CN1611579A - Method for producing different consistency vaselines - Google Patents
Method for producing different consistency vaselines Download PDFInfo
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- CN1611579A CN1611579A CN 200310104987 CN200310104987A CN1611579A CN 1611579 A CN1611579 A CN 1611579A CN 200310104987 CN200310104987 CN 200310104987 CN 200310104987 A CN200310104987 A CN 200310104987A CN 1611579 A CN1611579 A CN 1611579A
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- Prior art keywords
- vaseline
- temperature
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 20
- 238000000034 method Methods 0.000 claims abstract description 29
- 239000003054 catalyst Substances 0.000 claims abstract description 6
- 239000003814 drug Substances 0.000 claims abstract description 3
- 229940099259 vaseline Drugs 0.000 claims description 60
- 230000035515 penetration Effects 0.000 claims description 27
- 239000002994 raw material Substances 0.000 claims description 26
- 238000006243 chemical reaction Methods 0.000 claims description 21
- 239000001257 hydrogen Substances 0.000 claims description 17
- 229910052739 hydrogen Inorganic materials 0.000 claims description 17
- 150000002431 hydrogen Chemical class 0.000 claims description 10
- 239000003921 oil Substances 0.000 claims description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 7
- 229910017318 Mo—Ni Inorganic materials 0.000 claims description 5
- 239000002199 base oil Substances 0.000 claims description 4
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 7
- 239000000463 material Substances 0.000 abstract description 4
- 239000002537 cosmetic Substances 0.000 abstract description 2
- 239000012169 petroleum derived wax Substances 0.000 abstract description 2
- 235000019381 petroleum wax Nutrition 0.000 abstract description 2
- 238000006731 degradation reaction Methods 0.000 abstract 1
- XMHIUKTWLZUKEX-UHFFFAOYSA-N hexacosanoic acid Chemical compound CCCCCCCCCCCCCCCCCCCCCCCCCC(O)=O XMHIUKTWLZUKEX-UHFFFAOYSA-N 0.000 abstract 1
- 239000000047 product Substances 0.000 description 37
- 239000001993 wax Substances 0.000 description 13
- 238000007670 refining Methods 0.000 description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 230000001186 cumulative effect Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000010504 bond cleavage reaction Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000003209 petroleum derivative Substances 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 230000007017 scission Effects 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 125000000623 heterocyclic group Chemical group 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002674 ointment Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000012264 purified product Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 210000004243 sweat Anatomy 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
This invention opens one manufacturing method of geoline of different consistencies, especially one hydrofining method to produce geoline of different consistencies, with single component short residue cerate or its concoction as the materials. Characteristics of this method is that pricking degrees of hydrogenation materials can be changed by suitable degradation reaction. Any hydrofining catalyst of petroleum wax can be used in this method. This method solves the problem existing in current techology that different features of materials have to be prepared to produce geoline of different consistencies and can be flexibly and conveniently applied to produce products of different consistencies. Geoline produced by this method can be applied in medicine and cosmetics.
Description
Technical field
The present invention relates to a kind of production method of Vaseline, the method that particularly adopts the frivolous slack wax of single component vacuum residuum or its temper to produce Vaseline as the hydrofining of Vaseline raw material, specifically a kind of flexible production method that can obtain various denseness Vaseline products.
Background technology
Vaseline is the ointment shape petroleum products with certain characteristic.Conventional Vaseline production process is to carry out raw material earlier to be in harmonious proportion, and carries out the refining of temper again.Traditional Vaseline blend component is vacuum distillate base oil and the frivolous slack wax of vacuum residuum.But heterocycle materials such as the sulphur in the hydrogenation method effective elimination Vaseline raw material, nitrogen, oxygen, and make condensed-nuclei aromatics saturated.This method is three-waste free pollution in process of production, can produce high yield, high-quality Vaseline product.
Vaseline is as a kind of paste petroleum products, and its denseness is a very important character, in the Vaseline product standard, and many denseness with cone penetration index regulation Vaseline.The cone penetration of regulation medicinal vaseline is 130～250 1/10mm among the CNS GB1790-94; The cone penetration of regulation Vaseline is 100～300 1/10mm among the American Pharmacopeia USP-95.
