CN113072975A - System and process for producing lubricating oil base oil - Google Patents
System and process for producing lubricating oil base oil Download PDFInfo
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- CN113072975A CN113072975A CN202110269680.7A CN202110269680A CN113072975A CN 113072975 A CN113072975 A CN 113072975A CN 202110269680 A CN202110269680 A CN 202110269680A CN 113072975 A CN113072975 A CN 113072975A
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- 238000000034 method Methods 0.000 title claims abstract description 44
- 230000008569 process Effects 0.000 title claims abstract description 34
- 239000002199 base oil Substances 0.000 title claims abstract description 31
- 239000010687 lubricating oil Substances 0.000 title claims abstract description 29
- 239000001257 hydrogen Substances 0.000 claims abstract description 27
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 27
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 19
- 238000006317 isomerization reaction Methods 0.000 claims abstract description 17
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 13
- 238000007670 refining Methods 0.000 claims abstract description 11
- 239000000314 lubricant Substances 0.000 claims abstract description 8
- 230000009467 reduction Effects 0.000 claims abstract description 5
- 238000006243 chemical reaction Methods 0.000 claims description 22
- 239000003921 oil Substances 0.000 claims description 20
- 239000003054 catalyst Substances 0.000 claims description 12
- 239000007789 gas Substances 0.000 claims description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 239000012071 phase Substances 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
- 238000004821 distillation Methods 0.000 claims description 3
- 150000002431 hydrogen Chemical class 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 229910052717 sulfur Inorganic materials 0.000 claims description 3
- 239000011593 sulfur Substances 0.000 claims description 3
- 239000007791 liquid phase Substances 0.000 claims description 2
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- 229910017318 Mo—Ni Inorganic materials 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000000047 product Substances 0.000 description 8
- 238000004517 catalytic hydrocracking Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 230000000295 complement effect Effects 0.000 description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 3
- 239000002283 diesel fuel Substances 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- 239000012188 paraffin wax Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000000881 depressing effect Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000001050 lubricating effect Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000010705 motor oil Substances 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
Images
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
- C10G67/14—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 including at least two different refining steps in the absence of hydrogen
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/10—Lubricating oil
Abstract
The invention relates to the technical field of lubricating oil production, in particular to a system and a process for producing lubricating oil base oil. The system comprises a hydrotreating reactor, a high-pressure stripping tower, an isomerization dewaxing reactor, a supplementary refining reactor, a cold high-pressure separation tank, a cold low-pressure separation tank, an atmospheric tower and a pressure reduction tower which are sequentially connected, and the system also comprises a recycle hydrogen compressor; the top pipeline of the high-pressure stripping tower is communicated with the inlet of a recycle hydrogen compressor through a cold high-pressure separation tank, and the outlet of the recycle hydrogen compressor returns to the inlet of the hydrotreating reactor and the inlet of the isomerization dewaxing reactor through pipelines. The system is applied to produce the lubricant base oil by a one-stage hydrotreating-isodewaxing method. The system and the process can realize the production of the required lubricating oil only by one-stage hydrogenation process, and have the advantages of simple process, energy consumption reduction and cost reduction.
Description
Technical Field
The invention relates to the technical field of lubricant oil production, and belongs to a process method for producing lubricant base oil by hydrotreating and isodewaxing in the hydrogen state.
Background
In the traditional production of the base oil of the lubricating oil, solvent refining is adopted to remove non-ideal components such as aromatic hydrocarbon and the like, and solvent dewaxing is adopted to ensure the low-temperature flow property of the base oil. In recent years, as environmental protection requirements have become more stringent, higher and higher requirements have been made on the performance of lubricant base oils.
The quantity of paraffin-based crude oil suitable for producing high viscosity index lubricating oil base oil by the traditional process is gradually reduced due to the deterioration of crude oil worldwide, so the technology for producing the lubricating oil by the hydrogenation method is developed rapidly. The hydrogenation process refers to a process for producing the lubricant base oil by adopting a combined process of hydrotreating or hydrocracking process-hydrodewaxing or isodewaxing-hydrofining, and has the advantages of high flexibility of raw materials, high yield of the base oil, high value of byproducts and the like.
Lube isodewaxing is a new technology developed in the nineties of the last century to produce high quality API II/III lubricant base oils, the key to this technology being the isomerization catalyst. Isodewaxing is a technique in which straight-chain paraffins with a higher pour point in an oil product are isomerized into isoparaffins to reduce the pour point of the product and maintain a higher yield of lube base oil. Compared with solvent dewaxing and catalytic dewaxing, the isodewaxing base oil has high yield, low pour point and high viscosity index, and is an excellent blending component of modern high-performance internal combustion engine oil.
