CN205152158U - Coal tar suspension bed hydrocracking unit - Google Patents
Coal tar suspension bed hydrocracking unit Download PDFInfo
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- CN205152158U CN205152158U CN201520909746.4U CN201520909746U CN205152158U CN 205152158 U CN205152158 U CN 205152158U CN 201520909746 U CN201520909746 U CN 201520909746U CN 205152158 U CN205152158 U CN 205152158U
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Abstract
The utility model discloses a coal tar suspension bed hydrocracking unit, by suspension bed reactor, the thermal high separator, the temperature high -pressure separator, the cold anticyclone separator, the heat low separator, the cold low separator, the circulating oil pump, the recycle hydrogen compressor becomes with the atmospheric and vacuum distillation tower system, suspension bed reactor and thermal high separator intercommunication, the thermal high separator communicates with temperature high -pressure separator and heat low separator respectively, the thermal high separator still communicates with the ring oil pump, the temperature high -pressure separator communicates with cold anticyclone separator and heat low separator respectively, the heat low separator communicates with cold low separator and atmospheric and vacuum distillation tower respectively, the cold anticyclone separator communicates with cold low separator and recycle hydrogen compressor respectively, it is low that the device has reactor material back mixing degree, raw materials adaptability is wide, flexible in operation.
Description
Technical field
The present invention relates to a kind of coal tar suspension bed hydrocracked, treated technique of the full cut of high conversion of coal chemical technology, particularly relate to a kind of with high, medium and low temperature full fraction of coal tar, especially coal-tar heavy oil is the coal tar suspension bed method for hydrogen cracking of full cut and the device of raw material production petroleum naphtha and diesel oil distillate.
Background technology
Coal tar is coal at the liquid product of destructive distillation and gasification byproduct in process, and the difference according to pyrolysis temperature and method can obtain following several tar: 450 ~ 650 DEG C of low-temperature pyrolysis tar, 600 ~ 800 DEG C of low temperature and middle temperature producer gas tars, warm vertical heater tar and 1000 DEG C of high-temperature coking tar in 900 ~ 1000 DEG C.Coal tar chemical industry occupies critical role in chemical industry, current domestic annual production about 1,700 ten thousand tons, how effectively to utilize tar resource to become coking industry problem in the urgent need to address, and to adopt suitable hydrocracking technology heavy coal tar to be converted into light liquid fuel be the important means utilizing tar resource.
Coal tar is the chocolate thick liquid with irritating smell, and primarily of aromatics composition, and be the fused aromatic compounds of more than two rings mostly, alkane, alkene and cyclanes compound are little.The content of distillation residue pitch is very high, generally more than 50%.Compared with oil last running, coal-tar heavy oil has that content of heteroatoms is high, ash content is high, polycyclic aromatic hydrocarbon content is high, gum asphaltic content high, ubiquity beds coking when this makes to adopt conventional fixed bed reaction technical process process coal tar raw material, the problem that catalyzer work-ing life is short, device shutdown times is many, have a strong impact on the economic benefit that coal tar is produced.
A kind of coal tar heavy fractioning suspension bed hydrocracking method and system is refer in CN101962571A, enter floating bed hydrogenation reactor after being mixed with catalyzer and promotor by coal tar heavy fractioning to carry out hydrocracking reaction, reaction product is sent into high-pressure separator and is carried out gas-liquid separation, be separated the liquid-phase product feeding separation column obtained and carry out product separation, be greater than the tail oil component loops Returning reactor of 350 DEG C, part carrying device.This patent of invention can realize product liquid yield 72.6, improves the utilising efficiency of raw material and catalyzer.
But in that patent, catalyzer needs to arrange separately vulcanizing apparatus and carries out sulfuration, adds the cavitation risk of facility investment and high-pressure pump.Oil at the bottom of high-pressure separator tower directly enters separation column will be caused dissolving a large amount of hydrogen increasing separation column load and separating difficulty in oil, and there is string pressure risk greatly.Containing the wax oil cut of a large amount of 350-500 DEG C in Fractionator Bottom oil, this part wax oil will reduce device product yield as catalyst residue carrying device.
