CN204342741U - With the coal-tar heavy oil distillate hydrogenation device of low aromatic hydrocarbon oil circulation - Google Patents
With the coal-tar heavy oil distillate hydrogenation device of low aromatic hydrocarbon oil circulation Download PDFInfo
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- CN204342741U CN204342741U CN201420794599.6U CN201420794599U CN204342741U CN 204342741 U CN204342741 U CN 204342741U CN 201420794599 U CN201420794599 U CN 201420794599U CN 204342741 U CN204342741 U CN 204342741U
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Abstract
A kind of coal-tar heavy oil distillate hydrogenation device with low aromatic hydrocarbon oil circulation, comprise vacuum still, hydrofining reactor, separation system, thionizer, separation column, hydrocracking reactor, vacuum still is provided with coal-tar heavy oil entrance, heavy fraction outlet is arranged at bottom, and fraction outlets is arranged at top; The reaction feed mouth be connected with fraction outlets is arranged at hydrofining reactor top, and bottom is provided with discharge port and is connected with separation system; Separation system top is provided with hydrogen outlet, and bottom is provided with liquid-phase outlet and is connected with thionizer; The bottom of thionizer is provided with the liquid-phase outlet be connected with separation column, separation column is provided with fraction outlets, wherein be greater than 350 DEG C of cut parts and enter hydrocracking reactor as unconverted oil, another part is mixed into hydrofining reactor as low aromatic hydrocarbon oil and lighting end, the top of hydrocracking reactor is provided with opening for feed, and bottom is provided with the outlet be connected with separation system.Have rational in infrastructure, simple to operate, the manageable feature of temperature of reaction.
Description
Technical field
The utility model belongs to technical field of coal chemical industry, particularly relates to a kind of coal-tar heavy oil distillate hydrogenation device with low aromatic hydrocarbon oil circulation.
Background technology
Coal tar is one of important byproduct of coking of coal, in coal coke is produced, occupy certain share.Based on current coal coking technology, coal tar output accounts for 3.5% ~ 4.2%.But because downstream chemical industry falls behind the restriction of technology, the coal tar of the substantial amounts of coking by-product is difficult to there is high value added utilization.At present, three parts are mainly divided in the consumption market of China's coal-tar heavy oil, and one is by the fuel of crude coal tar heavy oil as an alternative, for the heat energy such as glass, pottery industry and as the raw material producing carbon black; Two is outlets; Three is produce the products such as NAPTHALENE FLAKES. (INDUSTRIAL GRADE）, washing oil, carbolineum and coal-tar pitch for deep processing.
In China, some areas, East China and market, south China have the substitute of coal-tar heavy oil as grade oil oil fuel, for burning glass, pottery, or the producer of other fuel applications.And at this part, coal-tar middle oil proportion is comparatively large, coal-tar heavy oil, is actually used in quantity combusted and successively decreases year by year.The tendency of doughnut industry has to the carbon black tendency taking coal-tar heavy oil as raw material the effect that can not be ignored.Continue falling by domestic economy slowdown in growth and each economic target to affect, the overall market in domestic car market in the first half of the year have no and are clearly better.The depression of automobile market decreases market to tire demand, and this also makes the market requirement of tire to carbon black reduce further.In recent years, although domestic coal tar production capacity is constantly expanded, affect by state control coal tar wet goods resource products export policy, under the overall background of can't get rid of in global economy slowdown in growth, Eurosis in addition, China's coal tar export volume reduces year by year.The products such as NAPTHALENE FLAKES. (INDUSTRIAL GRADE）, washing oil, carbolineum and coal-tar pitch are produced in conventional deep processing.NAPTHALENE FLAKES. (INDUSTRIAL GRADE） is generally used for the use of material of construction water reducer, and coal-tar pitch is generally used for aluminium industry.Washing oil, carbolineum, due to comparison of ingredients complexity, are difficult to the utilization carrying out high added value, are mainly used in coke oven gas purification, as the raw material of the products such as separation and Extraction biphenyl, methylnaphthalene, acenaphthene, fluorenes, dibenzofuran.The barrier of industrial chain that above-mentioned variety of problems becomes " coal-Jiao-change " development.Process coal-tar heavy oil distillate by the mode of hydrogenation at present, low sulfur naphtha and the clean fuel oil of high added value can be obtained, improve the utility value of coal tar.As the Chinese invention " a kind of full fraction of coal tar hydrogenation produces the method for light-weight fuel oil " that patent publication No. is CN103571533A, the method adopts hydrofining-hydrocracking combined process, upflowing hydrofining reactor is entered after full fraction of coal tar mixes with hydrogen, gained refining reaction product enters high-pressure separator, obtain light, weigh two kinds of cuts, enter downstriker hydrocracking reactor after last running mixes with hydrogen, cracked reaction product enters subsequent product separation system after mixing with the lighting end of refining reaction product.The method, in processing coal-tar heavy oil process, because coal-tar heavy oil asphalt content is high, easily makes catalyzer coking in hydrofining reactor; And aromaticity content is high in coal-tar heavy oil, in the process of hydrotreated lube base oil aromatic hydrocarbons, heat release is too violent, makes hydrofining reactor difficult control of temperature, operational difficulty.Therefore need to design a kind of coal-tar heavy oil distillate hydrogenation device, the exothermic heat of reaction of energy mild hydrogenation reaction, extends the cycle of operation of hydrofining reactor and hydrocracking reactor.
