CN101143802B - Technique for processing heavy benzene - Google Patents
Technique for processing heavy benzene Download PDFInfo
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- CN101143802B CN101143802B CN2007100471118A CN200710047111A CN101143802B CN 101143802 B CN101143802 B CN 101143802B CN 2007100471118 A CN2007100471118 A CN 2007100471118A CN 200710047111 A CN200710047111 A CN 200710047111A CN 101143802 B CN101143802 B CN 101143802B
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- Prior art keywords
- tower
- column
- interchanger
- storage tank
- cuts
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- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 20
- QPUYECUOLPXSFR-UHFFFAOYSA-N 1-methylnaphthalene Chemical compound C1=CC=C2C(C)=CC=CC2=C1 QPUYECUOLPXSFR-UHFFFAOYSA-N 0.000 claims abstract description 30
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000003921 oil Substances 0.000 claims abstract description 20
- 241000282326 Felis catus Species 0.000 claims description 14
- 150000002469 indenes Chemical class 0.000 claims description 13
- 239000000295 fuel oil Substances 0.000 claims description 7
- 238000004821 distillation Methods 0.000 claims description 5
- 239000000126 substance Substances 0.000 abstract description 6
- 239000010771 distillate fuel oil Substances 0.000 abstract description 5
- YBYIRNPNPLQARY-UHFFFAOYSA-N 1H-indene Chemical compound C1=CC=C2CC=CC2=C1 YBYIRNPNPLQARY-UHFFFAOYSA-N 0.000 abstract 4
- 239000002131 composite material Substances 0.000 abstract 1
- 239000000047 product Substances 0.000 description 30
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 9
- FYGHSUNMUKGBRK-UHFFFAOYSA-N 1,2,3-trimethylbenzene Chemical compound CC1=CC=CC(C)=C1C FYGHSUNMUKGBRK-UHFFFAOYSA-N 0.000 description 6
- IANQTJSKSUMEQM-UHFFFAOYSA-N 1-benzofuran Chemical compound C1=CC=C2OC=CC2=C1 IANQTJSKSUMEQM-UHFFFAOYSA-N 0.000 description 6
- QIMMUPPBPVKWKM-UHFFFAOYSA-N 2-methylnaphthalene Chemical compound C1=CC=CC2=CC(C)=CC=C21 QIMMUPPBPVKWKM-UHFFFAOYSA-N 0.000 description 6
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 description 6
- CWRYPZZKDGJXCA-UHFFFAOYSA-N acenaphthene Chemical compound C1=CC(CC2)=C3C2=CC=CC3=C1 CWRYPZZKDGJXCA-UHFFFAOYSA-N 0.000 description 6
- TXCDCPKCNAJMEE-UHFFFAOYSA-N dibenzofuran Chemical compound C1=CC=C2C3=CC=CC=C3OC2=C1 TXCDCPKCNAJMEE-UHFFFAOYSA-N 0.000 description 6
- ZUOUZKKEUPVFJK-UHFFFAOYSA-N diphenyl Chemical compound C1=CC=CC=C1C1=CC=CC=C1 ZUOUZKKEUPVFJK-UHFFFAOYSA-N 0.000 description 6
- 239000000284 extract Substances 0.000 description 6
- PQNFLJBBNBOBRQ-UHFFFAOYSA-N indane Chemical compound C1=CC=C2CCCC2=C1 PQNFLJBBNBOBRQ-UHFFFAOYSA-N 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 4
- HXGDTGSAIMULJN-UHFFFAOYSA-N acetnaphthylene Natural products C1=CC(C=C2)=C3C2=CC=CC3=C1 HXGDTGSAIMULJN-UHFFFAOYSA-N 0.000 description 3
- 235000010290 biphenyl Nutrition 0.000 description 3
- 239000004305 biphenyl Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 150000002220 fluorenes Chemical class 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- WTEOIRVLGSZEPR-UHFFFAOYSA-N boron trifluoride Chemical compound FB(F)F WTEOIRVLGSZEPR-UHFFFAOYSA-N 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000003317 industrial substance Substances 0.000 description 2
- KPAPHODVWOVUJL-UHFFFAOYSA-N 1-benzofuran;1h-indene Chemical compound C1=CC=C2CC=CC2=C1.C1=CC=C2OC=CC2=C1 KPAPHODVWOVUJL-UHFFFAOYSA-N 0.000 description 1
- 229910015900 BF3 Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a processing technique of heavy benzol. After undergoing heat exchange in a heat exchanger, the heavy benzol enters into a primary column, a light fuel oil fraction before the temperature of 181 DEG C is fractionated from the top of the column, a composite as an indene fraction at the temperature between 181 DEG C and 217 DEG C is fractionated from the lateral line of the column, after a fraction on the bottom of the column is heated, part of the fraction is returned to the primary column, the rest of the fraction enters into a rectifying column for being rectified, an industrial naphthalene fraction at the temperature between 217 DEG C and 218 DEG C is fractionated from the top of the rectifying column, a mixed methylnaphthalene fraction at the temperature between 240 DEG C and 245 DEG C is fractionated from the lateral line on the upper part of the column, and heavy wash oil is produced from the bottom of the column. Apart from the advantages of simple technique and convenient operation, the invention sufficiently utilizes many valuable chemical products in the heavy benzol and can not only abstract light fuel oil and indene fractions but also abstract inductrial naphthalene, mixed methylnaphthalene and heavy wash oil, thus better increasing the additional value of heavy benzol processing.
