CN103833499A - Preparation method of high-purity isohexane solvent oil - Google Patents
Preparation method of high-purity isohexane solvent oil Download PDFInfo
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- CN103833499A CN103833499A CN201210490616.2A CN201210490616A CN103833499A CN 103833499 A CN103833499 A CN 103833499A CN 201210490616 A CN201210490616 A CN 201210490616A CN 103833499 A CN103833499 A CN 103833499A
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- AFABGHUZZDYHJO-UHFFFAOYSA-N 2-Methylpentane Chemical compound CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 title claims abstract description 86
- 239000002904 solvent Substances 0.000 title claims abstract description 17
- 238000002360 preparation method Methods 0.000 title claims abstract description 15
- 238000009835 boiling Methods 0.000 claims abstract description 19
- 238000004821 distillation Methods 0.000 claims abstract description 16
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims abstract description 12
- 238000002407 reforming Methods 0.000 claims description 13
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 6
- 239000000843 powder Substances 0.000 claims description 6
- 239000003054 catalyst Substances 0.000 claims description 5
- 238000005984 hydrogenation reaction Methods 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 229910001868 water Inorganic materials 0.000 claims description 4
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 3
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 claims description 3
- 229910021502 aluminium hydroxide Inorganic materials 0.000 claims description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000005470 impregnation Methods 0.000 claims description 3
- 238000000465 moulding Methods 0.000 claims description 3
- 229910017604 nitric acid Inorganic materials 0.000 claims description 3
- 244000275012 Sesbania cannabina Species 0.000 claims 1
- 238000005520 cutting process Methods 0.000 abstract description 11
- 238000000034 method Methods 0.000 abstract description 9
- 238000005194 fractionation Methods 0.000 abstract description 8
- 239000002994 raw material Substances 0.000 abstract description 7
- 150000001336 alkenes Chemical class 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 5
- 150000004945 aromatic hydrocarbons Chemical class 0.000 abstract description 4
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 28
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 16
- 239000000470 constituent Substances 0.000 description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 4
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 3
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 3
- 229910052794 bromium Inorganic materials 0.000 description 3
- 230000003009 desulfurizing effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 241000219782 Sesbania Species 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000007323 disproportionation reaction Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 230000009257 reactivity Effects 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- HIXDQWDOVZUNNA-UHFFFAOYSA-N 2-(3,4-dimethoxyphenyl)-5-hydroxy-7-methoxychromen-4-one Chemical compound C=1C(OC)=CC(O)=C(C(C=2)=O)C=1OC=2C1=CC=C(OC)C(OC)=C1 HIXDQWDOVZUNNA-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 241000183024 Populus tremula Species 0.000 description 1
- 241000219793 Trifolium Species 0.000 description 1
- 239000003377 acid catalyst Substances 0.000 description 1
- 150000001555 benzenes Chemical class 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 1
- 150000005826 halohydrocarbons Chemical class 0.000 description 1
- BNZBILCDCUJDPC-UHFFFAOYSA-N hexane;2-methylpentane Chemical compound CCCCCC.CCCC(C)C BNZBILCDCUJDPC-UHFFFAOYSA-N 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000012454 non-polar solvent Substances 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 239000000341 volatile oil Substances 0.000 description 1
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Abstract
The invention relates to a preparation method of high-purity isohexane solvent oil; hydrofining the reformed raffinate oil by adopting a nickel catalyst, and adopting the following process conditions: the pressure is 0.2-2.0 Mpa, the temperature is 80-220 ℃, the airspeed is 2.0-4.0 h < -1 >, and the hydrogen-oil ratio is 40-200 v/v; cutting off fractions of more than 65 ℃ from hydrorefined reformed raffinate oil on a true boiling point distiller, repeating the steps for 3 times to collect fractions of less than or equal to 65 ℃, cutting the collected fractions of less than or equal to 65 ℃ on the true boiling point distiller, collecting products of different temperature sections from a tower top distillate product by adopting a plurality of small bottles, wherein each 0.5 ℃ is a distillation section, and obtaining an isohexane product with the purity of 95.323% at the temperature of 59.5-62 ℃; the method takes the reformed raffinate oil as a raw material, adopts a high-activity nickel catalyst to remove aromatic hydrocarbon and olefin through hydrofining, and obtains an isohexane product with the purity of not less than 95 percent through twice cutting and fractionation on a real boiling point distiller.
Description
Technical field
The present invention relates to a kind of preparation method of high purity isohexane solvent oil, is a kind of by preparation method refining, that separation means obtains high purity product.
