阅读说明：本技术 费托合成蜡的脱油方法及其应用 (Deoiling method and application of Fischer-Tropsch synthetic wax ) 是由 邵光涛 潘晓阳 金梦 黄浩 刘素丽 张安贵 金政伟 于 2020-10-23 设计创作，主要内容包括：本发明涉及化工领域,公开了一种费托合成蜡的脱油方法及其应用,该方法包括以下步骤：1)将熔化的费托合成蜡与脱油溶剂在加压条件下混合得到混合物的步骤；2)将步骤1)得到的混合物进行稀释降温得到结晶液的步骤；3)将步骤2)得到的结晶液进行固液分离得到蜡膏和上清液的步骤；4)从步骤3)得到的蜡膏除去并回收溶剂得到脱油蜡的步骤。通过该方法进行脱油的除油率高,得到的脱油蜡含油率低,且脱油效率高,脱油过程中溶剂损失少。(The invention relates to the field of chemical industry, and discloses a deoiling method of Fischer-Tropsch synthetic wax and an application thereof, wherein the method comprises the following steps: 1) mixing the molten Fischer-Tropsch wax and a deoiling solvent under a pressurized condition to obtain a mixture; 2) diluting and cooling the mixture obtained in the step 1) to obtain a crystallization liquid; 3) carrying out solid-liquid separation on the crystalline liquid obtained in the step 2) to obtain cerate and supernatant; 4) a step of removing and recovering the solvent from the cerate obtained in the step 3) to obtain deoiled wax. The deoiling rate of the deoiling performed by the method is high, the obtained deoiling wax has low oil content, the deoiling efficiency is high, and the solvent loss in the deoiling process is less.)

1. A method for deoiling Fischer-Tropsch wax is characterized by comprising the following steps:

1) mixing the molten Fischer-Tropsch wax and a deoiling solvent under a pressurized condition to obtain a mixture;

2) diluting and cooling the mixture obtained in the step 1) to obtain a crystallization liquid;

3) carrying out solid-liquid separation on the crystalline liquid obtained in the step 2) to obtain cerate and supernatant;

4) a step of removing and recovering the solvent from the cerate obtained in the step 3) to obtain deoiled wax.

2. The deoiling method according to claim 1, wherein, in the step 1), the pressure of the pressurization is 0.1-1 Mpa;

preferably, the pressure of the pressurization is 0.1 to 0.5 MPa.

3. The deoiling method according to claim 1, wherein in the step 1), the mass ratio of the deoiling solvent to the Fischer-Tropsch synthesis wax is 1-5: 1;

preferably, the mass ratio of the deoiling solvent to the Fischer-Tropsch synthesis wax is 1-3: 1.

4. the deoiling method according to any one of claims 1 to 3, wherein the deoiling solvent is one or more of a ketone solvent and an aromatic solvent;

preferably, the deoiling solvent is one or more of acetone, butanone, toluene, methyl propyl ketone, methyl isobutyl ketone, methyl butanone and methyl isoamyl ketone;

preferably, the deoiling solvent is one or more of acetone, butanone, toluene, methyl isobutyl ketone and methyl isoamyl ketone.

5. The deoiling method according to any one of claims 1 to 3, wherein in the step 2), the dilution ratio is 0.5 to 3, and the cooling rate is 1 to 10 ℃/min;

preferably, the dilution and temperature reduction are carried out for multiple times;

preferably, the dilution temperature reduction is 2-4 times.

6. The deoiling method according to claim 5, wherein the dilution temperature reduction is 4 times, the temperature of the first dilution is 50-100 ℃, and the temperature of the second dilution is 30-80 ℃; the temperature of the third dilution is 0-50 ℃; the temperature of the fourth dilution is-20-30 ℃.

7. The deoiling method according to claim 1, wherein in step 3), the solid-liquid separation is basket centrifugal filtration or membrane press filtration.

8. The deoiling process of claim 1, further comprising: washing the obtained cerate with a solvent after solid-liquid separation;

preferably, the mass ratio of the solvent to the cerate is 0.2-2: 1.

9. the deoiling process of claim 1, further comprising: removing and recovering the solvent in the supernatant obtained in the step 3) to obtain soft wax.