Description
Technical field
The present invention relates to organic chemical industry's production technical field, especially a kind of complete processing of heavy benzol.
Background technology
Heavy benzol is the by product that obtains in processing of acid wash coking benzene and the coking benzene hydrogenation process, it can only produce the complete processing of present heavy benzol oil fuel and adopt the boron trifluoride catalyst polymerization to produce coumarone-indene resin, also have a lot of value products not obtain to extract in the heavy benzol, the comprehensive utilization of resource is not high, causes the significant wastage of part resource.
Summary of the invention
A kind of heavy benzol complete processing of providing at the deficiencies in the prior art is provided, it not only can extract light-weight fuel oil, indenes cut from heavy benzol, but also can extract NAPTHALENE FLAKES. (INDUSTRIAL GRADE, mixed methylnaphthalene, heavy wash oil, for fine chemistry industry provides more industrial chemicals, thereby fully developed a lot of valuable chemical products in the heavy benzol, technology is simple, and is easy to operate, the quality of chemical products that extracts is stable, and energy consumption is low.
The object of the present invention is achieved like this: a kind of complete processing of heavy benzol may further comprise the steps:
A, fore-running
Heavy benzol after being heated to 180～220 ℃, interchanger is entered the primary tower distillation, cut before the cat head cut 181 ℃ returns cat head through interchanger heat exchange rear section, all the other advance the finished product storage tank as light-weight fuel oil, 181～217 ℃ of cuts that tower top side line cuts advance indenes cut storage tank as finished product after the interchanger heat exchange, overhead product at the bottom of the tower is heated at the bottom of 240～260 ℃ of rear sections return tower through process furnace, and all the other remove rectification working process.
B, rectifying
The bottomsstream that the fore-running operation is sent here advances rectifying tower rectifying, the 217-218 that cat head cuts ℃ cut returns cat head through interchanger heat exchange rear section, all the other advance the finished product storage tank as NAPTHALENE FLAKES. (INDUSTRIAL GRADE, the 240-245 ℃ of cut that tower top side line cuts advances the finished product storage tank as mixed methylnaphthalene after the interchanger heat exchange, the cut part that obtains at the bottom of the tower is returned tower after process furnace is heated to 280～350 ℃ at the bottom of, all the other advance the finished product storage tank as heavy wash oil.
Technology of the present invention is simple, easy to operate, it has obtained abundant development and utilization with a lot of valuable chemical products in the heavy benzol, not only can extract light-weight fuel oil, indenes cut, but also can extract NAPTHALENE FLAKES. (INDUSTRIAL GRADE, mixed methylnaphthalene, heavy wash oil, for fine chemistry industry provides more industrial chemicals, the quality of chemical products that extracts is stable, naphthalene concentration degree height, and energy consumption is low, thus promoted the added value of the present heavy benzol processing of China better.
Description of drawings
Fig. 1 is a process flow diagram of the present invention, wherein: 1-primary tower, 2-rectifying tower, 3,4,5,6, the 7-interchanger, 8, the 9-process furnace, 10-indenes cut storage tank, 11-oil fuel storage tank, 12, the 15-medial launder, 13,14-finished product storage tank.
Embodiment
Embodiment 1
Consult Fig. 1, the present invention is undertaken by following processing step:
A, fore-running
Heavy benzol after being heated to 190 ℃, interchanger 3 is entered primary tower 1 distillation, cut before the cat head cut 181 ℃ is through the laggard medial launder 12 of interchanger 4 heat exchange, cut part in the medial launder 12 is returned primary tower 1 and is used for trim the top of column liquid, all the other then advance light Fuel oil supply tank 11 for processed oil, 185 ℃ of cuts that tower top side line cuts advance indenes cut storage tank 10 as finished product after interchanger 7 heat exchange, overhead product at the bottom of the tower is heated at the bottom of 255 ℃ of rear sections return tower through process furnace 8, and all the other remove rectification working process.
