CN117487589A - Polystyrene white oil with moderate CN value and preparation method thereof - Google Patents
Polystyrene white oil with moderate CN value and preparation method thereof Download PDFInfo
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- CN117487589A CN117487589A CN202311709462.6A CN202311709462A CN117487589A CN 117487589 A CN117487589 A CN 117487589A CN 202311709462 A CN202311709462 A CN 202311709462A CN 117487589 A CN117487589 A CN 117487589A
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- 239000004793 Polystyrene Substances 0.000 title claims abstract description 50
- 229920002223 polystyrene Polymers 0.000 title claims abstract description 49
- 238000002360 preparation method Methods 0.000 title claims abstract description 19
- 239000003921 oil Substances 0.000 claims abstract description 96
- 239000010779 crude oil Substances 0.000 claims abstract description 28
- 239000002994 raw material Substances 0.000 claims abstract description 19
- 238000002156 mixing Methods 0.000 claims abstract description 12
- 238000000034 method Methods 0.000 claims abstract description 9
- 238000005520 cutting process Methods 0.000 claims abstract description 5
- 239000003054 catalyst Substances 0.000 claims description 24
- 238000005984 hydrogenation reaction Methods 0.000 claims description 18
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 16
- 229910052739 hydrogen Inorganic materials 0.000 claims description 16
- 239000001257 hydrogen Substances 0.000 claims description 16
- 238000004517 catalytic hydrocracking Methods 0.000 claims description 14
- 238000006317 isomerization reaction Methods 0.000 claims description 10
- 239000003223 protective agent Substances 0.000 claims description 8
- 238000002835 absorbance Methods 0.000 claims description 7
- 238000012360 testing method Methods 0.000 description 21
- 238000004821 distillation Methods 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 239000012188 paraffin wax Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 229910052785 arsenic Inorganic materials 0.000 description 2
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 2
- 239000013256 coordination polymer Substances 0.000 description 2
- 125000000753 cycloalkyl group Chemical group 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000000881 depressing effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000005461 lubrication Methods 0.000 description 1
- 239000002932 luster Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
-
- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- 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
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1096—Aromatics or polyaromatics
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a preparation method of polystyrene white oil with moderate CN value, which comprises the following steps: step S1, distilling the crude oil of the Zhonghai oil Xijiang and the crude oil of continent as raw materials, and then taking a fraction section at 450-540 ℃ to obtain a component A; s2, distilling the crude oil of Qinhuang island 26-2 and the crude oil of Nanbao which are used as raw materials, and then taking a fraction section at 450-540 ℃ to obtain a component B; step S3, component A and component B are mixed at 140 ℃ with 9:1 to 16: mixing the components in a mass ratio of 1 for 20min to obtain a component C; step S4, sequentially passing the component C through a first-stage device at a first temperature, a second-stage device at a second temperature and a third-stage device at a third temperature to obtain hydrogenated oil; and S5, cutting off the light fraction from the hydrogenated oil obtained in the step S4 to obtain polystyrene white oil with the distillate oil of which the temperature is more than 450 ℃ and the CN value is moderate. The preparation method has simple process, and the obtained polystyrene white oil has moderate CN value, high yield and stable quality.
Description
Technical Field
The invention relates to polystyrene white oil, in particular to a preparation method of polystyrene white oil with moderate CN value.
Background
The Polystyrene (PS) white oil is white oil applied to polystyrene production scenes, has the advantages of good photo-thermal stability, low aromatic hydrocarbon content, good processability, good compatibility with PS and the like, and can not only play roles in improving melt flowability and reducing melt adhesiveness, but also play roles in improving product color and luster and impact resistance, increasing product plasticity and toughness, reducing intermolecular friction and the like in the polystyrene production process.
At present, polystyrene white oil has no clear national or industry standard, but since polystyrene products are often used for food lubrication or food contact materials, polystyrene white oil should meet the standard of food grade white oil from the viewpoint of food safety (GB 4853-2008). Food grade white oils are typically paraffinic white oils (CN values less than 40, typically about 25) due to the stringent requirements for charrable, ultraviolet absorbance (260 nm-420 nm)/cm.
However, from the aspect of the performance of polystyrene products, the poor solubility of paraffin-based white oil often results in problems such as opaque particles, and the like, so that customers prefer cycloalkyl white oil (with a CN value of more than 40) relatively, while too high CN value often cannot easily meet the standards of food grade white oil. Thus, the CN value (CN value, i.e., naphthene carbon number) of the naphthene white oil is highly demanded.
