CN1043782C - Gasoline octane number-raising catalytic conversion method - Google Patents
Gasoline octane number-raising catalytic conversion method Download PDFInfo
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Abstract
The present invention relates to a catalytic conversion method for improving the octane number of a gasoline fraction with low quality. The present invention is characterized in that gasoline with low octane number is injected in any part of the lower part of the cracking stock inlet end of a catalytic cracking riser reactor so that the gasoline with low octane is in contact with a high temperature catalyst from a regenerator. Gasoline upgrading reaction is generated under a certain reaction condition, a generated mixture containing micro coke and reacting oil gas is upwards lifted and then is in contact with sprayed cracking stocks, and thus, a carbon containing mixture of a catalyst to be generated and the reacting oil gas is produced by reaction under cracking conditions and then is separated and regenerated. A method which has simple operation and can greatly improve the octane number of the gasoline with low quality can be obtained by partially improving a catalytic cracking riser device.
Description
The invention belongs to fluidifying and catalytic convertion process.More particularly, the present invention is the lower low-quality gasoline of bottom injection octane value that contains the catalytic cracking riser reactor of molecular sieve catalyst in employing, makes it that catalytic reforming reaction take place, to reach the purpose of boosting of octane rating.
The most frequently used method that improves gasoline octane rating is to add the tetraethyllead octane promoter, but owing to doped fuel waste gas after burning severe contamination atmosphere, so each state all uses doped fuel in restriction, development low lead gasoline and white gasoline.Straight-run spirit in the refining of petroleum, coker gasoline, viscosity breaking gasoline, hydrocracking gasoline etc. belong to low octane value gasoline, even these low-quality gasoline and gasoline with high-octane number component such as also inaccessible No. 90 gasoline of catalytically cracked gasoline blending.Therefore gasoline that some octane value is lower such as straight-run spirit are that method by catalytic reforming improves its octane value, or have the gasoline concoction of high-octane number component with other; Must just can advance reformer then earlier through hydrofining for the gasoline that closes sulphur, nitrogen and alkene such as coker gasoline, visbreaking gasoline, so just make work flow become complicated more.
Fluid catalytic cracking (FCC) also is that the catalytic gasoline research octane number (RON) can reach more than 90 after the important oil-processing units, particularly molecular sieve catalyst and riser reactor application of production high octane gasoline component.In order to obtain more stop bracket gasoline, its processing method is also in continuous improvement.For example the USP4869807 proposition is the shunt sprayed feed with the different positions that the raw material demultiplexing sprays into riser tube, and with raising gasoline octane rating and the rare hydrocarbon yield of increase, but the amplitude of the gasoline octane rating of this method raising is little; Take to improve the octane value that FCC apparatus improves low-quality gasoline in addition, as the multiple riser reactor of USP3784463 employing more than two or two, wherein a riser tube is imported low-quality gasoline, make it that catalytic reforming reaction takes place under certain conditions, this method equipment and operate all more complicated, and the amplitude that gasoline octane rating improves is also little.
Purpose of the present invention is exactly to utilize the catalytic cracking riser device contain molecular sieve catalyst, carry out part improve can obtain a kind of easy and simple to handle and can improve the method for gasoline octane number by a relatively large margin.
Major programme of the present invention:
Residue fluid catalytic cracking unit generally improves several meters to the feed entrance point of riser tube, the bottom is the catalyzer pre lift zone, catalyzer quickens herein in advance, to reach all even well-mixed purpose of raw material that makes of catalyst distribution, but meanwhile, formed a high temperature section in the bottom of riser tube feed entrance point, the present invention utilizes this high temperature section exactly, to be difficult for the low-quality gasoline of cracked and import this position, contact with new regenerated high temperature catalyst from revivifier, the gasoline upgrading reaction takes place under the condition of high temperature and high solvent-oil ratio, increase substantially its octane value, and production department divides liquefied gas simultaneously.The concrete operations step comprises:
1. the low octane value gasoline cut contacts with new regenerated high temperature catalyst from revivifier at first conversion zone of riser reactor, at 600～730 ℃ of temperature of reaction, weight space velocity 1～180h
-1, agent-oil ratio 6～180 condition under the gasoline upgrading reaction takes place, generate first and have the catalyzer that contains micro-charcoal and the logistics of reaction oil gas;
2. (1) goes on foot first logistics and upwards promotes, and the cracking stock that injects with second conversion zone contacts, and reacts under cracking conditions, generates second and has the reclaimable catalyst that contains charcoal and the logistics of reaction oil gas;
3. second logistics that (2) step is generated is input to segregation section, and reclaimable catalyst is separated with reaction oil gas, and reclaimable catalyst goes revivifier regeneration, and the catalyzer after the regeneration returns (1) and goes on foot and recycle.