10. Use of a de-oiling process according to any of claims 1 to 9 in the de-oiling of fischer-tropsch wax.

Technical Field

The invention relates to the field of chemical industry, in particular to a method for deoiling Fischer-Tropsch synthetic wax and application thereof.

Background

With the decreasing of the reserves of the paraffin-based crude oil in China and the increasingly mature Fischer-Tropsch synthesis technology, high-quality Fischer-Tropsch wax products gradually enter the market and show a faster growth situation. Compared with petroleum-based wax, Fischer-Tropsch wax has the characteristics of wide carbon number distribution, relatively simple composition and basically no cyclic hydrocarbon and aromatic hydrocarbon, the maximum carbon number of the Fischer-Tropsch wax can reach more than 200, more than 90 percent of the Fischer-Tropsch wax is normal straight-chain alkane, and the rest is basically short-chain branched alkane, so the Fischer-Tropsch synthetic crude wax is an ideal raw material for producing high-quality wax and high-melting-point wax.

Although the content of the Fischer-Tropsch wax normal paraffin is very high, the detection method of GB/T3554 can still detect that the oil content of the undeoiled medium-low melting point Fischer-Tropsch wax is higher than 3 wt%, the oil content of the high-melting point Fischer-Tropsch wax obtained by fine cutting is about 1 wt%, and the requirements that the oil content of a high-melting point wax or microcrystalline wax product is less than or equal to 1 wt% or the oil content of GB/T446-2010 fully refined paraffin is less than or equal to 0.8 wt% are not met. In order to meet the requirements of domestic and foreign high-end paraffin products on oil content indexes, deoiling is required to meet the requirements of some users on low oil content of final paraffin products.

At present, the deoiling process at home and abroad mainly aims at petroleum-based wax, the melting point of the petroleum-based wax is generally not higher than 75 ℃, and the deoiling process of paraffin wax mainly comprises three kinds of sweating process, solvent deoiling and spray deoiling, wherein the solvent deoiling is the most widely and mature technology at home and abroad and accounts for more than 80 percent of the deoiling device. The solvent deoiling technology is to separate oil from wax by utilizing the different solubility of solvent to oil and wax. Diluting a raw material to be dewaxed with a solvent, then sending the raw material to a crystallization system for crystallization, filtering a crystallized mixed solution through a filter, evaporating filtered cerate and filtrate respectively, evaporating the solvent in oil and wax to obtain dewaxed oil and wax, and recycling the recovered solvent. Solvent deoiling generally adopts methyl ethyl ketone + toluene, methyl propyl ketone, methyl isobutyl ketone, methyl isoamyl ketone, and methyl ethyl ketone + methyl isobutyl ketone as solvents to carry out solvent deoiling, and the mixed solvent of methyl ethyl ketone and toluene is most used. However, the solvent used in the existing solvent deoiling method has low dissolution rate and solubility for high-melting-point Fischer-Tropsch synthetic wax, so that the deoiling speed is low and the deoiling rate is low. In addition, the high melting point wax requires de-oiling at high temperature, resulting in substantial evaporation of the solvent during de-oiling, loss of solvent and contamination.

Disclosure of Invention

The invention provides a method for deoiling Fischer-Tropsch synthetic wax and application thereof, aiming at solving the problems of high oil content, low deoiling rate and more solvent loss of deoiled wax products in the prior art. The deoiling rate of the deoiling performed by the method is high, the obtained deoiling wax has low oil content, the deoiling production efficiency is high, and the solvent loss in the deoiling process is less.

In order to achieve the above object, a first aspect of the present invention provides a method for deoiling fischer-tropsch wax, comprising the steps of:

1) mixing the molten Fischer-Tropsch wax and a deoiling solvent under a pressurized condition to obtain a mixture;

2) diluting and cooling the mixture obtained in the step 1) to obtain a crystallization liquid;

3) carrying out solid-liquid separation on the crystalline liquid obtained in the step 2) to obtain cerate and supernatant;

4) a step of removing and recovering the solvent from the cerate obtained in the step 3) to obtain deoiled wax.

Preferably, in step 1), the pressure of the pressurization is 0.1 to 1 MPa.

Preferably, the pressure is between 0.1 and 0.5 MPa.

Preferably, in the step 1), the mass ratio of the deoiling solvent to the Fischer-Tropsch synthesis wax is 1-5: 1.

preferably, the mass ratio of the deoiling solvent to the Fischer-Tropsch synthesis wax is 1-3: 1.

preferably, the deoiling solvent is one or more of a ketone solvent and an aromatic solvent.