Summary of the invention
Technical problem to be solved in the utility model is to provide the coal-tar heavy oil distillate hydrogenation device of the low aromatic hydrocarbon oil circulation of a kind of band rational in infrastructure, simple to operate, the exothermic heat of reaction of energy mild hydrogenation reaction, extends the cycle of operation of hydrofining reactor and hydrocracking reactor.
The utility model solves the problems of the technologies described above adopted technical scheme: this coal-tar heavy oil distillate hydrogenation device circulated with low aromatic hydrocarbon oil, it is characterized in that: this device comprises vacuum still, hydrofining reactor, separation system, thionizer, separation column and hydrocracking reactor, described vacuum still be provided with coal-tar heavy oil entrance, the bottom of vacuum still is provided with heavy fraction outlet, the top of vacuum still is provided with fraction outlets, the top of described hydrofining reactor is provided with reaction feed mouth, the fraction outlets of vacuum still is connected with reaction feed mouth with the hydrogen handling machinery import of inputting hydrogen, the bottom of hydrofining reactor is provided with discharge port and is connected with separation system, the top of separation system is provided with pneumatic outlet and is connected with hydrogen conveyor conduit, the bottom of separation system is provided with liquid-phase outlet and is connected with thionizer, the top of thionizer is provided with gaseous phase outlet and is connected with corresponding process, bottom is provided with the liquid-phase outlet be connected with separation column, in separation column, be provided with boiling point be less than 215 DEG C of distillate outlets, boiling point exports at 215 ~ 320 DEG C of distillates, boiling point is greater than 350 DEG C of distillate outlets at 320 ~ 350 DEG C of cut oil outlets and boiling point, wherein 320 ~ 350 DEG C of cut parts enter hydrocracking reactor as unconverted oil, another part enters hydrofining reactor after mixing with lighting end as low aromatic hydrocarbon oil, the top of hydrocracking reactor is provided with hydrogen feed mouth, the bottom of hydrocracking reactor is provided with hydrocracking reaction product exit, hydrocracking reaction product exit is connected with separation system, more than connect and be pipeline connection.
As improvement, described hydrofining reactor and hydrocracking reactor all may be selected to be down-flow reactor.
Improve again, be positioned at catalyst bed interlayer in the middle part of described hydrofining reactor and also can be provided with quenching hydrogen entrance.
Improve again, be positioned at catalyst bed interlayer in the middle part of described hydrocracking reactor and also can be provided with quenching hydrogen entrance.
As improvement, described separation system comprises high-pressure separator and light pressure separator; Cooperatively interact operation.
As improvement, described thionizer is connected with the liquid-phase outlet of separation system by the liquid phase entrance at middle part.
As improvement, described separation column is connected with the liquid-phase outlet of thionizer by the feeding mouth at middle part.
As improvement, described coal-tar heavy oil entrance can be arranged at the side medium position of vacuum still.
Compared with prior art, the utility model has the advantage of: adding technique that inert oil circulates for controlling the aromaticity content in hydrofining raw material compared with the coal-tar heavy oil distillate hydrogenation technology of routine, controlling the temperature rise of hydrofining reaction process catalyst bed in rational scope by controlling aromaticity content.The utility model is rational in infrastructure, simple to operate, and temperature of reaction is easy to control, can the exothermic heat of reaction of effective mild hydrogenation reaction, extends the cycle of operation of hydrofining reactor and hydrocracking reactor.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of coal-tar heavy oil distillate hydrogenation device of the present utility model.
Embodiment
Below in conjunction with accompanying drawing embodiment, the utility model is described in further detail.
