CN103833499B - Preparation method of high-purity isohexane solvent oil - Google Patents
Preparation method of high-purity isohexane solvent oil Download PDFInfo
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- CN103833499B CN103833499B CN201210490616.2A CN201210490616A CN103833499B CN 103833499 B CN103833499 B CN 103833499B CN 201210490616 A CN201210490616 A CN 201210490616A CN 103833499 B CN103833499 B CN 103833499B
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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 20
- 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
- 150000001336 alkenes Chemical class 0.000 claims abstract description 6
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 5
- 238000002407 reforming Methods 0.000 claims description 15
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 7
- 239000005864 Sulphur Substances 0.000 claims description 7
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 6
- 239000003054 catalyst Substances 0.000 claims description 6
- 239000000843 powder Substances 0.000 claims description 6
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 claims description 5
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 claims description 5
- 229910052794 bromium Inorganic materials 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
- 241000219793 Trifolium Species 0.000 claims description 2
- 244000275012 Sesbania cannabina Species 0.000 claims 1
- 150000001335 aliphatic alkanes Chemical class 0.000 claims 1
- 238000005520 cutting process Methods 0.000 abstract description 12
- 238000000034 method Methods 0.000 abstract description 10
- 238000005194 fractionation Methods 0.000 abstract description 8
- 239000002994 raw material Substances 0.000 abstract description 7
- 230000000694 effects Effects 0.000 abstract description 5
- 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
- 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
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 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
- 238000007323 disproportionation reaction Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 231100000252 nontoxic Toxicity 0.000 description 2
- 230000003000 nontoxic effect Effects 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
- 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
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 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
- 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
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 239000000341 volatile oil Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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 refining, that separation means obtains high purity product preparation method.
Background technology
Along with the rapid growth of national economy, the demand of various varsol product constantly increases, and people to health environment-friendly be familiar with day by day deep, the quality of every profession and trade to varsol is made to it is also proposed stricter requirement, therefore, from seed output and quality two aspects, 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 the feasibility that other solvent oil products alternative are used for every profession and trade is subject to market favor gradually.
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 solvent for polymerization, agent released by precision instrumentation cleaning and oil, essential oil thinners etc., are mainly used in the product scopes such as non-toxic spray, solvent, clean-out system.At present, isohexane is domestic has part refinery to produce, such as, Lanzhou, Liaoyang, Dalian, the Yanshan Mountain, Yang Zi, output is many within 10,000 tons/year, all parts of the country are sold on the basis meeting our factory's consumption, sales situation is good, due to the few huge market demand of isohexane output, price was in ascendant trend always in recent years, the isohexane price of purity requirement in August 95% in 2012 is about 12000 yuan/ton, isohexane is in backorder status in China at present, major part depends on import, China now only has Herpu Chemical Co., Ltd., Guangzhou one to stablize provides isohexane in a large number, there is the isohexane production marketing of different purity on the flourishing ground such as city and Liaoyang, northeast of coastal economy, but mostly be only to sell and do not produce, and supply is all little.
CN95121454.3 discloses a kind of preparation method of the product containing 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
othe temperature exposure of the acid catalyst being greater than 8 between 0 ~ 150 ° of C and by iso-pentane raw material disproportionation, take out the product containing Trimethylmethane/isohexane.
CN200410027004.5 discloses a kind of manufacture method of isohexane solvent.The method is with 6# solvent oil for raw material, and adopt packing tower fractionation cutting to collect the cut of 58 ~ 63 DEG C, this cut finally obtains the isohexane containing more than 95% through hydrogenation.The method list tower continuous seepage, less investment, floor space is little, operates, manages simply, efficiently.
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.The method catalyzer operational condition is relatively gentle, de-aromatizing and desulfurizing Be very effective, features simple and practical process, and stable and reliable product quality, economical efficiency are high.
CN201110263745.3 mono-kind is by the processing method of thick hexane extraction normal hexane, isohexane, CN201120334519.5 mono-kind is by the device of thick hexane extraction normal hexane, isohexane, CN201120334491.5 mono-kind is by the hydro-refining unit of thick hexane extraction normal hexane, isohexane, CN201120334470.3 mono-kind is by the fractionation plant of thick hexane extraction normal hexane, isohexane, and above-mentioned four patents have carried out comprehensive description from the hydrofining unit of processing method, industrial installation, device and product fractionation unit four aspects to production 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, take reforming raffinate oil as raw material, adopt high reactivity nickel catalyst hydrofining Arene removal and alkene, true boiling point distillation instrument obtains by cutting twice fractionation the isohexane product that purity is not less than 95%.
The preparation method of high purity isohexane solvent oil of the present invention adopts following technical scheme:
(1) preparation of high reactivity nickel catalyst, adds sesbania powder, after nitric acid, phosphoric acid, water mediates in aluminium hydroxide dry powder, extruded moulding, 120 DEG C of dry 2h, 550 DEG C of roasting 4h, obtained support of the catalyst; Prepare nickeliferous and solution that is promoter metal, equivalent impregnation on alumina supporter, 120 DEG C of dry 2h, 500 DEG C of roasting 4h, obtained catalyzer, the active metal of catalyzer is in its content of NiO for 25% ~ 50%, and preferred metal content is 30% ~ 35%;
(2) reforming raffinate oil hydrofining on 100mL small hydrogenation device, adopts nickel catalyst prepared by step 1, at pressure range 0.2 ~ 2.0Mpa, and temperature range 80 ~ 220 DEG C, space velocity range 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), > 65 DEG C of cuts will be excised through the hydrorefined reforming raffinate oil of step 2 on true boiling point distillation instrument, this true boiling point distillation instrument meets ASTMD2892 standard, theoretical plate number 15 pieces, 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 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 bottle to collect differing temps section product, and every 0.5 DEG C is a fraction section, obtains the isohexane product that purity is 95.323% between 59.5-62 DEG C.
