fraction that the boiling range of T1 cat head extraction is 90 ℃～140 ℃, 140 ℃～190 ℃ is introduced respectively among extraction tower E2, the E3, and preferred lightweight polar solvent is as extraction agent.The preferred acetonitrile-water of present method is as extraction agent, and water-content is 40% in the extraction agent.Fraction gets into extraction agent at the bottom of tower, extraction agent gets into extraction tower from cat head, and the extraction agent consumption is not less than 2 times of fraction volume, the preferred 4 times of consumptions of present method.After passing through liquid-liquid extraction at normal temperatures, obtain highly purified saturated alkane respectively at cat head, extraction phase is introduced rectifying tower T2, T3 respectively at the bottom of the tower.In rectifying tower, add excessive acetonitrile, really make the acetonitrile consumption be higher than the ratio of acetonitrile and water formation azeotrope, so that water steams from cat head fully.Be not higher than 76 ℃ fraction at T2, T3 overhead collection boiling point, obtain water-content and be 15% acetonitrile-aqueous solution, add entry, make water-content reach 40%, return to extraction tower E2, E3 and recycle.At the bottom of the tower of T2, T3, obtain containing the high purity mixing primary alconol of minor amounts of acetonitrile.
The T1 tower bottoms is incorporated among the extraction tower E4.Preferred lightweight polar solvent is as extraction agent.Preferred acetonitrile-the methyl alcohol of present method is as extraction agent, and methanol content is 20% in the extraction agent, simultaneously, needs to add less water.The consumption of water is few as far as possible, promotes that layering acts on clearly as long as can reach, and is capable of reducing energy consumption in follow-up distillation operation like this.Present method is preferably 1/20th of extraction agent consumption.Extraction agent and water get into from extraction tower E4 cat head, and the T1 tower bottoms is introduced at the bottom of the extraction tower E4 tower, and the extraction agent consumption is not less than 2 times of fraction volume, the preferred 4 times of consumptions of present method.After carrying out liquid-liquid extraction under 50 ℃, obtain the higher saturated alkane of purity at cat head, extraction phase is introduced among the rectifying tower T4 at the bottom of the tower.Add excessive acetonitrile at rectifying tower, really make the acetonitrile consumption be higher than the ratio of acetonitrile and methyl alcohol formation azeotrope, the acetonitrile consumption also will be considered with the less water in the extraction phase, guarantees water all to be reclaimed at cat head through the method for azeotropic distillation.Be not higher than 76 ℃ fraction at T4 overhead collection boiling point, obtain methanol content and be acetonitrile-methanol solution of 19%, contain less water simultaneously.The adding small amount of methanol makes methanol content reach 20%, returns to extraction tower E4 to recycle.At the bottom of the T4 tower, obtain containing the higher mixing primary alconol of purity of minor amounts of acetonitrile.
Method separating effect provided by the invention is fine, can be used for separating of Fischer-Tropsch synthetic Semi-polarity solvent and non-polar solvent.Present method main purpose is to isolate highly purified primary alconol, but the purity of the saturated alkane that obtains from extraction agent is also very high, even is higher than the purity of primary alconol.
Following instance will the present invention will be described better, but can therefore not limit its application.
Specific embodiment:
Table 1 has provided in the liquid hydrocarbon stream to be formed and the each component boiling point.
Table 1
| Alcohols | Weight % | Boiling point/℃ | Saturated alkane | Weight % | Boiling point/℃ |
| Methyl alcohol | 3.32 | 64.05 | Skellysolve A | 8.14 | 36.3 |
| Ethanol | 1.14 | 76.98 | Normal hexane | 6.07 | 68.86 |
| Propyl alcohol | 1.78 | 96.23 | Normal heptane | 6.56 | 98.42 |
| Propyl carbinol | 4.10 | 116.85 | Octane | 8.56 | 125.91 |
| Pentyl alcohol | 5.85 | 136.46 | |||
| N-hexyl alcohol | 5.21 | 157.23 | N-decane | 6.85 | 173.87 |
| N-Heptyl alcohol | 3.96 | 176.26 | Undecane | 3.34 | 194.18 |
| N-Octanol | 5.00 | 195.25 | |||
| Nonylcarbinol | 4.88 | 230.56 | Dodecyl | 2.85 | 214.91 |
| Lauryl alcohol | 3.61 | 263.8 | Tridecane | 2.43 | 234.65 |
| Tetradecyl alcohol | 2.78 | 294.05 | The tetradecane | 3.02 | 252.93 |
| Hexadecanol | 1.79 | 321.6 | N-Hexadecane | 2.72 | 285.86 |
| Stearyl alcohol | 0.56 | 346.62 | Heptadecane | 1.63 | 301.11 |
| Octadecane | 1.40 | 314.62 | |||
| Nonadecane | 1.11 | 327.84 | |||
| Eicosane | 0.89 | 340.63 | |||
| Heneicosane | 0.44 | ||||
| Add up to | 43.99 | Add up to | 56.01 |
Liquid hydrocarbon stream carries out the fraction cutting through a rectifying tower, and the tower data are following:
Tower height: 1200mm
Tower diameter: 25mm
Filler: 33mm
Reflux ratio: 2: 1
Elder generation's total reflux is 30 minutes during the experiment beginning, so that filler is fully wetting, begins then according to the operation of design reflux ratio, and whole rectifying process continues about 20 hours.Table 2 has provided the result of fraction cutting.