In the Vaseline of routine was produced, treating process mainly played desulfurization nitrogen, decolouring and reduction condensed-nuclei aromatics, did not consider the variation of the cone penetration of refining raw material.If produce the Vaseline product of different denseness, must modulate the Vaseline raw material of multiple denseness, can cause the increase of storage facilities, the frequent replacement of refining plant raw material and the fluctuation of quality product so in process of production.Therefore, in the actual production process of Vaseline, all adopt the charging of the Vaseline raw material of single cone penetration as refining section, thereby guarantee the steady production of refining section, the Vaseline of being produced also is the Vaseline of single denseness.The disadvantage of conventional Vaseline production method is the production that different denseness series product are carried out in inconvenience.
CN 1156753A discloses a kind of Vaseline prescription, and this prescription is vacuum distillate pressed oil and the vacuum distillate sweat oil blend component as the Vaseline raw material, thereby has reduced the Vaseline raw materials cost, has enlarged the source of Vaseline raw material.CN 1061678C introduces a kind of hydrogenation refining of Vaseline method, and this method adopts the serial hydrogenation technology of two beds, has also only considered the removal effect to impurity, does not relate to and how to produce different denseness Vaseline products.
Summary of the invention
At the deficiencies in the prior art, the invention provides a kind of method of producing different denseness Vaseline products easily.
The inventive method detailed process is: in the presence of hydrogen, the Vaseline raw material is by two beds, first reaction bed hydrogen dividing potential drop 6MPa～16MPa, 320 ℃～410 ℃ of temperature of reaction, hydrogen to oil volume ratio 300～1000; 240 ℃～300 ℃ of second reaction bed hydrogen dividing potential drop 6MPa～16MPa, temperature of reaction, hydrogen to oil volume ratio 300～1000, two beds volume ratios are 1: 3～3: 1, two long-pending air speed 0.1h of overall reactor
-1～0.5h
-1Adjust the temperature of reaction of first beds, obtain the cone penetration of product under the differential responses temperature, draw product cone penetration and the corresponding relation curve of the first reaction bed temperature.When needs particular cone in-degree Vaseline product, can be according to the product cone penetration of drawing and the first reaction bed temperature relation curve, earlier find the first reaction bed temperature corresponding with the desired product cone penetration from curve, in treating process, the first reaction bed temperature is adjusted near this temperature value, can obtains the Vaseline product of required cone penetration value.
Vaseline production method of the present invention can be produced the Vaseline product of various denseness easily by adjusting operational condition, satisfies the demand of market to different denseness Vaseline.When adopting the hydrofining of polycomponent Vaseline raw material to produce the Vaseline product, can be by the Vaseline product of the different denseness of a kind of Vaseline raw material production of denseness, avoided the frequent replacing of refining plant raw material and the quality product fluctuation that causes thus and the loss of product yield; When adopting the hydrofining of the frivolous slack wax raw material of one-component vacuum residuum to produce the Vaseline product, simplified the traditional back of mediation earlier production method for refining, can in Vaseline production, save mediation equipment, shorten the technological process of production, help saving facility investment and reduce production costs.Also can in existing Vaseline industrial production, avoid industrial installation being stopped production because of other Vaseline feed composition shortage.
Description of drawings
Fig. 1 is the embodiment of the invention 1 product cone penetration and the first temperature of reactor graph of relation.
Fig. 2 is the embodiment of the invention 2 product cone penetrations and the first temperature of reactor graph of relation.
Fig. 3 is the embodiment of the invention 3 product cone penetrations and the first temperature of reactor graph of relation.
Embodiment
Hydrogenation refining of Vaseline method of the present invention can adopt the frivolous slack wax of single vacuum residuum or its temper as the hydrogenation refining of Vaseline raw material.Can comprise vacuum distillate base oil, vacuum distillate pressed oil and solvent-refined oil thereof with the component that the frivolous slack wax of vacuum residuum is in harmonious proportion.
Hydrogenation refining of Vaseline method of the present invention adopts two fixed-bed reactor, also can adopt two beds of a reactors in series, catalyzer can adopt any one petroleum wax series products Hydrobon catalyst, comprising W-Ni type Hydrobon catalyst and Mo-Ni type Hydrobon catalyst.Two reactors can load identical catalyzer, also can load different catalyzer.
Different raw materials and catalyzer generally need be drawn different product cone penetrations and the corresponding curve of first temperature of reactor, but the curve that is obtained by typical raw material and catalyzer has certain representativeness, can be used as the reference of other raw material and catalyzer.
