CN1546611A - Coking petrolatum oil processing method - Google Patents
Coking petrolatum oil processing method Download PDFInfo
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- CN1546611A CN1546611A CNA2003101214546A CN200310121454A CN1546611A CN 1546611 A CN1546611 A CN 1546611A CN A2003101214546 A CNA2003101214546 A CN A2003101214546A CN 200310121454 A CN200310121454 A CN 200310121454A CN 1546611 A CN1546611 A CN 1546611A
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- Prior art keywords
- catalytic cracking
- oil
- refining
- wax tailings
- slurry tank
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- 238000004939 coking Methods 0.000 title claims abstract description 13
- 238000003672 processing method Methods 0.000 title abstract description 3
- 239000004264 Petrolatum Substances 0.000 title abstract 3
- 229940066842 petrolatum Drugs 0.000 title abstract 3
- 235000019271 petrolatum Nutrition 0.000 title abstract 3
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 53
- 230000003068 static effect Effects 0.000 claims abstract description 7
- 239000002893 slag Substances 0.000 claims abstract description 5
- 239000003921 oil Substances 0.000 claims description 67
- 235000019198 oils Nutrition 0.000 claims description 67
- 238000007670 refining Methods 0.000 claims description 51
- 239000003795 chemical substances by application Substances 0.000 claims description 37
- 239000002002 slurry Substances 0.000 claims description 28
- 238000000034 method Methods 0.000 claims description 22
- 230000005684 electric field Effects 0.000 claims description 16
- 238000004062 sedimentation Methods 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 238000012545 processing Methods 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 230000003111 delayed effect Effects 0.000 claims description 6
- 238000004140 cleaning Methods 0.000 claims description 5
- 239000008157 edible vegetable oil Substances 0.000 claims description 3
- 239000013049 sediment Substances 0.000 claims description 2
- 229910052751 metal Inorganic materials 0.000 abstract description 4
- 239000002184 metal Substances 0.000 abstract description 4
- 150000002739 metals Chemical class 0.000 abstract description 2
- 150000004767 nitrides Chemical class 0.000 abstract description 2
- 238000000151 deposition Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 29
- 230000000694 effects Effects 0.000 description 13
- 239000003502 gasoline Substances 0.000 description 9
- 230000009466 transformation Effects 0.000 description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 239000002283 diesel fuel Substances 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 6
- 230000018044 dehydration Effects 0.000 description 6
- 238000006297 dehydration reaction Methods 0.000 description 6
- 239000000295 fuel oil Substances 0.000 description 6
- 229910052708 sodium Inorganic materials 0.000 description 6
- 239000011734 sodium Substances 0.000 description 6
- 238000005406 washing Methods 0.000 description 6
- 239000000571 coke Substances 0.000 description 5
- 238000012549 training Methods 0.000 description 5
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052791 calcium Inorganic materials 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 230000035484 reaction time Effects 0.000 description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000000638 solvent extraction Methods 0.000 description 3
- 239000003513 alkali Substances 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000000314 lubricant Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- KEAYESYHFKHZAL-UHFFFAOYSA-N Sodium Chemical compound [Na] KEAYESYHFKHZAL-UHFFFAOYSA-N 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000002199 base oil Substances 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 229910017464 nitrogen compound Inorganic materials 0.000 description 1
- 150000002830 nitrogen compounds Chemical class 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a coking petrolatum oil processing method comprising the steps of, (1) static state mixing, (2) depositing for separating slag, (3) purifying and dewatering, (4) catalytic cracking. The coking petrolatum oil refined solution can be used to effectively remove the alkaline nitrides and part metals in the coking wax oil.
Description
Technical field
The present invention relates to a kind of wax tailings working method, the invention belongs to the refining of petroleum field.