Therefore, the special white oil which has moderate CN value and better solubility property while meeting the food-grade white oil standard is produced, the white oil belongs to a high-end white oil product, and is greatly dependent on import, and the conventional production method is to select the finished product paraffin-based white oil and cycloalkyl white oil for blending, but the product obtained by the method is easy to disqualified and needs refining reaction again, so that the production cost is increased, and even if the product which meets the requirements of the food-grade white oil and reaches the moderate CN value can be blended occasionally, the product has wide distillation range and complex components and cannot exert the maximum efficacy.
Disclosure of Invention
Based on the above, it is necessary to provide a method for preparing polystyrene white oil with moderate CN value.
In order to solve the technical problems, the invention adopts the following technical scheme:
the invention discloses polystyrene white oil with moderate CN value, which is characterized in that the yield of the polystyrene white oil with moderate CN value is more than 40%, the CN value is between 30 and 35, the average relative molecular weight is more than 500, the density at 20 ℃ is between 0.86 and 0.88g/cm < 3 >, the kinematic viscosity at 40 ℃ is between 65 and 75mm < 2 >/s, the flash point is more than 250 ℃, the ultraviolet absorbance (260 nm-420 nm)/cm is less than 0.1, and the charrable matter (GB/T11079) passes.
The invention also discloses a preparation method of the polystyrene white oil with moderate CN value, which is characterized in that the preparation method of the polystyrene white oil with moderate CN value comprises the following steps:
step S1, distilling the crude oil of the Zhonghai oil Xijiang and the crude oil of continent as raw materials, and then taking a fraction section at 450-540 ℃ to obtain a component A;
s2, distilling the crude oil of Qinhuang island 26-2 and the crude oil of Nanbao which are used as raw materials, and then taking a fraction section at 450-540 ℃ to obtain a component B;
step S3, component A and component B are mixed at 140 ℃ with 9:1 to 16: mixing the components in a mass ratio of 1 for 20min to obtain a component C;
step S4, sequentially passing the component C through a first-stage device at a first temperature, a second-stage device at a second temperature and a third-stage device at a third temperature to obtain hydrogenated oil, wherein the first-stage device comprises a hydrogenation protecting unit, a hydrotreating unit and a hydrocracking unit, the second-stage device comprises an isomerization dewaxing unit, and the third-stage device comprises a hydrofining unit;
and S5, cutting off the light fraction from the hydrogenated oil obtained in the step S4 to obtain polystyrene white oil with the distillate oil of which the temperature is more than 450 ℃ and the CN value is moderate.
As a preferred example, the components a and B are described as 9 at 140 ℃: mixing for 20min at a mass ratio of 1 to obtain component C.
As a preferred embodiment, the first temperature is 381-386 ℃, the second temperature is 350-356 ℃, and the third temperature is 235-237 ℃.
As a preferred embodiment, in the hydrogenation protecting unit, a hydrogenation protecting agent is adopted, and the marks of the hydrogenation protecting agent are GSK-19 and GSK-10;
in the hydrotreating unit, a hydrotreating catalyst is adopted, and the brands of the hydrotreating catalyst are ICR187NAQ, ICR186NAQ and ICR514LAQ;
in the hydrocracking unit, a hydrocracking catalyst is adopted, and the brand of the hydrocracking catalyst is ICR250NAQ and ICR142v2LAQ;
in the isomerization dewaxing unit, an isomerization dewaxing catalyst is adopted, and the brand of the isomerization dewaxing catalyst is ICR425LAQ and ICR456LAQ;
in the hydrofining unit, a hydrofining catalyst is adopted, and the brand of the hydrofining catalyst is ICR419LAQ.
As a preferred embodiment, in the first-stage device, the hydrogen-oil volume ratio is 700:1, the volume space velocity is 0.98h < -1 >, and the hydrogen partial pressure is 15MPa;
in the second stage device, the hydrogen-oil volume ratio is 430:1, the volume space velocity is 1.48h < -1 >, and the hydrogen partial pressure is 15MPa;
in the third stage device, the hydrogen-oil volume ratio is 430:1, the volume space velocity is 1.48h < -1 >, and the hydrogen partial pressure is 15MPa.