Preferably, the deoiling solvent is one or more of acetone, butanone, toluene, methyl propyl ketone, methyl isobutyl ketone, methyl butanone and methyl isoamyl ketone.

Preferably, the deoiling solvent is one or more of acetone, butanone, toluene, methyl isobutyl ketone and methyl isoamyl ketone.

Preferably, in the step 2), the dilution ratio is 0.5-3, and the cooling rate is 1-10 ℃/min;

preferably, the dilution cooling is performed in multiple times.

Preferably, the dilution temperature reduction is 2-4 times.

Preferably, the dilution temperature is reduced for 4 times, the temperature of the first dilution is 50-100 ℃, and the temperature of the second dilution is 30-80 ℃; the temperature of the third dilution is 0-50 ℃; the temperature of the fourth dilution is-20-30 ℃.

Preferably, in the step 3), the solid-liquid separation is basket centrifugal filtration or membrane squeezing filtration.

Preferably, the method further comprises: a step of washing the obtained cerate with a solvent after solid-liquid separation.

Preferably, the mass ratio of the solvent to the cerate is 0.2-2: 1.

preferably, the method further comprises: removing and recovering the solvent in the supernatant obtained in the step 3) to obtain soft wax.

In a second aspect the invention provides the use of a de-oiling process according to the invention in the de-oiling of fischer-tropsch wax.

According to the deoiling method of the Fischer-Tropsch synthetic wax, the deoiling rate is high, the obtained deoiled wax is low in oil content, the deoiling production efficiency is high, and the solvent loss in the deoiling process is low.

Detailed Description

The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.

In the present invention, the "oil removal rate" is calculated by the following formula:

oil removal rate (%) (oil content of Fischer-Tropsch wax before deoiling-oil content of deoiled wax)/oil content of Fischer-Tropsch wax before deoiling.

"dilution ratio" means the mass ratio of solvent added during dilution to the initial Fischer-Tropsch wax.

In a first aspect, the invention provides a method for deoiling Fischer-Tropsch wax, which comprises the following steps:

1) mixing the molten Fischer-Tropsch wax and a deoiling solvent under a pressurized condition to obtain a mixture;

2) diluting and cooling the mixture obtained in the step 1) to obtain a crystallization liquid;

3) carrying out solid-liquid separation on the crystalline liquid obtained in the step 2) to obtain cerate and supernatant;

4) a step of removing and recovering the solvent from the cerate obtained in the step 3) to obtain deoiled wax.

According to the deoiling method provided by the invention, the Fischer-Tropsch wax and the deoiling solvent are mixed under a pressurized condition, so that the solubility and the dissolving speed of the Fischer-Tropsch wax in the common deoiling solvent are improved, the deoiling is more sufficient, and the deoiling rate is higher. In addition, the evaporation of the deoiling solvent in the deoiling process is reduced through pressurization, so that the solvent loss is low.

According to the present invention, pressurization of the system can improve the deoiling effect and reduce the solvent loss, but too high pressurization pressure can increase the process difficulty and cost, and it is preferable that the pressurization pressure is 0.1 to 1Mpa from the viewpoint of balancing the deoiling effect and the process difficulty; more preferably, the pressure is between 0.1 and 0.5 MPa.

In a particularly preferred embodiment of the present invention, the pressure is 0.2 to 0.4Mpa, and when the pressure is within the above range, the oil content of the resulting deoiled wax is low and the deoiling rate is particularly excellent.

According to the invention, in the step 1), the deoiling is insufficient due to the addition of too small amount of the deoiling solvent, the deoiling effect is not obviously improved by increasing the amount of the deoiling solvent when the amount of the deoiling solvent is too large, and the production cost is increased, and from the viewpoint of balancing the deoiling effect and the cost, the mass ratio of the deoiling solvent to the Fischer-Tropsch synthetic wax is preferably 1-5: 1; more preferably, the mass ratio of the deoiling solvent to the fischer-tropsch synthesis wax is from 1 to 3: 1.

according to the present invention, the kind of the deoiling solvent is not particularly limited, and may be any solvent commonly used in deoiling of paraffin wax or synthetic wax, for example, a ketone solvent or an aromatic solvent, and preferably, the deoiling solvent is one or more of acetone, butanone, toluene, methyl propyl ketone, methyl isobutyl ketone, methyl butanone, and methyl isoamyl ketone; more preferably, the deoiling solvent is one or more of acetone, butanone, toluene, methyl isobutyl ketone and methyl isoamyl ketone.