Continuous development along with Chinese national economy, the demand of oil fuel is growing, and crude oil has retrogradation to become heavy trend, and this just need rationally utilize limited resources, is heavy oil conversion as much as possible oil fuel, and catalytic cracking is the effective means that realizes this purpose.Straight-run gas oil is the good raw material of catalytic cracking, and with the wax tailings that vacuum residuum and catalytically cracked oil are produced, owing to aromatic hydrocarbons and nitrogen content height, is difficult to processing.At present, great majority have the refinery of coker that wax tailings is mixed catalytically cracked material in a large number, make the yield of light oil of catalytic cracking unit descend, this is not only the event of the difficult cracking of wax tailings itself, and the more important thing is, because " basic nitrogen compound " generally is several times of straight-run gas oil in the wax tailings, the existence of these alkali nitrogen is totally unfavorable to the catalytic cracking of wax tailings, it can be preferentially adsorbed in the acidity of catalyst in the heart, has reduced activity of such catalysts, distributes thereby the cracking that influences wax oil greatly influences the product of catalytic cracking, coke yield is risen, liquefied gas, yield of gasoline descends, and externally extracting oil increases, and has a strong impact on economic benefit.
Background technology
In order rationally to utilize wax tailings, many people have done unremitting effort.Hydrocracking is effective measures, but investment is big, and comprehensive benefit is bad.The US2934995 report is promptly used the aromatic hydrocarbons in first section coker distillate of solvent extraction with coker distillate selective solvent extracting, and send second section to carry out coking in the aromatic hydrocarbons of extracting out; Or the heavy oil fraction that coking fractional distillation column is told is through solvent extraction or solvent deasphalting, be divided into high carbon residue content product and low carbon residue content product, the product of low carbon residue content is all or part of as catalytically cracked material, the product circulation coking (US4534854) of high carbon residue content.Aforesaid method has not only reduced the catalytically cracked material amount, and need build the complete solvent extraction device of a cover, and investment and process cost are all quite big.
Summary of the invention
The purpose of this invention is to provide a kind of new wax tailings working method, promptly wax tailings is refining--catalytic cracking combined technique.This processing method adopts a kind of highly selective sulfur-preserving and denitrifying finishing agent (claiming finishing agent in this article) that is used for lubricant base of Chinese patent ZL94115190.5 invention, and wax tailings is made with extra care denitrogenation.Owing to carried out deep refining before lubricant base-oil denitrification is refining, not containing metal sodium, iron, calcium in the oil product, there is not the demetalization problem, and contain certain sodium Metal 99.5, iron, calcium in the wax tailings, when carrying out catalytic cracking, influence catalyst effect, this finishing agent in denitrogenation can and wax tailings in the part metals combination, and separate together, so remove some metal in the wax tailings simultaneously with nitride.Wax tailings after refining directly enters catalytic cracking unit and carries out the catalytic cracking processing, sends into catalytic cracking unit after wax tailings after maybe will making with extra care and straight-run gas oil mix by a certain percentage and carries out the catalytic cracking processing.
Method of the present invention comprises that wax tailings is behind interchanger heat exchange to 25～150 ℃, with the finishing agent of weight percent 0.2%～5% in static mixer after the hybrid reaction, natural subsidence or electric sedimentation layering in 1 to 6 hour, with upper strata edible vegetable oil weight percent is that 0.1～30% water is washed, treated oil and water in the electrofining slurry tank after electric field separates is refining.
By method provided by the invention, described heat exchange temperature is preferably 50-100 ℃, and the consumption of finishing agent is 0.2%～5% of a wax tailings weight, and preferable amount is 1%～5% of a wax tailings weight.For saving time preferred 1～3 hour of settling time.Electric field adopts intermittent type also can reach isolating purpose in the electrofining slurry tank, but when adopting in the continuous adjustable electrofining slurry tank electric field, operation can be more flexible, and electrofining strength of electric field is in 0 to 3000 volt/cm2 scope.
