CN106565402A - Method of preparing hexane oil with low benzene content through extractive distillation and hydrogenation - Google Patents
Method of preparing hexane oil with low benzene content through extractive distillation and hydrogenation Download PDFInfo
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- CN106565402A CN106565402A CN201610958494.3A CN201610958494A CN106565402A CN 106565402 A CN106565402 A CN 106565402A CN 201610958494 A CN201610958494 A CN 201610958494A CN 106565402 A CN106565402 A CN 106565402A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
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- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
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- B01J27/224—Silicon carbide
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
- C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
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Abstract
The invention relates to a method of preparing hexane oil with low benzene content through extractive distillation and hydrogenation and belongs to the technical field of petrochemical industry. The method comprises the following steps: sending 6# solvent oil into an extractive distillation tower, carrying out extractive distillation, adding a composite extractant simultaneously, and obtaining rough hexane oil subjected to forerunning on the tower top; and mixing the obtained rough hexane oil and hydrogen, adding the mixture in a hydrogenation reactor, carrying out hydrogenation refining in the presence of a catalyst, carrying out cooling separation on a reaction product to obtain refined hexane oil, and exhausting tail gas completely. According to the method of preparing the hexane oil with low benzene content through extractive distillation and hydrogenation, with integration of an extractive distillation method and a hydrogenation method, the benzene content in the prepared hexane oil is low, and the quality of a product is improved.
Description
Technical field
The present invention relates to a kind of extracting rectifying-Hydrogenation belongs to petrochemical industry skill for the method for the hexane oil of low benzene content
Art field.
Background technology
Normal hexane and the solvent oil product with normal hexane as main component are important refinery products, can be used as solvent
Or the base stock of production medicine intermediate, it is of many uses in Chemical Manufacture.In the market Related product can be roughly divided into 3
Individual grade：Solvent oil product of the hexane content in 65～70 DEG C of 80% or so, boiling range；The hexane product of content 95%；Content 97.5%
Above, smart hexane of the methyl cyclopentane content less than 1%.At present the method for production normal hexane mainly has absorption, rectification hydrogenation etc..
Foreign countries adopt molecular sieve adsorption, such as Watson factories of U.S. Richfield oil companies, with reforming raffinate oil as raw material, pass through
2 or more than 2 bed adsorptions, blood pressure lowering desorptions are recycled, higher (98%) normal hexane of purity is produced.It is domestic many using essence
The technique combined with the hydrogenation phase is evaporated, the normal hexane purity of production is all 60%～80%.Hexane produces azeotropic with benzene at ambient pressure, altogether
68.7 DEG C of boiling temperature, azeotropic composition (95% hexane, 5% benzene), and it is interval in hexane 85～95%, the two relative volatility connects
1 is bordering on, the two is difficult to be separated with conventional distillation.
Therefore, it is necessary to provide a kind of technique of the hexane oil that can produce low benzene content.
The content of the invention
The purpose of the present invention is：A kind of method of the hexane oil that can produce low benzene content is provided, mainly by adopting
Realized with extracting rectifying integrated hydrogenation method.
Technical scheme is as follows：
A kind of extracting rectifying-Hydrogenation comprises the steps for the method for high-purity hexane oil：
1st step, 6# solvent naphthas are sent in extractive distillation column, carry out extracting rectifying, while adding composite extractant, are obtained by tower top
To the thick hexane oil of fore-running；Described composite extractant is made up of following components in percentage by weight：Furfural 70
～80 parts, 4～8 parts of butyl, 10～15 parts of glycerol, 2～4 parts of calcium chloride, 2～4 parts of potassium acetate；Composite extractant
It is 1 with the weight proportion of the addition of 6# solvent naphthas：0.3～0.5；
2nd step, after the thick hexane oil that the 1st step is obtained mixes with hydrogen, adds in hydrogenation reactor in the effect one of catalyst
Hydrofinishing is carried out, product obtains refined hexane oil, tail gas emptying after refrigerated separation.