A kind of catalytic hydrogenation method and device is refer in CN102977916A.Comprise after coal tar raw material is carried out air distillation and obtain carbolic oil cut, diesel oil distillate, heavy oil fraction, floating bed hydrocracking is carried out to heavy oil fraction, separation is carried out to the crackate obtained and obtains each cut product.This patent of invention carries out the separation removal of catalyzer before carrying out fractionation by distillation to crackate, make to carry less heavy oil in the outer solid catalyst got rid of, and improves raw material availability.
But in that patent, solid-liquid separator is used to carry out filtering separation or centrifugation to reaction product, be difficult to realize for the catalyzer of small particle size size and being effectively continuously separated of high temperature heavy oil product in actual production, thus the granules of catalyst of most of inactivation may be caused at device internal recycle, and cause equipment, valve wear to be accelerated, and easily the coking of aggravation high temperature oil product is inclined to.Meanwhile, when device inlet amount changes, in reactor, flow velocity reduces, and the back-mixing of storeroom very easily occurs, affects reaction conversion ratio.
Summary of the invention
The invention provides a kind of coal tar suspension bed method for hydrogen cracking, overcome prior art defect, improve the feature such as transformation efficiency, operational cycle length.
A kind of coal tar suspension bed method for hydrogen cracking:
1) coal tar is mixed into uniform raw material slurry oil through pre-treatment and catalyzer, promotor, mix with hydrogen after pump boosting, heat up through process furnace and enter suspended-bed reactor, it is 380 ~ 500 DEG C in temperature of reaction, working pressure is that 10 ~ 25MPa carries out hydrocracking reaction, and reaction product enters step 2);
2) from step 1) high pressure hot separator that enters of reaction product, the hot high score oil of the part separated is mixed into suspended-bed reactor with raw material slurry oil, the hot high score oil of another part enters thermal low-pressure separators and is separated further, heat low point of gas that thermal low-pressure separators is separated enters step 4), heat low point of gas and oil that thermal low-pressure separators is separated enters step 5), the hot high score gas that high pressure hot separator is separated enters step 3);
3) from step 2) hot high score gas enters warm high-pressure separator, the part temperature high score oil separated enters thermal low-pressure separators, the warm high score gas separated enters cold high pressure separator, the cold high score gas that cold high pressure separator is separated is as recycle hydrogen, and the cold high score oil that cold high pressure separator is separated enters step 4);
4) from step 3) cold high score oil is separated with the cold low separator that enters together that thermal low-pressure separators is separated, the isolated cold low point of further recover hydrogen of gas, isolated cold low point of oil enters step 5);
5) from step 2) heat low point of gas and oil enter Atmospheric vacuum tripping device together with cold low point of oil, isolate various product and catalyzer, atmospheric tower bottoms divides whole heavy oil of heavy oil and VACUUM TOWER BOTTOM to return suspended-bed reactor entrance, and catalyzer reclaims.
Described suspended-bed reactor is at least one, and two or more are for being connected in series.
The described hot high score oil being recycled to suspended-bed reactor is 20% ~ 200% with the weight percent of coal tar raw material.
Hydrogen in described suspended-bed reactor divides and is pressed in 8 ~ 24MPaG.
Described coal tar is one or more at least high, medium and low temperature full fraction of coal tar.
Described promotor is the wherein one of molten sulfur, dithiocarbonic anhydride, dimethyl disulphide.Heavy oil circulation at the bottom of described atmospheric tower is 30% ~ 100% with the weight percent of coal tar raw material.
Described catalyzer is transition metal organic chelate, and wherein metal content is 1 ~ 40 % by weight, and be preferably 5 ~ 20 % by weight, transition metal is the metallic elements such as Fe, Co, Ni, V, MnCr>Mo, W.A kind of coal tar suspension bed hydroeracking unit, by suspended-bed reactor, high pressure hot separator, temperature high-pressure separator, cold high pressure separator, thermal low-pressure separators, cold low separator, circulating oil pump, circulating hydrogen compressor and ordinary decompression column composition, it is characterized in that: suspended-bed reactor is communicated with high pressure hot separator, high pressure hot separator is communicated with thermal low-pressure separators with warm high-pressure separator respectively, high pressure hot separator is also communicated with ring oil pump, temperature high-pressure separator is communicated with thermal low-pressure separators with cold high pressure separator respectively, thermal low-pressure separators is communicated with ordinary decompression column with cold low separator respectively, cold high pressure separator is communicated with circulating hydrogen compressor with cold low separator respectively.
