CN204079906U - High purity alkane solvent oil preparation facilities - Google Patents
High purity alkane solvent oil preparation facilities Download PDFInfo
- Publication number
- CN204079906U CN204079906U CN201420425822.XU CN201420425822U CN204079906U CN 204079906 U CN204079906 U CN 204079906U CN 201420425822 U CN201420425822 U CN 201420425822U CN 204079906 U CN204079906 U CN 204079906U
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- CN
- China
- Prior art keywords
- tank
- condenser
- rectifying tower
- digester
- solvent oil
- 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.)
- Expired - Lifetime
Links
- 239000002904 solvent Substances 0.000 title claims abstract description 22
- 150000001335 aliphatic alkanes Chemical class 0.000 title claims abstract description 18
- 238000002360 preparation method Methods 0.000 title claims abstract description 13
- 238000001179 sorption measurement Methods 0.000 claims abstract description 16
- 239000003610 charcoal Substances 0.000 claims abstract description 10
- 230000002745 absorbent Effects 0.000 claims abstract description 8
- 239000002250 absorbent Substances 0.000 claims abstract description 8
- 238000004061 bleaching Methods 0.000 claims abstract description 8
- 238000009833 condensation Methods 0.000 claims description 12
- 230000005494 condensation Effects 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 238000009835 boiling Methods 0.000 abstract description 13
- 239000002994 raw material Substances 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 238000000034 method Methods 0.000 abstract description 4
- 239000000126 substance Substances 0.000 abstract description 4
- 238000010521 absorption reaction Methods 0.000 abstract description 3
- 238000006477 desulfuration reaction Methods 0.000 abstract description 3
- 230000023556 desulfurization Effects 0.000 abstract description 3
- 239000004927 clay Substances 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 20
- 238000010992 reflux Methods 0.000 description 14
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- 239000005864 Sulphur Substances 0.000 description 5
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- AFABGHUZZDYHJO-UHFFFAOYSA-N 2-Methylpentane Chemical compound CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 4
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 2
- 229910052794 bromium Inorganic materials 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000004904 shortening Methods 0.000 description 2
- 239000003905 agrochemical Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001555 benzenes Chemical class 0.000 description 1
- 210000000988 bone and bone Anatomy 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 150000001924 cycloalkanes Chemical class 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000008157 edible vegetable oil Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000004434 industrial solvent Substances 0.000 description 1
- 239000000976 ink Substances 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 239000010985 leather Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 239000007965 rubber solvent Substances 0.000 description 1
- 239000002966 varnish Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model relates to a kind of high purity alkane solvent oil preparation facilities, and described device comprises head tank (1), the first digester (2), the second digester (3), bleaching earth adsorption tank (4), absorbent charcoal adsorption tank (5), still kettle (6), rectifying tower (7), the first condenser (8), return tank (9), the second condenser (10), receiving tank (11), tundish (12) and finished pot (13).Its method is through twice chemical desulfurization by the raw material in head tank, then high-efficient activated clay is utilized to adsorb, decolour through charcoal absorption again, and then successively through still kettle and rectifying tower, on rectifying tower, the cut on top is through the first condenser, return tank, the second condenser, is then made by receiving tank, tundish and finished pot.Product boiling range is narrow, and content purity is high, and production efficiency is high.
Description
Technical field
The utility model relates to a kind of high purity alkane solvent oil preparation facilities, belongs to solvent oil and refines purification techniques field.
Background technology
Alkane solvent oil system crude oil Light ends through the isolated product of deep processing, can be divided into positive structure, isomery, cycloalkanes and have a small amount of aromatic hydrocarbons mix wherein.
Domestic market GB product is 6# industrial solvent, 6# solvent for extraction, hexane solvent oil, 120# rubber solvent naphtha, 200# varnish makers' and painters' naphtha, kerosene, white oil; Enterprise is designated as D40, D60, D8, D90, D110 etc.According to incompletely statistics, 400-500 kind is had; By boiling range classification, by flash-point classification, classification by use, but its physical and chemical index is outward appearance substantially, look number, density, boiling range, aromaticity content, sulphur content, bromine number etc., and wherein boiling range is the key index of product purity height.Because the solvent oil product of a certain single-component (individual molecule), boiling range only has a boiling point.
Solvent oil is widely used in the aspects such as edible oil, printing-ink, leather, agricultural chemicals, medicine intermediate, chemical industry polymerization, closely related with the clothing, food, lodging and transportion--basic necessities of life of people.
Domestic solvent oil produce mostly with petroleum naphtha or processed raffinate oil as raw material, its boiling range is between 50-190 DEG C, i.e. C5-C9, meets international 6#, 120#, 200# solvent oil, its boiling range is respectively at 60-90,80-120,140-200, its initial boiling point to final boiling point at 30 DEG C, 40 DEG C, 60 DEG C.