The object of the present invention is achieved like this: a kind of wax oil with the refinery delayed coking unit is a raw material, by refining wax tailings working method of carrying out the catalytic cracking processing again, with the wax tailings raw material in interchanger heat exchange to 25-150 ℃, preferred heat exchange temperature is 50 ℃～100 ℃, after in static mixer, carrying out hybrid reaction with finishing agent again, enter that sedimentation divides slag in the slurry tank, sediment is discharged from the slurry tank bottom, treated oil with enter after cleaning water is mixed in the electric slurry tank through further refining separating oil of electric field and water, the oil after refining enters catalytic cracking unit after the interchanger heat exchange is to 200-500 ℃ carries out catalytic cracking and handles.The adding weight percent of finishing agent is 0.2%-5%.The preferred adding weight percent of finishing agent is 1%-5%.Electrofining strength of electric field in the electricity slurry tank is 0～～3000 volt/cm2 scope.The described preferred settling time is 1～6 hour.The described settling time is 1～3 hour.The consumption of cleaning water is 0.1～30% of a upper strata edible vegetable oil weight.Refining wax tailings can enter catalytic cracking unit separately and carry out the catalytic cracking processing, also can be mixed into catalytic cracking unit with straight-run gas oil and carry out the catalytic cracking processing, and the mixed weight ratio of refining wax tailings and straight-run gas oil is 1: 1～1: 10.
Description of drawings
Fig. 1 is the process flow sheet of wax tailings working method of the present invention.
Accompanying drawing number:
1 wax tailings, 2 finishing agents, 3 tailings, 4 cleaning water
5 waste water, 6 straight-run gas oils, 7 catalysis overhead products
A interchanger B static mixer C slurry tank
D electrofining slurry tank E interchanger F catalytic cracking unit
Embodiment
The present invention is achieved in that wax tailings (1) mixes in static mixer (B) with weight percent 0.5%-5% with finishing agent (2) through interchanger (A) heat exchange to 50 ℃-100 ℃, enter the middle sedimentation of slurry tank (C) 1～3 hour then, slag (3) is discharged from the slurry tank bottom, the upper strata clarified oil with enter electric slurry tank (D) after the water (4) of weight percent 0.1%-30% mixes, between strength of electric field 0-3000v/cm, dewater, treated oil flows out from electrofining slurry tank top, directly enters catalytic cracking system (F) through interchanger (E) heat exchange to 200 ℃-500 ℃ and carries out catalytic cracking and handle.
Another embodiment is: wax tailings (1) mixes in static mixer (B) with weight percent 0.5%-5% with finishing agent (2) through interchanger (A) heat exchange to 50 ℃-100 ℃, enter the middle sedimentation of slurry tank (C) 1～3 hour then, slag (3) is discharged from the slurry tank bottom, the upper strata clarified oil with enter electric slurry tank (D) after the water (4) of weight percent 0.1%-30% mixes, between strength of electric field 0-3000v/cm, dewater, treated oil from electrofining slurry tank top flow out with straight-run gas oil (6) by weight 1: 1-1: 10 be in harmonious proportion after, enter catalytic cracking system (F) through interchanger (E) heat exchange and carry out catalytic cracking and handle.It is conspicuous that catalytic cracking of the present invention is handled one skilled in the art, belongs to prior art.
The effect that the inventive method reached is that wax tailings alkali nitrogen can take off to 400-1200ppm from 1500-2800ppm, and the decalcification rate reaches 70%-80%, and the deferrization rate reaches 50%-80%, takes off the sodium rate and reaches 50%-60%.Refining separately back wax tailings is handled through catalytic cracking, and liquefied gas, gasoline, three sums of diesel oil improve more than 10% than not refining wax tailings.Mix the refining back wax tailings of refining straight-run gas oil and handle through catalytic cracking, liquefied gas, gasoline, three sums of diesel oil improve more than 3%, as table 1,2 than not refining wax tailings.
Catalytic cracking effect comparison before and after table 1 wax tailings is refining
| Project | 2% (finishing agent) made with extra care burnt wax | 1% (finishing agent) made with extra care burnt wax | Not refining wax tailings |
| ??C 3+C 4 | ?9.06 | ?8.43 | ??5.72 |
| Gasoline (C 5-204℃) | ?29.07 | ?26.39 | ??21.60 |
| Diesel oil/(203-350 ℃) | ?16.56 | ?19.77 | ??17.05 |
| The transformation efficiency sum | ?54.96 | ?54.59 | ??44.37 |
| Iron/μ g.g -1 | ?0.71 | ?0.82 | ??3.9 |
| Sodium/μ g.g -1 | ?0.43 | ?0.47 | ??0.91 |
| Calcium/μ g.g -1 | ?0.19 | ?0.21 | ??0.83 |
Table 2 straight-run gas oil is mixed training of vital essence system front and back wax tailings (40%) catalytic cracking effect comparison
| Project | Not refining wax tailings | The not refining wax tailings of 60% straight-run gas oil+40% | 60% straight-run gas oil+40% is made with extra care wax tailings |
| ??C 3+C 4 | ??10.09 | ?13.33 | ?14.05 |
| Gasoline (C 5-204℃) | ??21.21 | ?31.77 | ?34.09 |
| Diesel oil/(203-350 ℃) | ??20.40 | ?25.13 | ?26.16 |
| The transformation efficiency sum | ??51.70 | ?70.23 | ?74.30 |
The following examples are to further specify of the present invention, rather than limit the scope of the invention.Percentage ratio among the present invention is weight percentage if no special instructions.