According to the invention, in the step 1), the mixing temperature can be adjusted arbitrarily according to the melting point of the Fischer-Tropsch wax, and from the viewpoint of energy conservation, the mixing temperature is preferably 1-30 ℃ higher than the melting point of the Fischer-Tropsch wax; more preferably, the temperature of mixing is 4 to 20 ℃ higher than the melting point of the Fischer-Tropsch wax; further preferably, the temperature of mixing is from 10 to 20 ℃ above the melting point of the Fischer-Tropsch wax.

According to the invention, in the step 2), preferably, the dilution ratio of the dilution cooling is 0.5-3; more preferably, the dilution ratio of the dilution cooling is 1-1.5. Through making the dilution ratio be above-mentioned scope, have the effect that the ft synthesis wax crystallization is abundant, filtration efficiency is high, reduces the energy consumption.

According to the invention, in the step 2), preferably, the cooling rate of the dilution cooling is 1-10 ℃/min; more preferably, the cooling rate of the dilution cooling is 2-5 ℃/min. By setting the temperature reduction rate of dilution temperature reduction to the above range, the effect of making the crystal particle size uniform is obtained.

According to the invention, in step 2), preferably, the dilution cooling is performed for multiple times, and the number of times of dilution cooling is 2-4 times. By setting the number of dilution and temperature reduction within the above range, the wax-containing solution has the effects of small viscosity change, uniform crystal particle size and convenience for subsequent solid-liquid separation in the wax crystallization process.

According to the present invention, from the viewpoint of stabilizing the crystallization process and making the crystal grain size uniform, it is preferable that the dilution temperature is decreased by: cooling at constant speed, and adding solvent at constant speed while cooling.

According to the invention, preferably, the dilution temperature is reduced for 4 times, the temperature of the first dilution is 50-100 ℃, and the temperature of the second dilution is 30-80 ℃; the temperature of the third dilution is 0-50 ℃; the temperature of the fourth dilution is-20-30 ℃. The separation is then carried out at the fourth dilution temperature, which in the present invention means the temperature at which the dilution starts.

The wax dissolved in the deoiling solvent can be sufficiently crystallized and the crystal particle size is uniform by making the number of times of the multiple dilution and temperature reduction be 4 times and the dilution temperature be in the above range.

According to the present invention, in step 3), the solid-liquid separation method is not particularly limited, and may be a solid-liquid separation method which is common in the chemical field, and may be, for example, filtration or centrifugation, preferably filtration. From the viewpoint of making the solid-liquid separation more rapid and sufficient, it is preferable that in step 3), the method of solid-liquid separation is basket centrifugal filtration or membrane press filtration.

According to the present invention, when the method of solid-liquid separation is basket centrifugation, it is preferable that the conditions of the basket centrifugation are: the aperture of the basket is 500-; more preferably, the conditions of the basket centrifugal filtration are as follows: the aperture of the basket is 600 meshes and 800 meshes, and the centrifugal speed is 4000 rpm and 5000 rpm.

According to the present invention, when the method of solid-liquid separation is membrane press filtration, it is preferable that the conditions of the membrane press filtration are: the aperture of the filter cloth is 500-1000 meshes, and the filtering pressure is 1-4 MPa; more preferably, the conditions of the membrane press filtration are: the aperture of the filter cloth is 700 meshes and 900 meshes, and the filtering pressure is 1.5-2.5 MPa.

According to the invention, the temperature of the solid-liquid separation is between 0 and 50 ℃, preferably between 0 and 30 ℃.

According to the present invention, from the viewpoint of making the deoiling of the obtained deoiled wax more sufficient, preferably, the deoiling method further comprises: a step of washing the obtained cerate with a solvent after solid-liquid separation.