Below in conjunction with the thin description of flow process pattern characteristics of the present invention.
Accompanying drawing is a schematic flow sheet of the present invention.
By accompanying drawing as can be known, low-quality gasoline from feed nozzle 2 bottoms first conversion zone of the FCC riser 1 of routine comprise 3 and any position of bottom 4 inject, with contact from 660～750 ℃ of regenerated catalysts of regenerator 5 by inclined tube 6 and guiding valve 7, at 600～730 ℃ of reaction temperatures (best 660～720 ℃), weight space velocity 1～180h-1(best 10～100-1), the gasoline upgrading reaction takes place under the condition of oil ratio 6～180 (best 36～80), generate first logistics that comprises reaction oil gas and contain the catalyst of micro-charcoal; Second conversion zone that first logistics upwards is promoted to riser is that conventional cracked stock carries out nozzle 2 places, contact with cracked stock, under common catalytic cracking condition cracking reaction taking place, generates reclaimable catalyst and comprise that the mixed oil and gas of the reaction oil gas that the reaction of first paragraph gasoline upgrading generates is second logistics; Second logistics carried out initial gross separation through the quick disconnector 8 of riser 1 outlet, most of catalyst enters stripping section 9, oil gas separates with the cyclone separator 11 that the small part catalyst enters settler 10 tops, and oil gas enters fractionating system by settler 10 top collection chambers 12. Reclaimable catalyst enters stripping section 9 downwards by cyclone separator, and the reclaimable catalyst behind the stripping enters regenerator 5 coke burning regenerations, and the catalyst after the regeneration returns riser 1 first conversion zone and recycles.
The decanting point of the low-quality gasoline of described first conversion zone is any position that comprises the riser bottom below the conventional FCC riser reactor of second conversion zone feed entrance point.
Described low-quality gasoline comprises a kind of or its miscella in direct steaming gasoline, coker gasoline, visbreaking gasoline, hydrofined gasoline, hydrocracking gasoline, the reforming raffinate oil.
Described cracked stock comprises any of light diesel fuel, vacuum gas oil (VGO), decompression residuum, reduced crude, coker gas oil, deasphalted oil and crude oil or its miscella.
Second segment reaction condition of the present invention can adopt conventional RFCC condition, can also adopt the reaction condition of CN87105428 and CN91108425.8 (calling MGG in the following text) patented technology.
Solid acid catalyst of the present invention is with ZSM-5, contain rare-earth five-membered ring silica-rich zeolite and REY, comprise that a kind of or its mixture in the high-silicon Y-Zeolite of super steady Y is the catalyst of active component, comprise that the CN87105428 patent adopts faujasite, the faujasite of rare earth ion exchanged, the ZSM-5 that the faujasite of process chemistry and/or stabilization processes or the catalyst that its mixture is active component and CN91108425.8 patent adopt, the catalyst that REY and three kinds of zeolites of high silicon Y are active component, can also be the CN1085885A patent application adopt contain the rare-earth five-membered ring silica-rich zeolite, the catalyst that REY and three kinds of zeolites of high silicon Y are active component.
The conventional cracked stock atomizer of riser reactor of the present invention can adopt extra heavy pipe with underground pipelines (i.e. first conversion zone), its caliber determine that average linear speed with first logistics is greater than 0.2 meter per second, to form the fast bed conversion zone, increase the gasoline upgrading reaction time, improve conversion level.
Major advantage of the present invention:
1. method of the present invention need not to increase new device and equipment, can improve the octane value of low-quality gasoline by a relatively large margin, motor-method octane number can improve 18 more than the unit, organon method octane value can improve 25 more than the unit, and the gasoline that reformulated gasoline and cracking generate can reach the standard of No. 90 white gasolinees.
2. the gasoline that method of the present invention is injected can all or part of replacement riser reactor pre-lifting steam, not only cut down the consumption of energy, but also reduce the hydrothermal deactivation speed of catalyzer.
3. intensification when method of the present invention is injected gasoline, vaporization and a lot of heat of reaction needed, but the coke that generates is seldom, so not only can increase the agent-oil ratio of device, but also can increase the processing power of device or mix some residual oil of refining more.
Further describe characteristics of the present invention with example below.Low-quality gasoline property used in the example sees Table 1.Used catalyzer sees Table 2.RAG-1 is the catalyzer that is active ingredient with ZSM-5, REY and three kinds of zeolites of high silicon Y in the table; The catalyzer that RAG-2 is is active ingredient to contain rare-earth five-membered ring supersiliceous zeolite, REY and three kinds of zeolites of high silicon Y; ZCM-7 is to be the catalyzer of active ingredient with the high-silicon Y-Zeolite.Above-mentioned three kinds of catalyzer are produced by Qilu Petrochemical company catalyst plant.
