CN102757821A - Solvent dewaxing method for low waxy hydrocarbon oil - Google Patents
Solvent dewaxing method for low waxy hydrocarbon oil Download PDFInfo
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Abstract
The invention relates to a solvent dewaxing method for low waxy hydrocarbon oil. The method includes: mixing raw oil, dewaxing auxiliaries and dewaxing solvent, cooling the mixture to a filtering temperature, filtering to obtain filtrate and cerate, and removing the solvent from the filtrate to obtain dewaxed oil, wherein C17-C100 n-alkane mass content in the dewaxing auxiliaries is larger than or equal to 40%, and the mass ratio of the dewaxing auxiliaries to the raw oil ranges from 0.01:1 to 0.30:1. Compared with conventional solvent dewaxing techniques, the solvent dewaxing method has the advantage that the low waxy hydrocarbon oil can be dewaxed more effectively to lower dewaxing temperature difference and increase filtering speed.
Description
Technical field
The invention belongs to the process for dewaxing of hydrocarbon ils.Specifically, the present invention relates to a kind of solvent-dewaxing method of low content of wax hydrocarbon ils.
Background technology
In order to keep the low-temperature fluidity of lubricating oil, must in the production process of lubricant base, remove wax contained in the raw oil, to reduce the condensation point or the pour point of lubricant base.Be divided into paraffin and Microcrystalline Wax to the wax product of wax after de-oiling in the industry, paraffin is main with normal paraffin and a certain amount of isoparaffin, and Microcrystalline Wax then contains normal paraffin, isoparaffin and alkyl cyclic hydrocarbon, and contains a certain amount of alkylaromatic hydrocarbon.The method of lubricating oil dewaxing has a variety of, and wherein the most frequently used is solvent dewaxing process.The principle of solvent dewaxing is exactly that raw oil and dewaxing solvent is miscible; Progressively cooling then utilizes the solvent insoluble or oligodynamical and to the characteristic of other components dissolved, wax crystallization in solution is separated out to the wax component at low temperatures; Filter at last, oil is separated with wax.
The solvent dewaxing technology not only can be used for removing the wax of lube stock, also can be used for separating the component of the different zero pour of other oil products.For different oil products, because the difference that the different and product of the wax content of raw oil and wax molecular structure requires pour point, its solvent dewaxing process has than big-difference.For example: in the process of extracting oil production environment-friendly rubber extending oil with furfural treatment out, must remove the wax of extracting out in the oil earlier, then could be with its raw materials for production as environment-friendly rubber extending oil.Yet, very difficult with the wax that conventional solvent dewaxing process removes in the furfural treatment extraction oil.
The height of hydrocarbon ils wax content does not have the unified criteria for classifying.For lubricant base; It is generally acknowledged that the lube stock oil that is obtained by paraffinic crude is high waxy feeds oil; The lube stock oil that is obtained by naphthenic base crude is low waxy feeds oil; The wax content of the lube stock oil that is obtained by intermediate base crude oil is partial to naphthenic base crude more between between the two above-mentioned, and wax content is low more; And the isoparaffin in the wax component, the naphthenic hydrocarbon that has long side chain or aromatic hydrocarbons are many more, adopt the pour point of conventional solvent-dewaxing method reduction waxy oil more difficult.No matter be the content of wax hydrocarbon ils that obtains by the crude oil time processing; Still the content of wax hydrocarbon ils that obtains after the secondary processing; When the wax content of hydrocarbon ils is low to a certain degree the time, can't adopt conventional solvent-dewaxing method production to meet the pressed oil that pour point requires, this type hydrocarbon ils just is called low content of wax hydrocarbon ils.
Summary of the invention
The invention provides a kind of solvent-dewaxing method of low content of wax hydrocarbon ils, this method can more effectively remove the wax in the low content of wax hydrocarbon ils, reduces dewaxing differential, improves filtration velocity.