In the 1st described step, the theoretical cam curve of extractive distillation column is 70～80 pieces；The addition height of extractant is the 4th
～8 pieces of plate heights, the addition height of 6# solvent naphthas is at the 20th～30 piece of plate height.
In the 1st described step, 67～72 DEG C of the tower top temperature of extractive distillation column, tower top pressure（Absolute pressure）Scope 0.09～
0.1Mpa。
In the 1st described step, 115～125 DEG C of the column bottom temperature of extractive distillation column, tower bottom pressure（Absolute pressure）Scope 0.09～
0.1Mpa。
In the 2nd described step, hydrogen is 20～40 with the charge-mass ratio scope of thick hexane oil：1；Reaction temperature 120～
150℃。
In the 2nd described step, reaction pressure is 1～1.5Mpa, and the Feed space velocities scope in reactor is 1～3h-1。
In the 2nd described step, the preparation method of catalyst comprises the steps：By weight, in Ludox 50～60
3～5 parts of ferroso-ferric oxide, 6～12 parts of carborundum, 8～12 parts of cerous nitrate, 4～7 parts of nickel nitrate are added in part, after mix homogeneously,
20～25 parts of sodium carbonate is added, is stirred, then after mixture is dried, obtain powder solid, be washed with deionized into pH
Property, then dried, ball milling, be pressed into after granule, roasting and obtain final product.
The temperature range of described calcination stepses is 350～400 DEG C.
Solid content in described Ludox is 20wt%.
Beneficial effect
Extracting rectifying-Hydrogenation that the present invention is provided is integrated with extracting rectifying and hydrogenation for the method for the hexane oil of low benzene content
Method, makes the benzene content in the hexane oil for preparing very low, improves product quality.
Specific embodiment
The property composition of the 6# solvent naphthas employed in following examples is as follows：
Embodiment 1
1st step, 6# solvent naphthas are sent in extractive distillation column, carry out extracting rectifying, while adding composite extractant, are obtained by tower top
To the thick hexane oil of fore-running, the theoretical cam curve of extractive distillation column is 70 pieces；The addition height of extractant is in the 4th～8 block of column plate
Highly, 6# solvent naphthas addition height at the 20th piece of plate height, 67 DEG C of the tower top temperature of extractive distillation column, tower top pressure
（Absolute pressure）Scope 0.09Mpa, 115 DEG C of the column bottom temperature of extractive distillation column, tower bottom pressure（Absolute pressure）Scope 0.09Mpa；Described
Composite extractant is made up of following components in percentage by weight：70 parts of furfural, 4 parts of butyl, the third three
10 parts of alcohol, 2 parts of calcium chloride, 2 parts of potassium acetate；Composite extractant is 1 with the weight proportion of the addition of 6# solvent naphthas：0.3；
2nd step, after the thick hexane oil that the 1st step is obtained mixes with hydrogen, adds in hydrogenation reactor in the effect one of catalyst
Hydrofinishing is carried out, hydrogen is 40 with the charge-mass ratio scope of thick hexane oil：1；150 DEG C of reaction temperature, reaction pressure is
1.5Mpa, the Feed space velocities scope in reactor is 3h-1, product after refrigerated separation, obtain refined hexane oil, tail gas
Emptying.Wherein, the preparation method of catalyst comprises the steps：By weight, in Ludox（Solid content is 20wt%）60 parts
Middle 5 parts of ferroso-ferric oxide of addition, 12 parts of carborundum, 12 parts of cerous nitrate, 7 parts of nickel nitrate, after mix homogeneously, add sodium carbonate 20
～25 parts, stirring then after mixture is dried, obtains powder solid, be washed with deionized it is neutral to pH, then dried,
Ball milling, it is pressed into after granule, 400 DEG C of roastings and obtains final product.