According to the present invention, it is preferable that the mass ratio of the solvent to the wax cream is 0.2 to 2: 1; more preferably, the mass ratio of the solvent to the cerate is 0.5-1.5: 1.

the solvent is not particularly limited, and may be a solvent generally used in the field of deoiling of paraffin wax or synthetic wax, and may be, for example, one or more of acetone, methyl ethyl ketone, toluene, methyl propyl ketone, methyl isobutyl ketone, methyl ethyl ketone, and methyl isoamyl ketone. Preferably, the solvent is the same composition as the de-oiling solvent of the present invention.

According to the present invention, the deoiling method further comprises, from the viewpoint of cost saving and yield improvement of by-products: removing and recovering the solvent in the supernatant obtained in the step 3) to obtain the soft wax.

According to the present invention, the method for removing and recovering the solvent is not particularly limited, and may be a method for removing and recovering the solvent which is generally used in the chemical field, and for example, a method for heating evaporation and cooling reflux, evaporation under reduced pressure and cooling reflux, or a method for extracting and recovering the solvent may be used.

A second aspect of the invention provides the use of a deoiling process of the invention in the deoiling of a fischer-tropsch wax.

According to the invention, the Fischer-Tropsch synthesis wax and the deoiling solvent are mixed under a pressurized condition, so that the solubility and the dissolving speed of the Fischer-Tropsch synthesis wax in the solvent are improved, the Fischer-Tropsch synthesis wax and the deoiling solvent are more fully mixed, the deoiling effect is improved, the oil content of the obtained deoiling wax is low, the deoiling rate is improved, the deoiling production efficiency is high, and the solvent loss in the deoiling process is reduced.

Examples

The present invention will be described in detail below by way of examples, but the present invention is not limited to the following examples.

In the following examples, the fischer-tropsch wax was prepared by a short path distillation cutting process of fischer-tropsch refined wax.

Example 1

(1) Pumping liquid Fischer-Tropsch synthetic wax (melting point 70 ℃ and oil content 5.42 wt%) with temperature of 74 ℃ into a deoiling tank (with aperture of 800 meshes) with a basket (with aperture of 85 ℃ at 85 ℃, pressurizing to 0.25Mpa, adding toluene with mass 1.5 times of the Fischer-Tropsch synthetic wax into the deoiling tank: butanone 1: 1 (volume ratio), and turning on mechanical stirring (200rpm, 30min) to mix the materials uniformly.

(2) And (3) cooling the temperature of the deoiling tank to 60 ℃ at the speed of 5 ℃/min, and simultaneously adding toluene with the mass 0.8 times of that of the Fischer-Tropsch synthesis wax at a constant speed: butanone 1: 1 (volume ratio) of the mixed solvent, and stirred at 200rpm for 30 min. Cooling to 40 ℃ at the speed of 5 ℃/min, and simultaneously adding toluene with the mass 0.8 times of that of the Fischer-Tropsch synthetic wax at a constant speed: butanone 1: 1 (volume ratio) of the mixed solvent, and stirred at 200rpm for 30 min. Cooling to 15 ℃ at the speed of 5 ℃/min, and simultaneously adding toluene with the mass 0.8 times of that of the Fischer-Tropsch synthetic wax at a constant speed: butanone 1: 1 (volume ratio) of the mixed solvent, and stirred at 200rpm for 30 min. Cooling to 0 ℃ at the speed of 5 ℃/min, and simultaneously adding toluene with the mass 0.8 times of that of the Fischer-Tropsch synthetic wax at a constant speed: butanone 1: 1 (volume ratio) of the mixed solvent, and stirred at 200rpm for 30 min.

(3) Decompressing a deoiling tank to normal pressure, cooling, refluxing and recovering released solvent steam, centrifuging a basket at 5000rpm for 15min to obtain cerate and filtrate, and separating the filtrate by using toluene with the mass 0.6 times of that of Fischer-Tropsch synthesis wax: butanone 1: washing the cerate in the basket with 1 volume ratio of mixed solvent, continuously centrifuging at 5000rpm for 5min to obtain cerate containing solvent, and combining the washing liquid with the filtrate.

(4) Evaporating the solvent-containing cerate at 90 deg.C for 120min to obtain deoiled wax, cooling, refluxing to recover solvent, evaporating the filtrate at 90 deg.C for 120min to obtain soft wax, and cooling, refluxing to recover solvent.

