CN106883887A - A kind of method for producing soap manufacturing paraffin - Google Patents
A kind of method for producing soap manufacturing paraffin Download PDFInfo
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- CN106883887A CN106883887A CN201510928622.5A CN201510928622A CN106883887A CN 106883887 A CN106883887 A CN 106883887A CN 201510928622 A CN201510928622 A CN 201510928622A CN 106883887 A CN106883887 A CN 106883887A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
- C10G73/42—Refining of petroleum waxes
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Abstract
The invention discloses a kind of method for producing soap manufacturing paraffin.The method is on the basis of common sweating de-oiling technique, the oil of liquid is carried out to force to separate wax and oil by wax layer using air-flow in sweating effort, the gas that the decomposable asymmetric choice net material using dissolving in the feed is produced simultaneously forms micro-bubble in wax layer, the quick discharge of oil is also beneficial to, so as to improve purpose product yield while shortening the production cycle.The inventive method has the advantages that investment of production equipment is low, production process is simple and operating cost is low, solvent-free pollution.
Description
Technical field
The invention belongs to pertroleum wax production technical field, more particularly to a kind of method for producing soap manufacturing paraffin.
Background technology
The general name of the pertroleum wax obtained all kinds of wax products that are crude oil after refining processing from wax-containing distillate, including atoleine, soap manufacturing paraffin, paraffin and microwax.Soap manufacturing paraffin is that lube cut is produced through steps such as dewaxing, de-oiling, refined and shapings in crude oil, typically contains the components such as n-alkane, a small amount of isoparaffin and cycloalkane, and fusing point is 40 DEG C~52 DEG C.
Dewaxing is the process for preparing the slack wax that oil content is 10~30% or so as raw material with lube cut.De-oiling is the process for preparing scale wax of the oil content below 2% as raw material with slack wax, and de-oiling technique mainly has solvent deoiling and sweating de-oiling.Scale wax is again through clay-filtered or hydrofinishing and shaping, packaging and other steps, you can obtain commodity oil wax.
Solvent deoiling method is in selective solvent according to wax with oil（Acetone, benzene and toluene mixture；Or acetone, toluene；Or MEK, toluene）What the property of middle different solubility was separate.Solvent deoiling technique has the advantages that production process is continuous, wax high income, finished product wax oil content can very low, production cost it is relatively low, be the main flow de-oiling technique for mass producing petroleum paraffin product at present.But solvent deoiling technique productions equipment investment is big；Needed in production process largely using solvent, recycling design needs to consume substantial amounts of energy；Contain benzene homologues in solvent, environment can be impacted；Solvent is inflammable, easily causes production accident.
Sweating de-oiling method is separated using the wax property different with oily fusing point.The molecular weight of various hydro carbons and structure Bu Tong can all make its fusing point different in pertroleum wax.When being all n-alkane structure, the fusing point of the larger n-alkane of molecular weight is higher, and the fusing point of the less n-alkane of molecular weight is relatively low；When molecular weight is identical, the fusing point of isoparaffin and cycloalkane will be less than n-alkane, and isomery degree more high-melting-point is lower, or even be in just at normal temperatures liquid condition, i.e., usually said oil.
Common sweating de-oiling technique is mainly included the following steps that：（1）Preparation：Pad water（Sweatbox ware plate lower space is full of with water）After feed（Load sweatbox when raw material is heated to more than fusing point being in a liquid state）；（2）Crystallization：Raw material is progressively cooled to 10~20 DEG C below its fusing point with being not more than the rate of temperature fall of 4 DEG C/h.In cooling procedure, order of the various components by fusing point from high to low crystallizes to form solid successively；（3）Sweating：After wax layer temperature reaches default cooling final temperature, pad water is bled off；Raw material is lentamente heated to default sweating final temperature again.In sweating effort, order of the various components by fusing point from low to high is successively fused into liquid and flows out（Under wax）, the wax layer residue for finally obtaining（On wax）It is exactly high-melting-point, the wax of low oil-containing；（4）It is refined：Collect crude product（Sweating effort terminates follow-up high-temperature of continuing rising, is taken out on wax with melting, as crude product）, through clay-filtered（Predetermined temperature is warming up to after crude product is melted, carclazyte is added and constant temperature is stirred to the scheduled time filtering）Afterwards, reshaping, packaging are purpose product.
