CN1243085C - Method for producing soft microcrystalline wax - Google Patents
Method for producing soft microcrystalline wax Download PDFInfo
- Publication number
- CN1243085C CN1243085C CN 200310104975 CN200310104975A CN1243085C CN 1243085 C CN1243085 C CN 1243085C CN 200310104975 CN200310104975 CN 200310104975 CN 200310104975 A CN200310104975 A CN 200310104975A CN 1243085 C CN1243085 C CN 1243085C
- Authority
- CN
- China
- Prior art keywords
- hydroisomerizing
- microcrystalline wax
- content
- section
- hydrogen
- 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
- 239000004200 microcrystalline wax Substances 0.000 title claims abstract description 30
- 235000019808 microcrystalline wax Nutrition 0.000 title claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 title abstract description 9
- 238000000034 method Methods 0.000 claims abstract description 32
- 239000001257 hydrogen Substances 0.000 claims abstract description 21
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 21
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims abstract description 8
- 238000000926 separation method Methods 0.000 claims abstract description 7
- 239000007791 liquid phase Substances 0.000 claims abstract description 5
- 239000003054 catalyst Substances 0.000 claims description 25
- 238000006243 chemical reaction Methods 0.000 claims description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 239000003921 oil Substances 0.000 claims description 9
- 150000002431 hydrogen Chemical class 0.000 claims description 8
- 229910052751 metal Inorganic materials 0.000 claims description 8
- 239000002184 metal Substances 0.000 claims description 8
- 239000002808 molecular sieve Substances 0.000 claims description 7
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 7
- 239000012188 paraffin wax Substances 0.000 claims description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 5
- 239000005864 Sulphur Substances 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 5
- 229910052698 phosphorus Inorganic materials 0.000 claims description 5
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 4
- 239000007795 chemical reaction product Substances 0.000 claims description 4
- 229910052759 nickel Inorganic materials 0.000 claims description 4
- 239000011148 porous material Substances 0.000 claims description 4
- 229910052750 molybdenum Inorganic materials 0.000 claims description 3
- 239000011574 phosphorus Substances 0.000 claims description 3
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 claims description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 2
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 claims description 2
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 2
- 239000002671 adjuvant Substances 0.000 claims description 2
- 239000012752 auxiliary agent Substances 0.000 claims description 2
- 239000010953 base metal Substances 0.000 claims description 2
- 229910052796 boron Inorganic materials 0.000 claims description 2
- 239000000460 chlorine Substances 0.000 claims description 2
- 229910052801 chlorine Inorganic materials 0.000 claims description 2
- 239000011737 fluorine Substances 0.000 claims description 2
- 229910052731 fluorine Inorganic materials 0.000 claims description 2
- 229910052763 palladium Inorganic materials 0.000 claims description 2
- 229910052697 platinum Inorganic materials 0.000 claims description 2
- 238000007670 refining Methods 0.000 claims description 2
- 229910052703 rhodium Inorganic materials 0.000 claims description 2
- 229910052707 ruthenium Inorganic materials 0.000 claims description 2
- 229910052721 tungsten Inorganic materials 0.000 claims description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims 1
- 229910052814 silicon oxide Inorganic materials 0.000 claims 1
- 239000001993 wax Substances 0.000 abstract description 8
- 235000013305 food Nutrition 0.000 abstract description 6
- 239000003814 drug Substances 0.000 abstract description 2
- 235000021058 soft food Nutrition 0.000 abstract description 2
- 230000007547 defect Effects 0.000 abstract 1
- 238000004806 packaging method and process Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 23
- 239000002994 raw material Substances 0.000 description 13
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 7
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000011733 molybdenum Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000035515 penetration Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910017318 Mo—Ni Inorganic materials 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention discloses a method for producing white soft microcrystalline wax by hydrogenation. By adopting a two-stage method of hydrogen prerefining and hydroisomerizing, raw wax first enters a hydrofining stage reactor, and is processed by gas-liquid separation; separated liquid phases enter a hydroisomerizing stage reactor. The production method of the present invention has the advantages of simple operation and strong adaptability of raw oil; prepared microcrystalline wax products can meet the indexes of similar soft food grade microcrystalline wax abroad, have the advantages of high content of isoparaffin and high kinematic viscosity, overcome the defects of low content of the isoparaffin, poor flexibility and extensibility, crispness of products, easy rupture, limited application range, etc. of microcrystalline wax products produced by a traditional hydrofining method; the food grade microcrystalline wax products prepared by the present invention is suitable for medicine, make-up, food, food packaging, etc.