A kind of solvent-dewaxing method of low content of wax hydrocarbon ils comprises: raw oil, dewaxing agent and dewaxing solvent are mixed, be cooled to filtration temperature, filter and obtain dewaxed filtrate and dewaxing slack wax, after dewaxed filtrate removes solvent, obtain pressed oil; Dewaxing slack wax and de-oiling solvent are warmed up to filtration temperature, filter to obtain de-oiling filtrating and de-oiling slack wax; In the said dewaxing agent, mass content >=40% of C17～C100 normal paraffin; The mass ratio of dewaxing agent and raw oil is 0.01: 1 to 0.30: 1.
Described dewaxing agent is preferably petroleum paraffin and/or synthetic paraffin.When using petroleum paraffin and/or synthetic paraffin as dewaxing agent, the mass ratio of dewaxing agent and raw oil is preferably 0.01: 1 to 0.15: 1, more preferably 0.02: 1 to 0.12: 1.
Petroleum paraffin is meant the paraffin that from natural oil, obtains.The melting range of said petroleum paraffin is preferably between 52 ℃～72 ℃, more preferably between 56 ℃～68 ℃.The oleaginousness of said petroleum paraffin is preferably between 0.4%～5.0%, more preferably between 0.5%～2.0%.
Synthetic paraffin is meant the paraffin of synthetic, the paraffin of by-product or the paraffin that is obtained by the ethylene catalyst polymerization as with Fischer-Tropsch process synthesis of artificial oil the time.
" low the content of wax " among the present invention is meant that naphthenic hydrocarbon that has long side chain or the aromatic hydrocarbons in the lower and wax of the wax content of hydrocarbon ils is more, can't adopt conventional solvent-dewaxing method production to meet the pressed oil that pour point requires.
Raw oil of the present invention can be fraction oil of petroleum, frivolous asphalt oil and extract in the oil one or more by above-mentioned two types of raw materials out through solvent-refined oil that solvent treatment obtains and solvent treatment.
Raw oil pour point of the present invention is preferably between 5 ℃～40 ℃, more preferably between 10 ℃～35 ℃.
Under the preferred situation, earlier dewaxing agent is dissolved in raw oil, and then adds dewaxing solvent.The temperature that dewaxing agent is dissolved in raw oil is preferably 50 ℃～110 ℃, more preferably 75 ℃～90 ℃.
The filtration temperature of dewaxing in the step is preferably-25 ℃～0 ℃, more preferably-20 ℃～-10 ℃.
Described dewaxing solvent is the mixture of ketone and aromatic hydrocarbons, and ketone wherein is preferably acetone and/or butanone, and aromatic hydrocarbons is preferably benzene and/or toluene; More preferably adopt wax solubleness little and to these whole dissolved dewaxing solvents of oil base, like the mixture of butanone and toluene.
The mixture that adopts butanone and toluene is during as dewaxing solvent, is benchmark with the TV of butanone-toluene mixed solvent, and the volume content of butanone is 40% to 85%, is preferably 50% to 75%.
The mixture that adopts butanone and toluene is during as dewaxing solvent, and the mass ratio of butanone-toluene mixed solvent and raw oil is 1.0: 1 to 8.0: 1, is preferably 2.0: 1 to 5.5: 1.
Among the present invention, dewaxing solvent can disposablely add, and also can add several times, preferably divides 3 or 4 addings.
According to the ratio of solvent and low waxy feeds oil, those skilled in the art can easily confirm the additional proportion of each point diluting solvent.
According to the viscosity of material in the process of cooling, those skilled in the art can easily confirm the adding temperature of each point diluting solvent.
Described de-oiling solvent is the mixture of ketone and aromatic hydrocarbons, and ketone wherein is preferably acetone and/or butanone, and aromatic hydrocarbons is preferably benzene and/or toluene; More preferably adopt wax solubleness little and to these whole dissolved dewaxing solvents of oil base, like the mixture of butanone and toluene.
The mixture that adopts butanone and toluene is during as the de-oiling solvent, is benchmark with the TV of butanone-toluene mixed solvent, and the volume content of butanone is 40% to 85%, is preferably 50% to 75%.
