CN104342206A - Lubricating oil hydrodewaxing production technology - Google Patents
Lubricating oil hydrodewaxing production technology Download PDFInfo
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- CN104342206A CN104342206A CN201310322966.2A CN201310322966A CN104342206A CN 104342206 A CN104342206 A CN 104342206A CN 201310322966 A CN201310322966 A CN 201310322966A CN 104342206 A CN104342206 A CN 104342206A
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- hydrodewaxing
- oil
- reactor
- lubricating oil
- reaction
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- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1062—Lubricating oils
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- 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 provides a lubricating oil hydrodewaxing production technology, which solves the problem of low yield in a lubricating oil production technology in prior art, and the lubricating oil hydrodewaxing production technology comprises the following steps: 1)heating raw oil through pressure reduction by a heating furnace, introducing into a reactor, performing a catalytic reaction and then introducing into a normal pressure fractionate tower, introducing the normal pressure oil through fractionation at normal pressure in a hydrogenation depickling reactor; 2)introducing the deacidified oil product into a furfural treating tower, introducing the fully reacted furfural refining oil in a hydrodewaxing reactor for hydrodewaxing; and 3)introduced hydrodewaxed oil in a hydrogenation supplement refining reactor which is connected to the hydrodewaxing reactor in series for blending the finished product lubricating oil. The method employs a technical flow of hydrogenation and deacidification, furfural refining, hydrodewaxing and hydrogen supplement refining, the method has the advantages of simple flow and high benefit, and can produce the lubricating oil with low condensation point, the hydrodewaxing reactor and the hydrogenation supplement refining reactor are connected in series, hydrogen passes through the flow, hydrogen partial pressure is increased, and the equipment investment can be reduced.
Description
Technical field
The present invention relates to Oil Production field, refer to lubricating oil hydrodewaxing production technique especially.
Background technology
Now along with the raising of production mechanization level, the research and development of various advanced equipments of high grade and precision and use, also more and more higher to the requirement of lube product capability and performance.In addition the west development policy of China, the construction speed in west area is accelerated, but the operating environment of various engineering machinery is badly complicated, especially concerning the engineering machinery of western extremely frigid zones, the low-temperature fluidity of lube product is one of very important performance.------step of clay-filtered---hydrofining---lube product blending, not only productive rate is low, oil quality is poor, and whole track cost is high, and environmental pollution is high for propane deasphalting in lubricating oil processing technique, to adopt traditional solvent dewaxing.
Summary of the invention
The present invention proposes lubricating oil hydrodewaxing production technique, solves the problem that in prior art, in lubricating oil processing technique, productive rate is low.
Technical scheme of the present invention is achieved in that lubricating oil hydrodewaxing production technique, comprise following process steps, 1) stock oil that reduces pressure enters reactor through process furnace heating, and enter atmospheric fractional tower after carrying out catalyzed reaction, the normal pressure oil that normal pressure fractionates out enters hydrogenation deacidification reactor; 2) oil product after depickling enters furfural treatment tower, and the furfural refining oil reacted completely carries out pour point depression reaction entering in hydrodewaxing reactor; 3) oil after pour point depression enters concocts out finished lube with the hydrofinishing reactor of described hydrodewaxing reactors in series.
As preferred technical scheme, in described hydrodewaxing reactor, use catalyzer RDW-1; Catalyzer RN-1 is used in described hydrofinishing reactor.
As preferred technical scheme, described hydrogenation deacidification reactor temperature is 270 ~ 280 DEG C, pressure 5.0MPa, and the volume ratio adding hydrogen and reaction oil is 320 ~ 350, volume space velocity 0.65 ~ 0.75h
-1.
As preferred technical scheme, described furfural treatment column overhead temperatures 65 ~ 105 DEG C, column bottom temperature 35 ~ 75 DEG C.
As preferred technical scheme, the temperature of reaction of described hydrodewaxing reactor is 250 ~ 300 DEG C, pressure 3.0MPa, air speed 1.0h
-1, the volume ratio of hydrogen and reaction oil is 440: 1, reaction times 8h.
The present invention compares the beneficial effect of generation with background technology:
1) the present invention adopts hydrogenation deacidification, and---hydrogen post-refining process flow process is faced in furfural treatment---hydrodewaxing---, and this flow process is simple, high efficiency, can produce low condensation point lubricating oil.
2) hydrodewaxing reactor and hydrofinishing reactors in series, hydrogen once by flow process, improve hydrogen dividing potential drop, decrease facility investment.
3) RDW-1 catalyzer has the dual-function catalyst of hydrogenation and selective cracking effect, and oil product under the acting in conjunction of RDW-1 catalyzer and hydrogen, wax destructive distillation occurs and reacts, and makes its depression of pour point, reaches the requirement of base oil to pour point.
Accompanying drawing explanation
In order to be illustrated more clearly in the embodiment of the present invention or technical scheme of the prior art, be briefly described to the accompanying drawing used required in embodiment or description of the prior art below, apparently, accompanying drawing in the following describes is only some embodiments of the present invention, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
Fig. 1 is the technological process apparatus schematic diagram of an embodiment of the present invention;
Fig. 2 is process flow diagram of the present invention.