In the presence of hydrogen, the Vaseline raw material at first contacts with the catalyzer of first reactor, under higher relatively temperature, realize desulfurization removing nitric and decolouring, when needs improve Vaseline product cone penetration, suitably improve the temperature of first reactor, make the frivolous slack wax of vacuum residuum or its temper generation scission reaction to a certain degree, thereby improve the cone penetration of Vaseline product.The first reactor refined products enters second reactor after cooling, contact with catalyzer under relatively low temperature, reaches the purpose that aromatic hydrocarbons is saturated, improve the purified product stability.The refined products of second reactor obtains hydrogenated products after gas-liquid separation, stripping drying.
Through suitable scission reaction and refining reaction, can obtain the hydrogenated products of different denseness, other character of hydrogenated products meets the Vaseline product requirement.The Vaseline of producing according to the method for the invention can be used for medicine and makeup.
Specify effect of the present invention by the following examples.
64.0 ℃ of the dropping points of the frivolous slack wax of vacuum residuum that the embodiment of the invention adopts, cone penetration (25 ℃) 821/10mm; The raw material weight harmonic ratio that is in harmonious proportion is the frivolous slack wax of vacuum residuum: No. 150 base oils=60: 40,50.3 ℃ of dropping points, cone penetration (25 ℃) 180 1/10mm.
The character of the W-Ni catalyzer that the embodiment of the invention adopts is WO
329.8%, NiO 4.5%, specific surface area 232m
2/ g, pore volume 0.48ml/g, the character of the Mo-Ni catalyzer of employing is MoO
318.9%, NiO 4.2%, specific surface area 262m
2/ g, pore volume 0.56ml/g.
The embodiment of the invention and comparative example adopt two reactor equal-volume fillings.Two reactor charge are with a kind of catalyzer or two kinds of catalyzer.
The hydrorefined operational condition of the embodiment of the invention and the results are shown in Table 1～3.
It is as shown in the table for the cone penetration of embodiment of the invention product and dropping point, and other character meets GB1790 medicinal vaseline and SH0008 cosmetic Vaseline standard-required.
Table 1 embodiment 1 hydroprocessing condition and result
| Project | Embodiment 1 | ||||
| Raw material | Frivolous slack wax | ||||
| Operational condition | |||||
| Catalyzer | ????????????????????????????W-Ni | ||||
| The hydrogen dividing potential drop, MPa | ????????????????????????????6 | ||||
| Two anti-temperature, ℃ | ????????????????????????????270 | ||||
| The cumulative volume air speed, h -1 | ????????????????????????????0.15 | ||||
| Hydrogen wax volume ratio | ????????????????????????????700 | ||||
| One anti-temperature, ℃ | ????320 | ????350 | ????370 | ????385 | ????400 |
| Product property | |||||
| Dropping point, ℃ | ????63.0 | ????58.0 | ????53.4 | ????48.7 | ????42.2 |
| Cone penetration (25 ℃), 1/10mm | ????89 | ????112 | ????160 | ????204 | ????259 |
Table 2 embodiment 2 hydroprocessing condition and results
| Project | Embodiment 2 | ||||
| Raw material | Frivolous slack wax | ||||
| Operational condition | |||||
| Catalyzer | ????????????????????????????Mo-Ni | ||||
| The hydrogen dividing potential drop, MPa | ????????????????????????????13 | ||||
| Two anti-temperature, ℃ | ????????????????????????????260 | ||||
| The cumulative volume air speed, h -1 | ????????????????????????????0.2 | ||||
| Hydrogen wax volume ratio | ????????????????????????????500 | ||||
| One anti-temperature, ℃ | ????320 | ????340 | ????360 | ????380 | ????400 |
| Product property | |||||
| Dropping point, ℃ | ????63.5 | ????61.0 | ????57.2 | ????52.2 | ????45.5 |
| Cone penetration (25 ℃), 1/10mm | ????87 | ????95 | ????125 | ????178 | ????238 |
Table 3 embodiment 3 hydroprocessing condition and results
| Project | Embodiment 3 | ||||
| Raw material | Blending stock | ||||
| Operational condition | |||||
| Catalyzer | The first reactor Mo-Ni/, the second reactor W-Ni | ||||
| The hydrogen dividing potential drop, MPa | ??????????????????????????8 | ||||
| Two anti-temperature, ℃ | ??????????????????????????250 | ||||
| The cumulative volume air speed, h -1 | ??????????????????????????0.2 | ||||
| Hydrogen wax volume ratio | ??????????????????????????500 | ||||
| One anti-temperature, ℃ | ??320 | ??335 | ??360 | ??380 | ??400 |
| Product property | |||||
| Dropping point, ℃ | ??50.0 | ??49.5 | ??48.5 | ??46.7 | ??43.5 |