The mixture that adopts butanone and toluene is during as the de-oiling solvent, and the mass ratio of butanone-toluene mixed solvent and raw oil is 0.2: 1 to 2.5: 1, is preferably 0.3: 1 to 1.3: 1.
Among the present invention, the de-oiling solvent can disposablely add, and also can add several times, preferred disposable adding.
Filtration temperature in the de-oiling step (de-oiling temperature) is between 10 ℃～40 ℃, preferably between 15 ℃～30 ℃.
The present invention can carry out a de-oiling again after the de-oiling step, the temperature of de-oiling for the second time is greater than or equal to the temperature of de-oiling for the first time.The present invention preferably only carries out a de-oiling.
The present invention can once dewax after the dewaxing step again; Dewax filtration temperature for the second time between the filtration temperature that dewaxes for the first time is extremely than its scope of low 5 ℃; And then will filter the slack wax that obtains for the second time and carry out de-oiling; Be used as dewaxing solvent for the first time with filtering the filtrating that obtains for the second time, preferably be used as secondary, three times or four diluting solvents in the dewaxing for the first time.
Under the preferred situation, the present invention can be with de-oiling slack wax cyclically utilizing, and instead of part or whole dewaxing agents are to practice thrift the consumption of dewaxing agent.The present invention has no particular limits the reuse ratio of de-oiling slack wax.
Method of the present invention also comprises, the de-oiling slack wax is removed solvent, obtains dewaxed oil.The present invention can recycle dewaxed oil as dewaxing agent.Equally, the present invention also has no particular limits the ratio of dewaxed oil as dewaxing agent.
Method of the present invention also comprises, from de-oiling filtrating, isolates sweat oil.
Under the preferred situation, in the said dewaxing agent, mass content >=40% of C17～C70 normal paraffin.
The method of solvent is well known in the art in said separating filtrate and the slack wax, for example respectively logistics is sent into solvent recovery tower except that desolvating, and recovered solvent recycles.Among the present invention, the solvent after the recovery can contain a spot of raw oil component.
All relate in the different components blended step among the present invention, preferably adopt mixing tank enhancing mixed effect.Described mixing tank belongs to prior art, and the present invention can adopt the conventional liquid mixer in this area.
No matter be the content of wax hydrocarbon ils that obtains by the crude oil time processing; Still the content of wax hydrocarbon ils that obtains after the secondary processing; Low the arriving to a certain degree of wax content when hydrocarbon ils; In the time of can't adopting conventional solvent-dewaxing method production to meet the pressed oil that pour point requires, just can adopt method of the present invention to produce the pressed oil that meets the pour point requirement.
Wax with conventional solvent dewaxing process removes in the low content of wax hydrocarbon ils is very difficult, and major cause is: the wax content in the 1. low content of wax hydrocarbon ils is lower, and high melting point component content still less causes the brilliant granule density of wax in the mixed solution lower; 2. the more important thing is; Wax major part in the low content of wax hydrocarbon ils is naphthenic hydrocarbon or the aromatic hydrocarbons that has long side chain, and the wax crystalline substance that in the solvent dewaxing process, forms is more tiny, and little wax crystalline substance penetrates filter cloth easily; Get in the pressed oil, cause dewaxing differential increase, dewaxing effect to reduce; 3. in addition, big slightly wax crystalline substance is stuck in the filter cloth duct, stop up to filter the duct, reduces the filter of filter cloth and passes through performance, and the temperature that has a strong impact on filtration velocity and increase filter cloth is washed the frequency.With the solvent dewaxing compared with techniques of routine, the present invention can more effectively remove the wax in the low content of wax hydrocarbon ils, reduces dewaxing differential, improves filtration velocity.
Description of drawings
Accompanying drawing is the block diagram of a kind of preferred implementation of the present invention
Embodiment
Below in conjunction with accompanying drawing, a kind of preferred implementation of the present invention is described.