In figure: 1-first circular-arc gear pump; 2-process furnace; 3-reactor; 4-hydrogenation deacidification reactor; 5-second circular-arc gear pump; 6-furfural treatment tower; 7-hydrodewaxing reactor; 8-first drying machine; 9-second drying machine; 10-hydrofinishing reactor.
Embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, be clearly and completely described the technical scheme in the embodiment of the present invention, obviously, described embodiment is only the present invention's part embodiment, instead of whole embodiments.Based on the embodiment in the present invention, those of ordinary skill in the art, not making the every other embodiment obtained under creative work prerequisite, belong to the scope of protection of the invention.
Lubricating oil hydrodewaxing production technique, comprises following process steps, 1) decompression stock oil through process furnace heating enter reactor, enter atmospheric fractional tower after carrying out catalyzed reaction, the normal pressure oil that normal pressure fractionates out enters hydrogenation deacidification reactor; 2) oil product after depickling enters furfural treatment tower, and the furfural refining oil reacted completely carries out pour point depression reaction entering in hydrodewaxing reactor; 3) oil after pour point depression enters concocts out finished lube with the hydrofinishing reactor of described hydrodewaxing reactors in series.
As preferred technical scheme, in described hydrodewaxing reactor, use catalyzer RDW-1; Catalyzer RN-1 is used in described hydrofinishing reactor.
As preferred technical scheme, described hydrogenation deacidification reactor temperature is 270 ~ 280 DEG C, pressure 5.0MPa, and the volume ratio adding hydrogen and reaction oil is 320 ~ 350, volume space velocity 0.65 ~ 0.75h
-1.
As preferred technical scheme, described furfural treatment column overhead temperatures 65 ~ 105 DEG C, column bottom temperature 35 ~ 75 DEG C.
As preferred technical scheme, the temperature of reaction of described hydrodewaxing reactor is 250 ~ 300 DEG C, pressure 3.0MPa, air speed 1.0h
-1, the volume ratio of hydrogen and reaction oil is 440: 1, reaction times 8h.
As shown in Figure 1 and Figure 2, decompression stock oil is heated to 300 ~ 350 DEG C from tank field with the first circular-arc gear pump 1 suction process furnace 2, after enter reactor 3, the reaction such as cracking, isomerization is carried out under catalyst action, reaction is thermo-negative reaction, reactor cooling 35 ~ 45 DEG C, and reacted product enters in tower and carries out normal pressure fractionation, the distillate wax content such as normal two wires, atmosphere 3rd side cut, second line of distillation after fractionation is few, and character is in table 1.
Table 1
If distillate solvent refining---clay finishing technique, then because naphthenic acid content in raw material is high, acidity is high, not only easily make equipment coking, and oil yield is low, extraction oil quality is poor, performance of enterprises loss is serious, but adopt hydrogenation deacidification that distillate acid number can be made to decline, remove part organosulfur, in hydrogenation deacidification reactor 4, temperature is 270 ~ 280 DEG C, pressure 5.0MPa, the volume ratio adding hydrogen and reaction oil is 320 ~ 350, volume space velocity 0.65 ~ 0.75h
-1condition under carry out, each line oil property after hydrogenation deacidification is in table 2.
Table 2
Contrast table 1, table 2 can be found out, obvious from hydrogenation deacidification reactor 4 oil product acid number fall out, and acid removal rate is more than 98%, and also sloughed part organosulfur, desulfurization degree is between 20 ~ 40%, and oil product condensation point is gone up to some extent simultaneously.
The reacted oil product of hydrogenation deacidification sends into furfural treatment tower 6 by the second circular-arc gear pump 5 again, tower top temperature 65 ~ 105 DEG C, column bottom temperature 35 ~ 75 DEG C, carries out under the condition of solvent ratio 2 ~ 2.5, in tower, react duration is 10h, and the related properties of each line furfural refining oil see the following form 3.
Table 3
As shown in Table 3, in furfural refining oil, sulphur, nitrogen content obviously decline, and desulfurization degree is below 50%, and denitrification percent is between 65% ~ 77%, and oil product condensation point is gone up further.
Furfural refining oil enters hydrodewaxing reactor 7, uses catalyzer RDW-1 in hydrodewaxing reactor 7, and temperature of reaction is 250 ~ 300 DEG C, pressure 3.0MPa, air speed 1.0h
-1, the volume ratio of hydrogen and reaction oil is 440: 1, reaction times 8h, hydrodewaxing reactor 7 is connected with the first drying machine 8, after furfural refining oil is reacted in hydrodewaxing reactor 7, first drying machine 8 is started working, deviate from the moisture of catalyzer RDW-1, from hydrodewaxing reactor 7, oil product out enters hydrofinishing reactor 10, hydrofinishing reactor 10 is connected with hydrodewaxing reactor 7, catalyzer RN-1 is wherein housed, hydrofinishing reactor 10 is connected with the second drying machine 9, second drying machine 9 is for sloughing the moisture of catalyzer RN-1, temperature of reaction is 200 ~ 250 DEG C, pressure 2.5MPa, air speed 1.0h
-1, the volume ratio of hydrogen and reaction oil is 400: 1, reaction times 12h, and after reaction, each line product property is as following table 4.