Embodiment 2
1st step, 6# solvent naphthas are sent in extractive distillation column, carry out extracting rectifying, while adding composite extractant, are obtained by tower top
To the thick hexane oil of fore-running, the theoretical cam curve of extractive distillation column is 80 pieces；The addition height of extractant is in the 8th piece of column plate height
Degree, 6# solvent naphthas addition height at the 30th piece of plate height, 72 DEG C of the tower top temperature of extractive distillation column, tower top pressure（Absolutely
Pressure）Scope 0.1Mpa, 125 DEG C of the column bottom temperature of extractive distillation column, tower bottom pressure（Absolute pressure）Scope 0.1Mpa；Described compound extraction
Take agent to be made up of following components in percentage by weight：80 parts of furfural, 8 parts of butyl, 15 parts of glycerol,
4 parts of calcium chloride, 4 parts of potassium acetate；Composite extractant is 1 with the weight proportion of the addition of 6# solvent naphthas：0.5；
2nd step, after the thick hexane oil that the 1st step is obtained mixes with hydrogen, adds in hydrogenation reactor in the effect one of catalyst
Hydrofinishing is carried out, hydrogen is 40 with the charge-mass ratio scope of thick hexane oil：1；150 DEG C of reaction temperature, reaction pressure is
1.5Mpa, the Feed space velocities scope in reactor is 3h-1, product after refrigerated separation, obtain refined hexane oil, tail gas
Emptying.Wherein, the preparation method of catalyst comprises the steps：By weight, in Ludox（Solid content is 20wt%）60 parts
Middle 5 parts of ferroso-ferric oxide of addition, 12 parts of carborundum, 12 parts of cerous nitrate, 7 parts of nickel nitrate, after mix homogeneously, add sodium carbonate 25
Part, stirring then after mixture is dried, obtains powder solid, be washed with deionized it is neutral to pH, then dried, ball milling,
It is pressed into after granule, 400 DEG C of roastings and obtains final product.
Embodiment 3
1st step, 6# solvent naphthas are sent in extractive distillation column, carry out extracting rectifying, while adding composite extractant, are obtained by tower top
To the thick hexane oil of fore-running, the theoretical cam curve of extractive distillation column is 70～80 pieces；The addition height of extractant is in the 6th block of column plate
Highly, 6# solvent naphthas addition height at the 20th～30 piece of plate height, 70 DEG C of the tower top temperature of extractive distillation column, tower top pressure
Power（Absolute pressure）Scope 0.09Mpa, 119 DEG C of the column bottom temperature of extractive distillation column, tower bottom pressure（Absolute pressure）Scope 0.1Mpa；Described
Composite extractant is made up of following components in percentage by weight：75 parts of furfural, 6 parts of butyl, the third three
13 parts of alcohol, 3 parts of calcium chloride, 3 parts of potassium acetate；Composite extractant is 1 with the weight proportion of the addition of 6# solvent naphthas：0.4；
2nd step, after the thick hexane oil that the 1st step is obtained mixes with hydrogen, adds in hydrogenation reactor in the effect one of catalyst
Hydrofinishing is carried out, hydrogen is 30 with the charge-mass ratio scope of thick hexane oil：1；150 DEG C of reaction temperature, reaction pressure is
1.2Mpa, the Feed space velocities scope in reactor is 2h-1, product after refrigerated separation, obtain refined hexane oil, tail gas
Emptying.Wherein, the preparation method of catalyst comprises the steps：By weight, in Ludox（Solid content is 20wt%）55 parts
Middle 4 parts of ferroso-ferric oxide of addition, 8 parts of carborundum, 10 parts of cerous nitrate, 6 parts of nickel nitrate, after mix homogeneously, add sodium carbonate 22
Part, stirring then after mixture is dried, obtains powder solid, be washed with deionized it is neutral to pH, then dried, ball milling,
It is pressed into after granule, 380 DEG C of roastings and obtains final product.
Reference examples 1
It is with the difference of embodiment 3：Calcium chloride is not added in composite extractant.