Low waxy feeds oil through pipeline 1 with mix from the dewaxing agent of pipeline 2 and/or the dewaxed oil of pipeline 25; Heat in well heater 4 through pipeline 3, mixture mixes in mixing tank 6 through pipeline 5, in water cooler 10, is cooled to dewaxing temperature through pipeline 9 through pipeline 7 and dewaxing solvent from pipeline 8; Getting into strainer 12 through pipeline 11 filters; Dewaxed filtrate removes solvent through pipeline 13 regenerating column 14 that desolvates, and obtains pressed oil through pipeline 15, does not mark the trend that removes solvent among the figure.The dewaxing slack wax is warming up to the de-oiling temperature through pipeline 16 and de-oiling solvent from pipeline 17 through pipeline 18 in well heater 19; Getting into strainer 21 through pipeline 20 filters; De-oiling filtrating removes solvent through pipeline 22 in solvent recovery tower 23; Obtain sweat oil through pipeline 24, do not mark the trend that removes solvent among the figure.The de-oiling slack wax removes solvent through pipeline 26 regenerating column 27 that desolvates, and dewaxed oil can join in the raw oil through pipeline 25 pipelines and use as dewaxing agent, also can obtain dewaxed oil through pipeline 28, does not mark the trend that removes solvent among the figure.
Below further specify the present invention through embodiment.
Raw oil is for subtracting four line distillates, and its character is seen table 1.The mass ratio of dewaxing agent and raw oil is 0.07: 1, and dewaxing solvent is butanone-toluene mixed solvent, and the volume content of butanone is 50%, adopts multipoint dilution technology, total agent-oil ratio 3.8: 1.The de-oiling solvent is identical with dewaxing solvent, adopts once dilution, and agent-oil ratio is 0.3: 1 (with respect to a raw oil).Press the flow preparation pressed oil of accompanying drawing 1, detailed process is following:
(1) with the paraffin of 68 ℃ of fusing points as dewaxing agent
The paraffin that fusing point is 68 ℃ joins in the raw oil as dewaxing agent, is heated to 75 ℃, after fully melting and mixing, adds each time diluting solvent successively.Be cooled to-15 ℃,, obtain pressed oil after filtrating removes solvent through filtering dewaxed filtrate and dewaxing slack wax.In slack wax, add diluting solvent and mix, be heated to 30 ℃, through filtering de-oiling filtrating and de-oiling slack wax, filtrating obtains sweat oil after removing solvent, and slack wax obtains dewaxed oil after removing solvent.The part dewaxed oil recycles as dewaxing agent, and recovered solvent recycles as dewaxing solvent.
(2) with the paraffin of 68 ℃ of dewaxed oil and fusing points as dewaxing agent
The paraffin that uses 68 ℃ of dewaxed oil and fusing points is as dewaxing agent, and the mass ratio of dewaxed oil and 68 ℃ of paraffin of fusing point is 8: 2, and all the other operations are identical with (1) with test conditions.The dewaxed oil that obtains in (1) is used in test for the first time, the dewaxed oil that each later on test uses last test to obtain, and revision test repeatedly when double test-results is identical, is got the result of last test, sees table 2.
Comparative Examples 1
Except that specifying, the raw material in this Comparative Examples, operation and test conditions are all identical with embodiment 1.Only carry out the dewaxing process in (1), and do not use dewaxing agent, the dewaxing result sees table 2.
Comparative Examples 2
Except that specifying, the raw material in this Comparative Examples, operation and test conditions are all identical with embodiment 1.(1) do not add dewaxing agent in.(2) only increase the wax content of raw oil in dewaxed oil; The mass ratio of dewaxed oil and raw oil is 0.07: 1, and the dewaxed oil that obtains in (1) is used in test for the first time, the dewaxed oil that each later on test uses last test to obtain; Revision test repeatedly; When double test-results is identical, get the result of last test, see table 2.