Table 2
| 30℃~90℃ | 90℃~140℃ | 140℃~190℃ | At the bottom of the tower | |
| Methyl alcohol | 11.35 | |||
| Ethanol | 4.33 | |||
| Pentane | 27.35 | 0.30 | ||
| Propyl alcohol | 6.13 | 0.84 | ||
| Hexane | 21.67 | 0.45 | ||
| Butanols | 3.21 | 16.06 | ||
| Heptane | 21.70 | 4.22 | ||
| Amylalcohol | 28.53 | 1.77 | ||
| Octane | 4.22 | 39.75 | 0.00 | |
| Pure | 4.45 | 15.03 | ||
| Enanthol | 17.23 | |||
| Decane | 5.39 | 19.40 | ||
| Octanol | 19.63 | 0.64 | ||
| Undecane | 14.01 | 0.36 | ||
| Dodecyl | 7.94 | 3.76 | ||
| Decyl alcohol | 3.55 | 13.97 | ||
| Tridecane | 1.45 | 7.89 | ||
| The tetradecane | 11.30 | |||
| Lauryl alcohol | 12.75 | |||
| N-Hexadecane | 10.45 | |||
| Tetradecyl alcohol | 9.89 | |||
| Heptadecane | 6.04 | |||
| Octadecane | 5.16 | |||
| Hexadecanol | 6.38 | |||
| Nonadecane | 4.01 | |||
| Eicosane | 3.46 | |||
| Stearyl alcohol | 2.04 | |||
| Heneicosane | 1.93 | |||
| Add up to | 100 | 100 | 100 | 100 |
First section fraction introduced extraction tower, mixes with 1/2 times of water, carries out liquid-liquid extraction at normal temperatures.Table 3 has provided first section result after the fraction extraction.
Table 3
| Component | Extraction phase | Extracting phase |
| Methyl alcohol | 15.35 | 0 |
Second, third section fraction is introduced extraction tower, and extraction agent is that water cut is 40% acetonitrile-aqueous solution, and consumption is 4 times of fraction volume, under normal temperature, extracts.Extraction phase is introduced rectifying tower, gathers boiling point at cat head and is not higher than 76 ℃ component.Table 4 has provided the result after second section fraction extraction, the rectifying.Table 5 has provided the result after the 3rd section fraction extraction, the rectifying.
Table 4
| Component | Extraction phase | Extracting phase | Cat head | At the bottom of the tower |
| Propyl alcohol | 0.06 | 0 | 0 | 0 |
| |
0 | 0.68 | 0 | 0 |
| Butanols | 3.06 | 0.35 | 0.14 | 40.72 |
| |
0 | 7.72 | 0 | 0.00 |
| Amylalcohol | 5.20 | 2.11 | 0 | 55.12 |
| |
0 | 77.74 | 0 | 0 |
| Hexanol | 0.61 | 0.22 | 0.10 | 3.85 |
| |
0 | 11.18 | 0 | 0 |
| Acetonitrile | 54.70 | 0 | 90.37 | 0.31 |
| Water | 36.37 | 0 | 9.39 | 0 |
| Add up to | 100 | 100 | 100 | 100 |
Table 5
| Component | Extraction phase | Extracting phase | Cat head | At the bottom of the tower |
| Amylalcohol | 0.33 | 0.22 | 0.33 | 1.05 |
| Pure | 2.79 | 2.64 | 0 | 22.39 |
| Enanthol | 3.07 | 4.36 | 0 | 24.40 |
| Decane | 0.28 | 37.04 | 7.77 | 0.38 |
| Octanol | 3.38 | 6.91 | 0 | 38.51 |
| Undecane | 0.17 | 27.62 | 0 | 0 |
| Dodecyl | 0.21 | 16.11 | 0 | 0 |
| Decyl alcohol | 0.47 | 2.18 | 0 | 4.37 |
| Tridecane | 0 | 2.94 | 0 | 0 |
| Acetonitrile | 54 | 0 | 82.80 | 2.28 |
| Water | 36 | 0 | 8.00 | 0 |
The 4th section fraction introduced extraction tower, and extraction agent is that water cut is acetonitrile-methanol solution of 20%, and consumption is 4 times of fraction volume, adds less water and promotes layering, and the consumption of water is 1/20 of an extraction agent consumption, extracts in 50 ℃.Extraction phase is introduced rectifying tower, gathers boiling point at cat head and is not higher than 76 ℃ component.Table 6 has provided the result after the 4th section fraction extraction, the rectifying.