The coal tar suspension bed hydroeracking unit of described one, is characterized in that: be provided with distributing disc or tubulose sparger bottom suspended-bed reactor.
The coal tar suspension bed hydroeracking unit of described one, is characterized in that: suspended-bed reactor is at least a reactor, during two or more suspended-bed reactors, is connected in series.
The coal tar suspension bed hydroeracking unit of described one, is characterized in that: suspended-bed reactor is also communicated with furnace outlet.
The coal tar suspension bed hydroeracking unit of described one, is characterized in that: be communicated with process furnace entrance bottom ordinary decompression column.
The advantage of present invention process method mainly includes:
1) suspended-bed reactor structure is simple, there is not reactor bed blocking and causes pressure drop excessive thus the risk causing device to be stopped work, ensure that the long-term operation of device;
2) be provided with hot high score oil circulating system, effectively control the axial flow velocity in suspended-bed reactor, ensure that in suspended-bed reactor to be plug flow reaction, effectively reduce the material back-mixing in reactor, improve one-pass reaction conversion ratio;
3) have employed the reaction effluent separation process of hot high score+low point of warm high score+heat, the temperature requirement that atmospheric tower charging process furnace still can ensure atmospheric tower charging is not set, the coking of device interior can be avoided, the long-term operation of assurance device simultaneously;
4) the direct Hybrid Heating of hot high score gas preheating reaction feed, cycling hot high score oil and the charging of reaction feed furnace outlet is utilized, eliminate the heat exchange of easy coking reaction product containing solid catalyst particle and stock oil, avoid the coking in high pressure heat exchanger and blocking risk, simultaneously due to existence that hot high score is oil circulation, reaction feed furnace outlet temperature can suitably reduce, and decreases the risk that coking occurs heavy feed stock in boiler tube;
5) high-low pressure separator efficient recovery hydrogen is set, ensure that catalyzer can not enter compressor assembly with liquid-phase product outflow and affect its steady running by the high efficiency separation parts in separator;
6) oil product is separated and adopts Atmospheric vacuum double-column process, while obtaining product cut, the cut of >350 DEG C is cut, wherein 350 DEG C-500 DEG C all or part of circulations of wax oil cut return suspended-bed reactor, and >500 DEG C of residue oil fraction component loops returns suspended-bed reactor.This Matter Transfer technique can improve raw material availability further, increases product yield, reduces reaction severity simultaneously, is adapted to the production of different coal tar raw material, enhance the handiness of device operation by adjustment residual oil internal circulating load.
7) solid catalyst particle except part with turning oil except system internal recycle, all the other reclaim with outside VACUUM TOWER BOTTOM residual oil carrying device, avoid occurring that in operate continuously process, the not good catalyzer that causes of solid-liquid separation is constantly accumulated in system.
Accompanying drawing explanation
Fig. 1 is a kind of coal tar suspension bed hydroeracking unit schematic diagram.
Wherein:
1. feed material preparation units, 2 material slurry oil arrangement units, 3. fresh feed pump, 4. reaction feed process furnace, 5 suspended-bed reactors, 6. high pressure hot separator, 7. warm high-pressure separator, 8. cold high pressure separator, 9. thermal low-pressure separators, 10. cold low separator, 11. circulating oil pumps, 12. circulating hydrogen compressors, 13. atmospheric towers, 14. vacuum distillation towers, 15. coal tar, 16. catalyzer, 17. promotors, 18. raw material slurry oils, 19. parallel feedings, 20. reaction feed, 21. reaction product, 22. cycling hot high score oil, 23. acyclic hot high score oil, 24. hot high score gas, 25. warm high score gas, 26. warm high score oil, 27. cold high score gas, 28. recycle hydrogens, 29. new hydrogen, 30. cold high score oil, 31. heat low point of gas, 32. cold low point of gas, 33. cold low point of oil, 34. heat low point of oil, 35. lighter hydrocarbons, 36 naphtha fractions, 37. ordinary pressure diesel cuts, circulation heavy oil at the bottom of 38. atmospheric towers, 39. vacuum distillation tower chargings, 40. vacuum gas cuts, 41. decompressed wax oils, 42. catalyst residues and vacuum residuum
Embodiment
With specifically embodiment, the present invention is described below, but does not limit the scope of the invention.