To common sweating de-oiling technique, although wax and oily two classes component are respectively at solid and liquid condition in sweating effort, but also are difficult to be kept completely separate.For the oil content for making final products meets the requirements, generally using the method for extending sweating sessions and improve sweating final temperature.Extension sweating sessions can cause the production cycle to extend；Improving sweating final temperature can cause product yield to decline.
Compared with solvent deoiling, sweating de-oiling technique is intermittently operated, and product yield is relatively low, the production cycle is more long, but sweating de-oiling technique has, and small investment, production process be simple, the low advantage of operating cost, still has part producer producing soap manufacturing paraffin product using the method at present.
For many years, sweating method has obtained some development, such as CN89214332 in production equipment and process aspect（Vertical square multipul sections spacer diaphoresis tank）、CN94223980.6（Ware type sudorific device）、CN98233254.8（Paraffin sweating pot）、CN200920033500.X（Novel paraffin sweating tank）、CN201210508905.0（A kind of Efficient paraffin sweatbox）、CN201320127680.4（Tubular type paraffin deoiler）Deng being improved in sweating equipment；CN91206202（A kind of high-efficient sweat pot for paraffin wax）Improved in sweating de-oiling technique.But these methods there are still product yield it is relatively low, the production cycle is more long the shortcomings of.
Sweating de-oiling technique is to be currently known the unique solvent-free de-oiling method for commercial scale soap manufacturing paraffin product, and the concern of people is increasingly subject in today of promotion environmental protection, low-carbon energy-saving.
The content of the invention
In view of the shortcomings of the prior art, the present invention provides a kind of method for producing soap manufacturing paraffin, specifically using sweatbox, on the basis of common sweating de-oiling technique, adds oil-soluble decomposable asymmetric choice net to produce the material of gas after raw material heating fusing；And the oil of liquid is carried out to force to separate wax and oil by wax layer using air-flow in sweating effort, enhance separating effect and accelerate separating rate.The inventive method improves the yield of purpose product and shortens the production cycle, and has the advantages that plant investment is low, production process is simple and operating cost is low, solvent-free pollution.
A kind of method for producing soap manufacturing paraffin of the invention, including herein below：
（1）Charging：With oil content less than 30%, slack wax that fusing point is 25 DEG C~45 DEG C as raw material, load sweatbox after heating fusing；
（2）Crystallization：8 DEG C~20 DEG C below raw material fusing point of predetermined temperature is cooled to the speed of 1.0 DEG C/h~4.0 DEG C/h；
（3）Sweating：Heated up with the speed of 0.5 DEG C/h~3.0 DEG C/h；Wax layer is forced air flow through in temperature-rise period；Wax layer stops sweating after reaching predetermined temperature；
（4）It is refined：Collect on wax, purpose product is after refined, shaping.
In the method for production soap manufacturing paraffin of the invention, the oil content of the raw material slack wax（In mass）Less than 30%, its melting range is generally 25 DEG C~45 DEG C.Slack wax raw material can be the slack wax that atmosphere 3rd side cut or normal four lines distillate are obtained through dewaxing.
In the method for the present invention, after raw material heating fusing, the oil soluble material that decomposable asymmetric choice net produces gas is preferably added to.Concrete operations are first to heat sweating raw material and melt, then produce the material of gas to load sweatbox after being dissolved in raw material oil-soluble decomposable asymmetric choice net.One or more of described oil-soluble decomposable asymmetric choice net material including organic azo compound, sulfonyl hydrazines compound, organic nitroso compounds, organic peroxide etc., preferably in organic azo compound and organic peroxide.The addition of oil-soluble decomposable asymmetric choice net material is the 0.01%~15.00% of raw material weight, preferably 0.03%~8.00%.
Wherein, described organic azo compound is selected from ABVN（ABVN）, azodiisobutyronitrile（AIBN）, azo diisopropyl imidazoline hydrochloride（ACCN）The one group of material for constituting；Described sulfonyl hydrazines compound is selected from benzene sulfonyl hydrazide, unifor, 4,4 '-bis oxide（Benzene sulfonyl hydrazide）The one group of material for constituting；Described organic nitroso compounds are selected from dinitrosopentamethylene tetramine and/or N, N '-dimethyl N, N '-dinitroso phthalic amide；The organic peroxide is selected from dibenzoyl peroxide（BPO）, dilauroyl peroxide（LPO）, diacetyl peroxide, peroxy dicarbonate isopropyl ester（IPP）, di-cyclohexylperoxy di-carbonate（DCPO）Etc. one group of material of composition.