Compared with the prior art, the invention has the following beneficial effects:
the invention provides a preparation method of polystyrene white oil with moderate CN value, which has the characteristics of simple process, high yield and stable quality, and products with high added value are obtained from raw materials with low added value, the composition and the proportion of the raw materials are optimized, and the polystyrene white oil obtained by three-stage high-pressure hydrogenation process of hydrofining, isomerization pour point depressing and supplementary refining has the advantages of moderate CN value. The preparation method of the invention optimizes the composition and the proportion from the raw material end, and is formed by three sections of high-pressure hydrogenation and one-time distillation and cutting, the obtained polystyrene white oil has short distillation range and fine quality, and can exert more excellent energy absorption in the polystyrene production scene. In addition, the polystyrene white oil CN value obtained by the preparation method is moderate, and the polystyrene white oil has good solubility while meeting the food-grade white oil, so that the problems of opaque polystyrene particles and the like can be effectively solved.
Detailed Description
The following detailed description of the preferred embodiments of the invention is provided to enable those skilled in the art to more readily understand the advantages and features of the invention and to make a clear and concise definition of the scope of the invention.
The preparation method of the polystyrene white oil with moderate CN value comprises the following steps:
step S1, distilling the crude oil of the Zhonghai oil Xijiang and the crude oil of continent as raw materials, and then taking a fraction section at 450-540 ℃ to obtain a component A;
s2, distilling the crude oil of Qinhuang island 26-2 and the crude oil of Nanbao which are used as raw materials, and then taking a fraction section at 450-540 ℃ to obtain a component B;
step S3, component A and component B are mixed at 140 ℃ with 9:1 to 16: mixing the components in a mass ratio of 1 for 20min to obtain a component C;
step S4, sequentially passing the component C through a first-stage device at a first temperature, a second-stage device at a second temperature and a third-stage device at a third temperature to obtain hydrogenated oil, wherein the first-stage device comprises a hydrogenation protecting unit, a hydrotreating unit and a hydrocracking unit, the second-stage device comprises an isomerism dewaxing unit, and the third-stage device comprises a hydrofining unit;
and S5, cutting off the light fraction from the hydrogenated oil obtained in the step S4 to obtain polystyrene white oil with the distillate oil of which the temperature is more than 450 ℃ and the CN value is moderate.
The first temperature is 381-386 ℃, the second temperature is 350-356 ℃, and the third temperature is 235-237 ℃.
In addition, in the hydrogenation protecting unit, a hydrogenation protecting agent is adopted, and the brand of the hydrogenation protecting agent is GSK-19 and GSK-10.
In the hydrotreating unit, hydrotreating catalysts are employed, which are numbered ICR187NAQ, ICR186NAQ, and ICR514LAQ.
In the hydrocracking unit, a hydrocracking catalyst was used, which was designated ICR250NAQ and ICR142v2LAQ.
In the isodewaxing unit, isodewaxing catalysts are employed, which are identified by the designations ICR425LAQ and ICR456LAQ.
In the hydrofining unit, a hydrofining catalyst was used, which was named ICR419LAQ.
In addition, in the first stage device, the volume ratio of hydrogen to oil is 700:1, the volume space velocity is 0.98h < -1 >, and the hydrogen partial pressure is 15MPa;
in this second stage unit, the hydrogen to oil volume ratio is 430:1, the volume space velocity is 1.48h < -1 >, and the hydrogen partial pressure is 15MPa;
in this third stage unit, the hydrogen to oil volume ratio is 430:1, the volume space velocity is 1.48h < -1 >, and the hydrogen partial pressure is 15MPa.
The yield of the polystyrene white oil with moderate CN value is above 40%, the CN value is above 30-35, the average relative molecular mass is above 500, the density at 20 ℃ is between 0.86-0.88 g/cm < 3 >, the kinematic viscosity at 40 ℃ is between 65-75mm < 2 >/s, the flash point is above 250 ℃, the ultraviolet absorbance (260-420 nm)/cm is within 0.1, and the charrable matter (GB/T11079) passes.
The preparation method of the polystyrene white oil with moderate CN value is further described below.