Embodiment 1
Coal tar raw material 15 carries out desalination at feed material preparation units 1, dehydration, with circulation heavy oil 38 at the bottom of atmospheric tower after de-mechanical impurity, decompressed wax oil 41, catalyzer 16, promotor 17 is mixed into raw material slurry oil in raw material slurry oil arrangement unit 2, raw material slurry oil and mixed hydrogen merge into parallel feeding and the heat exchange of hot high score gas, enter reaction feed process furnace 4 to heat up, reach after outlet of still and cycling hot high score oil 22 mixes and react the temperature required suspended-bed reactor 5 that enters and carry out hydrocracking reaction, a suspended-bed reactor is set, temperature of reaction is 380 DEG C, working pressure is 10MPa, first the reaction product 21 of suspended-bed reactor 5 enters in high pressure hot separator 6 carries out gas, solid-liquor separation, enter warm high-pressure separator 7 after the heat exchange of hot high score gas 24 to be separated further, solid catalyst flows out bottom high pressure hot separator with hot high score oil, part high score oil 22 is by circulating oil pump 11 boost cycle Returning reactor entrance, the weight percent of internal circulating load and coal tar raw material is 20%, other hot high score oil oil 23 enter thermal low-pressure separators 9 together with warm high score oil 26, the temperature of thermal low-pressure separators is controlled by the heat exchange final temperature of warm high score oil, ensure the vaporization rate excessively entering atmospheric tower oil product, cold high pressure separator 8 is entered after temperature high score gas 25 is cooled to 50 DEG C, be separated the cold high score gas 27 obtained to boost through circulating hydrogen compressor 12, as recycle hydrogen 28 Returning reactor together with the fresh hydrogen 29 of supplementing, the hydrogen maintained in reactor divides and is pressed in 8MPaG, cold low separator 10 is entered together with cold high score oil 30 and heat low point of gas 31, the hydrogen dissolved in further recovery high score oil product, enter atmospheric tower together with cold low point of oil 33 and heat low point of oil to carry out cut and cut into naphtha fraction 36 from overhead extraction, cutting final boiling point is decided to be 170 DEG C, ordinary pressure diesel cut 37 is from side take-off, cutting final boiling point is decided to be 350 DEG C, be atmospheric residue and all solids catalyzer of >350 DEG C at the bottom of tower, circulation heavy oil 38 at the bottom of part atmospheric tower loops back raw material slurry oil arrangement unit, internal circulating load is to the weight percent 30% of coal tar raw material, all the other enter vacuum still as vacuum distillation tower charging 39 and carry out deep drawing, the vacuum gas cut 40 be dissolved in heavy oil is obtained at first side line, final boiling point is 350 DEG C, as product together with the diesel oil distillate of atmospheric tower extraction, the decompressed wax oil 41 of 350 DEG C ~ 500 DEG C is obtained at second side line, loop back suspended-bed reactor entrance in whole or in part, be catalyst residue and the vacuum residuum 42 of >500 DEG C at the bottom of tower, this part oil product can carry out settlement separate or residue is shaping, but do not loop back reactor.
Embodiment 2
With the raw material that the full cut coal-tar heavy oil of table 1 is floating bed hydrocracking, reaction conditions is 455 DEG C, 19MPaG, and hydrogen-oil ratio is 1350, and air speed is 0.5h
-1, the oil circulation amount weight percent of high score is 50%, and atmospheric residue internal circulating load weight percent is 60%, and decompressed wax oil all circulates, and vacuum residuum and catalyst residue do not participate in circulating.The products distribution obtained and yield are in table 2.