Examples 2 to 4, comparative example 1

The Fischer-Tropsch wax was deoiled in the same manner as in example 1, except that the melting point of the Fischer-Tropsch wax, the oil content of the Fischer-Tropsch wax, the pressurization pressure in step (1) and the ratio of the amount of the solvent added in step (1) to the mass of the Fischer-Tropsch wax were the values shown in Table 1.

TABLE 1

Example 5

(1) Pumping liquid Fischer-Tropsch synthetic wax (melting point 103 ℃, oil content 1.24 wt%) with temperature of 115 ℃ into a deoiling tank (aperture 800 meshes) with a basket at 115 ℃, pressurizing to 0.3Mpa, and adding toluene with the mass 3 times of the Fischer-Tropsch synthetic wax into the deoiling tank: butanone 1: 1 (volume ratio), and turning on mechanical stirring (200rpm, 30min) to mix the materials uniformly.

(2) And (3) cooling the temperature of the deoiling tank to 90 ℃ at the speed of 5 ℃/min, and simultaneously adding toluene with the mass 0.8 times of that of the Fischer-Tropsch synthesis wax at a constant speed: butanone 1: 1 (volume ratio) of the mixed solvent, and stirred at 200rpm for 30 min. Cooling to 70 ℃ at the speed of 5 ℃/min, and simultaneously adding toluene with the mass 0.8 times of that of the Fischer-Tropsch synthetic wax at a constant speed: butanone 1: 1 (volume ratio) of the mixed solvent, and stirred at 200rpm for 30 min. Cooling to 50 ℃ at the speed of 5 ℃/min, and simultaneously adding toluene with the mass 0.8 times of that of the Fischer-Tropsch synthetic wax at a constant speed: butanone 1: 1 (volume ratio) of the mixed solvent, and stirred at 200rpm for 30 min. Cooling to 20 ℃ at the speed of 5 ℃/min, and simultaneously adding toluene with the mass 0.8 times of that of the Fischer-Tropsch synthetic wax at a constant speed: butanone 1: 1 (volume ratio) of the mixed solvent, and stirred at 200rpm for 30 min.

(3) Decompressing a deoiling tank to normal pressure, cooling, refluxing and recovering released solvent steam, centrifuging a basket at 5000rpm for 15min to obtain cerate and filtrate, and separating the filtrate by using toluene with the mass 0.6 times of that of Fischer-Tropsch synthesis wax: butanone 1: washing the cerate in the basket with 1 volume ratio of mixed solvent, continuously centrifuging at 5000rpm for 5min to obtain cerate containing solvent, and combining the washing liquid with the filtrate.

(4) Evaporating the solvent-containing cerate at 90 deg.C for 120min to obtain deoiled wax, cooling, refluxing to recover solvent, evaporating the filtrate at 90 deg.C for 120min to obtain soft wax, and cooling, refluxing to recover solvent.

Example 6

A Fischer-Tropsch wax was deoiled in the same manner as in example 5, except that the toluene-butanone mixed solvent was replaced with methyl isobutyl ketone.

Comparative example 2

A Fischer-Tropsch wax was de-oiled as in example 5, except that in step (1), no pressurisation was applied.

Test example 1

The oil contents of the deoiled waxes obtained in examples and comparative examples were measured (method reference GB/T3554), and the oil contents were calculated according to the following formula:

oil removal rate (%) (oil content of Fischer-Tropsch wax before deoiling-oil content of deoiled wax)/oil content of Fischer-Tropsch wax before deoiling.

The total mass of the recovered solvents in examples and comparative examples was measured, and the solvent loss rate was calculated according to the following formula:

solvent loss (%) - (total mass of added solvent-total mass of recovered solvent)/total mass of added solvent × 100%.

The qualities of the deoiled waxes obtained in examples and comparative examples were measured, and the yield of the deoiled wax was calculated according to the following formula:

yield (%) of the deoiled wax is the mass of the deoiled wax/mass of the Fischer-Tropsch synthesized wax.

The quality of the soft wax obtained in the examples and comparative examples was measured, and the yield of the soft wax was calculated according to the following formula:

yield (%) of soft wax is the mass of deoiled wax/mass of Fischer-Tropsch wax.

The results are shown in Table 2.

TABLE 2

From the deoiling result, the deoiling method of the invention is used for deoiling, the obtained deoiled wax has low oil content, high deoiling rate and less solvent loss, and particularly, the Fischer-Tropsch wax with high melting point has relatively less solvent loss.

The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.