Table 4
As can be seen from Table 4, sulphur content and the condensation point of oil product all obviously reduce, wherein normal two wires pour point depression oil can be used for blending No. 45 transformer oil, low temperature instrument wet goods lubricating oil, atmosphere 3rd side cut pour point depression oil can be used for concocting serial refrigerator wet goods lube product, and second line of distillation pour point depression oil can be used for the products such as blending lithium soap grease.
The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention, within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (5)
1. lubricating oil hydrodewaxing production technique, is characterized in that, comprises following process steps:
1) stock oil that reduces pressure enters reactor through process furnace heating, and enter atmospheric fractional tower after carrying out catalyzed reaction, the normal pressure oil that normal pressure fractionates out enters hydrogenation deacidification reactor;
2) oil product after depickling enters furfural treatment tower, and the furfural refining oil reacted completely carries out pour point depression reaction entering in hydrodewaxing reactor;
3) oil after pour point depression enters concocts out finished lube with the hydrofinishing reactor of described hydrodewaxing reactors in series.
2. lubricating oil hydrodewaxing production technique as claimed in claim 1, is characterized in that:
Catalyzer RDW-1 is used in described hydrodewaxing reactor;
Catalyzer RN-1 is used in described hydrofinishing reactor.
3. lubricating oil hydrodewaxing production technique as claimed in claim 1, is characterized in that:
Described hydrogenation deacidification reactor temperature is 270 ~ 280 DEG C, pressure 5.0MPa, and the volume ratio adding hydrogen and reaction oil is 320 ~ 350, volume space velocity 0.65 ~ 0.75h
-1.
4. lubricating oil hydrodewaxing production technique as claimed in claim 1, is characterized in that:
Described furfural treatment column overhead temperatures 65 ~ 105 DEG C, column bottom temperature 35 ~ 75 DEG C.
5. lubricating oil hydrodewaxing production technique as claimed in claim 1, is characterized in that:
The temperature of reaction of described hydrodewaxing reactor is 250 ~ 300 DEG C, pressure 3.0MPa, air speed 1.0h
-1, the volume ratio of hydrogen and reaction oil is 440: 1, reaction times 8h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310322966.2A CN104342206A (en) | 2013-07-29 | 2013-07-29 | Lubricating oil hydrodewaxing production technology |
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| CN201310322966.2A CN104342206A (en) | 2013-07-29 | 2013-07-29 | Lubricating oil hydrodewaxing production technology |
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| CN104342206A true CN104342206A (en) | 2015-02-11 |
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| CN201310322966.2A Pending CN104342206A (en) | 2013-07-29 | 2013-07-29 | Lubricating oil hydrodewaxing production technology |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112625773A (en) * | 2019-10-09 | 2021-04-09 | 中国海洋石油集团有限公司 | Preparation method of transformer oil base oil |
Citations (5)
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|---|---|---|---|---|
| CN1258721A (en) * | 1998-12-30 | 2000-07-05 | 广饶县金利润滑油厂 | Lubricating oil non-hydrogen condensation point reducing production process |
| CN1982417A (en) * | 2005-12-14 | 2007-06-20 | 中国石油化工股份有限公司 | Production of naphthenic lube oil and base oil |
| CN102485846A (en) * | 2010-12-03 | 2012-06-06 | 中国石油天然气股份有限公司 | Preparation method of base oil of transformer oil |
| CN103045303A (en) * | 2011-10-17 | 2013-04-17 | 中国石油天然气股份有限公司 | Preparation method of base oil of refrigerator oil |
| CN103102953A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Pretreatment method for crude lube stock |
-
2013
- 2013-07-29 CN CN201310322966.2A patent/CN104342206A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1258721A (en) * | 1998-12-30 | 2000-07-05 | 广饶县金利润滑油厂 | Lubricating oil non-hydrogen condensation point reducing production process |
| CN1982417A (en) * | 2005-12-14 | 2007-06-20 | 中国石油化工股份有限公司 | Production of naphthenic lube oil and base oil |
| CN102485846A (en) * | 2010-12-03 | 2012-06-06 | 中国石油天然气股份有限公司 | Preparation method of base oil of transformer oil |
| CN103045303A (en) * | 2011-10-17 | 2013-04-17 | 中国石油天然气股份有限公司 | Preparation method of base oil of refrigerator oil |
| CN103102953A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Pretreatment method for crude lube stock |
Non-Patent Citations (4)
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| 梁文杰: "《石油化学》", 31 March 1995 * |
| 汤规成，等: "辽河稠油生产低凝点润滑油基础油", 《石油炼制与化工》 * |
| 王雷，李会鹏: "《炼油工艺学》", 30 June 2011 * |
| 祖德光: "润滑油基础油生产技术的新进展", 《润滑油》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112625773A (en) * | 2019-10-09 | 2021-04-09 | 中国海洋石油集团有限公司 | Preparation method of transformer oil base oil |
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