In the method for the present invention, described sweatbox is sweating ware, and increases vacuum plant in wax layer pressue device added above and/or below wax layer.It is described force air flow through wax layer and use increase above wax layer air pressure and/or air pressure is reduced below wax layer, wax layer upper and lower is formed pressure differential and realize.Described pressure differential is generally 0.1~5.0 atmospheric pressure, preferably 0.2~2.0 atmospheric pressure, to force air flow through wax layer.
In the method for the present invention, the rate of temperature fall preferably 2.0 DEG C/h~3.0 DEG C/h of the raw material wax layer crystallization process.
In the method for the present invention, 10 DEG C~15 DEG C below the cooling final temperature preferred feedstock slack wax fusing point of the raw material wax layer crystallization process.
In the method for the present invention, the heating rate preferably 1.0 DEG C/h~2.0 DEG C/h of the raw material wax layer sweating effort.The predetermined temperature of the intensification is 2 DEG C~10 DEG C of the fusing point less than purpose product.
In the method for the present invention, the programming rate and cooling rate of said wax layer can be controlled, it is preferred to use water-bath or oil bath by air bath, water-bath, oil bath or other feasible modes.When controlling wax layer heating rate and rate of temperature fall using water-bath or oil bath mode, chuck can be increased outside sweating ware, chuck is connected with removable coil pipe and the circulatory system, chuck, coil pipe etc. can make wax layer lifting/lowering temperature process faster, wax layer more uniform temperature；The circulatory system has programmed cooling/heating function, and the circulatory system adds the materials such as water or conduction oil as circulatory mediator.
It is described to force air flow through wax layer and implement in sweating effort any stage in the method for the present invention, preferably implement at the sweating initial stage.
In the method for the present invention, the described wax layer that forces air flow through is utilized in what increase air pressure in wax layer top was realized, and 0.2~2.0 atmospheric pressure can be such as applied above wax layer（Gauge pressure）Pressure, and wax layer lower section remain normal pressure.
In the method for the present invention, the described wax layer that forces air flow through is utilized in what reduction air pressure in wax layer lower section was realized, and normal pressure can be such as kept above wax layer, and -0.2~-1.0 atmospheric pressure are maintained below wax layer（Gauge pressure）Pressure.
Sweating de-oiling method is to be separated to produce soap manufacturing paraffin using the wax property different with oily fusing point, but in sweating effort, the wax of solid-state and the oil of liquid are difficult to be kept completely separate in wax layer, and this is that intermolecular force is larger because wax and oily two kinds of components are all nonpolar hydrocarbon molecules；The wax crystallization of solid-state forms capillary pipe structure simultaneously, there is stronger suction-operated to oil, and this results in and only is difficult to be kept completely separate by wax in the common sweating effort of gravity natural separation and oil.Generally the oil content of final products is set to meet the requirements using methods such as extension sweating sessions, raising sweating final temperatures, but this can cause production cycle extension, the reduction of wax product yield again.These have impact on the extensive use of sweating de-oiling method.
The present invention is difficult to be kept completely separate reason by the further investigation to common sweating effort for wax and oil, forces the separation of wax and oil by the method that wax layer carries out fluid oil using air-flow in sweating effort, enhances separating effect and accelerates separating rate.Oil-soluble decomposable asymmetric choice net material further preferably is added after raw material heating fusing simultaneously, these material decomposable asymmetric choice nets produce gas, and have preferable dissolubility in the feed and be dispersed in wax layer.Wax layer is in softer solid state in the time that raw material terminates after being cooled to below fusing point to sweating effort, decomposable asymmetric choice net material slowly decomposes the gas for discharging during this, dispersed micro-bubble can be formed in wax layer, the space that these micro-bubbles are formed is easy to form some tiny passages in wax layer in sweating effort, so as to be conducive to the discharge of oil in sweating effort.The nontoxic gases without special odor such as preferred oil-soluble decomposable asymmetric choice net substance decomposition generation nitrogen or carbon dioxide, and the other materials molecular weight for generating is low, and wax layer will be discharged with the oil of liquid in sweating effort.The oil of liquid is carried out to force to separate wax and oil by wax layer using air-flow in sweating effort simultaneously, separating effect is enhanced and is accelerated separating rate.