US6676827 discloses a process for the production of low pour point lubricant base oils by isodewaxing. A hydrocracking-isodewaxing two-stage hydrogenation process route is adopted, and both hydrocracking and isodewaxing have respective hydrogen circulation systems, which is the main process for producing the lubricating oil base oil by the current hydrogenation method. Because two-stage process is used, the process flow is complex, the equipment is more, and the running cost is high.
US 4283272 discloses a process for producing lube base stock by a hydrocracking-hydrodewaxing-post refining one stage process. The technology adds an adsorption unit behind a hydrocracking unit, so that hydrogen sulfide and ammonia in a hydrocracking product can be removed, then the material flow directly enters a hydrodewaxing and complementary refining unit, the hydrocracking product of the technology completely enters the hydrodewaxing and complementary refining unit without distillation separation, and the purpose of producing lubricating oil is realized by adding the adsorption unit, so that the reaction efficiency is greatly reduced, the device investment is increased, the operation cost such as energy consumption is increased, and the process is more complex.
CN 103627430B discloses a hydrogenation method for directly producing low-condensation-point lubricating oil base oil, which adopts a hydrofining-hydrocracking-hydrofining process route, and the effluent of a post-refining reactor is separated and fractionated to obtain the lubricating oil base oil with low condensation point, high viscosity index and good oxidation stability, and simultaneously, the low-condensation-point high-quality diesel oil, naphtha, aviation kerosene and other light products can be co-produced.
Disclosure of Invention
Based on the problems existing in the prior art, the invention provides a hydrotreating method for producing lubricating base oil by a one-stage hydrotreating-isodewaxing method and simultaneously producing high-quality white oil, diesel oil and the like as byproducts. The method overcomes the problem that qualified lubricating oil base oil can be obtained only by two-stage hydrogenation or subsequent independent pour point depressing process and supplementary refining process in the prior art, and has simpler flow and lower energy consumption of devices.
In order to realize the purpose, the invention adopts the following technical scheme:
the invention provides a system for producing lubricating oil base oil, which comprises a hydrotreating reactor, a high-pressure stripping tower, an isomerization dewaxing reactor, a complementary refining reactor, a cold high-pressure separation tank, a cold low-pressure separation tank, an atmospheric tower and a pressure reduction tower which are sequentially connected, and the system also comprises a recycle hydrogen compressor; and the top pipeline of the high-pressure stripping tower is communicated with the inlet of a recycle hydrogen compressor through a cold high-pressure separation tank, and the outlet of the recycle hydrogen compressor returns to the inlet of the hydrotreating reactor and the inlet of the isomerization dewaxing reactor through pipelines.
In another aspect of the present invention, a process for producing lube base oil by one-stage hydroprocessing is provided, where the process employs the above system, and the method includes:
(1) mixing raw oil with hydrogen, feeding the mixture into a hydrotreating reactor, and contacting the mixture with a catalyst to perform reaction;
(2) removing H from the reaction effluent of the hydrotreating reactor by a high-pressure stripping tower2S, then entering an isomerization dewaxing reactor, contacting with a catalyst for reaction, and separating and fractionating reactor effluent to obtain heavy lubricating oil, medium lubricating oil and light lubricating oil;
in the above technical scheme, further, in the step (2), after passing through the high-pressure stripping tower, the reaction effluent of the hydrotreating reactor is mixed with recycle hydrogen and enters the isomerization dewaxing reactor for hydrogenation, and after cold high-pressure separation of the gas phase, the gas phase enters the recycle hydrogen compressor for pressure increase, and then enters the hydrotreating section and the isomerization dewaxing section again.
In the above technical solution, further, the catalyst is a hydrotreating catalyst, and the active component thereof is Mo — Ni.
In the above technical scheme, further, the raw oil is straight-run vacuum distillate oil, and the distillation range of the raw oil is 300-600 ℃.
In the technical scheme, the sulfur content in the oil product entering the isomerization dewaxing reactor is less than or equal to 6 mu g/g, and the nitrogen content is less than or equal to 2 mu g/g.
In the above technical scheme, further, the reaction conditions of the hydrotreating reactor are as follows: the reaction temperature is 300-450 ℃, the reaction pressure is 3.0-20.0 MPa, the volume ratio of hydrogen to raw oil is 300-2000, and the volume space velocity is 0.1-5.0 h-1。
In the technical scheme, further, the operating condition of the high-pressure stripping tower is 3.0-20.0 MPa, and stripping gas adopted by the high-pressure stripping tower is fresh hydrogen.
