CN103468306B - Solvent dewaxing method of low wax content hydrocarbon oil - Google Patents
Solvent dewaxing method of low wax content hydrocarbon oil Download PDFInfo
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Abstract
The present invention relates to a solvent dewaxing method of low wax content hydrocarbon oil. The solvent dewaxing method comprises: mixing raw material oil from a crude oil pressure reduction fraction segment, petroleum micro crystalline wax and a dewaxing solvent, cooling to achieve a filtration temperature, filtering to obtain a dewaxing filtrate and a dewaxing cerate, removing the solvent from the dewaxing filtrate to obtain dewaxing oil, mixing the dewaxing cerate and a deoiling solvent, heating to achieve a filtration temperature, and filtering to obtain a deoiling filtrate and a deoiling cerate, wherein a petroleum micro crystalline wax dropping-melting point is 67-92 DEG C, and a mass ratio of the petroleum micro crystalline wax to the raw material oil is 0.005:1-0.2:1. Compared with the conventional solvent dewaxing technology, the solvent dewaxing method of the present invention has the following characteristics that: wax in the low wax content hydrocarbon oil can be effectively removed, dewaxing temperature difference can be reduced, and a filtration rate can be increased.
Description
Technical field
The invention belongs to the process for dewaxing of hydrocarbon ils.Specifically, the present invention relates to the solvent-dewaxing method of the low content of wax hydrocarbon oil crude material of a kind of oil reduced pressure distillate section.
Background technology
In order to keep the low-temperature fluidity of lubricating oil, wax contained in stock oil must be removed in the production process of lubricant base, to reduce condensation point or the pour point of lubricant base.Wax is divided into paraffin and Microcrystalline Wax through the wax product of de-oiling, and paraffin is based on normal paraffin and a certain amount of isoparaffin, and Microcrystalline Wax then containing 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 be exactly by stock oil and dewaxing solvent miscible, then progressively cool, utilize insoluble to wax the component at low temperatures or oligodynamical of solvent and characteristic to other components dissolved, make wax crystallization in the solution, finally filter, oil is separated with wax.
Solvent dewaxing technology not only may be used for the wax removed in lube stock, also may be used for the component being separated different zero pour in other oil products.For different oil products, due to the difference that the wax content of stock oil and the difference of wax molecular structure and product require pour point, its solvent dewaxing process has larger difference.Such as: producing in the process of environment-friendly rubber extending oil with furfural extract oil, first must remove the wax extracted out in oil, then just can it can be used as the raw materials for production of environment-friendly rubber extending oil.But the wax removed in furfural extract oil with the solvent dewaxing process of routine is very difficult.
The criteria for classifying that the height of hydrocarbon ils wax content is ununified.For lubricant base is produced, it is generally acknowledged that the lube stock oil obtained by paraffinic crude is high-content wax stock oil, the lube stock oil obtained by naphthenic base crude is low waxy feeds oil, the wax content of the lube stock oil obtained by intermediate base crude oil is between the two above-mentioned, more be partial to naphthenic base crude, wax content is lower, and the isoparaffin in wax component, with the naphthenic hydrocarbon of long side chain or aromatic hydrocarbons more, adopt conventional solvent-dewaxing method to reduce the pour point of waxy oil more difficult.The content of wax hydrocarbon ils obtained after the content of wax hydrocarbon ils obtained by crude oil time processing or crude oil secondary processing, when the wax content of hydrocarbon ils low to a certain extent time, conventional solvent-dewaxing method cannot be adopted to produce the pressed oil meeting pour point and require, this class hydrocarbon ils is just 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, the method more effectively can remove the wax in the low content of wax hydrocarbon ils of oil reduced pressure distillate section, reduces dewaxing differential, improves filtration velocity, reduces Microcrystalline Wax consumption.