CN200910083134.3 discloses a kind of preparation method of narrow fraction nontoxic high-purity isohexane.The method is raw material with reforming raffinate oil, selects active metal nickel to be benzene series catalytic hydrogenation catalyst, under the effect of catalyzer, carries out total composition shortening, de-aromatizing and desulfurizing; Product through de-aromatizing and desulfurizing is introduced lightness-removing column, removes the light constituent of cut≤60 DEG C; Introduce weight-removing column by through de-light residue cut, remove the heavy constituent of cut >=75 DEG C; Carrying out meticulous fractionation by introducing isohexane tower through de-heavy residue cut (60 ~ 75 DEG C), cutting 60 ~ 64.5 DEG C of cuts and being required product.But adopt shortening Porous deproteinized bone, complex process, energy consumption is large.And the cut that can separate is only 60 ~ 64.5 DEG C of cuts, other boiling range is difficult to accomplish close-cut fraction high purity.
Summary of the invention
The purpose of this utility model is to overcome above-mentioned deficiency, there is provided that a kind of fraction is narrow, alkane component is more single, other assorted component is relatively few, purity is higher, sulphur content is less than 0.01% lower than 10PPM, aromatic hydrocarbons (benzene) content, normal hexane content is less than 0.1%, the high purity alkane solvent oil preparation facilities of Determination of Alkane Content more than 99%.
The purpose of this utility model is achieved in that a kind of high purity alkane solvent oil preparation facilities, and described device comprises head tank, the first digester, the second digester, bleaching earth adsorption tank, absorbent charcoal adsorption tank, still kettle, rectifying tower, the first condenser, return tank, the second condenser, receiving tank, tundish and finished pot.
Head tank, the first digester, the second digester, bleaching earth adsorption tank, absorbent charcoal adsorption tank, still kettle, rectifying tower are arranged in series successively, described rectifying tower tower top is arranged in series the first condenser, described first condenser is connected with return tank, described return tank is connected with rectifying tower by the second condenser, described return tank is series connection closed cans successively, tundish and finished pot also, and described second condenser is also connected with receiving tank.
First time condensation is normal temperature water temperature, and water of condensation is by refrigerator setup control for the second time, the low 30-50 degree of water temperature control ratio object fraction, and such as object fraction is 100 degree, and water temperature controls at 50-70 degree;
The reflux ratio of 1.5-2 grade is reduced during throughput ratio condensation during time condensation.
Compared with prior art, the beneficial effects of the utility model are:
The utility model adopts two-layer desulfurization, again respectively through twice absorption, the high alkane solvent oil of preparation, purity is higher, sulphur content is less than 0.01% lower than 10PPM, aromatic hydrocarbons (benzene) content, normal hexane content is less than 0.1%, and Determination of Alkane Content, more than 99%, adopts twice reflux condensation mode, boiling range is narrow, content purity is high, and production efficiency is high, and energy consumption is low.
Accompanying drawing explanation
Fig. 1 is the structural representation of the utility model high purity alkane solvent oil preparation facilities.
Fig. 2 is employing condensing reflux and twice condensing reflux energy consumption comparison of production figure,
Wherein:
Head tank 1, first digester 2, second digester 3, bleaching earth adsorption tank 4, absorbent charcoal adsorption tank 5, still kettle 6, rectifying tower 7, first condenser 8, return tank 9, second condenser 10, receiving tank 11, tundish 12, finished pot 13.
Embodiment
See Fig. 1, a kind of high purity alkane solvent oil preparation facilities that the utility model relates to, described device comprises head tank 1, first digester 2, second digester 3, bleaching earth adsorption tank 4, absorbent charcoal adsorption tank 5, still kettle 6, rectifying tower 7, first condenser 8, return tank 9, second condenser 10, receiving tank 11, tundish 12 and finished pot 13.
Head tank 1, first digester 2, second digester 3, bleaching earth adsorption tank 4, absorbent charcoal adsorption tank 5, still kettle 6, rectifying tower 7 are arranged in series successively, described rectifying tower 7 tower top is arranged in series the first condenser 8, described first condenser 8 is connected with return tank 9, described return tank 9 is connected with rectifying tower 7 by the second condenser 10, described return tank 9 is series connection closed cans successively 11, tundish 12 and finished pot 13 also, and described second condenser 10 is also connected with receiving tank 11.
A kind of high purity alkane solvent oil preparation method, by the raw material in head tank through twice chemical desulfurization, then high-efficient activated clay is utilized to adsorb, decolour through charcoal absorption again, and then successively through still kettle and rectifying tower, on rectifying tower, the cut on top is through the first condenser, return tank, the second condenser, strictly controls flow, water temperature, then makes narrow-fraction high-purity degree alkane solvent oil by receiving tank, tundish and finished pot.