Description
1, technical field
The present invention relates to a kind of production method of Microcrystalline Wax, particularly a kind of method by hydrogenation method direct production white soft mlcrocrystalline wax product.
2, background technology
Compare with external Microcrystalline Wax product, there is following shortcoming in China's Microcrystalline Wax product: snappiness and extensibility are poor, the product embrittlement, and easy fracture, use range is very limited.This is owing to be subjected to the low restriction of isoparaffin content in China's Microcrystalline Wax raw material, causes that isoparaffin content is generally less than 50wt% in the product, and in the external like product isoparaffin content generally greater than 70wt%.
CN1157315A discloses a kind of Microcrystalline Wax hydrogenation technique, adopts two sections serial flows, and first reactor uses protective material and Hydrobon catalyst, and second section is used Hydrobon catalyst.US5205923 has proposed the hydrogenation technique of a kind of Microcrystalline Wax or paraffin, in same reactor, load two beds in this technology, wherein first bed loads Hydrodemetalation catalyst, molybdenum in the catalyzer, nickel, phosphorus all are immersed in the monomer aluminum oxide with oxide compound or sulfide, second bed filling hydrotreating catalyst, metal all is to exist with molybdenum, nickel, phosphorus form; This technology can make wax decoloring more thorough, can prolong the work-ing life of catalyzer.
More than two kinds of processing methodes all adopt traditional hydrofinishing process, can only remove impurity such as sulphur in the Microcrystalline Wax, nitrogen, oxygen, unsaturated hydrocarbons, can not change the composition of isoparaffin in the product, adopt the Microcrystalline Wax raw material of China just can't produce the high Microcrystalline Wax product of isoparaffin content like this, limited the quality of Microcrystalline Wax product, thus the range of application of having dwindled Microcrystalline Wax.
3, summary of the invention
At the deficiencies in the prior art, the object of the present invention is to provide a kind of method that raw material is adapted to by force, increases the production soft mlcrocrystalline wax of Microcrystalline Wax product snappiness and extensibility.
The method of production soft mlcrocrystalline wax of the present invention is to adopt hydrogenation pre-refining-as hydrogen isomery two-stage method, comprise the steps: that paraffin at first enters hydrofining section reactor, in the presence of hydrogen and Hydrobon catalyst, carry out hydrogenation reaction, reaction product enters gas-liquid separator, isolated liquid phase enters hydroisomerizing section reactor, carry out the hydroisomerizing reaction in the presence of hydrogen and hydroisomerization catalyst, reaction product gets the Microcrystalline Wax product again after gas-liquid separation, gas are carried.
Among the present invention, described hydrorefined reaction conditions is: temperature is 270 ℃～370 ℃, preferred 290 ℃～350 ℃, and hydrogen dividing potential drop 10.0MPa～16.0MPa, preferred 13.0MPa～16.0MPa, volume space velocity is 0.3h
-1～1.2h
-1, preferred 0.5h
-1～1.0h
-1, hydrogen to oil volume ratio 300: 1～1200: 1, preferred 400: 1～800: 1.The reaction conditions of described hydroisomerizing is: temperature is 220 ℃～340 ℃, and preferred 240 ℃～310 ℃, the hydrogen dividing potential drop is 4.0MPa～12.0MPa, and preferred 6.0～10.0MPa, volume space velocity are 0.6h
-1～1.8h
-1, preferred 0.8h
-1～1.5h
-1, hydrogen to oil volume ratio 300: 1～1200: 1, preferred 500: 1～800: 1.
By controlling suitable hydrofining condition, sulphur content is less than 10 μ g/g in the liquid product that gas-liquid separation goes out to make the hydrofining reaction product, and nitrogen content is less than 5 μ g/g, as the charging of hydroisomerizing section.