A solvent-dewaxing method for low content of wax hydrocarbon ils, comprising: the stock oil of crude oil reduced pressure distillate section, oil Microcrystalline Wax and dewaxing solvent are mixed, be cooled to filtration temperature, filters and obtains dewaxed filtrate and dewaxing slack wax, after dewaxed filtrate desolvation, obtain pressed oil; Dewaxing slack wax and de-oiling solvent, be warmed up to filtration temperature, filters and obtain de-oiling filtrate and de-oiling slack wax; The melt drop temperature of described oil Microcrystalline Wax is between 67 DEG C ~ 92 DEG C; The mass ratio of oil Microcrystalline Wax and stock oil is 0.005: 1 to 0.2: 1.
The mass ratio of oil Microcrystalline Wax and stock oil is preferably 0.008: 1 to 0.15: 1, is more preferably 0.01: 1 to 0.12: 1.
The melting range of described oil Microcrystalline Wax preferably between 67 DEG C ~ 92 DEG C, more preferably between 75 DEG C ~ 84 DEG C.The oleaginousness of described oil Microcrystalline Wax preferably between 0.4% ~ 5%, more preferably between 1% ~ 3%.
" the low content of wax " in the present invention refer to the lower and naphthenic hydrocarbon with long side chain in wax of the wax content of oil reduced pressure distillate section hydrocarbon oil crude material or aromatic hydrocarbons more, conventional solvent-dewaxing method cannot be adopted to produce the pressed oil meeting pour point and require.
The stock oil of reduced pressure distillate section can be the vacuum distillate of crude oil, the solvent-refined oil obtained through solvent treatment by vacuum distillate and solvent treatment extract oil out, extracted out hydrotreatment oil that oil obtains through hydrotreatment by above-mentioned vacuum distillate, solvent-refined oil and solvent treatment in one or more.Described vacuum distillate preferably subtracts three line distillates or subtracts four line distillates.
Stock oil pour point of the present invention preferably between 5 DEG C ~ 40 DEG C, more preferably between 10 DEG C ~ 35 DEG C.
In preferred situation, first oil Microcrystalline Wax is dissolved in stock oil, and then adds dewaxing solvent.Temperature oil Microcrystalline Wax being dissolved in stock oil is preferably 70 DEG C ~ 110 DEG C, is more preferably 80 DEG C ~ 100 DEG C.
Filtration temperature in hydrodewaxing step is preferably-25 DEG C ~ 0 DEG C, is more preferably-20 DEG C ~-10 DEG C.
Described dewaxing solvent is the mixture of ketone and aromatic hydrocarbons, and ketone is wherein preferably acetone and/or butanone, and aromatic hydrocarbons is preferably benzene and/or toluene; More preferably adopt little to wax solubleness and to this dewaxing solvent all dissolved of oil base, as the mixture of butanone and toluene.
When adopting the mixture of butanone and toluene as dewaxing solvent, with the cumulative volume of butanone-toluene Mixed Solvent for benchmark, the volume content of butanone is 40% to being less than 100%, preferably 50% to 95%.
When adopting the mixture of butanone and toluene as dewaxing solvent, the mass ratio of butanone-toluene Mixed Solvent and stock oil is 1: 1 to 8: 1, is preferably 2: 1 to 6: 1.
In the present invention, dewaxing solvent can disposablely add, and also can add several times, preferably divides and adds for 3 times or 4 times.
According to the ratio of solvent and low waxy feeds oil, those skilled in the art easily can determine the additional proportion of each point diluting solvent.
According to the viscosity of material in process of cooling, what those skilled in the art easily can determine each point diluting solvent adds temperature.
Described de-oiling solvent is the mixture of ketone and aromatic hydrocarbons, and ketone is wherein preferably acetone and/or butanone, and aromatic hydrocarbons is preferably benzene and/or toluene; More preferably adopt little to wax solubleness and to this dewaxing solvent all dissolved of oil base, as the mixture of butanone and toluene.
When adopting the mixture of butanone and toluene as de-oiling solvent, with the cumulative volume of butanone-toluene Mixed Solvent for benchmark, the volume content of butanone is 40% to being less than 100%, preferably 50% to 95%.