Embodiment 1
The delayed coking of the vacuum residuum of Yizheng commingled crude production is handled and is obtained wax tailings raw material, its character: density 0.9188 density/g.cm
-3(20 ℃), basic n content are 2100 μ g.g
-1, handle with 1% finishing agent, sedimentation 3 hours, with entering electric slurry tank (D) after the washing of 5% weight percent, in strength of electric field 2000v/cm dehydration, the basic n content of refining back treated oil is 1205 μ g.g
-1Handle with 2% finishing agent, sedimentation 3 hours, with entering electric slurry tank (D) after the washing of 5% weight percent, in strength of electric field 2000v/cm dehydration, the basic n content of refining back treated oil is 890 μ g.g
-1, treated oil catalytic cracking effect such as following table:
Catalytic cracking effect comparison before and after table 3 wax tailings is refining
| Test sample | 2% (finishing agent) made with extra care burnt wax | 1% (finishing agent) made with extra care burnt wax | Not refining wax tailings |
| Operational condition | |||
| Temperature of reaction/℃ | ?510 | ?510 | ??510 |
| Reaction times/s | ?2.24 | ?2.24 | ??2.28 |
| Agent/oil | ?6.26 | ?6.24 | ??6.22 |
| Productive rate/m% | |||
| Coke | ?3.54 | ?4.48 | ??4.35 |
| Reacted gas | ?9.76 | ?9.16 | ??6.36 |
| C 3+C 4 | ?9.06 | ?8.43 | ??5.72 |
| Gasoline (C 5-204℃) | ?29.07 | ?26.39 | ??21.60 |
| Diesel oil/(203-350 ℃) | ?16.56 | ?19.77 | ??17.05 |
| Heavy oil/(＞350 ℃) | ?40.36 | ?39.45 | ??49.76 |
| Loss | ?0.71 | ?0.75 | ??0.88 |
| Amount to | ?100.00 | ?100.00 | ??100.00 |
| Transformation efficiency/% | ?43.08 | ?40.78 | ??33.19 |
| Light oil yield/% | ?46.83 | ?45.78 | ??38.65 |
| Iron/μ g.g -1 | ?0.71 | ?0.82 | ??3.9 |
| Sodium/μ g.g -1 | ?0.43 | ?0.47 | ??0.91 |
| Calcium/μ g.g -1 | ?0.19 | ?0.21 | ??0.83 |
As can be seen from Table 3, adopt 1% (weight) finishing agent purified wax tailings than light oil yield after making with extra care the wax tailings catalytic cracking and improve 7.18, the decalcification rate reaches 78%, and deferrization rate 79% is taken off the sodium rate and reached 52%; Light oil yield improves 8.13 after adopting 2% (weight) finishing agent purified wax tailings than not refining wax tailings catalytic cracking, and the decalcification rate reaches 82%, and deferrization rate 81% is taken off the sodium rate and reached 53%.