Examples
The embodiment provides polystyrene white oil with moderate CN value, which is prepared by the following preparation method:
step S1, distilling the crude oil of the Zhonghai oil Xijiang and the crude oil of continent as raw materials, and then taking a fraction section at 450-540 ℃ to obtain a component A;
step S3, distilling the crude oil of Qinhuang island 26-2 and the crude oil of Nanbao which are used as raw materials, and then obtaining a fraction section at 450-540 ℃ to obtain a component B;
step S3, mixing the component A and the component B at 140 ℃ with 16: mixing the components in a mass ratio of 1 for 20min to obtain a component C;
and S4, sequentially passing the component C through a first-stage device at 381 ℃, a second-stage device at 350 ℃ and a third-stage device at 235 ℃ to obtain hydrogenated oil. The first stage unit includes a hydrogenation protecting unit, a hydrotreating unit, and a hydrocracking unit, the second stage unit includes an isomerization dewaxing unit, and the third stage unit includes a hydrofinishing unit. In the hydrogenation protecting unit, a hydrogenation protecting agent is adopted, and the brand of the hydrogenation protecting agent is GSK-19 and GSK-10. In the hydrotreating unit, hydrotreating catalysts are employed, which are numbered ICR187NAQ, ICR186NAQ, and ICR514LAQ. In the hydrocracking unit, a hydrocracking catalyst was used, which was designated ICR250NAQ and ICR142v2LAQ. In the isodewaxing unit, isodewaxing catalysts are employed, which are identified by the designations ICR425LAQ and ICR456LAQ. In the hydrofining unit, a hydrofining catalyst was used, which was named ICR419LAQ. In addition, the hydrogen-oil volume ratio of the three-stage device is 700:1, 430:1 and 430:1, the volume airspeeds are respectively 0.98h < -1 >, 1.48h < -1 > and 1.48h < -1 >, the hydrogen partial pressure is 15MPa, and the obtained hydrogenated oil is cut off into light fractions to obtain the polystyrene white oil with the distillate oil of more than 450 ℃ and moderate CN value.
Examples
The embodiment provides polystyrene white oil with moderate CN value, which is prepared by the following preparation method:
step S1, distilling the crude oil of the Zhonghai oil Xijiang and the crude oil of continent as raw materials, and then taking a fraction section at 450-540 ℃ to obtain a component A;
step S3, distilling the crude oil of Qinhuang island 26-2 and the crude oil of Nanbao which are used as raw materials, and then obtaining a fraction section at 450-540 ℃ to obtain a component B;
step S3, mixing the component A and the component B at 140 ℃ with 12: mixing the components in a mass ratio of 1 for 20min to obtain a component C;
in step S4, the hydrogenated oil is obtained by passing the component C through the first stage device at 383 ℃ and the second stage device at 352 ℃ and the third stage device at 237 ℃ in sequence, and the first stage device, the second stage device and the third stage device are the same as those in example 1, and the description is not repeated. The hydrogen-oil volume ratio of the three-stage device is 700:1, 430:1 and 430:1, the volume airspeeds are respectively 0.98h < -1 >, 1.48h < -1 > and 1.48h < -1 >, the hydrogen partial pressure is 15MPa, and the obtained hydrogenated oil is cut off into light fractions to obtain the polystyrene white oil with the distillate oil of more than 450 ℃ and moderate CN value.
Examples
The embodiment provides polystyrene white oil with moderate CN value, which is prepared by the following preparation method:
step S1, distilling the crude oil of the Zhonghai oil Xijiang and the crude oil of continent as raw materials, and then taking a fraction section at 450-540 ℃ to obtain a component A;
step S3, distilling the crude oil of Qinhuang island 26-2 and the crude oil of Nanbao which are used as raw materials, and then obtaining a fraction section at 450-540 ℃ to obtain a component B;
step S3, component A and component B are mixed at 140 ℃ with 9: mixing the components in a mass ratio of 1 for 20min to obtain a component C;
in step S4, the hydrogenated oil is obtained by passing the component C through the first stage device at 386℃and the second stage device at 356℃and the third stage device at 237℃in this order, and the first stage device, the second stage device and the third stage device are the same as those in example 1, and the description thereof will not be repeated. The hydrogen-oil volume ratio of the three-stage device is 700:1, 430:1 and 430:1, the volume airspeeds are respectively 0.98h < -1 >, 1.48h < -1 > and 1.48h < -1 >, the hydrogen partial pressure is 15MPa, and the obtained hydrogenated oil is cut off into light fractions to obtain the polystyrene white oil with the distillate oil of more than 450 ℃ and moderate CN value.