Among the present invention, described Hydrobon catalyst can adopt conventional Hydrobon catalyst, and its reactive metal is group vib and/or group VIII base metal, one or more among preferred W, Ni, Co, the Mo, and carrier is Al
2O
3Or Al
2O
3-SiO
2, can contain auxiliary agents such as P, Ti, B.Use procatalyst to need prevulcanized, make hydrogenation active metals in reaction process, be in sulphided state.Described hydroisomerization catalyst, carrier is the NU-10 molecular sieve of aluminum oxide and TON structure or the ZSM-22 molecular sieve of aluminum oxide and TON structure, the content of molecular sieve in catalyzer is 30wt%～80wt%, is preferably 40wt%～70wt%, also can add partial oxidation silicon in the carrier; Active metal component be among Pt, Pd, Ru, Rh and the Ni one or more, the content in catalyzer is 0.1wt%～30.0wt%.Selectable adjuvant component is one or more in boron, fluorine, chlorine and the phosphorus, and the content in catalyzer is 0.1wt%～5.0wt%; The specific surface of this catalyzer is 150～500m
2/ g, pore volume are 0.15～0.60ml/g.Before using catalyzer is reduced, hydrogenation active metals is in reaction process goes back ortho states.
It is hydrogenation pre-refining-hydroisomerizing method that the present invention adopts two-stage method, and what adopt in hydrogenation pre-refining section is conventional Hydrobon catalyst, with impurity removals such as sulphur, nitrogen, oxygen in the raw material; In the employing of hydroisomerizing conversion zone is the hydroisomerizing dual-function catalyst, have suitable hydrocracking and isomery function, can under suitable condition, change Microcrystalline Wax macromole straight-chain paraffin into the macromole isoparaffin, produce the high Microcrystalline Wax of isoparaffin content.Method of the present invention can be produced the Microcrystalline Wax product that meets different isomerization alkane content requirement by the reaction conditions of control hydroisomerizing conversion zone.
In hydrogenation pre-refining-hydroisomerizing two-stage method that the present invention takes, the hydroisomerizing conversion zone can adopt the mesolow operation, reduces investment and process cost.
Production method of the present invention is simple to operate, and stock oil adaptability is strong.Prepared Microcrystalline Wax product can satisfy external similar soft food level Microcrystalline Wax index, the isoparaffin content height (＞70wt%), kinematic viscosity is big, and (viscosity (100 ℃) is greater than 17.0mm
2/ s), overcome that the Microcrystalline Wax product isoparaffin content that adopts traditional hydrofinishing process to produce is low, snappiness and extensibility is poor, product embrittlement, easy fracture, use range are limited etc. shortcoming.
The prepared food grade Microcrystalline Wax product of the present invention is applicable to medicine, cosmetic, food and food product pack etc.
4, embodiment
Further set forth technical scheme of the present invention and effect below in conjunction with embodiment.
Concrete grammar of the present invention is as follows:
(1), the mixture of Microcrystalline Wax raw material and hydrogen is introduced into hydrofining reactor, under the effect of Hydrobon catalyst, by controlling suitable reaction conditions, mainly carry out hydrogenating desulfurization, denitrification reaction, reacted resultant is through gas-liquid separation, sulphur content is less than 10 μ g/g in the control liquid phase, and nitrogen content is less than 5 μ g/g, as the charging of hydroisomerizing section.
(2), the above-mentioned liquid phase that goes out through gas-liquid separation enters hydroisomerizing section reactor, under the effect of hydroisomerization catalyst, by controlling suitable reaction conditions, mainly carry out the hydroisomerizing reaction, from the effusive resultant of hydroisomerization reactor, after carrying, process gas-liquid separation, gas gets white soft mlcrocrystalline wax product.
Used Hydrobon catalyst A is Mo-Ni/Al among each embodiment
2O
3Catalyzer is a benchmark with the weight of catalyzer, MoO
3Content be 29.34%, the content of NiO is 4.45%, the content of P is 2.25%; Its specific surface is 249m
2/ g, pore volume are 0.413ml/g.