It is an advantage of the invention that：By forcing the separation of wax and oil by the method that wax layer carries out fluid oil using air-flow in sweating effort, enhance separating effect and accelerate separating rate；The gas for being produced using oil-soluble decomposable asymmetric choice net substance decomposition simultaneously forms dispersed micro-bubble in wax layer, is also beneficial to the quick discharge of oil, so as to reach the purpose for improving wax product yield and shortening the production cycle.Method of the present invention plant investment is low, production process is simple and operating cost is low, it is solvent-free pollution environment the advantages of so that sweating de-oiling it is this it is solvent-free production soap manufacturing paraffin method more highly effective.
Specific embodiment
Sweating ware top connects dismountable sealing device and is connected with pressurized buffer tank and compressor, and/or connects pressure-reducing cushioning tank and vavuum pump in sweating ware bottom；The material that oil-soluble decomposable asymmetric choice net produces gas is melted and is preferably added in raw material heating；Wax layer heating-cooling speed is controlled with water-bath；In sweating effort, start compressor with wax layer malleation formed above, and/or start vavuum pump in wax layer negative pressure formed below, to be used to force air flow through wax layer；Wax layer temperature stops sweating effort after reaching preset temperature；It is purpose product to be after clay-filtered, shaping, packaging on wax.Can be reduced in the case of 30%~40% in the time in sweating stage by these means, purpose product yield is improved 5~10 percentages.
The method that present invention production soap manufacturing paraffin is illustrated below by way of specific embodiment.
Comparative example
1
This comparative example includes：（1）Preparation,（2）Crystallization,（3）Sweating,（4）The process such as refined.
（1）Preparation
Sweating ware ware plate lower section pad water.The sealing system of sweating ware is connected with pressurized buffer tank and compressor；Pressure-reducing cushioning tank is installed in sweating ware bottom and vavuum pump is connected；Sweating ware chuck and removable coil pipe are connected with the circulatory system, coil pipe is fixed on sweating ware；With water as medium, start the heating function of the circulatory system, recirculated water is warming up to 43 DEG C.
With normal four lines slack wax（41.5 DEG C of fusing point, oil content 13.2%）It is raw material, sweating ware is added after being heated to 43 DEG C of fusings.
（2）Crystallization
Start the refrigerating function of the circulatory system, control wax layer temperature drops to 30.0 DEG C so that wax layer is crystallized to form solid with the rate of temperature fall of 2.0 DEG C/h.Close the refrigerating function of the circulatory system.
（3）Sweating
Discharge sweating ware pad water.The outlet of sweating ware connects intermediate storage tank to receive under wax；The sealing system on sweating ware top is installed；Start compressor and keep pressurized buffer pressure inside the tank stabilization in 1.2~1.4 atmospheric pressure（Gauge pressure）, sweating ware ware plate lower section keeps normal pressure.Start the heating function of the circulatory system, wax layer temperature is increased to 36.0 DEG C with the heating rate of 1.5 DEG C/h；Stop compressor.
Start vavuum pump and keep pressure-reducing cushioning pressure inside the tank stabilization in -0.5~-0.7 atmospheric pressure（Gauge pressure）, wax layer top air pressure holding normal pressure；Continuation makes wax layer temperature be increased to 42.0 DEG C with the heating rate of 1.5 DEG C/h carries out sweating.Stop vavuum pump, terminate sweating effort（Sweating phases-time is 8 hours）.
（4）It is refined
The outlet of sweating ware is changed to connect crude product storage tank；Continue heat cycles water and be warming up to 60 DEG C to melt on taking-up wax, as crude product（Ⅰ）.
Crude product（Ⅰ）It is purpose product after clay-filtered, shaping, packaging.
Product（Ⅰ）Property：46.3 DEG C of fusing point, oil content 1.76%, meet the associated specifications of commodity soap manufacturing paraffin top grade product.Soap manufacturing paraffin product yield is 41.5%（Relative raw material slack wax）.
Embodiment
1
The present embodiment includes：（1）Preparation,（2）Crystallization,（3）Sweating,（4）The process such as refined.
（1）Preparation
Sweating ware ware plate lower section pad water.The sealing system of sweating ware is connected with pressurized buffer tank and compressor；Pressure-reducing cushioning tank is installed in sweating ware bottom and vavuum pump is connected；Sweating ware chuck and removable coil pipe are connected with the circulatory system, coil pipe is fixed on sweating ware.With water as medium.Start the heating function of the circulatory system, recirculated water is warming up to 43 DEG C.