The polystyrene white oils obtained in examples 1-3 were tested as follows:
(1) Yield (relative to component C),%;
(2) Density (20 ℃), g/cm3: testing according to SH/T0604-2000;
(3) Kinematic viscosity at 40 ℃, mm2/s: testing was performed according to GB/T265-1988;
(4) Kinematic viscosity at 100 ℃, mm2/s: testing according to GB/T265;
(5) Flash point (opening), c: testing was performed according to GB/T3536;
(6) CN value,%: the test was performed according to SH/T0725;
(7) CP value,%: the test was performed according to SH/T0725;
(8) Initial point, DEG C: testing was performed according to SH/T0558;
(9) 5% (mass fraction) distillation point carbon number: testing was performed according to SH/T0558;
(10) 5% (mass fraction) distillation point temperature, DEG C: testing was performed according to SH/T0558;
(11) Average relative molecular mass, tested according to GB/T17282:
(12) Color, sibort color number: testing was performed according to GB/T3555;
(13) Polycyclic aromatic hydrocarbon, ultraviolet absorbance, (260 nm-420 nm)/cm: testing was performed according to NB/SH/T0415;
(14) Lead (Pb), wt ppm: testing was performed according to Q/ZHTS-048;
(15) Arsenic (Ab), wt ppm: testing was performed according to Q/ZHTS-048;
(16) Weight content, wt ppm: testing was performed according to Q/ZHTS-048;
(17) Easy carbide: testing was performed according to GB/T11079;
(18) Solid paraffin: testing was performed according to SH/T0134;
(19) Water-soluble acids or bases: testing according to GB/T259-1988
(20) Pour point, c: testing according to GB/T3535-2006;
(21) Refractive index (20 ℃ C.): the test was carried out according to GB/T6488.
The test results are summarized in table 1 below.
Table 1 test comparison
| Project | Example 1 | Example 2 | Example 3 |
| Yield% | 37 | 39.7 | 42 |
| Density (20 ℃), g/cm3 | 0.8619 | 0.8639 | 0.8649 |
| Kinematic viscosity at 40 ℃ and mm2/s | 73.12 | 72 | 70.91 |
| Kinematic viscosity at 100 ℃ and mm2/s | 9.55 | 9.39 | 9.24 |
| Flash point (open) DEG C | 265 | 269 | 272 |
| CN value,% | 30.4 | 31.3 | 32.4 |
| CP value,% | 69.6 | 68.7 | 67.8 |
| Initial point of distillation, DEG C | 406 | 409 | 411 |
| 5% (mass fraction) distillation point carbon number | 29 | 29 | 29 |
| Distillation point temperature of 5% (mass fraction), DEG C | 439 | 436 | 435 |
| Average relative molecular mass | 508 | 500 | 493 |
| Color, siebold color number | ＞+30 | ＞+30 | ＞+30 |
| Polycyclic aromatic hydrocarbon, ultraviolet absorbance, (260 nm-420 nm)/cm | 0.072 | 0.039 | 0.024 |
| Lead (Pb), wt ppm | ＜0.02 | ＜0.02 | ＜0.02 |
| Arsenic (Ab), wt ppm | ＜0.2 | ＜0.2 | ＜0.2 |
| Weight content, wt ppm | ＜2 | ＜2 | ＜2 |
| Easy charring material | By passing through | By passing through | By passing through |
| Solid paraffin wax | By passing through | By passing through | By passing through |
| Water-soluble acids or bases | Without any means for | Without any means for | Without any means for |
| Pour point, C | -15 | -12 | -12 |
| Refractive index (20 ℃ C.) | 1.4747 | 1.4749 | 1.4752 |
As can be seen from the analysis of the data in Table 1, the polystyrene obtained by the preparation method of the invention has a yield of more than 40%, a CN value of between 30 and 35, an average relative molecular mass of more than 500, a density of between 0.86 and 0.88g/cm < 3 >, a kinematic viscosity of between 65 and 75mm < 2 >/s at a temperature of 20 ℃, a flash point of more than 250 ℃, an ultraviolet absorbance (260 nm to 420 nm)/cm of less than 0.1 and a charrable matter (GB/T11079) passing through. The preparation method disclosed by the invention is simple in process, the product with high added value is obtained by using the raw materials with low added value, the food-grade white oil is satisfied, meanwhile, the product has good solubility, the problems of opaque polystyrene particles and the like can be effectively solved, and the overall economic benefit of the technology is higher.