Raw oil is for subtracting three-way furfural refining oil, and its character is seen table 1.The mass ratio of dewaxing agent and raw oil is 0.02: 1, and dewaxing solvent is butanone-toluene mixed solvent, and the volume content of butanone is 75%, adopts multipoint dilution technology, total agent-oil ratio 2.0: 1.The de-oiling solvent is identical with dewaxing solvent, adopts once dilution, and agent-oil ratio is 1.3: 1 (with respect to a raw oil).Press the flow preparation pressed oil of accompanying drawing 1, detailed process is following:
(1) with the paraffin of 56 ℃ of fusing points as dewaxing agent
The paraffin that fusing point is 56 ℃ adds in the raw oil as dewaxing agent, is heated to 90 ℃, after fully melting and mixing, adds each time diluting solvent successively.Be cooled to-20 ℃,, obtain pressed oil after filtrating removes solvent through filtering dewaxed filtrate and dewaxing slack wax.In slack wax, add diluting solvent and mix, be heated to 15 ℃, through filtering de-oiling filtrating and de-oiling slack wax, filtrating obtains sweat oil after removing solvent, and slack wax obtains dewaxed oil after removing solvent.The dewaxed oil that all uses the de-oiling section to produce is recycled to the dewaxing section as dewaxing agent, and recovered solvent recycles as dewaxing solvent.
(2) with dewaxed oil as dewaxing agent
Only with dewaxed oil as dewaxing agent, all the other operations are identical with (1) with test conditions.The dewaxed oil that obtains in (1) is used in test for the first time, the dewaxed oil that each later on test uses last test to obtain, and revision test repeatedly when double test-results is identical, is got the result of last test, sees table 2.
Comparative Examples 3
Except that specifying, the raw material in this Comparative Examples, operation and test conditions are all identical with embodiment 2.(1) do not add dewaxing agent in.(2) only increase the wax content of raw oil in dewaxed oil; The mass ratio of dewaxed oil and raw oil is 0.02: 1, and the dewaxed oil that obtains in (1) is used in test for the first time, the dewaxed oil that each later on test uses last test to obtain; Revision test repeatedly; When double test-results is identical, get the result of last test, see table 2.
Raw oil is extracted oil out for subtracting three-way solvent treatment, and its character is seen table 1.The mass ratio of dewaxing agent and raw oil is 0.12: 1, and dewaxing solvent is butanone-toluene mixed solvent, and the volume content of butanone is 65%, adopts multipoint dilution technology, total agent-oil ratio 5.5: 1.The de-oiling solvent is identical with dewaxing solvent, adopts once dilution, and agent-oil ratio is 0.7: 1 (with respect to a raw oil).Press the flow preparation pressed oil of accompanying drawing 1, detailed process is following:
(1) with the paraffin of 62 ℃ of fusing points as dewaxing agent
The paraffin that fusing point is 62 ℃ adds in the raw oil as dewaxing agent, and heating paraffin to 80 ℃ after fully melting and mixing, adds each time diluting solvent successively.Be cooled to-10 ℃,, obtain pressed oil after filtrating removes solvent through filtering dewaxed filtrate and dewaxing slack wax.In slack wax, add diluting solvent and mix, be heated to 20 ℃, through filtering de-oiling filtrating and de-oiling slack wax, filtrating obtains sweat oil after removing solvent, and slack wax obtains dewaxed oil after removing solvent.The part dewaxed oil recycles as dewaxing agent, and recovered solvent recycles as dewaxing solvent.
(2) with the paraffin of 62 ℃ of dewaxed oil and fusing points as dewaxing agent
The paraffin that uses 62 ℃ of dewaxed oil and fusing points is as dewaxing agent, and the mass ratio of dewaxed oil and 62 ℃ of paraffin of fusing point is 6: 4, and all the other operations are identical with (1) with test conditions.The dewaxed oil that obtains in (1) is used in test for the first time, the dewaxed oil that each later on test uses last test to obtain, and revision test repeatedly when double test-results is identical, is got the result of last test, sees table 2.