Embodiment 2
The delayed coking of the vacuum residuum of Yizheng commingled crude production is handled and is obtained wax tailings raw material, its character: density 0.9188 density/g.cm
-3(20 ℃), basic n content are 2100 μ g.g
-1, handle with 1% finishing agent, sedimentation 3 hours, with entering electric slurry tank (D) after the washing of 5% weight percent, in strength of electric field 2000v/cm dehydration, the basic n content of refining back treated oil is 1205 μ g.g
-1Handle with 2% finishing agent, sedimentation 3 hours, with entering electric slurry tank (D) after the washing of 5% weight percent, in strength of electric field 2000v/cm dehydration, the basic n content of refining back treated oil is 890 μ g.g
-1Straight-run gas oil character: density 0.9108 density/g.cm
-3(20 ℃), basic n content are 636 μ g.g
-1Straight-run gas oil is mixed training of vital essence system front and back wax tailings catalytic cracking effect such as following table:
Table 4 straight-run gas oil is mixed training of vital essence system front and back wax tailings (25%) catalytic cracking effect
| Experiment numbers | ????1 # | ????2 # | ????3 # |
| Operational condition | |||
| Temperature of reaction/℃ | ????510 | ????510 | ????510 |
| Reaction times/s | ????2.19 | ????2.16 | ????2.21 |
| Agent/oil | ????6.25 | ????6.24 | ????6.24 |
| Productive rate/m% | |||
| Coke | ????3.69 | ????3.74 | ????3.85 |
| Reacted gas | ????10.36 | ????10.19 | ????9.50 |
| C 3+C 4 | ????9.74 | ????9.58 | ????8.86 |
| Gasoline (C 5-204 ℃) | ????37.27 | ????36.38 | ????32.72 |
| Diesel oil/(203-350 ℃) | ????21.28 | ????21.70 | ????22.21 |
| Heavy oil/(＞350 ℃) | ????26.66 | ????27.25 | ????30.83 |
| Loss | ????0.74 | ????0.74 | ????0.89 |
| Amount to | ????100.00 | ????100.00 | ????100.00 |
| Transformation efficiency/% | ????52.06 | ????51.05 | ????46.96 |
| Light oil yield/% | ????58.55 | ????58.08 | ????54.93 |
1
#: 2% (finishing agent) made with extra care wax oil 25%+ straight-run gas oil 75%; 2
#: 1% (finishing agent) made with extra care the straight wax 75% of wax oil 25%+; 3
#: the straight wax 75% of burnt wax 25%+.
As can be seen from Table 4, light oil yield improved 3.62 after 2% finishing agent was made with extra care wax oil (25%) and mixed refining straight-run gas oil (75%) and mix the catalytic cracking of refining straight wax (75%) than refining burnt wax (25%), adopt 1% (weight) finishing agent purified wax tailings than refining wax tailings catalytic cracking after light oil yield improve 3.15.
Embodiment 3
The delayed coking of the vacuum residuum of Yizheng+Xijiang River commingled crude production is handled and is obtained wax tailings raw material, its character: density 0.9152 density/g.cm
-3(20 ℃), basic n content are 1987 μ g.g
-1, handle with 2% finishing agent, sedimentation 2 hours, with entering electric slurry tank (D) after the washing of 3% weight percent, in strength of electric field 800v/cm dehydration, the basic n content of the treated oil after making with extra care is 805 μ g.g
-1Straight-run gas oil character: density 0.9056 density/g.cm
-3(20 ℃), basic n content are 516 μ g.g
-1Straight-run gas oil is mixed training of vital essence system front and back wax tailings catalytic cracking effect such as following table:
Table 5 straight-run gas oil is mixed training of vital essence system front and back wax tailings (40%) catalytic cracking effect
| Experiment numbers | Not refining wax tailings | The not refining wax tailings of 60% straight-run gas oil+40% | 60% straight-run gas oil+40% is made with extra care wax tailings |
| Operational condition | |||
| Temperature of reaction/℃ | ????490 | ?490 | ?490 |
| Reaction times/s | ????2.15 | ?2.11 | ?2.13 |
| Agent/oil | ????5 | ?5 | ?5 |
| Productive rate/m% | |||
| Coke | ????5.69 | ?4.12 | ?3.91 |
| Reacted gas | ????1.03 | ?1.21 | ?1.23 |
| ??C 3+C 4 | ????10.09 | ?13.33 | ?14.05 |
| Gasoline (C 5-204℃) | ????21.21 | ?31.77 | ?34.09 |
| Diesel oil/(203-350 ℃) | ????20.40 | ?25.13 | ?26.16 |
| Heavy oil/(＞350 ℃) | ????41.54 | ?22.41 | ?20.56 |
| 205 ℃ of transformation efficiency/% | ????38.02 | ?51.46 | ?53.28 |
| 365 ℃ of transformation efficiency/% | ????58.42 | ?75.59 | ?79.44 |
As can be seen from Table 5, light oil yield improved 3.85 after the refining wax oil (40%) in refining back was mixed refining straight-run gas oil (60%) and mixed the catalytic cracking of refining straight wax (60%) than refining burnt wax (40%).