Microcrystalline Wax raw material properties used in the various embodiments of the present invention sees Table 1, and the character of used hydroisomerization catalyst sees Table 2, and the concrete processing condition of each embodiment see Table 3, and product property sees Table 4.
Table 1 Microcrystalline Wax feedstock property
| The raw material numbering | 1 | 2 |
| Melt drop temperature, ℃ | 81.6 | 83 |
| Penetration degree, 1/10mm | 8 | 12 |
| Oleaginousness, wt% | 0.67 | 1.39 |
| Colourity D1500 | 5～6 | 4～5 |
| Kinematic viscosity (100 ℃), mm 2/s | 12.9 | 13.2 |
| S/N，μg/g | 405/145 | 349/86 |
| Normal paraffin, wt% | 54.76 | 50.10 |
| Isoparaffin, wt% | 45.24 | 47.90 |
The character of each embodiment catalyst system therefor of table 2
| Analysis project | Catalyst B | Catalyzer C | Catalyzer D | Catalyzer E |
| Active ingredient | ||||
| Ni，wt％ | — | — | — | 30 |
| Pt，wt％ | 0.45 | 0.15 | — | — |
| Pd，wt％ | — | 1.35 | 1.6 | — |
| P，wt％ | 3.31 | 3.35 | 4.3 | 1.5 |
| Carrier | ||||
| Molecular sieve NU-10, wt% | 53 | — | 70 | 46 |
| ZSM-22，wt％ | — | 55 | — | — |
| Aluminum oxide, wt% | Surplus | Surplus | Surplus | Surplus |
| The character of catalyzer | ||||
| Pore volume, ml/g | 0.32 | 0.38 | 0.55 | 0.21 |
| Specific surface area, m 2/g | 310 | 330 | 500 | 195 |
The processing condition of each embodiment of table 3
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 |
| Raw material | Raw material 1 | Raw material 2 | Raw material 1 | Raw material 1 | Raw material 1 |
| Hydroisomerization catalyst | B | B | C | D | E |
| Hydrofining section reaction conditions | |||||
| Temperature, ℃ | 350 | 320 | 320 | 330 | 320 |
| The hydrogen dividing potential drop, MPa | 14.5 | 15.0 | 15.5 | 15.5 | 14.0 |
| Volume space velocity, h -1 | 1.0 | 0.7 | 0.8 | 1.0 | 0.7 |
| Hydrogen to oil volume ratio | 600 | 700 | 500 | 500 | 700 |
| Hydroisomerizing section reaction conditions | |||||
| Temperature, ℃ | 260 | 270 | 310 | 240 | 275 |
| The hydrogen dividing potential drop, MPa | 7.0 | 8.0 | 9.0 | 9.0 | 7.0 |
| Volume space velocity, h -1 | 1.0 | 1.0 | 1.5 | 0.8 | 1.2 |
| Hydrogen to oil volume ratio | 700 | 750 | 600 | 700 | 800 |
The character of each embodiment product of table 4
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 |
| The hydrotreated product main character | |||||
| S/N，μg/g | 7.3/＜1 | 6.2/＜1 | 7.3/＜1 | 9.8/＜1 | 5.2/＜1 |
| Hydroisomerizing product main character | |||||
| Melt drop temperature, ℃ | 79.8 | 80.2 | 79.3 | 78.0 | 79.8 |
| Penetration degree, 1/10mm | 26 | 27 | 28 | 25 | 27 |
| Oleaginousness, wt% | 2.11 | 2.83 | 2.35 | 2.97 | 1.83 |
| Saybolt color, number | +24 | +27 | +26 | +28 | +25 |
| Kinematic viscosity (100 ℃), mm 2/s | 17.91 | 17.65 | 18.10 | 17.11 | 17.35 |
| Easy carbon | By | By | By | By | By |
| Condensed-nuclei aromatics ultraviolet absorptivity/cm | |||||
| 280nm-289nm | 0.095 | 0.098 | 0.084 | 0.085 | 0.088 |
| 290nm-299nm | 0.061 | 0.067 | 0.039 | 0.051 | 0.069 |
| 300nm-359nm | 0.035 | 0.04 | 0.020 | 0.037 | 0.045 |
| 360nm-400nm | 0.010 | 0.011 | 0.010 | 0.011 | 0.010 |
| Normal paraffin, wt% | 28.2 | 26.8 | 27.1 | 28.8 | 29.2 |
| Isoparaffin, wt% | 71.8 | 73.2 | 72.9 | 72.2 | 70.8 |
By table 4 as seen, adopt the soft mlcrocrystalline wax product of the inventive method preparation, isoparaffin content reaches more than 70%, and kinematic viscosity (100 ℃) reaches 17mm
2More than/the s, Saybolt color has reached the performance index of external like product more than+No. 20.