Table 6
| Component | Extraction phase | Extracting phase | Cat head | At the bottom of the tower |
| Octanol | 0.10 | 0.16 | 0 | 2.44 |
| Undecane | 0.02 | 0.35 | 0 | 0 |
| Dodecyl | 0.15 | 3.91 | 0.22 | 1.06 |
| Decyl alcohol | 2.32 | 2.13 | 0 | 19.62 |
| Tridecane | 0.29 | 9.34 | 0 | 2.70 |
| The tetradecane | 0.35 | 14.81 | 0 | 3.43 |
| Lauryl alcohol | 2.17 | 3.30 | 0 | 18.01 |
| N-Hexadecane | 0.22 | 15.18 | 0 | 2.23 |
| Tetradecyl alcohol | 1.55 | 3.94 | 0 | 12.87 |
| Heptadecane | 0.11 | 9.12 | 0 | 1.08 |
| Octadecane | 0.08 | 8.06 | 0 | 0.77 |
| Hexadecanol | 0.86 | 3.72 | 0 | 7.32 |
| Nonadecane | 0.17 | 6.45 | 0 | 0.53 |
| Eicosane | 0.07 | 5.71 | 0 | 0.40 |
| Stearyl alcohol | 0.21 | 1.64 | 0 | 1.95 |
| Heneicosane | 0.02 | 3.26 | 0 | 0.18 |
| Acetonitrile | 75 | 0.75 | 79 | 25.87 |
| |
15 | 8.17 | 20 | 0 |
| Water | 1.251 | 0 | 0.78 | 0 |
| Add up to | 100 | 100 | 100 | 100 |
| Ethanol | 5.75 | 0 |
| |
0 | 34.78 |
| Propyl alcohol | 6.80 | 1.44 |
| |
0 | 28.23 |
| Butanols | 2.50 | 1.70 |
| |
0 | 28.39 |
| |
0 | 5.46 |
| Water | 69.60 | 0 |
| Add up to | 100 | 100 |
| Add up to | 100 | 100 | 100 | 100 |
Claims (7)
- One kind with the saturated alkane in the liquid hydrocarbon stream with mix the isolating method of primary alconol, liquid hydrocarbon stream is the mixture of saturated straight chain alkane and straight chain primary alcohol; It is characterized in that this method comprises three parts: the one, adopt the method for cut cutting that raw material is carried out pre-treatment; The 2nd, adopt extraction agent to carry out extracting operation to each section cut; The 3rd, mix the purification of primary alconol and the recovery of extraction agent.
- 2. the method for claim 1 is characterized in that adopting the method for each section cut cutting that raw material is carried out pre-treatment, and the cut TR of cat head institute extraction is respectively: 0～90 ℃, 90 ℃～140 ℃, 140 ℃～190 ℃.
- 3. method as claimed in claim 2 is characterized in that first section fraction, introduces extraction tower, adopts water as extraction agent, and the extraction agent consumption is no less than the half the of first section fraction volume.
- 4. method as claimed in claim 2 is characterized in that second section fraction introducing extraction tower, adopts acetonitrile-water as extraction agent, and the extraction agent water cut is 40%, and consumption is 4 times of second section fraction volume, and extraction temperature is 20 ℃.
- 5. method as claimed in claim 2 is characterized in that the 3rd section fraction introducing extraction tower, adopts acetonitrile-water as extraction agent, and the extraction agent water cut is 40%, and consumption is 4 times of the 3rd section fraction volume, and extraction temperature is 20 ℃.
- 6. method as claimed in claim 2 is characterized in that the 4th section fraction introducing extraction tower, adopts acetonitrile-methyl alcohol as extraction agent, adds entry as the layering agent, and it is 20% that extraction agent contains quantity of methyl alcohol, and consumption is 4 times of the 3rd section fraction volume, and extraction temperature is 50 ℃.