1st step, 6# solvent naphthas are sent in extractive distillation column, carry out extracting rectifying, while composite extractant is added, by tower
Top obtains the thick hexane oil of fore-running, and the theoretical cam curve of extractive distillation column is 70～80 pieces；The addition height of extractant is at the 6th piece
Plate height, 6# solvent naphthas addition height at the 20th～30 piece of plate height, 70 DEG C of the tower top temperature of extractive distillation column, tower
Pressure on top surface（Absolute pressure）Scope 0.09Mpa, 119 DEG C of the column bottom temperature of extractive distillation column, tower bottom pressure（Absolute pressure）Scope 0.1Mpa；Institute
The composite extractant stated is made up of following components in percentage by weight：75 parts of furfural, 6 parts of butyl,
13 parts of glycerol, 3 parts of potassium acetate；Composite extractant is 1 with the weight proportion of the addition of 6# solvent naphthas：0.4；
2nd step, after the thick hexane oil that the 1st step is obtained mixes with hydrogen, adds in hydrogenation reactor in the effect one of catalyst
Hydrofinishing is carried out, hydrogen is 30 with the charge-mass ratio scope of thick hexane oil：1；150 DEG C of reaction temperature, reaction pressure is
1.2Mpa, the Feed space velocities scope in reactor is 2h-1, product after refrigerated separation, obtain refined hexane oil, tail gas
Emptying.Wherein, the preparation method of catalyst comprises the steps：By weight, in Ludox（Solid content is 20wt%）55 parts
Middle 4 parts of ferroso-ferric oxide of addition, 8 parts of carborundum, 10 parts of cerous nitrate, 6 parts of nickel nitrate, after mix homogeneously, add sodium carbonate 22
Part, stirring then after mixture is dried, obtains powder solid, be washed with deionized it is neutral to pH, then dried, ball milling,
It is pressed into after granule, 380 DEG C of roastings and obtains final product.
Reference examples 2
It is with the difference of embodiment 3：Butyl is not added in composite extractant.
1st step, 6# solvent naphthas are sent in extractive distillation column, carry out extracting rectifying, while composite extractant is added, by tower
Top obtains the thick hexane oil of fore-running, and the theoretical cam curve of extractive distillation column is 70～80 pieces；The addition height of extractant is at the 6th piece
Plate height, 6# solvent naphthas addition height at the 20th～30 piece of plate height, 70 DEG C of the tower top temperature of extractive distillation column, tower
Pressure on top surface（Absolute pressure）Scope 0.09Mpa, 119 DEG C of the column bottom temperature of extractive distillation column, tower bottom pressure（Absolute pressure）Scope 0.1Mpa；Institute
The composite extractant stated is made up of following components in percentage by weight：75 parts of furfural, 13 parts of glycerol, calcium chloride
3 parts, 3 parts of potassium acetate；Composite extractant is 1 with the weight proportion of the addition of 6# solvent naphthas：0.4；
2nd step, after the thick hexane oil that the 1st step is obtained mixes with hydrogen, adds in hydrogenation reactor in the effect one of catalyst
Hydrofinishing is carried out, hydrogen is 30 with the charge-mass ratio scope of thick hexane oil：1；150 DEG C of reaction temperature, reaction pressure is
1.2Mpa, the Feed space velocities scope in reactor is 2h-1, product after refrigerated separation, obtain refined hexane oil, tail gas
Emptying.Wherein, the preparation method of catalyst comprises the steps：By weight, in Ludox（Solid content is 20wt%）55 parts
Middle 4 parts of ferroso-ferric oxide of addition, 8 parts of carborundum, 10 parts of cerous nitrate, 6 parts of nickel nitrate, after mix homogeneously, add sodium carbonate 22
Part, stirring then after mixture is dried, obtains powder solid, be washed with deionized it is neutral to pH, then dried, ball milling,
It is pressed into after granule, 380 DEG C of roastings and obtains final product.
Reference examples 3
It is with the difference of embodiment 3：Carborundum is not added in the preparation of catalyst.