Described property of raw material: 1) boiling range is between 60 DEG C-200 DEG C; 2) sulphur content is within 20PPM; 3) aromatic hydrocarbons total content is less than less than 0.1%; 4) look is number more than+28; 5) bromine number is less than 100.
First time condensation is normal temperature water temperature, and water of condensation is by refrigerator setup control for the second time, the low 30-50 degree of water temperature control ratio object fraction, and such as object fraction is 100 degree, and water temperature controls at 50-70 degree;
The reflux ratio of 1.5-2 grade is reduced during throughput ratio condensation during time condensation.
The principle of rectifying is that reflux ratio determines the purity of product under theoretical tray certain (constant).Reflux ratio=quantity of reflux/quantum of output.Adopt the method for a condensing reflux in prior art, in actually operating, energy consumption is comparatively large, and tower top temperature domination number and actual sample intermediate controlled metrical error are at 5-8 degree.
Can quantity of reflux be reduced after secondary back liquid condensing control temperature, reduce reflux ratio, significantly can reduce reflux ratio.
Adopt a condensing reflux and twice condensing reflux energy consumption comparison of production figure, as Fig. 2.
The solvent oil made, purity is higher, and sulphur content is less than 0.01% lower than 10PPM, aromatic hydrocarbons (benzene) content, normal hexane content is less than 0.1%, and Determination of Alkane Content is more than 99%.
Claims (2)
1. a high purity alkane solvent oil preparation facilities, is characterized in that: described device comprises head tank (1), the first digester (2), the second digester (3), bleaching earth adsorption tank (4), absorbent charcoal adsorption tank (5), still kettle (6), rectifying tower (7), the first condenser (8), return tank (9), the second condenser (10), receiving tank (11), tundish (12) and finished pot (13);
Described head tank (1), first digester (2), second digester (3), bleaching earth adsorption tank (4), absorbent charcoal adsorption tank (5), still kettle (6), rectifying tower (7) is arranged in series successively, described rectifying tower (7) tower top is arranged in series the first condenser (8), described first condenser (8) is connected with return tank (9), described return tank (9) is connected with rectifying tower (7) by the second condenser (10), described return tank (9) is series connection closed cans successively (11) also, tundish (12) and finished pot (13), described second condenser (10) is also connected with receiving tank (11).
2. high purity alkane solvent oil preparation facilities according to claim 1, is characterized in that: described first time condensation is normal temperature water temperature, and second time condensation water of condensation is by refrigerator setup control.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420425822.XU CN204079906U (en) | 2014-07-31 | 2014-07-31 | High purity alkane solvent oil preparation facilities |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420425822.XU CN204079906U (en) | 2014-07-31 | 2014-07-31 | High purity alkane solvent oil preparation facilities |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204079906U true CN204079906U (en) | 2015-01-07 |
Family
ID=52172642
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420425822.XU Expired - Lifetime CN204079906U (en) | 2014-07-31 | 2014-07-31 | High purity alkane solvent oil preparation facilities |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204079906U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104119951A (en) * | 2014-07-31 | 2014-10-29 | 江阴市五洋化工有限公司 | Device for preparing high-purity alkane solvent oil and preparation method of high-purity alkane solvent oil |
-
2014
- 2014-07-31 CN CN201420425822.XU patent/CN204079906U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104119951A (en) * | 2014-07-31 | 2014-10-29 | 江阴市五洋化工有限公司 | Device for preparing high-purity alkane solvent oil and preparation method of high-purity alkane solvent oil |
| CN104119951B (en) * | 2014-07-31 | 2016-07-06 | 江阴市五洋化工有限公司 | High-purity alkane solvent oil preparation facilities and preparation method thereof |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170522 Address after: 214415, C, 75-80, 301, Gu Gu Road, No. 29, Gu Gu Town, Jiangsu, Jiangyin Co-patentee after: JIANGSU WUYANG HYDROCARBON TECHNICAL CO.,LTD. Patentee after: JIANGYIN WUYANG CHEMICAL Co.,Ltd. Address before: Zhu Tang Zhen Zhu Huang Lu 85 No. 214415 Jiangsu city of Wuxi province Jiangyin City Patentee before: JIANGYIN WUYANG CHEMICAL Co.,Ltd. |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170606 Address after: 214415, C, 75-80, 301, Gu Gu Road, No. 29, Gu Gu Town, Jiangsu, Jiangyin Co-patentee after: JIANGSU WUYANG HYDROCARBON TECHNICAL CO.,LTD. Patentee after: JIANGYIN WUYANG CHEMICAL Co.,Ltd. Address before: Zhu Tang Zhen Zhu Huang Lu 85 No. 214415 Jiangsu city of Wuxi province Jiangyin City Patentee before: JIANGYIN WUYANG CHEMICAL Co.,Ltd. |
|
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20150107 |