Background technology
Be accompanied by the rapid growth of national economy, the demand of various varsol products constantly increases, and day by day deep to health environment-friendly understanding of people, make every profession and trade also propose stricter requirement to the quality of varsol, therefore, from output and two aspects of quality, varsol has the huge market space and development space in China, special solvent oil is developed into from usual vehicle oil to the demand of solvent oil in market, wherein low impurity, narrow boiling range, just highly purified/isoparaffin solvent oil has good solvability because of it, higher security, less toxicity, suitable volatility, and alternative other solvent oil products are subject to market favor gradually for the feasibility of every profession and trade.
Isohexane is a kind of non-polar solvent, water insoluble, is dissolved in ethanol, ether, can also dissolve other hydro carbons and halohydrocarbon, be mainly used in polymerization solvent, precision instrumentation cleans and oil is released agent, essential oil thinners etc., are mainly used in the product scopes such as poisonless spray agent, solvent, clean-out system.At present, isohexane is domestic has part refinery to produce, for example, Lanzhou, Liaoyang, Dalian, the Yanshan Mountain, Yang Zi, output is many in 10,000 tons/year, on the basis that meets our factory's consumption, sell to all parts of the country, sales situation is good, due to the few huge market demand of isohexane output, price was always in ascendant trend in recent years, the isohexane price of purity requirement in August 95% in 2012 is 12000 yuan/ton of left and right, isohexane at present in China in state in short supply, major part depends on import, China now only has one of Herpu Chemical Co., Ltd., Guangzhou to stablize provides isohexane in a large number, there is the isohexane production marketing of different purity on the ground such as the flourishing city of coastal economy and Liaoyang, northeast, sell and do not produce but mostly only be, and supply is all little.
CN95121454.3 discloses a kind of preparation method of the product that contains Trimethylmethane/isohexane.The method comprises sends iso-pentane raw material into disproportionation step, under the existence of alkene and/or senior branched paraffin by with acidity H
obe greater than the temperature contact between 0～150 ° of C of 8 acid catalyst and by iso-pentane raw material disproportionation, take out the product that contains Trimethylmethane/isohexane.
CN200410027004.5 discloses a kind of manufacture method of isohexane solvent.The method, taking 6# solvent oil as raw material, adopts packing tower fractionation cutting to collect the cut of 58～63 DEG C, and this cut finally obtains containing more than 95% isohexane through hydrogenation.The method list tower is produced continuously, less investment, and floor space is little, and operation, management are simply, efficient.
CN200910083134.3 discloses a kind of preparation method of narrow fraction nontoxic high-purity isohexane.The method is taking reforming raffinate oil as raw material, and selecting active metal nickel is benzene series catalytic hydrogenation catalyst, carries out total composition shortening, de-aromatizing and desulfurizing under the effect of catalyzer; Product through de-aromatizing and desulfurizing is introduced to lightness-removing column, remove the light constituent of cut≤60 DEG C; To introduce weight-removing column through de-light residue cut, remove the heavy constituent of cut >=75 DEG C; Carry out meticulous fractionation by introducing isohexane tower through de-heavy residue cut (60～75 DEG C), cut 60～64.5 DEG C of cuts and be required product.The method catalyzer operational condition is relatively gentle, and de-aromatizing and desulfurizing effect is remarkable, features simple and practical process, and stable and reliable product quality, economical efficiency are high.
CN201110263745.3 processing method by thick hexane extraction normal hexane, isohexane, CN201120334519.5 device by thick hexane extraction normal hexane, isohexane, CN201120334491.5 hydro-refining unit by thick hexane extraction normal hexane, isohexane, CN201120334470.3 fractionation plant by thick hexane extraction normal hexane, isohexane, above-mentioned four patents have been carried out comprehensive description from hydrofining unit and four aspects of product fractionation unit of processing method, industrial installation, device to producing just/isohexane.
Summary of the invention
The object of this invention is to provide a kind of preparation method of high purity isohexane solvent oil, taking reforming raffinate oil as raw material, adopt high reactivity nickel catalyst hydrofining Arene removal and alkene, on true boiling point distillation instrument, obtain purity by cutting twice fractionation and be not less than 95% isohexane product.
The preparation method of high purity isohexane solvent oil of the present invention adopts following technical scheme:
(1) preparation of high reactivity nickel catalyst, after adding sesbania powder, nitric acid, phosphoric acid, water to mediate in aluminium hydroxide dry powder, extruded moulding, 120 DEG C of dry 2h, 550 DEG C of roasting 4h, make support of the catalyst; Prepare nickeliferous and solution promoter metal, equivalent impregnation to alumina supporter, 120 DEG C of dry 2h, 500 DEG C of roasting 4h, make catalyzer, the active metal of catalyzer is taking its content of NiO as 25%～50%, preferred metal content is 30%～35%;
(2) reforming raffinate oil hydrofining on 100mL small hydrogenation device, the nickel catalyst that adopts step 1 to prepare, at pressure range 0.2～2.0Mpa, 80～220 DEG C of temperature ranges, air speed scope 2.0～4.0h
-1, under the processing condition of hydrogen-oil ratio scope 40～200v/v, product sulphur content < 0.5 μ g/g, bromine index < 0.2mgBr/100g, aromaticity content < 0.001m%.