B, rectifying
The bottomsstream that the fore-running operation is sent here enters rectifying tower 2 rectifying, 217 ℃ of cuts that cat head cuts are through the laggard medial launder 15 of interchanger 5 heat exchange, cut part in the medial launder 15 is returned rectifying tower 2 and is used for trim the top of column liquid, all the other then advance finished product storage tank 14 for NAPTHALENE FLAKES. (INDUSTRIAL GRADE, 240 ℃ of cuts that tower top side line cuts advance finished product storage tank 13 as mixed methylnaphthalene after interchanger 6 heat exchange, the heavy wash oil part that obtains at the bottom of the tower is returned tower after process furnace 9 is heated to 350 ℃ at the bottom of, all the other advance storage tank 12 as processed oil.
The raw material composition:
Benzene: 0.384%
Toluene: 0.325%
Ethylbenzene: 0.142%
Trimethylbenzene: 1.876%
Coumarone: 0.446%
Indane: 1.953%
Indenes: 6.259%
Naphthalene: 46.016%
Quinoline: 0.824%
2-methylnaphthalene: 8.721%
1-methylnaphthalene: 3.735%
Biphenyl: 3.799%
Acenaphthene: 5.577%
Dibenzofuran: 2.984%
Fluorenes: 1.283%
Product is formed: (weight ratio)
| Light-weight fuel oil | The indenes cut | NAPTHALENE FLAKES. (INDUSTRIAL GRADE (95%) | Mixed methylnaphthalene (65%) | Heavy wash oil | |
| Product is formed % | 7.65 | 6.22 | 43.49 | 14.60 | 27.24 |
Embodiment 2
A, fore-running
Heavy benzol after being heated to 200 ℃, interchanger 3 is entered primary tower 1 distillation, cut before the cat head cut 181 ℃ is through the laggard medial launder 12 of interchanger 4 heat exchange, medial launder 12 interior cut parts are returned primary tower 1 and are used for trim the top of column liquid, all the other then advance light Fuel oil supply tank 11 for processed oil, 200 ℃ of cuts that tower top side line cuts advance indenes cut storage tank 10 as finished product after interchanger 7 heat exchange, overhead product at the bottom of the tower is heated at the bottom of 260 ℃ of rear sections return tower through process furnace 8, and all the other remove rectification working process.
B, rectifying
The bottomsstream that the fore-running operation is sent here enters rectifying tower 2 rectifying, 218 ℃ of cuts that cat head cuts are through the laggard medial launder 15 of interchanger 5 heat exchange, cut part in the medial launder 15 is returned rectifying tower 2 and is used for trim the top of column liquid, all the other then advance finished product storage tank 14 for NAPTHALENE FLAKES. (INDUSTRIAL GRADE, 245 ℃ of cuts that tower top side line cuts advance finished product storage tank 13 as mixed methylnaphthalene after interchanger 6 heat exchange, the heavy wash oil part that obtains at the bottom of the tower is returned tower after process furnace 9 is heated to 300 ℃ at the bottom of, all the other advance storage tank 12 as processed oil.
The raw material composition:
Benzene: 2.237%
Toluene: 3.601%
Ethylbenzene: 2.198%
Trimethylbenzene: 1.481%
Coumarone: 1.036%
Indane: 0.122%
Indenes: 13.538%
Naphthalene: 38.496%
Quinoline: 1.467%
2-methylnaphthalene: 12.046%
1-methylnaphthalene: 4.748%
Biphenyl: 1.639%
Acenaphthene: 3.490%
Dibenzofuran: 0.847%
Fluorenes: 0.280%
Product is formed: (weight ratio)
| Light-weight fuel oil | The indenes cut | NAPTHALENE FLAKES. (INDUSTRIAL GRADE (95%) | Mixed methylnaphthalene (65%) | Heavy wash oil | |
| Product is formed % | 14.25 | 14.02 | 36.27 | 24.50 | 10.06 |
Embodiment 3
A, fore-running
Heavy benzol after being heated to 210 ℃, interchanger 3 is entered primary tower 1 distillation, cut before the cat head cut 181 ℃ is through the laggard medial launder 12 of interchanger 4 heat exchange, cut part in the medial launder 12 is returned primary tower 1 and is used for trim the top of column liquid, all the other then advance light Fuel oil supply tank 11 for processed oil, 210 ℃ of cuts that tower top side line cuts advance indenes cut storage tank 10 as finished product after interchanger 7 heat exchange, overhead product at the bottom of the tower is heated at the bottom of 250 ℃ of rear sections return tower through process furnace 8, and all the other remove rectification working process.