With normal four lines slack wax（Property is with comparative example 1）It is raw material, is heated to 43 DEG C of fusings, add 0.30% peroxy dicarbonate isopropyl ester, sweating ware is added after stirring.
（2）Crystallization
Start the refrigerating function of the circulatory system, control wax layer temperature drops to 30.0 DEG C so that wax layer is crystallized to form solid with the rate of temperature fall of 2.0 DEG C/h.Close the refrigerating function of the circulatory system.
（3）Sweating
Discharge sweating ware pad water.The outlet of sweating ware connects intermediate storage tank to receive under wax；The sealing system on sweating ware top is installed；Start compressor and keep pressurized buffer pressure inside the tank stabilization in 1.2~1.4 atmospheric pressure（Gauge pressure）, sweating ware ware plate lower section keeps normal pressure.Start the heating function of the circulatory system, wax layer temperature is increased to 36.0 DEG C with the heating rate of 1.5 DEG C/h, stop compressor.
Start vavuum pump and keep pressure-reducing cushioning pressure inside the tank stabilization in -0.5~-0.7 atmospheric pressure（Gauge pressure）, wax layer top air pressure holding normal pressure；Continuation makes wax layer temperature be increased to 42.0 DEG C with the heating rate of 1.5 DEG C/h carries out sweating.Stop vavuum pump, terminate sweating effort（Sweating phases-time is 8 hours）.
（4）It is refined
The outlet of sweating ware is changed to connect crude product storage tank；Continue heat cycles water and be warming up to 60 DEG C to melt on taking-up wax, as crude product（Ⅱ）.
Crude product（Ⅱ）It is purpose product after clay-filtered, shaping, packaging.
Product（Ⅱ）Property：46.8 DEG C of fusing point, oil content 1.47%, meet the associated specifications of commodity soap manufacturing paraffin top grade product.Soap manufacturing paraffin product yield is 44.0%（Relative raw material slack wax）.
Comparative example
2
With normal four lines slack wax（Property is with embodiment 1）It is raw material, common sweat tank is added after heating fusing.Wax layer temperature drop to 30.0 DEG C is made with the rate of temperature fall of 2.0 DEG C/h；Wax layer temperature is increased to 42.0 DEG C with the heating rate of 1.0 DEG C/h carries out sweating de-oiling（Sweating phases-time is 12 hours）.Sweating is taken out on wax after terminating, and is purpose product after clay-filtered, shaping.
Product property：47.3 DEG C of fusing point, oil content 1.71%, meet the technical requirements of commodity soap manufacturing paraffin.Soap manufacturing paraffin product yield is 34.1%.
The method that present invention production soap manufacturing paraffin is can be seen that by embodiment 1 and comparative example 1-2, forces the separation of wax and oil using air-flow in sweating effort by the method that wax layer carries out fluid oil, enhances separating effect and accelerates separating rate；The gas produced using oil-soluble decomposable asymmetric choice net material forms the quick discharge that dispersed micro-bubble is more favorable to oil in wax layer, so as to improve purpose wax product yield.Compared with comparative example 1, the yield of purpose wax increased 2.5 percentage points to embodiment 1, and oil content reduces 0.29 percentage point.Compared with comparative example 2, the yield of purpose wax increased 9.9 percentage points to embodiment 1, and oil content reduces 0.24 percentage point.And compared with comparative example 2, the time in the sweating stage of embodiment 1, reduce 33%.
Claims (16)
1. a kind of method for producing soap manufacturing paraffin, including herein below：
（1）Charging：With oil content less than 30%, slack wax that fusing point is 25 DEG C~45 DEG C as raw material, add oil-soluble decomposable asymmetric choice net to produce the material of gas after heating fusing, load sweatbox；
（2）Crystallization：8 DEG C~20 DEG C below raw material fusing point of predetermined temperature is cooled to the speed of 1.0 DEG C/h~4.0 DEG C/h；
（3）Sweating：Heated up with the speed of 0.5 DEG C/h~3.0 DEG C/h；Wax layer is forced air flow through in temperature-rise period；Wax layer stops sweating after reaching predetermined temperature；
（4）It is refined：Collect on wax, purpose product is after refined, shaping.
2. in accordance with the method for claim 1, it is characterised in that it is the 0.01%~15% of raw material weight that described oil-soluble decomposable asymmetric choice net produces the addition of the material of gas.