As shown in Figure 1, the coal-tar heavy oil distillate hydrogenation device of the low aromatic hydrocarbon oil circulation of band of the present embodiment, comprise vacuum still 1, hydrofining reactor 2, separation system 3, thionizer 4, separation column 5 and hydrocracking reactor 6, the middle part of described vacuum still 1 is provided with coal-tar heavy oil entrance, the bottom of vacuum still 1 is provided with heavy fraction outlet, the top of vacuum still 1 is provided with fraction outlets, the top of described hydrofining reactor 2 is provided with reaction feed mouth, reaction feed mouth is connected with the fraction outlets of vacuum still 1, the bottom of hydrofining reactor 2 is provided with discharge port and is connected with separation system 3, the top of separation system 3 is provided with pneumatic outlet and is connected with hydrogen handling machinery 9, after hydrogen handling machinery 9 processes, hydrofining reactor 2 and hydrocracking reactor 6 is returned as recycle hydrogen, the bottom of separation system 3 is provided with liquid-phase outlet and is connected with thionizer 4, the top of thionizer 4 is provided with gaseous phase outlet, bottom is provided with the liquid-phase outlet be connected with separation column 5, separation column 5 is provided with three fraction outlets, respectively: be less than 160 DEG C of boiling point fraction outlets 51, 160 ~ 350 DEG C of boiling point fraction outlets, 52 and 320 ~ 350 DEG C of boiling point fraction outlets 53, wherein be greater than 350 DEG C of boiling point fraction export 53 separating oil a part enter hydrocracking reactor 6 as unconverted oil 8, another part enters hydrofining reactor 2 after mixing with lighting end 11 as low aromatic hydrocarbon oil 7, the top of hydrocracking reactor 6 is provided with opening for feed, the bottom of hydrocracking reactor 6 is provided with hydrocracking reaction product exit, hydrocracking reaction product exit is connected with separation system 8, more than connect and be pipeline connection, described hydrofining reactor 2 and hydrocracking reactor 6 are down-flow reactor, the middle part of described hydrofining reactor 2 and hydrocracking reactor 6 is positioned at catalyst bed interlayer and is provided with quenching hydrogen entrance, described separation system 3 comprises high-pressure separator and light pressure separator, and the middle part of described thionizer 4 is provided with the liquid phase entrance be connected with the liquid-phase outlet of separation system 3, the middle part of described separation column 5 is provided with the feeding mouth be connected with the liquid-phase outlet of thionizer 11.
Concrete processing process is: enter vacuum still 1 through dehydration and the coal-tar heavy oil 12 that removes mechanical impurity and carry out fractionation, obtain lighting end 11 and last running 13, the cut point of lighting end 11 and last running 13 is 350 ~ 400 DEG C, gained last running 13 is discharged from the bottom heavy fraction outlet of vacuum still 1, modifying asphalt can be used as, heavy fuel oil (HFO), or be used as coking raw material, lighting end 11 enters hydrofining reactor 2 after mixing with hydrogen 31 and low aromatic hydrocarbon oil 7, contact with Hydrobon catalyst with hydrogenation protecting catalyst successively, carry out hydrogenation reaction, wherein low aromatic hydrocarbon oil and lighting end and blending ratio are 0.5: 1 ~ 3: 1 (mass ratio), the operational condition of hydrofining reactor is: reaction pressure 10.0 ~ 20.0MPa, temperature of reaction 250 ~ 450 DEG C, hydrogen to oil volume ratio 800 ~ 1500: 1, volume space velocity 0.1 ~ 1.0h
-1, gained hydrofining effluent 21 is discharged from the bottom discharge mouth of hydrofining reactor 2 and is entered separation system 3, after separation system 3 is separated, gained vapor phase hydrogen 31 returns hydrofining reactor 2 and hydrocracking reactor 6 as recycle hydrogen, isolated liquid phase oil 32 removes after hydrogen sulfide and gas products 41 through thionizer 4, liquid phase oil 42 enters separation column 5 from the outlet at bottom of thionizer 4, obtain the separating oil being less than 160 DEG C of fraction outlets 51 respectively, separating oil and the separating oil be greater than in 350 DEG C of fraction outlets 53 of 160 DEG C ~ 350 DEG C of fraction outlets 52, wherein, be less than 160 DEG C of fraction outlets 51 separating oil and can do gasoline blending component or catalytic reforming raw material, 160 ~ 350 DEG C of fraction outlets 52 separating oil can do diesel oil blending component, a separating oil part for 320 ~ 350 DEG C of fraction outlets 53 enters hydrocracking reactor 6 as unconverted oil 8, another part enters hydrogen refining reaction device 2 after mixing with lighting end 11 as low aromatic hydrocarbon oil 7, under hydrogen 31 exists, unconverted oil 8 contacts with hydrocracking catalyst, carry out cracking reaction, the operational condition of hydrofining reactor is: reaction pressure 10.0 ~ 20.0MPa, temperature of reaction 250 ~ 450 DEG C, hydrogen to oil volume ratio 800 ~ 1500: 1, volume space velocity 0.1 ~ 1.0h
-1, hydrocracking reaction product 61 is discharged from the outlet at bottom of hydrocracking reactor 6 and is entered separation system 3, is incorporated to follow-up system.