When adopting the mixture of butanone and toluene as de-oiling solvent, the mass ratio of butanone-toluene Mixed Solvent and stock oil is 0.2: 1 to 2.5: 1, is preferably 0.3: 1 to 1.5: 1.
In the present invention, de-oiling solvent can disposablely add, and also can add several times, preferably disposablely adds.
Filtration temperature (de-oiling temperature) in de-oiling step between 10 DEG C ~ 45 DEG C, preferably between 15 DEG C ~ 40 DEG C.
The present invention can carry out a de-oiling again after de-oiling step, and second time de-oiling temperature is greater than or equal to first time de-oiling temperature.The present invention preferably only carries out a de-oiling.
The present invention once can dewax after hydrodewaxing step again, second time dewaxing filtration temperature is between the scope of first time dewaxing filtration temperature to low 5 DEG C than it, and then carry out de-oiling by filtering the slack wax obtained for the second time, being used as filtering the dewaxed filtrate obtained for the second time the diluting solvent that dewaxes for the first time, being preferably used as the secondary in first time dewaxing, three times or four diluting solvents.
In preferred situation, the present invention by de-oiling slack wax cyclically utilizing, can replace part or all of Microcrystalline Wax, to reduce the consumption of Microcrystalline Wax.The reuse ratio of the present invention to de-oiling slack wax has no particular limits.
Method of the present invention also comprises, and by de-oiling slack wax desolvation, obtains dewaxed oil.Dewaxed oil can recycle by the present invention, replaces part or all of oil Microcrystalline Wax.Equally, the present invention also has no particular limits the ratio that dewaxed oil recycles.
Method of the present invention also comprises, from de-oiling filtrate, isolate sweat oil.
In described separating filtrate and slack wax, the method for solvent is well known in the art, and such as respectively material is sent into solvent recovery tower except desolventizing, recovered solvent recycles.In the present invention, the solvent after recovery can containing a small amount of stock oil component.
Allly in the present invention relate in the step of different components mixing, preferably adopt mixing tank enhancing mixed effect.Described mixing tank belongs to prior art, and the present invention can adopt the liquid mixer of this area routine.
When the wax content of the stock oil of reduced pressure distillate section is to a certain extent low, during the pressed oil that conventional solvent-dewaxing method cannot be adopted to produce meet pour point to require, just method of the present invention can be adopted produce the pressed oil meeting pour point requirement.
The wax removed in oil reduced pressure distillate section low content of wax hydrocarbon ils with the solvent dewaxing process of routine is very difficult, and major cause is: the wax content 1. in low content of wax hydrocarbon oil crude material is lower, and high melting point component content is few, causes the wax recovery concentration in mixed solution lower; 2. the more important thing is, wax major part in low content of wax hydrocarbon oil crude material is naphthenic hydrocarbon with long side chain or aromatic hydrocarbons, and the wax crystalline substance formed in solvent dewaxing process is more tiny, and little wax crystalline substance easily penetrates filter cloth, enter in pressed oil, cause dewaxing differential increase, dewaxing effect reduction; 3. in addition, slightly large wax crystalline substance is stuck in filter cloth duct, and duct is filtered in blocking, reduces the permeability energy of filter cloth, has a strong impact on filtration velocity and the temperature increasing filter cloth washes the frequency.Compared with the solvent dewaxing technology of routine, the present invention with the addition of high melt drop temperature oil Microcrystalline Wax in low content of wax hydrocarbon ils, more effectively can remove the wax in the low content of wax hydrocarbon ils of oil reduced pressure distillate section, reduces dewaxing differential, improves filtration velocity.