- 7. realize in the liquid hydrocarbon stream of claim 1 saturated alkane with mix the primary alconol separation system, it is characterized in that comprising the pre-treatment rectifying tower, extraction tower and extraction phase rectifying tower; Pre-treatment rectifying tower cat head has three bursts of cut extraction according to the different temperature interval, is connected with three extraction towers respectively and carries out extracting operation; Bottom product also is connected with extraction tower as a plume thigh and carries out extracting operation; Extraction phase after the process extraction is connected with the extraction phase rectifying tower respectively and carries out distillation operation, thereby makes the mixing primary alconol obtain separating purification with saturated alkane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101856405A CN102719270A (en) | 2012-06-07 | 2012-06-07 | Method and system for separating saturated alkane in liquid hydrocarbon material flow from mixed primary alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101856405A CN102719270A (en) | 2012-06-07 | 2012-06-07 | Method and system for separating saturated alkane in liquid hydrocarbon material flow from mixed primary alcohol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102719270A true CN102719270A (en) | 2012-10-10 |
Family
ID=46945148
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012101856405A Pending CN102719270A (en) | 2012-06-07 | 2012-06-07 | Method and system for separating saturated alkane in liquid hydrocarbon material flow from mixed primary alcohol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102719270A (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2746984A (en) * | 1951-06-22 | 1956-05-22 | Ruhrchemie Ag | Process for the separation of aliphatic alchols from hydrocarbon-alcohol mixtures |
| CN101891589A (en) * | 2010-06-21 | 2010-11-24 | 中国海洋石油总公司 | Method for extracting fatty alcohols |
| CN102036726A (en) * | 2008-03-25 | 2011-04-27 | 台湾中油股份有限公司 | Improved extractive distillation processes using water-soluble extractive solvents |
-
2012
- 2012-06-07 CN CN2012101856405A patent/CN102719270A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2746984A (en) * | 1951-06-22 | 1956-05-22 | Ruhrchemie Ag | Process for the separation of aliphatic alchols from hydrocarbon-alcohol mixtures |
| CN102036726A (en) * | 2008-03-25 | 2011-04-27 | 台湾中油股份有限公司 | Improved extractive distillation processes using water-soluble extractive solvents |
| CN101891589A (en) * | 2010-06-21 | 2010-11-24 | 中国海洋石油总公司 | Method for extracting fatty alcohols |
Non-Patent Citations (1)
| Title |
|---|
| 周付军: "从费托合成产物中分离混合伯醇", 《天津大学硕士论文》, 30 August 2010 (2010-08-30) * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105777467B (en) | A kind of method that oxygenatedchemicals and 1- hexenes are detached from oil from Fischer-Tropsch synthesis | |
| Kiss | Novel applications of dividing‐wall column technology to biofuel production processes | |
| CN102060660B (en) | Method for separating alcohol compound from Tropsch synthesis reaction water | |
| CN103553877B (en) | Method for rectifying ethylene glycol during production of ethylene glycol from calcium carbide furnace gas | |
| CN102604677B (en) | High and low-temperature Fischer-Tropsch synthesis co-production technology | |
| CN102666458A (en) | Recovery of butanol from a mixture of butanol, water, and an organic extractant | |
| CN102452888A (en) | Method for refining 1-hexene from fischer tropsch synthetic oils | |
| KR101973172B1 (en) | System and method for diesel and jet fuel production using Fischer-Tropsch synthetic oil | |
| CN102471785A (en) | Recovery of butanol from a mixture of butanol, water and an organic extractant | |
| CN102471195A (en) | Recovery of butanol from a mixture of butanol, water, and an organic extractant | |
| EP3307853B1 (en) | Systems and methods for reducing resource consumption in production of alcohol fuel by conversion to hydrocarbon fuels | |
| CN102666457A (en) | Recovery of butanol from a mixture of butanol, water, and an organic extractant | |
| CN103146426B (en) | Method of converting fischer-tropsch synthesis products into naphtha, diesel and liquefied petroleum gas | |
| CN101492360A (en) | Process for the separation of aqueous phase by-product of fischer-tropsch synthesis reaction | |
| CN104208983A (en) | Decarburization method of coal-based indirect liquefaction Fischer-Tropsch synthesis tail gas | |
| CN105152882B (en) | Method for preparing DMM3-5 from hypercoagulable polyoxymethylene dimethyl ether component DMM6+ and dimethoxymethane DMM | |
| CN103205274B (en) | Method for converting fischer-tropsch synthesis products into naphtha, diesel and liquefied petroleum gas | |
| CN101492345B (en) | Method for extractive distillation with salt for separating acetone and methanol | |
| CN104784953A (en) | Reaction product separation system for preparing propylene with methanol and quenching system of reaction product separation system | |
| CN103044217A (en) | Method for separating and recovering non-acidic oxygenated organic substances in Fischer-Tropsch synthesis reaction water | |
| CN102351358B (en) | Method and system for treating phenol-containing acidic water by direct liquefaction with coal | |
| CN107417495A (en) | A kind of ammonia from coal, LNG, the Poly-generation method and device of liquid fuel | |
| CN102719270A (en) | Method and system for separating saturated alkane in liquid hydrocarbon material flow from mixed primary alcohol | |
| CN212504657U (en) | System for hydrogenation and extractive distillation of crude benzene | |
| CN105085165A (en) | Ethylene glycol and diethylene glycol separation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20121010 |