Embodiment 4
The delayed coking of the vacuum residuum of Yizheng+Daqing Mixing crude production is handled and is obtained wax tailings raw material, its character: density 0.9112 density/g.cm
-3(20 ℃), basic n content are 2213 μ g.g
-1, handle with 0.5%, 1% and 4% refining agent consumption amount respectively, sedimentation 2 hours, with entering electric slurry tank (D) after the washing of 3% weight percent, in strength of electric field 1500v/cm dehydration, the basic n content of refining back treated oil is respectively 1687 μ g.g
-1, 1412 μ g.g
-1With 616 μ g.g
-1Wax tailings catalytic cracking effect such as following table before and after refining:
The different refining agent consumption amount of table 6 are made with extra care wax tailings catalytic cracking effect
| Experiment numbers | Not refining wax tailings | 0.5% refining wax tailings | 1% refining wax tailings | 4% refining wax tailings |
| Operational condition | ||||
| Temperature of reaction/℃ | ??490 | ???490 | ?490 | ?490 |
| Reaction times/s | ??2.15 | ???2.11 | ?2.14 | ?2.13 |
| Agent/oil | ??3 | ???3 | ?3 | ?3 |
| Productive rate/m% | ||||
| Coke | ??3.83 | ???3.81 | ?3.28 | ?3.24 |
| Reacted gas | ??1.06 | ???1.07 | ?0.97 | ?1.16 |
| ??C 3+C 4 | ??6.26 | ???6.31 | ?6.16 | ?8.75 |
| Gasoline (C 5-204℃) | ??18.38 | ???19.73 | ?20.30 | ?28.10 |
| Diesel oil/(203-350 ℃) | ??12.63 | ???13.24 | ?13.60 | ?16.35 |
| Heavy oil/(＞350 ℃) | ??57.58 | ???55.53 | ?55.77 | ?42.02 |
| ??L+G+D | ??37.24 | ???39.28 | ?40.06 | ?53.20 |
| 205 ℃ of transformation efficiency/% | ??29.5 | ???30.9 | ?30.7 | ?41.3 |
As can be seen from Table 6,205 ℃ of transformation efficiencys improve 10.6 after adopting the refining wax tailings catalytic cracking of 1% (weight) finishing agent purified wax tailings ratio, adopt 4% (weight) finishing agent purified wax tailings than 205 ℃ of transformation efficiencys after making with extra care the wax tailings catalytic cracking and improve 11.8.
Claims (10)
1. the wax oil with the refinery delayed coking unit is a raw material, by refining wax tailings working method of carrying out the catalytic cracking processing again, it is characterized in that: with wax tailings raw material (1) in interchanger (A) heat exchange 25-150 ℃, after in static mixer (B), carrying out hybrid reaction with finishing agent (2) again, enter the middle sedimentation of slurry tank (C) and divide slag, sediment (3) is discharged from slurry tank (C) bottom, treated oil with enter after cleaning water (4) is mixed in the electric slurry tank (D) through further refining separating oil of electric field and water, the oil after refining enters catalytic cracking unit (F) after interchanger (E) heat exchange is to 200-500 ℃ carries out catalytic cracking and handles.
2. method according to claim 1 is characterized in that: the adding weight percent of finishing agent (2) is 0.2%-5%.
3. method according to claim 1 is characterized in that; The adding weight percent of finishing agent (2) is 1%-5%.
4. method according to claim 1, its feature also is: the electrofining strength of electric field in the electric slurry tank (D) is at 0～3000 volt/cm
2Scope.
5. method according to claim 1, its feature also is: described treated oil flows out from electrofining slurry tank top, directly enters catalytic cracking unit (F) through interchanger (E) heat exchange to 200-500 ℃ and carries out the catalytic cracking processing.