1st step, 6# solvent naphthas are sent in extractive distillation column, carry out extracting rectifying, while composite extractant is added, by tower
Top obtains the thick hexane oil of fore-running, and the theoretical cam curve of extractive distillation column is 70～80 pieces；The addition height of extractant is at the 6th piece
Plate height, 6# solvent naphthas addition height at the 20th～30 piece of plate height, 70 DEG C of the tower top temperature of extractive distillation column, tower
Pressure on top surface（Absolute pressure）Scope 0.09Mpa, 119 DEG C of the column bottom temperature of extractive distillation column, tower bottom pressure（Absolute pressure）Scope 0.1Mpa；Institute
The composite extractant stated is made up of following components in percentage by weight：75 parts of furfural, 6 parts of butyl,
13 parts of glycerol, 3 parts of calcium chloride, 3 parts of potassium acetate；Composite extractant is 1 with the weight proportion of the addition of 6# solvent naphthas：0.4；
2nd step, after the thick hexane oil that the 1st step is obtained mixes with hydrogen, adds in hydrogenation reactor in the effect one of catalyst
Hydrofinishing is carried out, hydrogen is 30 with the charge-mass ratio scope of thick hexane oil：1；150 DEG C of reaction temperature, reaction pressure is
1.2Mpa, the Feed space velocities scope in reactor is 2h-1, product after refrigerated separation, obtain refined hexane oil, tail gas
Emptying.Wherein, the preparation method of catalyst comprises the steps：By weight, in Ludox（Solid content is 20wt%）55 parts
Middle 4 parts of ferroso-ferric oxide of addition, 10 parts of cerous nitrate, 6 parts of nickel nitrate, after mix homogeneously, add 22 parts of sodium carbonate, stir, then
After mixture is dried, powder solid is obtained, be washed with deionized neutral to pH, then dried, ball milling, be pressed into
Obtain final product after grain, 380 DEG C of roastings.
As can be seen from the table, the hexane oil for being prepared by the present invention has higher normal hexane content, and benzene content is very
It is low.In addition, embodiment 3 is for reference examples 1, do not add calcium chloride to improve extraction efficiency in composite extractant, make
Benzene content declines, it may be possible to due to the separating degree that can be improved in extraction process that is introduced into of calcium chloride；Additional embodiment 3 is relative to right
As usual for 2, butyl is added in composite extractant, can also increase the separation efficiency of composite extractant；Implement
Example 3 during catalyst is prepared, introduces carborundum compared with reference examples 3 in Ludox, due to Ludox in
Grain is relatively thin, and the addition of carborundum can be such that the silicon oxide in Ludox is attached on granule, after sintering, can occur living
Load on active rare-earth granule and silicon oxide, and silicon oxide particle appendix can make the catalysis of catalyst on silicon-carbide particle
Efficiency is improved, and then reduces benzene content.
Claims (9)
1. a kind of extracting rectifying-Hydrogenation is for the oily method of high-purity hexane, it is characterised in that comprise the steps：
1st step, 6# solvent naphthas are sent in extractive distillation column, carry out extracting rectifying, while adding composite extractant, are obtained by tower top
To the thick hexane oil of fore-running；Described composite extractant is made up of following components in percentage by weight：Furfural 70
～80 parts, 4～8 parts of butyl, 10～15 parts of glycerol, 2～4 parts of calcium chloride, 2～4 parts of potassium acetate；Composite extractant
It is 1 with the weight proportion of the addition of 6# solvent naphthas：0.3～0.5；
2nd step, after the thick hexane oil that the 1st step is obtained mixes with hydrogen, adds in hydrogenation reactor in the effect one of catalyst
Hydrofinishing is carried out, product obtains refined hexane oil, tail gas emptying after refrigerated separation.