| Cone penetration (25 ℃), 1/10mm | ??180 | ??183 | ??202 | ??228 | ??270 |
Claims (7)
1, a kind of production method of different denseness Vaseline, comprise following process: in the presence of hydrogen, the Vaseline raw material is by two beds, first reaction bed hydrogen dividing potential drop 6MPa～16MPa, 320 ℃～410 ℃ of temperature of reaction, hydrogen to oil volume ratio 300～1000; 240 ℃～300 ℃ of second reaction bed hydrogen dividing potential drop 6MPa～16MPa, temperature of reaction, hydrogen to oil volume ratio 300～1000, two beds volume ratios are 1: 3～3: 1, two long-pending air speed 0.1h of overall reactor
-1～0.5h
-1Adjust the temperature of reaction of first beds, obtain the cone penetration of product under the differential responses temperature, draw product cone penetration and the corresponding relation curve of the first reaction bed temperature; When needs particular cone in-degree Vaseline product, can be according to the product cone penetration of drawing and the first reaction bed temperature relation curve, earlier find the first reaction bed temperature corresponding with the desired product cone penetration from curve, in treating process, the first reaction bed temperature is adjusted near this temperature value, can obtains the Vaseline product of required cone penetration value.
2, in accordance with the method for claim 1, it is characterized in that described Vaseline raw material comprises the frivolous slack wax of single vacuum residuum or its temper.
3, in accordance with the method for claim 2, it is characterized in that the described component that is in harmonious proportion with the frivolous slack wax of vacuum residuum comprises vacuum distillate base oil, vacuum distillate pressed oil and solvent-refined oil thereof.
4, in accordance with the method for claim 1, it is characterized in that described catalyzer is selected from W-Ni type Hydrobon catalyst and Mo-Ni type Hydrobon catalyst.
5, in accordance with the method for claim 1, it is characterized in that adopting two fixed-bed reactor, or adopt two beds of a reactors in series.
6, in accordance with the method for claim 5, it is characterized in that described two fixed-bed reactor or two identical catalyzer of beds filling, or load different catalyzer.
7, in accordance with the method for claim 1, it is characterized in that resulting Vaseline product is used for medicine and makeup.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310104987 CN1259396C (en) | 2003-10-31 | 2003-10-31 | Method for producing different consistency vaselines |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310104987 CN1259396C (en) | 2003-10-31 | 2003-10-31 | Method for producing different consistency vaselines |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1611579A true CN1611579A (en) | 2005-05-04 |
| CN1259396C CN1259396C (en) | 2006-06-14 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200310104987 Expired - Lifetime CN1259396C (en) | 2003-10-31 | 2003-10-31 | Method for producing different consistency vaselines |
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| Country | Link |
|---|---|
| CN (1) | CN1259396C (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102453549A (en) * | 2010-10-14 | 2012-05-16 | 中国石油化工股份有限公司 | Production method of vaseline |
| CN109988597A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | Flexible vaseline hydrogenation technique |
| CN109988616A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | A kind of flexible vaseline liquid-phase hydrogenatin technique |
| CN109988619A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | A kind of flexible vaseline hydrogenation technique |
-
2003
- 2003-10-31 CN CN 200310104987 patent/CN1259396C/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102453549A (en) * | 2010-10-14 | 2012-05-16 | 中国石油化工股份有限公司 | Production method of vaseline |
| CN109988597A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | Flexible vaseline hydrogenation technique |
| CN109988616A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | A kind of flexible vaseline liquid-phase hydrogenatin technique |
| CN109988619A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | A kind of flexible vaseline hydrogenation technique |
| CN109988597B (en) * | 2017-12-29 | 2021-05-04 | 中国石油化工股份有限公司 | Flexible vaseline 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 |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1259396C (en) | 2006-06-14 |
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Granted publication date: 20060614 |