Claims (11)
1, a kind of hydrogenation method is produced the method for Microcrystalline Wax, it is characterized in that this method is to adopt hydrogenation pre-refining one hydroisomerizing two-stage method, paraffin at first enters hydrofining section reactor, and its reaction product is after gas-liquid separation, and isolated liquid phase enters hydroisomerizing section reactor;
The reaction conditions of wherein hydrofining section is: temperature is 270 ℃～370 ℃, and hydrogen dividing potential drop 10.0MPa～16.0MPa, volume space velocity are 0.3h
-1～1.2h
-1, hydrogen to oil volume ratio 300: 1～1200: 1; The reaction conditions of hydroisomerizing section is: temperature is 220 ℃～340 ℃, and the hydrogen dividing potential drop is 4.0MPa～12.0MPa, and volume space velocity is 0.6h
-1～1.8h
-1, hydrogen to oil volume ratio 300: 1～1200: 1.
2, method according to claim 1 is characterized in that the reaction conditions of described hydrofining section is: temperature is 290 ℃～350 ℃, and hydrogen dividing potential drop 13.0MPa～16.0MPa, volume space velocity are 0.5h
-1～1.0h
-1, hydrogen to oil volume ratio 400: 1～800: 1.
3, method according to claim 1 is characterized in that the reaction conditions of described hydroisomerizing section is: temperature is 240 ℃～310 ℃, and the hydrogen dividing potential drop is 6.0～10.0MPa, and volume space velocity is 0.8h
-1～1.5h
-1, hydrogen to oil volume ratio 500: 1～800: 1.
4, method according to claim 1 is characterized in that sulphur content is less than 10 μ g/g in the charging of described hydroisomerizing section reactor, and nitrogen content is less than 5 μ g/g.
5, method according to claim 1 is characterized in that the Hydrobon catalyst that described hydrofining section is adopted, and carrier is Al
2O
3Or Al
2O
3-SiO
2, reactive metal is group vib and/or group VIII base metal.
6, method according to claim 5 is characterized in that the Hydrobon catalyst that described hydrofining section is adopted, and reactive metal is one or more among W, Ni, Co, the Mo, in the weight of catalyzer, WO
3And/or MoO
3Content account for 20%～35%, the content of NiO or CoO accounts for 3%～10%.
7, method according to claim 5 is characterized in that needing prevulcanized before described Hydrobon catalyst uses.
8, method according to claim 5 is characterized in that the Hydrobon catalyst that described hydrofining section is adopted, and contains among auxiliary agent P, Ti and the B one or more.
9, method according to claim 1 is characterized in that the hydroisomerization catalyst that the hydroisomerizing section is adopted, and carrier is the NU-10 molecular sieve of aluminum oxide and TON structure or the ZSM-22 molecular sieve of aluminum oxide and TON structure; The content of molecular sieve in catalyzer is 30wt%～80wt%; Active metal component be among Pt, Pd, Ru, Rh and the Ni one or more, the content in catalyzer is 0.1wt%～30.0wt%; Its specific surface is 150～500m
2/ g, pore volume are 0.15～0.60ml/g.
10, method according to claim 9 is characterized in that silicon oxide-containing in the carrier of described hydroisomerization catalyst; Contain adjuvant component in the catalyzer and be in boron, fluorine, chlorine and the phosphorus one or more, the content in catalyzer is 0.1wt%～5.0wt%.