Analysis of examples 1-2 and 3 shows that examples 1-2 are not as good as example 3, since during analysis 9:1, the charring substances are easy to be blocked, so that the proportion of the component B is not easy to be further increased, and the most preferable 9 in the preparation method is shown as follows: 1, the polystyrene formed by the proportion of the raw materials and the matched technological parameters has better performance.
Without being limited thereto, any changes or substitutions that are not contemplated by the inventors are intended to be included within the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the protection scope defined by the claims.
Claims (6)
1. The polystyrene white oil with moderate CN value is characterized in that the yield of the polystyrene white oil with moderate CN value is more than 40%, the CN value is between 30 and 35, the average relative molecular mass is more than 500, the density at 20 ℃ is between 0.86 and 0.88g/cm < 3 >, the kinematic viscosity at 40 ℃ is between 65 and 75mm < 2 >/s, the flash point is more than 250 ℃, the ultraviolet absorbance (260 nm-420 nm)/cm is within 0.1, and the easy charring matter (GB/T11079) passes.
2. The preparation method of the polystyrene white oil with moderate CN value is characterized by comprising the following steps:
step S1, distilling the crude oil of the Zhonghai oil Xijiang and the crude oil of continent as raw materials, and then taking a fraction section at 450-540 ℃ to obtain a component A;
s2, distilling the crude oil of Qinhuang island 26-2 and the crude oil of Nanbao which are used as raw materials, and then taking a fraction section at 450-540 ℃ to obtain a component B;
step S3, component A and component B are mixed at 140 ℃ with 9:1 to 16: mixing the components in a mass ratio of 1 for 20min to obtain a component C;
step S4,
Passing the component C through a first stage device at a first temperature, a second stage device at a second temperature and a third stage device at a third temperature in sequence to obtain hydrogenated oil,
the first-stage device comprises a hydrogenation protecting unit, a hydrotreating unit and a hydrocracking unit,
the second stage unit comprises an isomerization dewaxing unit,
the third-stage device comprises a hydrofining unit;
and S5, cutting off the light fraction from the hydrogenated oil obtained in the step S4 to obtain polystyrene white oil with the distillate oil of which the temperature is more than 450 ℃ and the CN value is moderate.
3. The method for preparing polystyrene white oil with moderate CN value as claimed in claim 2, wherein,
the components A and B are mixed at 140 ℃ in a ratio of 9: mixing for 20min at a mass ratio of 1 to obtain component C.
4. The method for preparing polystyrene white oil with moderate CN value as claimed in claim 2, wherein,
the first temperature is 381-386 ℃,
the second temperature is 350-356 ℃,
the third temperature is 235-237 ℃.
5. The method for preparing polystyrene white oil with moderate CN value as claimed in claim 2, wherein,
in the hydrogenation protecting unit, a hydrogenation protecting agent is adopted, and the marks of the hydrogenation protecting agent are GSK-19 and GSK-10;
in the hydrotreating unit, a hydrotreating catalyst is adopted, and the brands of the hydrotreating catalyst are ICR187NAQ, ICR186NAQ and ICR514LAQ;
in the hydrocracking unit, a hydrocracking catalyst is adopted, and the brand of the hydrocracking catalyst is ICR250NAQ and ICR142v2LAQ;
in the isomerization dewaxing unit, an isomerization dewaxing catalyst is adopted, and the brand of the isomerization dewaxing catalyst is ICR425LAQ and ICR456LAQ;
in the hydrofining unit, a hydrofining catalyst is adopted, and the brand of the hydrofining catalyst is ICR419LAQ.
6. The method for preparing polystyrene white oil with moderate CN value as claimed in claim 2, wherein,
in the first-stage device, the volume ratio of hydrogen to oil is 700:1, the volume space velocity is 0.98h < -1 >, and the hydrogen partial pressure is 15MPa;
in the second stage device, the hydrogen-oil volume ratio is 430:1, the volume space velocity is 1.48h < -1 >, and the hydrogen partial pressure is 15MPa;
in the third stage device, the hydrogen-oil volume ratio is 430:1, the volume space velocity is 1.48h < -1 >, and the hydrogen partial pressure is 15MPa.
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