The full cut coal-tar heavy oil character of table 1
Certain full cut coal-tar heavy oil character of table 2
Embodiment 3
Coal tar raw material 15 carries out desalination at feed material preparation units 1, dehydration, with circulation heavy oil 38 at the bottom of atmospheric tower after de-mechanical impurity, decompressed wax oil 41, catalyzer 16, promotor 17 is mixed into raw material slurry oil in raw material slurry oil arrangement unit 2, raw material slurry oil and mixed hydrogen merge into parallel feeding and the heat exchange of hot high score gas, enter reaction feed process furnace 4 to heat up, reach after outlet of still and cycling hot high score oil 22 mixes and react the temperature required suspended-bed reactor 5 that enters and carry out hydrocracking reaction, a suspended-bed reactor is set, temperature of reaction is 500 DEG C, working pressure is 25MPa, first the reaction product 21 of suspended-bed reactor 5 enters in high pressure hot separator 6 carries out gas, solid-liquor separation, enter warm high-pressure separator 7 after the heat exchange of hot high score gas 24 to be separated further, solid catalyst flows out bottom high pressure hot separator with hot high score oil, part high score oil 22 is by circulating oil pump 11 boost cycle Returning reactor entrance, the weight percent of internal circulating load and coal tar raw material is 40%, other hot high score oil oil 23 enter thermal low-pressure separators 9 together with warm high score oil 26, the temperature of thermal low-pressure separators is controlled by the heat exchange final temperature of warm high score oil, ensure the vaporization rate excessively entering atmospheric tower oil product, cold high pressure separator 8 is entered after temperature high score gas 25 is cooled to 50 DEG C, be separated the cold high score gas 27 obtained to boost through circulating hydrogen compressor 12, as recycle hydrogen 28 Returning reactor together with the fresh hydrogen 29 of supplementing, the hydrogen maintained in reactor divides and is pressed in 20MPaG, cold low separator 10 is entered together with cold high score oil 30 and heat low point of gas 31, the hydrogen dissolved in further recovery high score oil product, enter atmospheric tower together with cold low point of oil 33 and heat low point of oil to carry out cut and cut into naphtha fraction 36 from overhead extraction, cutting final boiling point is decided to be 170 DEG C, ordinary pressure diesel cut 37 is from side take-off, cutting final boiling point is decided to be 350 DEG C, be atmospheric residue and all solids catalyzer of >350 DEG C at the bottom of tower, circulation heavy oil 38 at the bottom of part atmospheric tower loops back raw material slurry oil arrangement unit, internal circulating load is to the weight percent 30% of coal tar raw material, all the other enter vacuum still as vacuum distillation tower charging 39 and carry out deep drawing, the vacuum gas cut 40 be dissolved in heavy oil is obtained at first side line, final boiling point is 350 DEG C, as product together with the diesel oil distillate of atmospheric tower extraction, the decompressed wax oil 41 of 350 DEG C ~ 500 DEG C is obtained at second side line, loop back suspended-bed reactor entrance in whole or in part, be catalyst residue and the vacuum residuum 42 of >500 DEG C at the bottom of tower, this part oil product can carry out settlement separate or residue is shaping, but do not loop back reactor.
Embodiment 4
A kind of coal tar suspension bed hydroeracking unit, by suspended-bed reactor, high pressure hot separator, temperature high-pressure separator, cold high pressure separator, thermal low-pressure separators, cold low separator, circulating oil pump, circulating hydrogen compressor and ordinary decompression column composition, suspended-bed reactor is communicated with high pressure hot separator, high pressure hot separator is communicated with thermal low-pressure separators with warm high-pressure separator respectively, high pressure hot separator is also communicated with ring oil pump, temperature high-pressure separator is communicated with thermal low-pressure separators with cold high pressure separator respectively, thermal low-pressure separators is communicated with ordinary decompression column with cold low separator respectively, cold high pressure separator is communicated with circulating hydrogen compressor with cold low separator respectively, distributing disc or tubulose sparger is provided with bottom suspended-bed reactor, a reactor, floating bed reactor is also communicated with furnace outlet, be communicated with process furnace entrance bottom ordinary decompression column.