(3), will on true boiling point distillation instrument, excise 65 DEG C of cuts of > through the hydrorefined reforming raffinate oil of step 2, this true boiling point distillation instrument meets ASTM D2892 standard, 15 of theoretical plate numbers, tower reactor volume 20L, trim the top of column is than 10～20:1, and tower reactor heats aperture 20%～40%.
(4), step 3 is repeated to 3 times and collect≤65 DEG C of cuts, ≤ 65 DEG C of fractions consistings are in table 1, by collect≤65 DEG C of cuts cut on true boiling point distillation instrument again, trim the top of column compares 20:1, tower reactor heating aperture 20%, tower top distillates product and adopts multiple bottles to collect differing temps section products, and every 0.5 DEG C is a cut section, obtains purity and be 95.323% isohexane product between 59.5-62 DEG C.
Invention effect
1, the present invention carries out hydrogenation taking reforming raffinate oil as raw material, and catalyst activity is high, and product property is good, can carry out according to the finished product target comprehensive utilization of separation to raffinating oil, and reducing target product needs rear refining necessity.
2, the nickel catalyst that prepared by the present invention can make hydrogenated products take off to containing hardly alkene and aromatic hydrocarbons under the processing condition that relax, and hydrofining effect is very remarkable.
3, the present invention has carried out cutting twice fractionation to hydrorefined raffinating oil on the true boiling point distillation instrument of 15, use cleverly every 0.5 DEG C to be one and to heat up in a steamer Fractional Collections product, investigate the purity of each cut section isohexane, search out optimum cutting temperature section.
4, the present invention is in product separation process, adopts every 0.5 DEG C of multiple bottles to be one and to heat up in a steamer Fractional Collections product, is the key of obtaining high purity isohexane product on the lower true boiling point distillation instrument of theoretical plate number.
Brief description of the drawings
Fig. 1 flowsheeting schema.
Embodiment
A preparation method for high purity isohexane solvent oil, is characterized in that:
(1), the preparation of nickel catalyst
After adding sesbania powder, nitric acid, phosphoric acid, water to mediate in aluminium hydroxide dry powder, extruded moulding, 120 DEG C of dry 2h, 550 DEG C of roasting 4h, make support of the catalyst; Prepare nickeliferous and solution promoter metal, equivalent impregnation to alumina supporter, 120 DEG C of dry 2h, 500 DEG C of roasting 4h, make catalyzer.
The active metal of catalyzer is taking its content of NiO as 25m%～50m%, and preferred metal content is 30m%～35m%, and profile is trifolium bar Ф 1.3 × 3～8mm, and bulk density is 0.9～1.1g/ml, and specific surface area is 120～160cm
2/ g, intensity>=220N/cm.
(2) reforming raffinate oil hydrofining removes sulphur, alkene and aromatic hydrocarbons
In reforming raffinate oil, isohexane content is 18%～35%, and boiling range≤130 DEG C, sulphur content≤3.0 μ g/g, bromine index≤4000mgBr/100g, aromaticity content are 0.90%～1.90%.
Reforming raffinate oil hydrofining on 100mL small hydrogenation device, the nickel catalyst that adopts step 1 to prepare, at pressure range 0.2～2.0Mpa, 80～220 DEG C of temperature ranges, air speed scope 2.0～4.0h
-1, under the processing condition of hydrogen-oil ratio scope 40～200v/v, product sulphur content < 0.5 μ g/g, bromine index < 0.2mgBr/100g, aromaticity content < 0.001m%.
(3), on true boiling point distillation instrument, remove heavy constituent
To on true boiling point distillation instrument, excise 65 DEG C of > through the hydrorefined reforming raffinate oil of step 2, this true boiling point distillation instrument meets ASTM D2892 standard, 15 of theoretical plate numbers, tower reactor volume 20L, trim the top of column is than 10～20:1, and tower reactor heats aperture 20%～40%.