2. extracting rectifying-Hydrogenation according to claim 1 is for the oily method of high-purity hexane, it is characterised in that：Described
In 1st step, the theoretical cam curve of extractive distillation column is 70～80 pieces；Extractant addition height in the 4th～8 piece of plate height,
The addition height of 6# solvent naphthas is at the 20th～30 piece of plate height.
3. extracting rectifying-Hydrogenation according to claim 1 is for the oily method of high-purity hexane, it is characterised in that：Described
In 1st step, 67～72 DEG C of the tower top temperature of extractive distillation column, tower top pressure（Absolute pressure）0.09～0.1Mpa of scope.
4. extracting rectifying-Hydrogenation according to claim 1 is for the oily method of high-purity hexane, it is characterised in that：Described
In 1st step, 115～125 DEG C of the column bottom temperature of extractive distillation column, tower bottom pressure（Absolute pressure）0.09～0.1Mpa of scope.
5. extracting rectifying-Hydrogenation according to claim 1 is for the oily method of high-purity hexane, it is characterised in that：Described
In 2nd step, hydrogen is 20～40 with the charge-mass ratio scope of thick hexane oil：1；120～150 DEG C of reaction temperature.
6. extracting rectifying-Hydrogenation according to claim 1 is for the oily method of high-purity hexane, it is characterised in that：Described
In 2nd step, reaction pressure is 1～1.5Mpa, and the Feed space velocities scope in reactor is 1～3h-1。
7. extracting rectifying-Hydrogenation according to claim 1 is for the oily method of high-purity hexane, it is characterised in that：Described
In 2nd step, the preparation method of catalyst comprises the steps：By weight, four are added to aoxidize in 50～60 parts of Ludox
3～5 parts of three-iron, 6～12 parts of carborundum, 8～12 parts of cerous nitrate, 4～7 parts of nickel nitrate, after mix homogeneously, add sodium carbonate 20
～25 parts, stirring then after mixture is dried, obtains powder solid, be washed with deionized it is neutral to pH, then dried,
Ball milling, it is pressed into after granule, roasting and obtains final product.
8. extracting rectifying-Hydrogenation according to claim 1 is for the oily method of high-purity hexane, it is characterised in that：Described
The temperature range of calcination stepses is 350～400 DEG C.
9. extracting rectifying-Hydrogenation according to claim 1 is for the oily method of high-purity hexane, it is characterised in that：Described
Solid content in Ludox is 20wt%.
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| CN201510927195 | 2015-12-14 | ||
| CN2015109271959 | 2015-12-14 |
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| CN106565402A true CN106565402A (en) | 2017-04-19 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2920113A (en) * | 1956-07-27 | 1960-01-05 | Phillips Petroleum Co | Recovery of a vaporizable hydrocarbon from liquid mixtures |
| CN101234947A (en) * | 2008-02-15 | 2008-08-06 | 南京大学 | Method for removing micro-benzene in solvent oil or hexane refining process |
| CN101696359A (en) * | 2009-10-30 | 2010-04-21 | 河北科技大学 | Method for preparing normal hexan solvent oil by using absorption-method deep debenzolization |
| CN106433777A (en) * | 2016-08-25 | 2017-02-22 | 王树宽 | Method for preparing monomer naphthenic hydrocarbon and megilp by using coal cornerstone cerebral |
-
2016
- 2016-10-28 CN CN201610958494.3A patent/CN106565402B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2920113A (en) * | 1956-07-27 | 1960-01-05 | Phillips Petroleum Co | Recovery of a vaporizable hydrocarbon from liquid mixtures |
| CN101234947A (en) * | 2008-02-15 | 2008-08-06 | 南京大学 | Method for removing micro-benzene in solvent oil or hexane refining process |
| CN101696359A (en) * | 2009-10-30 | 2010-04-21 | 河北科技大学 | Method for preparing normal hexan solvent oil by using absorption-method deep debenzolization |
| CN106433777A (en) * | 2016-08-25 | 2017-02-22 | 王树宽 | Method for preparing monomer naphthenic hydrocarbon and megilp by using coal cornerstone cerebral |
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