Embodiment 5
A kind of coal tar suspension bed hydroeracking unit, by suspended-bed reactor, high pressure hot separator, temperature high-pressure separator, cold high pressure separator, thermal low-pressure separators, cold low separator, circulating oil pump, circulating hydrogen compressor and ordinary decompression column composition, suspended-bed reactor is communicated with high pressure hot separator, high pressure hot separator is communicated with thermal low-pressure separators with warm high-pressure separator respectively, high pressure hot separator is also communicated with ring oil pump, temperature high-pressure separator is communicated with thermal low-pressure separators with cold high pressure separator respectively, thermal low-pressure separators is communicated with ordinary decompression column with cold low separator respectively, cold high pressure separator is communicated with circulating hydrogen compressor with cold low separator respectively, distributing disc or tubulose sparger is provided with bottom suspended-bed reactor, two floating bed reactors in series connect, floating bed reactor is also communicated with furnace outlet, be communicated with process furnace entrance bottom ordinary decompression column.
Claims (5)
1. a coal tar suspension bed hydroeracking unit, by suspended-bed reactor, high pressure hot separator, temperature high-pressure separator, cold high pressure separator, thermal low-pressure separators, cold low separator, circulating oil pump, circulating hydrogen compressor and ordinary decompression column composition, it is characterized in that: suspended-bed reactor is communicated with high pressure hot separator, high pressure hot separator is communicated with thermal low-pressure separators with warm high-pressure separator respectively, high pressure hot separator is also communicated with ring oil pump, temperature high-pressure separator is communicated with thermal low-pressure separators with cold high pressure separator respectively, thermal low-pressure separators is communicated with ordinary decompression column with cold low separator respectively, cold high pressure separator is communicated with circulating hydrogen compressor with cold low separator respectively.
2. according to the coal tar suspension bed hydroeracking unit of one according to claim 1, be characterised in that: bottom suspended-bed reactor, be provided with distributing disc or tubulose sparger.
3. according to the coal tar suspension bed hydroeracking unit of one according to claim 1, it is characterized in that: suspended-bed reactor is at least a reactor, during two or more suspended-bed reactors, is connected in series.
4., according to the coal tar suspension bed hydroeracking unit of one according to claim 1, it is characterized in that: suspended-bed reactor is also communicated with furnace outlet.
5. according to the coal tar suspension bed hydroeracking unit of one according to claim 1, it is characterized in that: atmospheric tower bottom is communicated with process furnace entrance.
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| CN201520909746.4U CN205152158U (en) | 2015-11-13 | 2015-11-13 | Coal tar suspension bed hydrocracking unit |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107281980A (en) * | 2017-08-11 | 2017-10-24 | 中国化学工程第六建设有限公司 | Suspension bed oil hydrogenation device and its application |
| CN111925821A (en) * | 2020-07-21 | 2020-11-13 | 武汉金中石化工程有限公司 | Separation method of high-solid-content heavy sump oil |
| CN116218560A (en) * | 2023-01-10 | 2023-06-06 | 孙少哲 | Coal hydrogenation upgrading method |
-
2015
- 2015-11-13 CN CN201520909746.4U patent/CN205152158U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107281980A (en) * | 2017-08-11 | 2017-10-24 | 中国化学工程第六建设有限公司 | Suspension bed oil hydrogenation device and its application |
| CN111925821A (en) * | 2020-07-21 | 2020-11-13 | 武汉金中石化工程有限公司 | Separation method of high-solid-content heavy sump oil |
| CN111925821B (en) * | 2020-07-21 | 2022-08-12 | 武汉金中石化工程有限公司 | Separation method of high-solid-content heavy sump oil |
| CN116218560A (en) * | 2023-01-10 | 2023-06-06 | 孙少哲 | Coal hydrogenation upgrading method |
| CN116218560B (en) * | 2023-01-10 | 2023-10-27 | 上海竣铭化工工程设计有限公司 | Coal hydrogenation upgrading method |
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