11, method according to claim 9 is characterized in that will reducing to catalyzer before described hydroisomerization catalyst uses.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310104975 CN1243085C (en) | 2003-10-31 | 2003-10-31 | Method for producing soft microcrystalline wax |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310104975 CN1243085C (en) | 2003-10-31 | 2003-10-31 | Method for producing soft microcrystalline wax |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1611581A CN1611581A (en) | 2005-05-04 |
| CN1243085C true CN1243085C (en) | 2006-02-22 |
Family
ID=34757133
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200310104975 Expired - Lifetime CN1243085C (en) | 2003-10-31 | 2003-10-31 | Method for producing soft microcrystalline wax |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1243085C (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100432193C (en) * | 2005-10-19 | 2008-11-12 | 中国石油化工股份有限公司 | Paraffin-hydrogenating refining process |
| CN102311805B (en) * | 2010-07-07 | 2014-03-05 | 中国石油化工股份有限公司 | Vaseline production method |
| CN103865580A (en) * | 2012-12-10 | 2014-06-18 | 中国石油天然气股份有限公司 | Preparation method of food-grade microcrystalline wax |
| CN109988616B (en) * | 2017-12-29 | 2021-05-04 | 中国石油化工股份有限公司 | Flexible liquid-phase hydrogenation process for vaseline |
| CN109988637B (en) * | 2017-12-29 | 2021-05-04 | 中国石油化工股份有限公司 | Flexible paraffin hydrogenation process |
| CN109988597B (en) * | 2017-12-29 | 2021-05-04 | 中国石油化工股份有限公司 | Flexible vaseline hydrogenation process |
| CN109988627B (en) * | 2017-12-29 | 2021-07-09 | 中国石油化工股份有限公司 | Flexible paraffin hydrogenation process |
| CN109988619B (en) * | 2017-12-29 | 2021-05-04 | 中国石油化工股份有限公司 | Flexible vaseline hydrogenation process |
-
2003
- 2003-10-31 CN CN 200310104975 patent/CN1243085C/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| CN1611581A (en) | 2005-05-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101333460B (en) | Combined technological process for producing lube oil base stock | |
| CN101173191B (en) | Method for producing lubricating oil basic oil | |
| CN101591565B (en) | Hydrogenation and refining method of gasoline with poor quality | |
| CN102041029B (en) | Comprehensive utilization method of hydrocracking tail oil | |
| CN103773466B (en) | Method for producing lubricant base oil by hydrocracking-isodewaxing combination | |
| CN1243085C (en) | Method for producing soft microcrystalline wax | |
| CN102746895A (en) | Single-reactor hydrogenation technology of Fischer-Tropsch synthetic full fraction products | |
| CN101760236B (en) | Method for producing lube base oil | |
| CN1865405A (en) | Process for hydrogenating and refining oil from Fischer-Tropsch synthesis | |
| CN101314735A (en) | Hydrogenation method for reducing aromatic hydrocarbon content of diesel oil cut fraction and improving its cetane number | |
| CN102911726A (en) | Production method for base oil of high velocity index lubricating oil | |
| CN1944587A (en) | Method for producing food grade white oil by hydrogenating tail oil | |
| CN103059974B (en) | Hydrotreatment method for producing food grade solvent naphtha | |
| CN100558862C (en) | The method of white oil is produced in a kind of hydrofining | |
| CN102465027B (en) | Hydrotreating method of heavy distillate oil | |
| CN1171979C (en) | Method for producing micro crystal wax | |
| CN1313573C (en) | Process for deep desulfating of diesel oil fractional oil | |
| CN112143520B (en) | Hydroconversion composition and method for hydroconversion of Fischer-Tropsch wax | |
| CN1769395A (en) | Method for producing white microcrystalline wax by one-step hydrogenation | |
| CN1769380A (en) | One-step hydrogenation method for producing super white oil | |
| CN103102954A (en) | Production method for high-viscosity index lubricant base oil | |
| CN103102947A (en) | Production method for high-viscosity index lubricant base oil | |
| CN103387847B (en) | A kind of production method of lubricant base | |
| CN1233796C (en) | Technology for hydrogenating treatment of synthetizing diesel oil | |
| CN100594233C (en) | Method for producing white microcrystal wax by two-section hydrogenation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20060222 |
|
| CX01 | Expiry of patent term |