Accompanying drawing explanation
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 mixes with from the oil Microcrystalline Wax of pipeline 2 and/or the dewaxed oil of pipeline 25 through pipeline 1, heat in well heater 4 through pipeline 3, mixture mixes in mixing tank 6 through pipeline 5, in water cooler 10, dewaxing temperature is cooled to through pipeline 9 through pipeline 7 and the dewaxing solvent from pipeline 8, enter strainer 12 through pipeline 11 to filter, dewaxed filtrate, through pipeline 13 desolventizing recovery tower 14 desolvation, obtains pressed oil through pipeline 15, does not mark the trend of desolvation in figure.Dewaxing slack wax is warming up to de-oiling temperature through pipeline 18 through pipeline 16 and the de-oiling solvent from pipeline 17 in well heater 19, enter strainer 21 through pipeline 20 to filter, de-oiling filtrate is through pipeline 22 desolvation in solvent recovery tower 23, obtain sweat oil through pipeline 24, in figure, do not mark the trend of desolvation.De-oiling slack wax is through pipeline 26 desolventizing recovery tower 27 desolvation, and dewaxed oil can join in stock oil through pipeline 25 and replace oil Microcrystalline Wax to use, and also can obtain dewaxed oil through pipeline 28, not mark the trend of desolvation in figure.
Further illustrate the present invention by the following examples.
Embodiment 1
To subtract four extraction oil as raw material, its character is in table 1.The mass ratio of Microcrystalline Wax and stock oil is 0.12: 1, and dewaxing solvent is butanone-toluene Mixed Solvent, and the volume content of butanone is 95%, adopts multipoint dilution technique, total agent-oil ratio 2: 1.De-oiling solvent is identical with dewaxing solvent, and adopt and once dilute, agent-oil ratio is 0.7: 1 (relative to stock oil).Prepare pressed oil by the flow process of accompanying drawing 1, detailed process is as follows:
(1) be that the oil Microcrystalline Wax of 75 DEG C joins in stock oil by melt drop temperature, be heated to 80 DEG C, fully melt and after mixing, add each diluting solvent successively.Be cooled to-15 DEG C, obtain dewaxed filtrate and dewaxing slack wax after filtration, after filtrate desolvation, obtain pressed oil.In slack wax, add diluting solvent and mix, being heated to 15 DEG C, obtaining de-oiling filtrate and de-oiling slack wax after filtration, after filtrate desolvation, obtain sweat oil, after slack wax desolvation, obtain dewaxed oil.Part dewaxed oil recycles, and for replacing oil Microcrystalline Wax, recovered solvent recycles as dewaxing solvent.
(2) replace the Microcrystalline Wax of the melt drop temperature 75 DEG C of part with dewaxed oil, the mass ratio of dewaxed oil and melt drop temperature 75 DEG C of Microcrystalline Waxes is 7: 3, and all the other operations are identical with (1) with test conditions.First time tests the dewaxed oil obtained in use (1), and each test use is last later tests the dewaxed oil obtained, and revision test repeatedly, when double test-results is identical, gets the result of last test, in table 2.
Comparative example 1
Unless otherwise indicated, the raw material in this comparative example, operation and test conditions are all identical with embodiment 1.Only carry out the dewaxing process in (1), and do not use oil Microcrystalline Wax, dewaxing results is in table 2.
Comparative example 2
Unless otherwise indicated, the raw material in this comparative example, operation and test conditions are all identical with embodiment 1.(1) oil Microcrystalline Wax is not added in.(2) wax content of stock oil is only increased in dewaxed oil, the mass ratio of dewaxed oil and stock oil is 0.12: 1, first time tests the dewaxed oil obtained in use (1), each test later uses the last time to test the dewaxed oil obtained, revision test repeatedly, when double test-results is identical, get the result of last test, in table 2.