B, rectifying
The bottomsstream that the fore-running operation is sent here enters rectifying tower 2 rectifying, 217 ℃ of cuts that cat head cuts are through the laggard medial launder 15 of interchanger 5 heat exchange, cut part in the medial launder 15 is returned rectifying tower 2 and is used for trim the top of column liquid, all the other then advance finished product storage tank 14 for NAPTHALENE FLAKES. (INDUSTRIAL GRADE, 240 ℃ of cuts that tower top side line cuts advance finished product storage tank 13 as mixed methylnaphthalene after interchanger 6 heat exchange, the heavy wash oil part that obtains at the bottom of the tower is returned tower after process furnace 9 is heated to 320 ℃ at the bottom of, all the other advance storage tank 12 as processed oil.
The raw material composition:
Toluene: 0.188%
Trimethylbenzene: 0.873%
Coumarone: 0.265%
Indane: 0.171%
Indenes: 5.333%
Naphthalene: 55.503%
Quinoline: 1.460%
2-methylnaphthalene: 13.599%
1-methylnaphthalene: 5.925%
Biphenyl: 2.686%
Acenaphthene: 3.785%
Dibenzofuran: 1.236%
Fluorenes: 0.205%
Product is formed: (weight ratio)
| Light-weight fuel oil | The indenes cut | NAPTHALENE FLAKES. (INDUSTRIAL GRADE (95%) | Mixed methylnaphthalene (65%) | Heavy wash oil | |
| Product is formed % | 2.44 | 6.11 | 52.50 | 28.20 | 10.05 |
Claims (1)
1. the complete processing of a heavy benzol is characterized in that may further comprise the steps:
A, fore-running
Heavy benzol after being heated to 180～220 ℃, interchanger (3) is entered primary tower (1) distillation, the cut that cat head cuts before 181 ℃ returns cat head through interchanger (4) heat exchange rear section, all the other advance finished product storage tank (11) as light-weight fuel oil, 181～217 ℃ of cuts that tower top side line cuts advance indenes cut storage tank (10) as finished product after interchanger (7) heat exchange, overhead product at the bottom of the tower is heated at the bottom of 240-260 ℃ of rear section return tower through process furnace (8), and all the other remove rectification working process;
B, rectifying
The bottomsstream that the fore-running operation is sent here advances rectifying tower (2) rectifying, 217～218 ℃ of cuts that cat head cuts return cat head through interchanger (5) heat exchange rear section, all the other advance finished product storage tank (14) as NAPTHALENE FLAKES. (INDUSTRIAL GRADE, the 240-245 ℃ of cut that tower top side line cuts advances finished product storage tank (13) as mixed methylnaphthalene after interchanger (6) heat exchange, the cut part that obtains at the bottom of the tower is returned tower after process furnace (9) is heated to 280～350 ℃ at the bottom of, all the other advance finished product storage tank (12) as heavy wash oil.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007100471118A CN101143802B (en) | 2007-10-17 | 2007-10-17 | Technique for processing heavy benzene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007100471118A CN101143802B (en) | 2007-10-17 | 2007-10-17 | Technique for processing heavy benzene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101143802A CN101143802A (en) | 2008-03-19 |
| CN101143802B true CN101143802B (en) | 2010-07-21 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2007100471118A Expired - Fee Related CN101143802B (en) | 2007-10-17 | 2007-10-17 | Technique for processing heavy benzene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101143802B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101475435B (en) * | 2009-02-02 | 2012-06-13 | 济宁碳素工业总公司 | Method for preparing industrial naphthalin by single-furnace double-tower vacuum distillation |
| CN101712888B (en) * | 2009-11-26 | 2012-09-12 | 湖南长岭石化科技开发有限公司 | Hydrofining technology of heavy benzol |
| CN102617264B (en) * | 2012-03-14 | 2015-07-15 | 江苏华达化工集团有限公司 | Method for separating indene, naphthalene and methylnaphthalene from heavy benzol through low temperature side stream fractionation |
| CN103611328B (en) * | 2013-12-03 | 2015-03-25 | 天津市创举科技有限公司 | Process for extracting naphthalene by continuously rectifying heavy benzol |
| CN110527540B (en) * | 2019-09-30 | 2024-02-02 | 河南博海化工有限公司 | Washing oil distillation device |
| CN113559541A (en) * | 2021-08-09 | 2021-10-29 | 中冶焦耐(大连)工程技术有限公司 | Process and system for recovering light components in heavy benzene by using waste heat of medium-temperature asphalt |
-
2007
- 2007-10-17 CN CN2007100471118A patent/CN101143802B/en not_active Expired - Fee Related
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| Publication number | Publication date |
|---|---|
| CN101143802A (en) | 2008-03-19 |
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Assignee: Jiangsu Huada Chemical Group Co., Ltd. Assignor: Yang Dongping Contract record no.: 2012320000250 Denomination of invention: Technique for processing heavy benzene Granted publication date: 20100721 License type: Exclusive License Open date: 20080319 Record date: 20120316 |
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