Claims (8)
1. the coal-tar heavy oil distillate hydrogenation device of the low aromatic hydrocarbon oil circulation of band, it is characterized in that: this device comprises vacuum still (1), hydrofining reactor (2), separation system (3), thionizer (4), separation column (5) and hydrocracking reactor (6), described vacuum still (1) be provided with coal-tar heavy oil (12) entrance, the bottom of vacuum still (1) is provided with heavy fraction outlet, the top of vacuum still (1) is provided with fraction outlets, the top of described hydrofining reactor (2) is provided with reaction feed mouth, the fraction outlets of vacuum still (1) is connected with reaction feed mouth with hydrogen handling machinery (9) import of inputting hydrogen, the bottom of hydrofining reactor (2) is provided with discharge port and is connected with separation system (3), the top of separation system (3) is provided with pneumatic outlet and is connected with hydrogen handling machinery (9) pipeline, the bottom of separation system (3) is provided with liquid-phase outlet and is connected with thionizer (4), the top of thionizer (4) is provided with gaseous phase outlet and is connected with corresponding process, bottom is provided with the liquid-phase outlet be connected with separation column (5), in separation column (14), be provided with boiling point be less than 215 DEG C of distillates outlet (51), boiling point exports (52) at 215 ~ 320 DEG C of distillates, boiling point is greater than 350 DEG C of distillates outlet (54) 320 ~ 350 DEG C of cut oil outlets (53) and boiling point, wherein 320 ~ 350 DEG C of cut (53) parts enter hydrocracking reactor (6) as unconverted oil (8), another part enters hydrofining reactor (2) after mixing with lighting end (11) as low aromatic hydrocarbon oil (7), the top of hydrocracking reactor (6) is provided with hydrogen feed mouth, the bottom of hydrocracking reactor (6) is provided with hydrocracking reaction product exit, hydrocracking reaction product exit is connected with separation system (3), more than connect and be pipeline connection.
2. coal-tar heavy oil distillate hydrogenation device according to claim 1, is characterized in that: described hydrofining reactor (2) and hydrocracking reactor (6) are down-flow reactor.
3. coal-tar heavy oil distillate hydrogenation device according to claim 1, is characterized in that: described hydrofining reactor (2) middle part is positioned at catalyst bed interlayer and is provided with quenching hydrogen entrance.
4. coal-tar heavy oil distillate hydrogenation device according to claim 1, is characterized in that: described hydrocracking reactor (6) middle part is positioned at catalyst bed interlayer and is also provided with quenching hydrogen entrance.
5. coal-tar heavy oil distillate hydrogenation device according to claim 1, is characterized in that: described separation system (3) comprises high-pressure separator and light pressure separator.
6. coal-tar heavy oil distillate hydrogenation device according to claim 1, is characterized in that: described thionizer (4) is connected with the liquid-phase outlet of separation system (3) by the liquid phase entrance at middle part.
7. coal-tar heavy oil distillate hydrogenation device according to claim 1, is characterized in that: described separation column (5) is connected with the liquid-phase outlet of thionizer (4) by the feeding mouth at middle part.
8., according to described coal-tar heavy oil distillate hydrogenation device arbitrary in claim 1 to 7, it is characterized in that: described coal-tar heavy oil (12) entrance is arranged at the side medium position of vacuum still (1).
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| CN201420794599.6U CN204342741U (en) | 2014-12-12 | 2014-12-12 | With the coal-tar heavy oil distillate hydrogenation device of low aromatic hydrocarbon oil circulation |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107011942A (en) * | 2017-05-03 | 2017-08-04 | 武汉工程大学 | A kind of method for reducing extractant regeneration energy consumption in gasoline sweetening process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107011942A (en) * | 2017-05-03 | 2017-08-04 | 武汉工程大学 | A kind of method for reducing extractant regeneration energy consumption in gasoline sweetening process |
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Address after: 8 / F, building e, Hefeng creative Plaza, 435 Jiangdong North Road, Yinzhou District, Ningbo City, Zhejiang Province Patentee after: Ningbo Antai Environmental Chemical Engineering Design Co.,Ltd. Address before: 315040 8/F, Building E, Hefeng Creative Plaza, 435 Jiangbei Road, Ningbo City, Zhejiang Province Patentee before: NINGBO RESEARCH & DESIGN INSTITUTE OF CHEMICAL INDUSTRY CO.,LTD. |