Embodiment 2
To subtract three hydrotreatment oil for raw material, its character is in table 1.The mass ratio of oil Microcrystalline Wax and stock oil is 0.06: 1, and dewaxing solvent is butanone-toluene Mixed Solvent, and the volume content of butanone is 50%, adopts multipoint dilution technique, total agent-oil ratio 6: 1.De-oiling solvent is identical with dewaxing solvent, and adopt and once dilute, agent-oil ratio is 1.5: 1 (relative to stock oils).Prepare pressed oil by the flow process of accompanying drawing 1, detailed process is as follows:
(1) the oil Microcrystalline Wax of melt drop temperature 80 DEG C is added in stock oil, be heated to 90 DEG C, fully melt and after mixing, add each diluting solvent successively.Be cooled to-10 DEG C, obtain dewaxed filtrate and dewaxing slack wax after filtration, after filtrate desolvation, obtain pressed oil.In slack wax, add diluting solvent and mix, being heated to 30 DEG C, obtaining de-oiling filtrate and de-oiling slack wax after filtration, after filtrate desolvation, obtain sweat oil, after slack wax desolvation, obtain dewaxed oil.By the dewaxed oil cyclically utilizing that de-oiling section is produced, replace whole oil Microcrystalline Waxes, recovered solvent recycles as dewaxing solvent.
(2) replace the oil Microcrystalline Wax of whole melt drop temperature 80 DEG C with dewaxed oil, all the other operations are identical with (1) with test conditions.First time tests the dewaxed oil obtained in use (1), and each test use is last later tests the dewaxed oil obtained, and revision test repeatedly, when double test-results is identical, gets the result of last test, in table 2.
Comparative example 3
Unless otherwise indicated, the raw material in this comparative example, operation and test conditions are all identical with embodiment 2.(1) oil Microcrystalline Wax is not added in.(2) wax content of stock oil is only increased in dewaxed oil, the mass ratio of dewaxed oil and stock oil is 0.06: 1, first time tests the dewaxed oil obtained in use (1), each test later uses the last time to test the dewaxed oil obtained, revision test repeatedly, when double test-results is identical, get the result of last test, in table 2.
Embodiment 3
To subtract three furfural refining oil for raw material, its character is in table 1.The mass ratio of oil Microcrystalline Wax and stock oil is 0.01: 1, and dewaxing solvent is butanone-toluene Mixed Solvent, and the volume content of butanone is 70%, adopts multipoint dilution technique, total agent-oil ratio 4: 1.De-oiling solvent is identical with dewaxing solvent, and adopt and once dilute, agent-oil ratio is 0.3: 1 (relative to stock oil).Prepare pressed oil by the flow process of accompanying drawing 1, detailed process is as follows:
(1) the oil Microcrystalline Wax of melt drop temperature 84 DEG C is added in stock oil, be heated to 100 DEG C, fully melt and after mixing, add each diluting solvent successively.Be cooled to-20 DEG C, obtain dewaxed filtrate and dewaxing slack wax after filtration, after filtrate desolvation, obtain pressed oil.In slack wax, add diluting solvent and mix, being heated to 40 DEG C, obtaining de-oiling filtrate and de-oiling slack wax after filtration, after filtrate desolvation, obtain sweat oil, after slack wax desolvation, obtain dewaxed oil.Part dewaxed oil recycles, and for replacing oil Microcrystalline Wax, recovered solvent recycles as dewaxing solvent.
(2) replace the Microcrystalline Wax of part melt drop temperature 84 DEG C with dewaxed oil, the mass ratio of dewaxed oil and melt drop temperature 84 DEG C of Microcrystalline Waxes is 5: 5, and all the other operations are identical with (1) with test conditions.First time tests the dewaxed oil obtained in use (1), and each test use is last later tests the dewaxed oil obtained, and revision test repeatedly, when double test-results is identical, gets the result of last test, in table 2.
Comparative example 4
Unless otherwise indicated, the raw material in this comparative example, operation and test conditions are all identical with embodiment 3.Only carry out the dewaxing process in (1), and do not use oil Microcrystalline Wax, dewaxing results is in table 2.