The invention has the beneficial effects that: the invention does not adopt a thermal high-temperature system of the traditional lubricating oil hydrogenation process, is only suitable for one set of cold high-temperature process, reduces the quantity of process equipment, saves the investment of devices, and has simple process, reduces energy consumption and reduces cost because only one section of hydrogenation process is needed to realize the production of the required lubricating oil.
Drawings
FIG. 1 is a process diagram of the system of the present invention;
in the figure, 1, a hydrotreating reactor, 2, a high-pressure stripping tower, 3, a cold high-pressure separation tank, 4, a cold low-pressure separation tank, 5, an isomerization dewaxing reactor, 6, a complementary refining reactor, 7, an atmospheric tower, 8, a vacuum tower and 9, a recycle hydrogen compressor.
Detailed Description
The invention is further illustrated but is not in any way limited by the following specific examples.
Example 1
Raw oil enters a hydrotreating reactor 1 from a raw oil buffer tank to react, the reaction pressure is 14.65Mpa, the reaction temperature is 367-415 ℃, a reaction product enters a high-pressure stripping tower 2, the high-pressure stripping tower 2 adopts new hydrogen stripping, the tower bottom oil and hydrogen of the high-pressure stripping tower 2 are mixed and enter an isomerization dewaxing reactor 5, the reaction pressure is 15.1Mpa, the reaction temperature is 345-400 ℃, under the action of a noble metal catalyst and hydrogen, a macromolecular paraffin isomerization reaction occurs, the isomerization dewaxing reaction product enters a supplementary refining reactor 6, the reaction pressure is 15.1Mpa, the reaction temperature is 220-260 ℃, an aromatic hydrocarbon and olefin saturation reaction occurs under the action of the noble metal catalyst, and the color and stability of the product are improved. The hydrogenation catalyst used in this example was HR 1058, the component being MO-Ni.
The refined reaction product and the top effluent of the stripping tower enter a cold high-pressure separation tank 3 for gas-liquid separation, the liquid phase enters a cold low-pressure separation tank 4 for gas-oil-water separation again, and the separated oil phase passes through an atmospheric tower 7 and a vacuum tower 8 to obtain the lubricating oil base oil fraction such as light lubricating oil, medium lubricating oil and heavy lubricating oil and other oil products such as diesel oil. The hydrogen flowing out from the top of the cold high-pressure separation tank 3 is pressurized by a recycle hydrogen compressor and returns to the inlets of the hydrotreating reactor 1 and the isomerization dewaxing reactor 5.
Under the above process conditions, the yield of the base oils II and III of the present invention is not less than 61.5%. The properties of the group II and group III base oils are shown in tables 1-3.
TABLE 1 guaranteed values of HVIH group II base oil properties
TABLE 2 guaranteed values for VHVI III base oils properties
TABLE 3 guaranteed values of the properties of the technical white oil
| |
5# crude white oil | No. 10 crude white oil | Analytical method |
| Kinematic viscosity (40 ℃) at/mm2. s-1 | 3～＜6 | 8～＜12 | GB/T 265 |
| Flash point (open)/°c | ≮110 | ≮140 | GB/T 3536 |
| Pour point/. degree.C | ≯3 | ≯-6 | GB/T 3535 |
| Sulfur content/mg.kg-1 | ≯10 | ≯10 | SH/T 0689 |
| Water (mass% /) | Is free of | Is free of | GB/T 260 |
| Mechanical impurities (mass% /) | Is free of | Is free of | GB/T 511 |
| Aromatic hydrocarbons (mass% /) | ≯10 | ≯10 | NB/SH/T 0966 |
| Corrosion of copper sheet, 3 h/grade | 1(50℃) | 1(100℃) | GB/T 5096 |
| Saybolt colour, number | ≮+20 | ≮+20 | GB/T 3555 |
As can be seen from the results in the table above, the method of the invention can obtain qualified II and III lubricating oil base oils only by a one-stage hydrogenation process.
It will be apparent to those skilled in the art from this disclosure that many changes and modifications can be made, or equivalents modified, in the embodiments of the invention without departing from the scope of the invention. Therefore, any simple modification, equivalent change and modification made to the above embodiments according to the technical essence of the present invention shall still fall within the protection scope of the technical solution of the present invention, unless the contents of the technical solution of the present invention are departed.