(4), light constituent segmentation cutting and product-collecting
The product composition (wt%) that table 1 is collected
| Cut title | Yield, % | Normal hexane | Isohexane | Carbon six naphthenic hydrocarbon |
| ≤ 65 DEG C of cuts | / | 14.121 | 76.593 | 4.514 |
| 58.5-59.5℃ | 4.70 | 1.55 | 91.880 | 0.242 |
| 59.5-60℃ | 5.15 | 1.994 | 93.652 | 0.449 |
| 60-60.5°C | 6.55 | 2.463 | 95.224 | 0.531 |
| 60.5-61℃ | 9.46 | 2.605 | 96.624 | 0.637 |
| 61-61.5℃ | 7.53 | 3.055 | 96.129 | 0.788 |
| 61.5-62℃ | 6.32 | 4.573 | 94.364 | 0.978 |
| 62-62.5℃ | 5.87 | 5.681 | 92.810 | 1.233 |
| 59.5-62℃ | 35.01 | 3.028 | 95.323 | 0.713 |
The catalyzer, hydrofining technology technology and the isohexane product separation purification mode that adopt above-mentioned preparation, the high purity isohexane solvent oil product property of gained is in table 2.
Table 2 isohexane product property
(5), the software simulation of double tower fractionation cutting calculates
True boiling point distillation instrument theoretical plate number deficiency, can not obtain the isohexane product of purity requirement by single flash cutting, the hydrorefined reforming raffinate oil of step 2 calculates distillation cutting isohexane product on Aspen HYSYS flowsheeting software, adopt cascade towers successively to remove heavy constituent and light constituent, the schema that simulation adopts is shown in Fig. 1.Reforming raffinate oil 7 enters tower 1, removes restructuring 4, and light constituent 3 enters tower 2, and tower top is discharged undesirable components 5, obtains isohexane product 6 at the bottom of tower.
The operating parameters of simulation is in table 3, and isohexane product purity and yield are respectively 95.380% and 87.30%.
Table 3 operating parameters
| Project | Tower 1 | Tower 2 |
| Theoretical plate number, piece | 40 | 20 |
| Reflux ratio, m/m | 8 | 20 |
| Tower top/bottom pressure, KPa | 5/50 | 5/50 |
| Tower top temperature, DEG C | 57.17 | 37.68 |
| Tower reactor temperature, DEG C | 97.51 | 72.72 |
Claims (1)
1. a preparation method for high purity isohexane solvent oil, is characterized in that:
(1) preparation of nickel catalyst, after adding sesbania powder, nitric acid, phosphoric acid, water to mediate in aluminium hydroxide dry powder, extruded moulding, 120 DEG C of dry 2h, 550 DEG C of roasting 4h, make support of the catalyst; Prepare nickeliferous and solution promoter metal, equivalent impregnation to alumina supporter, 120 DEG C of dry 2h, 500 DEG C of roasting 4h, make catalyzer, the active metal of catalyzer is taking its content of NiO as 25m%～50m%;
(2) reforming raffinate oil hydrofining on 100mL small hydrogenation device, the nickel catalyst that adopts step 1 to prepare, processing condition: pressure is 0.2～2.0Mpa, temperature is 80～220 DEG C, air speed is 2.0～4.0h
-1, hydrogen-oil ratio is 40～200v/v;
(3) will on true boiling point distillation instrument, excise 65 DEG C of cuts of > through the hydrorefined reforming raffinate oil of step 2, this true boiling point distillation instrument meets ASTM D2892 standard, 15 of theoretical plate numbers, tower reactor volume 20L, trim the top of column is than 10～20:1, and tower reactor heats aperture 20%～40%;
(4) step 3 is repeated to 3 times and collect≤65 DEG C of cuts, by collect≤65 DEG C of cuts cut on true boiling point distillation instrument again, trim the top of column compares 20:1, tower reactor heating aperture 20%, tower top distillates product and adopts multiple bottles to collect differing temps section product, every 0.5 DEG C is a cut section, obtains purity and be 95.323% isohexane product between 59.5-62 DEG C.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104673381A (en) * | 2015-01-21 | 2015-06-03 | 安徽海德石油化工有限公司 | Method for preparing solvent oil |
| CN113004112A (en) * | 2021-03-04 | 2021-06-22 | 滁州市润达溶剂有限公司 | Isohexane preparation process |
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| CN102351627A (en) * | 2011-09-07 | 2012-02-15 | 洛阳金达石化有限责任公司 | Process method for extracting normal hexane and isohexane from crude hexane |
| CN202246472U (en) * | 2011-09-07 | 2012-05-30 | 洛阳金达石化有限责任公司 | Device for extracting normal hexane and isohexane from crude hexane |
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- 2012-11-27 CN CN201210490616.2A patent/CN103833499B/en active Active
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| Title |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104673381A (en) * | 2015-01-21 | 2015-06-03 | 安徽海德石油化工有限公司 | Method for preparing solvent oil |
| CN113004112A (en) * | 2021-03-04 | 2021-06-22 | 滁州市润达溶剂有限公司 | Isohexane preparation process |
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| Publication number | Publication date |
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| CN103833499B (en) | 2016-03-09 |
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