6. method according to claim 1, its feature also is: the described settling time is 1～6 hour.
7. method according to claim 6, its feature also is: the described settling time is 1～3 hour.
8. method according to claim 1, its feature also is: the consumption of cleaning water is 0.1～30% of a upper strata edible vegetable oil weight.
9. method according to claim 1, its feature also is: the heat exchange temperature in the described interchanger (A) is 50 ℃～100 ℃.
10. method according to claim 1, its feature also is: refining wax tailings can enter catalytic cracking unit (F) separately and carry out the catalytic cracking processing, also can and straight-run gas oil (6) be mixed into catalytic cracking unit (F) and carry out catalytic cracking and handle, the mixed weight ratio of refining wax tailings and straight-run gas oil is 1: 1～1: 10.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101214546A CN100348696C (en) | 2003-12-17 | 2003-12-17 | Coking petrolatum oil processing method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101214546A CN100348696C (en) | 2003-12-17 | 2003-12-17 | Coking petrolatum oil processing method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1546611A true CN1546611A (en) | 2004-11-17 |
| CN100348696C CN100348696C (en) | 2007-11-14 |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101144031B (en) * | 2006-09-13 | 2010-09-01 | 中国石油天然气股份有限公司 | Preprocessing method for coking wax oil used as hydrocracking raw material |
| CN101955797A (en) * | 2010-10-22 | 2011-01-26 | 华东理工大学 | Method for inhibiting alkaline nitrides in coker gatch |
| CN102485842A (en) * | 2010-12-03 | 2012-06-06 | 中国石油天然气股份有限公司 | Method for processing fixed bed fishing coker gas oil |
| CN102676208A (en) * | 2012-03-31 | 2012-09-19 | 中国石油大学(华东) | Method for refining complexed and denitrified oil |
| CN101928597B (en) * | 2010-02-04 | 2013-07-17 | 涿州贝尔森生化科技发展有限公司 | Vacuum residue processing method |
| CN103289728A (en) * | 2012-03-03 | 2013-09-11 | 辽宁石油化工大学 | Straight-run diesel oil desulfurating method |
| CN111849531A (en) * | 2020-07-28 | 2020-10-30 | 神州节能科技集团有限公司 | Method for purifying electric tar and using device thereof |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1091460C (en) * | 1998-12-29 | 2002-09-25 | 中国石油化工集团公司 | Solvent refining and hydrocracking combined process for poor-quality wax oil |
| FI124814B (en) * | 2010-10-18 | 2015-01-30 | Lappeenrannan Teknillinen Yliopisto | Electric machine stator and electric machine |
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2003
- 2003-12-17 CN CNB2003101214546A patent/CN100348696C/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101144031B (en) * | 2006-09-13 | 2010-09-01 | 中国石油天然气股份有限公司 | Preprocessing method for coking wax oil used as hydrocracking raw material |
| CN101928597B (en) * | 2010-02-04 | 2013-07-17 | 涿州贝尔森生化科技发展有限公司 | Vacuum residue processing method |
| CN101955797A (en) * | 2010-10-22 | 2011-01-26 | 华东理工大学 | Method for inhibiting alkaline nitrides in coker gatch |
| CN102485842A (en) * | 2010-12-03 | 2012-06-06 | 中国石油天然气股份有限公司 | Method for processing fixed bed fishing coker gas oil |
| CN102485842B (en) * | 2010-12-03 | 2014-01-15 | 中国石油天然气股份有限公司 | Method for processing fixed bed fishing coker gas oil |
| CN103289728A (en) * | 2012-03-03 | 2013-09-11 | 辽宁石油化工大学 | Straight-run diesel oil desulfurating method |
| CN102676208A (en) * | 2012-03-31 | 2012-09-19 | 中国石油大学(华东) | Method for refining complexed and denitrified oil |
| CN111849531A (en) * | 2020-07-28 | 2020-10-30 | 神州节能科技集团有限公司 | Method for purifying electric tar and using device thereof |
| CN111849531B (en) * | 2020-07-28 | 2021-06-01 | 神州节能科技集团有限公司 | Rubber-plastic electric tar-capturing purification method and use device thereof |
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