Comparative Examples 4
Except that specifying, the raw material in this Comparative Examples, operation and test conditions are all identical with embodiment 3.Only carry out the dewaxing process in (1), and do not use dewaxing agent, the dewaxing result sees table 2.
Table 1
| Subtract four distillates | Subtract three chaff essential oils | Subtract three and extract oil out | |
| Pour point/ |
15 | 12 | 25 |
| 100 ℃ of viscosity/(mm 2/s) | 11.44 | 7.593 | 26.47 |
| 20 ℃ of density/(kg/m 3) | 912.5 | 885.4 | 1005.6 |
| Carbon residue/% | 0.28 | 0.09 | 0.88 |
| Flash-point/℃ | 270 | 250 | 245 |
| Boiling range/ |
|||
| 10％ | 449 | 430 | / |
| 30/％ | 469 | 447 | / |
| 50/％ | 483 | 462 | / |
| 70/％ | 498 | 475 | / |
Table 2
Can find out from the solvent dewaxing and de-oiling result of each embodiment and corresponding Comparative Examples thereof, compare with corresponding Comparative Examples, adopt method of the present invention, the dewaxing filtration velocity all significantly improves, and dewaxing differential reduces.
Solvent dewaxing result by embodiment 1,2 and 3 can find out; No matter be that distillate with the low content of wax is as raw material; Still extract oil out as raw material with the solvent-refined oil or the solvent treatment of the low content of wax, can improve the dewaxing filtration velocity, reduce dewaxing differential through method of the present invention.Increase the addition of circulation dewaxed oil in the dewaxing raw material, can not add or add less paraffin, reduce the solvent dewaxing cost of low waxy feeds.
Claims (30)
1. the solvent-dewaxing method of a low content of wax hydrocarbon ils comprises: raw oil, dewaxing agent and dewaxing solvent are mixed, be cooled to filtration temperature, filter and obtain dewaxed filtrate and dewaxing slack wax, after dewaxed filtrate removes solvent, obtain pressed oil; Dewaxing slack wax and de-oiling solvent are warmed up to filtration temperature, filter to obtain de-oiling filtrating and de-oiling slack wax; In the said dewaxing agent, mass content >=40% of C17～C100 normal paraffin; The mass ratio of dewaxing agent and raw oil is 0.01: 1 to 0.30: 1.
2. according to the described method of claim 1, it is characterized in that dewaxing agent is petroleum paraffin and/or synthetic paraffin.
3. according to the described method of claim 2, it is characterized in that the mass ratio of dewaxing agent and raw oil is 0.01: 1 to 0.15: 1.
4. according to the described method of claim 3, it is characterized in that the mass ratio of dewaxing agent and raw oil is 0.02: 1 to 0.12: 1.
5. according to the described method of claim 2, it is characterized in that the melting range of petroleum paraffin is between 52 ℃～72 ℃.
6. according to the described method of claim 5, it is characterized in that the melting range of petroleum paraffin is between 56 ℃～68 ℃.
7. according to the described method of claim 1, it is characterized in that raw oil is fraction oil of petroleum, frivolous asphalt oil and extracts in the oil one or more by above-mentioned two types of raw materials out through solvent-refined oil that solvent treatment obtains and solvent treatment.
8. according to the described method of claim 1, it is characterized in that the raw oil pour point is between 5 ℃～40 ℃.
9. according to the described method of claim 8, it is characterized in that the raw oil pour point is between 10 ℃～35 ℃.
10. according to the described method of claim 1, it is characterized in that, earlier dewaxing agent is dissolved in raw oil, and then add dewaxing solvent, the temperature that dewaxing agent is dissolved in raw oil is 50 ℃～110 ℃.
11., it is characterized in that the temperature that dewaxing agent is dissolved in raw oil is 75 ℃～90 ℃ according to the described method of claim 10.
12., it is characterized in that dewaxing solvent is the mixture of ketone and aromatic hydrocarbons according to the described method of claim 1.
13., it is characterized in that described ketone is acetone and/or butanone according to the described method of claim 12, described aromatic hydrocarbons is benzene and/or toluene.