3. in accordance with the method for claim 2, it is characterised in that it is the 0.03%~8% of raw material weight that described oil-soluble decomposable asymmetric choice net produces the addition of gaseous matter.
4. in accordance with the method for claim 1, it is characterised in that described oil-soluble decomposable asymmetric choice net produces the material of gas to be selected from one group of material that organic azo compound, sulfonyl hydrazines compound, organic nitroso compounds, organic peroxide are constituted.
5. in accordance with the method for claim 2, it is characterised in that described organic azo compound is selected from one group of material that ABVN, azodiisobutyronitrile, azodicarbonamide and azo diisopropyl imidazoline hydrochloride are constituted；Described sulfonyl hydrazines compound is selected from one group of material that benzene sulfonyl hydrazide, unifor, 4,4 '-bis oxide (benzene sulfonyl hydrazide) are constituted；Described organic nitroso compounds are selected from dinitrosopentamethylene tetramine and/or N, N '-dimethyl N, N '-dinitroso phthalic amide；Described organic peroxide is selected from one group of material that dibenzoyl peroxide, dilauroyl peroxide, di-tert-butyl peroxide, peroxy dicarbonate isopropyl ester and di-cyclohexylperoxy di-carbonate are constituted.
6. in accordance with the method for claim 1, it is characterised in that it is organic azo compound and/or organic peroxide that described oil-soluble decomposable asymmetric choice net produces the material of gas.
7. in accordance with the method for claim 1, it is characterised in that step（2）Described in lower the temperature speed be 2.0 DEG C/h~3.0 DEG C/h.
8. in accordance with the method for claim 1, it is characterised in that step（2）Described in predetermined temperature for 10 DEG C~15 DEG C below raw material fusing point.
9. in accordance with the method for claim 1, it is characterised in that step（3）Described in heat up speed be 1.0 DEG C/h~2.0 DEG C/h.
10. in accordance with the method for claim 1, it is characterised in that step（3）Described in the predetermined temperature that heats up be 2 DEG C~10 DEG C of fusing point less than purpose product.
11. in accordance with the method for claim 1, it is characterised in that the described wax layer that forces air flow through is implemented at the sweating initial stage.
12. in accordance with the method for claim 1, it is characterised in that step（3）Described in the wax layer that forces air flow through use to increase above wax layer and air pressure and/or air pressure reduced below wax layer, wax layer upper and lower is formed pressure differential and realize, described pressure differential is 0.1~5.0 atmospheric pressure.
13. in accordance with the method for claim 12, it is characterised in that the described wax layer that forces air flow through uses the increase air pressure above wax layer to realize, 0.2~2.0 gauge of atmospheric pressure is applied above wax layer, and wax layer lower section remains normal pressure.
14. in accordance with the method for claim 12, it is characterised in that the described wax layer that forces air flow through uses the reduction air pressure below wax layer to realize that air pressure keeps normal pressure above wax layer, and -0.2~-1.0 gauges of atmospheric pressure are maintained below wax layer.
15. in accordance with the method for claim 12, it is characterised in that described pressure differential is 0.2~2.0 atmospheric pressure.
16. in accordance with the method for claim 1, it is characterised in that described sweatbox is sweating ware.
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| CN201510928622.5A CN106883887B (en) | 2015-12-15 | 2015-12-15 | A method of producing soap manufacturing paraffin |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB687235A (en) * | 1950-03-24 | 1953-02-11 | Bataafsche Petroleum | Improvements in and relating to the treatment of paraffin wax |
| CN1760278A (en) * | 2004-10-12 | 2006-04-19 | 中国石油天然气股份有限公司 | Wax-for preventing rubber |
| CN101649119A (en) * | 2009-03-20 | 2010-02-17 | 上海绿菱特种蜡制品厂 | Novel rubber protective wax |
-
2015
- 2015-12-15 CN CN201510928622.5A patent/CN106883887B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB687235A (en) * | 1950-03-24 | 1953-02-11 | Bataafsche Petroleum | Improvements in and relating to the treatment of paraffin wax |
| CN1760278A (en) * | 2004-10-12 | 2006-04-19 | 中国石油天然气股份有限公司 | Wax-for preventing rubber |
| CN101649119A (en) * | 2009-03-20 | 2010-02-17 | 上海绿菱特种蜡制品厂 | Novel rubber protective wax |
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