Claims (8)
1. The system for producing the lubricating oil base oil is characterized by comprising a hydrotreating reactor, a high-pressure stripping tower, an isomerization dewaxing reactor, a supplementary refining reactor, a cold high-pressure separation tank, a cold low-pressure separation tank, an atmospheric tower and a pressure reduction tower which are sequentially connected, and the system also comprises a recycle hydrogen compressor; and the top pipeline of the high-pressure stripping tower is communicated with the inlet of a recycle hydrogen compressor through a cold high-pressure separation tank, and the outlet of the recycle hydrogen compressor returns to the inlet of the hydrotreating reactor and the inlet of the isomerization dewaxing reactor through pipelines.
2. A process for producing a lubricant base oil by one-stage hydroprocessing, the process employing the system of claim 1, the method comprising:
(1) mixing raw oil with hydrogen, feeding the mixture into a hydrotreating reactor, and contacting the mixture with a catalyst to perform reaction;
(2) removing H from the reaction effluent of the hydrotreating reactor by a high-pressure stripping tower2And (4) allowing the S to enter an isomerization dewaxing reactor, contacting with a catalyst for reaction, and separating and fractionating reactor effluent to obtain heavy lubricating oil, medium lubricating oil and light lubricating oil.
3. The process for producing lube base stock by hydrotreating as claimed in claim 2, wherein in step (2), the reaction effluent from the hydrotreating reactor is passed through a high-pressure stripper, the liquid phase is mixed with recycle hydrogen and fed into an isodewaxing reactor for hydrogenation, the gas phase is separated by cold high-pressure separation, fed into a recycle hydrogen compressor for pressure increase, and fed into the hydrotreating section and the isodewaxing section again.
4. The process for producing lube base stock by hydrotreating as claimed in claim 2 wherein the catalyst is a hydrotreating catalyst whose active component is Mo-Ni.
5. The process for producing lube base stock by hydrotreating as claimed in claim 2, wherein the feedstock is straight run vacuum distillate and the distillation range of the feedstock is 300-600 ℃.
6. The process of claim 2, wherein the oil entering the isodewaxing reactor has a sulfur content of 6 μ g/g or less and a nitrogen content of 2 μ g/g or less.
7. The process for producing lube base stock by hydrotreating as claimed in claim 2 in which the reaction conditions in the hydrotreating reactor are: the reaction temperature is 300-450 ℃, the reaction pressure is 3.0-20.0 MPa, the volume ratio of hydrogen to raw oil is 300-2000, and the volume space velocity is 0.1-5.0 h-1。
8. The process for producing the lubricating oil base oil by the hydrotreating as claimed in claim 2, wherein the operating conditions of the high-pressure stripping tower are 3.0-20.0 MPa, and the stripping gas adopted by the high-pressure stripping tower is fresh hydrogen.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110269680.7A CN113072975A (en) | 2021-03-12 | 2021-03-12 | System and process for producing lubricating oil base oil |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110269680.7A CN113072975A (en) | 2021-03-12 | 2021-03-12 | System and process for producing lubricating oil base oil |
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| CN113072975A true CN113072975A (en) | 2021-07-06 |
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| CN202110269680.7A Pending CN113072975A (en) | 2021-03-12 | 2021-03-12 | System and process for producing lubricating oil base oil |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103305267A (en) * | 2013-06-25 | 2013-09-18 | 中石化南京工程有限公司 | Method for producing high-grade lubricant base oil through hydrogenating of hydrocracking tail oil |
| US20130253238A1 (en) * | 2010-09-07 | 2013-09-26 | Dalian Institute Of Chemical Physics (Dicp), Chinese Academy Of Sciences (Cas) | Method for producing lubricating base oil with low cloud point and high viscosity index |
| CN103773466A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Method for producing lubricant base oil by hydrocracking-isodewaxing combination |
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- 2021-03-12 CN CN202110269680.7A patent/CN113072975A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130253238A1 (en) * | 2010-09-07 | 2013-09-26 | Dalian Institute Of Chemical Physics (Dicp), Chinese Academy Of Sciences (Cas) | Method for producing lubricating base oil with low cloud point and high viscosity index |
| CN103773466A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Method for producing lubricant base oil by hydrocracking-isodewaxing combination |
| CN103305267A (en) * | 2013-06-25 | 2013-09-18 | 中石化南京工程有限公司 | Method for producing high-grade lubricant base oil through hydrogenating of hydrocracking tail oil |
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