14., it is characterized in that dewaxing solvent is butanone and toluene according to the described method of claim 13, be benchmark with the TV of butanone-toluene mixed solvent, the volume content of butanone is 40% to 85%.
15., it is characterized in that according to the described method of claim 14, be benchmark with the TV of butanone-toluene mixed solvent, the volume content of butanone is 50% to 75%.
16., it is characterized in that the mass ratio of dewaxing solvent and raw oil is 1.0: 1 to 8.0: 1 according to the described method of claim 14.
17., it is characterized in that the mass ratio of dewaxing solvent and raw oil is 2.0: 1 to 5.5: 1 according to the described method of claim 16.
18., it is characterized in that the de-oiling solvent is the mixture of ketone and aromatic hydrocarbons according to the described method of claim 1.
19., it is characterized in that described ketone is acetone and/or butanone according to the described method of claim 18, described aromatic hydrocarbons is benzene and/or toluene.
20., it is characterized in that the de-oiling solvent is butanone and toluene according to the described method of claim 19, be benchmark with the TV of butanone-toluene mixed solvent, the volume content of butanone is 40% to 85%.
21., it is characterized in that according to the described method of claim 20, be benchmark with the TV of butanone-toluene mixed solvent, the volume content of butanone is 50% to 75%.
22., it is characterized in that the mass ratio of de-oiling solvent and raw oil is 0.2: 1 to 2.5: 1 according to the described method of claim 20.
23., it is characterized in that the mass ratio of de-oiling solvent and raw oil is 0.3: 1 to 1.3: 1 according to the described method of claim 22.
24., it is characterized in that according to the described method of claim 1, after the de-oiling step, carry out a de-oiling again, the temperature of de-oiling for the second time is greater than or equal to the temperature of de-oiling for the first time.
25., it is characterized in that the filtration temperature in the de-oiling step is between 10 ℃～40 ℃ according to the described method of claim 1.
26., it is characterized in that the filtration temperature in the de-oiling step is between 15 ℃～30 ℃ according to the described method of claim 25.
27. according to the described method of claim 1; It is characterized in that; After the dewaxing step, once dewax again; Dewax filtration temperature for the second time between the filtration temperature that dewaxes for the first time is extremely than its scope of low 5 ℃, and then will filter the slack wax that obtains for the second time and carry out de-oiling, be used as dewaxing solvent for the first time filtering the filtrating that obtains the second time.
28. according to claim 1 or 2 described methods, it is characterized in that, with de-oiling slack wax cyclically utilizing, instead of part or whole dewaxing agents.
29., it is characterized in that according to claim 1 or 2 described methods, the de-oiling slack wax is removed solvent, obtain dewaxed oil.
30. according to the described method of claim 29, it is characterized in that, dewaxed oil recycled as dewaxing agent.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109694747A (en) * | 2017-10-24 | 2019-04-30 | 中国石油化工股份有限公司 | A kind of benzol-kentone dewaxing technique of low waxy feeds |
| CN109694729A (en) * | 2017-10-24 | 2019-04-30 | 中国石油化工股份有限公司 | A kind of preparation method of white oil |
| CN110094637A (en) * | 2018-01-31 | 2019-08-06 | 中国石油天然气股份有限公司 | Circulation paraffin removal device |
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Cited By (4)
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| CN109694747A (en) * | 2017-10-24 | 2019-04-30 | 中国石油化工股份有限公司 | A kind of benzol-kentone dewaxing technique of low waxy feeds |
| CN109694729A (en) * | 2017-10-24 | 2019-04-30 | 中国石油化工股份有限公司 | A kind of preparation method of white oil |
| CN109694729B (en) * | 2017-10-24 | 2021-06-11 | 中国石油化工股份有限公司 | Preparation method of white oil |
| CN110094637A (en) * | 2018-01-31 | 2019-08-06 | 中国石油天然气股份有限公司 | Circulation paraffin removal device |
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