Invention effect
1, the present invention is that raw material carries out hydrogenation with reforming raffinate oil, and catalyst activity is high, and product property is excellent, can carry out comprehensive utilization of separation according to the finished product target to raffinating oil, and reduces the necessity of refining after target product needs.
2, the nickel catalyst that prepared by the present invention can make hydrogenated products take off to containing alkene and aromatic hydrocarbons hardly under the processing condition comparatively relaxed, and hydrofining effect is very remarkable.
3, the true boiling point distillation instrument of 15 pieces has carried out cutting twice fractionation to hydrorefined raffinating oil in the present invention, having used every 0.5 DEG C is cleverly that a fraction section collects product, investigate the purity of each fraction section isohexane, search out optimum cutting temperature section.
4, the present invention is in product separation process, and adopting every 0.5 DEG C of multiple bottle to be that a fraction section collects product, is the key obtaining high purity isohexane product on the true boiling point distillation instrument that theoretical plate number is lower.
Accompanying drawing explanation
Fig. 1 flowsheeting schema.
Embodiment
A preparation method for high purity isohexane solvent oil, is characterized in that:
(1), the preparation of nickel catalyst
In aluminium hydroxide dry powder, add sesbania powder, after nitric acid, phosphoric acid, water mediates, extruded moulding, 120 DEG C of dry 2h, 550 DEG C of roasting 4h, obtained support of the catalyst; Prepare nickeliferous and solution that is promoter metal, equivalent impregnation is on alumina supporter, and 120 DEG C of dry 2h, 500 DEG C of roasting 4h, obtain catalyzer.
The active metal of catalyzer is in its content of NiO for 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, adopts nickel catalyst prepared by step 1, at pressure range 0.2 ~ 2.0Mpa, and temperature range 80 ~ 220 DEG C, space velocity range 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), true boiling point distillation instrument removes heavy constituent
> 65 DEG C will be excised on true boiling point distillation instrument through the hydrorefined reforming raffinate oil of step 2, this true boiling point distillation instrument meets ASTMD2892 standard, theoretical plate number 15 pieces, 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
Step 3 is repeated 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 bottle to collect differing temps section product, and every 0.5 DEG C is a fraction section, and composition is in table 1.The isohexane product that purity is 95.323% is obtained between 59.5-62 DEG C.
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 |
Adopt the catalyzer of above-mentioned preparation, hydrofining technology technology and isohexane product separation purification mode, the high purity isohexane solvent oil production character 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 is not enough, the isohexane product of purity requirement can not be obtained by single flash cutting, the hydrorefined reforming raffinate oil of step 2 calculates distillation cutting isohexane product on AspenHYSYS process simulation 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 discharges 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, block | 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 |
Bottom 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, adds sesbania powder, after nitric acid, phosphoric acid, water mediates in aluminium hydroxide dry powder, extruded moulding, 120 DEG C of dry 2h, 550 DEG C of roasting 4h, obtained support of the catalyst; Prepare nickeliferous and solution that is promoter metal, equivalent impregnation on alumina supporter, 120 DEG C of dry 2h, 500 DEG C of roasting 4h, obtained catalyzer, the active metal of catalyzer in its content of NiO for 25m% ~ 50m%;
Catalyst appearance is trifolium bar Φ 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, dissident's alkane 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, adopt nickel catalyst prepared by step 1, processing condition: pressure is 0.2 ~ 2.0Mpa, temperature is 80 ~ 220 DEG C, and air speed is 2.0 ~ 4.0h
-1, hydrogen-oil ratio is under the processing condition of 40 ~ 200v/v, and product sulphur content <0.5 μ g/g, bromine index <0.2mgBr/100g, aromaticity content are <0.001m%;
(3) > 65 DEG C of cuts will be excised through the hydrorefined reforming raffinate oil of step 2 on true boiling point distillation instrument, this true boiling point distillation instrument meets ASTMD2892 standard, theoretical plate number 15 pieces, 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 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 bottle to collect differing temps section product, every 0.5 DEG C is a fraction section, obtains the isohexane product that purity is 95.323% between 59.5-62 DEG C.
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CN1569782A (en) * | 2004-04-27 | 2005-01-26 | 广州赫尔普化工有限公司 | Method for preparing isohexane solvent |
CN101875594A (en) * | 2009-04-30 | 2010-11-03 | 中国海洋石油总公司 | Method for preparing narrow fraction nontoxic high-purity isohexane |
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 |
CN202237321U (en) * | 2011-09-07 | 2012-05-30 | 洛阳金达石化有限责任公司 | Fractionation plant for extracting n-hexane and isohexane from crude hexane |
CN102675023A (en) * | 2012-05-19 | 2012-09-19 | 淄博汇佳橡胶新型材料有限公司 | Preparation method of narrow-fraction high-purity isohexane |
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Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
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CN1569782A (en) * | 2004-04-27 | 2005-01-26 | 广州赫尔普化工有限公司 | Method for preparing isohexane solvent |
CN101875594A (en) * | 2009-04-30 | 2010-11-03 | 中国海洋石油总公司 | Method for preparing narrow fraction nontoxic high-purity isohexane |
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 |
CN202237321U (en) * | 2011-09-07 | 2012-05-30 | 洛阳金达石化有限责任公司 | Fractionation plant for extracting n-hexane and isohexane from crude hexane |
CN102675023A (en) * | 2012-05-19 | 2012-09-19 | 淄博汇佳橡胶新型材料有限公司 | Preparation method of narrow-fraction high-purity isohexane |
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