Table 1
| Subtract four extraction oil | Subtract three hydrotreatment oil | Subtract three chaff essential oils | |
| Pour point/DEG C | 36 | 18 | 15 |
| 100 DEG C of viscosity/(mm 2/s) | 61.83 | 7.284 | 7.807 |
| 20 DEG C of density/(kg/m 3) | 1003.8 | 867.1 | 869.9 |
| Carbon residue/% | 3.71 | ＜0.05 | ＜0.05 |
| Flash-point/DEG C | / | 242 | 245 |
| Boiling range/DEG C | |||
| 10％ | / | 435 | 438 |
| 30％ | / | 442 | 447 |
| 50％ | / | 457 | 461 |
| 70％ | / | 483 | 486 |
Table 2
As can be seen from the solvent dewaxing result of each embodiment and corresponding comparative example thereof, compared with corresponding comparative example, adopt method of the present invention, dewaxing filtration velocity all significantly improves, and dewaxing differential reduces.
As can be seen from the solvent dewaxing result of embodiment 1,2 and 3, no matter be extract oil out as raw material using the solvent treatment of the low content of wax, or using the hydrotreatment of the low content of wax oil or solvent-refined oil as raw material, dewaxing filtration velocity can be improved through method of the present invention, reduce dewaxing differential.Increase in dewaxed feedstock the addition of the dewaxed oil that circulates, can not add or add Microcrystalline Wax less, the solvent dewaxing cost of low waxy feeds can be reduced.
Claims (28)
1. the solvent-dewaxing method of one kind low content of wax hydrocarbon ils, comprise: the stock oil of crude oil reduced pressure distillate section, oil Microcrystalline Wax and dewaxing solvent are mixed, is cooled to filtration temperature, filter and obtain dewaxed filtrate and dewaxing slack wax, after dewaxed filtrate desolvation, obtain pressed oil; Dewaxing slack wax and de-oiling solvent, be warmed up to filtration temperature, filters and obtain de-oiling filtrate and de-oiling slack wax; The melt drop temperature of described oil Microcrystalline Wax is between 67 DEG C ~ 92 DEG C; The mass ratio of oil Microcrystalline Wax and stock oil is 0.005: 1 to 0.2: 1; The stock oil of described reduced pressure distillate section be the vacuum distillate of crude oil, the solvent-refined oil obtained through solvent treatment by vacuum distillate and solvent treatment extract oil out, extracted out hydrotreatment oil that oil obtains through hydrotreatment by above-mentioned vacuum distillate, solvent-refined oil and solvent treatment in one or more, described vacuum distillate is for subtracting three line distillates or subtracting four line distillates.
2. in accordance with the method for claim 1, it is characterized in that, the mass ratio of oil Microcrystalline Wax and stock oil is 0.008: 1 to 0.15: 1.
3. in accordance with the method for claim 2, it is characterized in that, the mass ratio of oil Microcrystalline Wax and stock oil is 0.01: 1 to 0.12: 1.
4. in accordance with the method for claim 1, it is characterized in that, the melt drop temperature scope of oil Microcrystalline Wax is between 67 DEG C ~ 92 DEG C.
5. in accordance with the method for claim 4, it is characterized in that, the melt drop temperature scope of oil Microcrystalline Wax is between 75 DEG C ~ 84 DEG C.
6. in accordance with the method for claim 1, it is characterized in that, stock oil pour point is between 5 DEG C ~ 40 DEG C.
7. in accordance with the method for claim 6, it is characterized in that, stock oil pour point is between 10 DEG C ~ 35 DEG C.
8. in accordance with the method for claim 1, it is characterized in that, first oil Microcrystalline Wax is dissolved in stock oil, and then adds dewaxing solvent, temperature oil Microcrystalline Wax being dissolved in stock oil is 70 DEG C ~ 110 DEG C.
9. in accordance with the method for claim 8, it is characterized in that, temperature oil Microcrystalline Wax being dissolved in stock oil is 80 DEG C ~ 100 DEG C.
10. in accordance with the method for claim 1, it is characterized in that, described dewaxing solvent is the mixture of ketone and aromatic hydrocarbons.
11. in accordance with the method for claim 10, it is characterized in that, described ketone is acetone and/or butanone, and described aromatic hydrocarbons is benzene and/or toluene.
12. in accordance with the method for claim 11, it is characterized in that, dewaxing solvent is butanone and toluene, and with the cumulative volume of butanone-toluene Mixed Solvent for benchmark, the volume content of butanone is 40% to being less than 100%.
13. in accordance with the method for claim 12, it is characterized in that, with the cumulative volume of butanone-toluene Mixed Solvent for benchmark, the volume content of butanone is 50% to 95%.
14. in accordance with the method for claim 12, it is characterized in that, the mass ratio of dewaxing solvent and stock oil is 1: 1 to 8: 1.
15. in accordance with the method for claim 14, it is characterized in that, the mass ratio of dewaxing solvent and stock oil is 2: 1 to 6: 1.
16. in accordance with the method for claim 1, it is characterized in that, de-oiling solvent is the mixture of ketone and aromatic hydrocarbons.
17. in accordance with the method for claim 16, it is characterized in that, described ketone is acetone and/or butanone, and described aromatic hydrocarbons is benzene and/or toluene.
18. in accordance with the method for claim 17, it is characterized in that, de-oiling solvent is butanone and toluene, and with the cumulative volume of butanone-toluene Mixed Solvent for benchmark, the volume content of butanone is 40% to being less than 100%.
19. in accordance with the method for claim 18, it is characterized in that, with the cumulative volume of butanone-toluene Mixed Solvent for benchmark, the volume content of butanone is 50% to 95%.
20. in accordance with the method for claim 18, it is characterized in that, the mass ratio of de-oiling solvent and stock oil is 0.2: 1 to 2.5: 1.
21. in accordance with the method for claim 20, it is characterized in that, the mass ratio of de-oiling solvent and stock oil is 0.3: 1 to 1.5: 1.
22. in accordance with the method for claim 1, it is characterized in that, after de-oiling step, carry out a de-oiling again to the slack wax that a de-oiling obtains, and second time de-oiling temperature is greater than or equal to first time de-oiling temperature.
23. in accordance with the method for claim 1, it is characterized in that, the filtration temperature in de-oiling step is between 10 DEG C ~ 45 DEG C.
24. in accordance with the method for claim 23, it is characterized in that, the filtration temperature in de-oiling step is between 15 DEG C ~ 40 DEG C.
25. in accordance with the method for claim 1, it is characterized in that, after hydrodewaxing step, the slack wax obtained that once dewaxes once is dewaxed again, second time dewaxing filtration temperature is between the scope of first time dewaxing filtration temperature to low 5 DEG C than it, and then carry out de-oiling by filtering the slack wax obtained for the second time, be used as filtering the filtrate obtained for the second time the diluting solvent that dewaxes for the first time.
26. in accordance with the method for claim 1, it is characterized in that, by de-oiling slack wax cyclically utilizing, replaces part or all of oil Microcrystalline Wax.
27. in accordance with the method for claim 1, it is characterized in that, by de-oiling slack wax desolvation, obtains dewaxed oil.
28. in accordance with the method for claim 27, it is characterized in that, recycled by dewaxed oil, replaces part or all of oil Microcrystalline Wax.
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| SU1675322A1 (en) * | 1989-05-03 | 1991-09-07 | Московский Институт Нефти И Газа Им.И.М.Губкина | Method of producing solid hydrocarbons |
| CN1648216A (en) * | 2004-01-19 | 2005-08-03 | 中国石油化工股份有限公司 | Solvent dewaxing method |
| CN102952572A (en) * | 2011-08-25 | 2013-03-06 | 中国石油化工股份有限公司 | Solvent dewaxing method of low-wax content heavy hydrocarbon oil |
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| SU1675322A1 (en) * | 1989-05-03 | 1991-09-07 | Московский Институт Нефти И Газа Им.И.М.Губкина | Method of producing solid hydrocarbons |
| CN1648216A (en) * | 2004-01-19 | 2005-08-03 | 中国石油化工股份有限公司 | Solvent dewaxing method |
| CN102952572A (en) * | 2011-08-25 | 2013-03-06 | 中国石油化工股份有限公司 | Solvent dewaxing method of low-wax content heavy hydrocarbon oil |
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