Example 1
On small-scale fixed bed pilot plant, use catalyst A, with under different agent-oil ratios, carry out the catalytic reforming test at 680 ℃, 120KPa, weight space velocity 30～35 to managing defeated straight-run spirit, the results are shown in Table 3.
Found out by table 3, adopt the present invention, to managing defeated straight-run spirit upgrading, can make the gasoline motor-method octane number improve 20.7 units when agent-oil ratio 18, research octane number (RON) improves 26.8 units.
Example 2
This example is on small-scale fixed bed pilot plant, adopts catalyst B, at 680 ℃, 120KPa, weight space velocity 30～35, under different agent-oil ratio, carries out the catalytic reforming test to managing defeated straight-run spirit, the results are shown in Table 4.
Found out that by table 4 under agent-oil ratio 19 conditions, the gasoline motor-method octane number improves 18.7 units, research octane number (RON) improves 25.8 units.
Example 3
This example is to mix on the catalytic cracking unit of oil refining at the processing wax oil, adopts method of the present invention, uses catalyzer C, and its operational condition: temperature is 520 ℃, and pressure is 140KPa, agent-oil ratio 6.3.The results are shown in Table 5.
Found out that by table 5 straight-run spirit trips out device with the catalytic gasoline one of conventional FCC behind upgrading, its octane value motor method is more than 80, and organon reaches more than 90, can directly dispatch from the factory as No. 90 gasoline.
Example 4
This example is to adopt method of the present invention to test on the MGG device of processing paraffinic base long residuum, uses catalyst B, operational condition: 532 ℃ of temperature of reaction, pressure 126KPa, agent-oil ratio 6.5.The results are shown in Table 6.
Found out that by table 6 behind the straight-run spirit upgrading, motor-method octane number reaches 78.3, research octane number (RON) reaches 92.4.
Example 5
This example is at small-scale fixed bed pilot plant, adopts catalyst A and C that grand celebration straight-run spirit and grand celebration coker gasoline are carried out the upgrading test.Operational condition: 680 ℃ of temperature, pressure 120KPa, weight space velocity 2.79～3.07, agent-oil ratio 25～30.The results are shown in Table 7.
Found out that by table 7 behind the grand celebration straight-run spirit upgrading, motor-method octane number improves more than 14 units, research octane number (RON) improves more than 20; Grand celebration coker gasoline motor-method octane number improves 18 units, and research octane number (RON) improves 24 more than the unit.
Example 6
This example is on small-scale fixed bed pilot plant, adopt catalyst A under the condition of 690 ℃, 120KPa, weight space velocity 180, agent-oil ratio 180 (be equivalent to riser tube bottom spray into a little about 80% place to conventional FCC cracking stock oil inject gasoline), carry out catalytic reforming and test managing the defeated coker gasoline of defeated straight-run spirit and pipe.Test-results sees Table 8.
By table 8 data as can be known, the gasoline octane rating behind the upgrading all has raising by a relatively large margin.
Example 7
The test conditions of this example is except that 685 ℃ of temperature, agent-oil ratio 100 (be equivalent to riser tube bottom to conventional FCC cracking stock oil and spray into a little 50% place injection gasoline), and other condition is with example 6.Experimental result sees Table 9.
As shown in Table 9, behind defeated straight-run spirit of pipe and the defeated coker gasoline upgrading of pipe, gasoline octane rating all has raising by a relatively large margin.
Example 8
This example is to test actual conditions under the condition that adopts lower air speed and agent-oil ratio on the small fixed testing apparatus: use catalyst A, 680 ℃ of temperature of reaction, pressure 120KP, weight space velocity 5, agent-oil ratio 10.Test-results sees Table 10.
By table 10 data as can be known, adopt method of the present invention, gasoline octane number is greatly improved.
Table 1 gasoline stocks character
| Project | Grand celebration straight-run spirit | The defeated straight-run spirit of pipe | The grand celebration coker gasoline | The defeated coker gasoline of pipe |
| Density, 20 ℃ of g/cm 3S, ppm N, the ppm boiling range, 10% 50%. 90% of ℃ initial boiling point is done octane value RON MON | 0.7432 - - 60 97 141 184 205 45.7 43.7 | 0.7469 158.9 2.2 66 94 123 153 177 58.2 56.3 | 0.7414 100 140 62 89 127 162 192 52.3 50.3 | 0.7413 4200 200 57 91 129 167 192 64 62 |
Table 2 catalyst property
| The catalyzer code name | A | B | C |
| The catalyzer trade names | RAG-1 | RAG-2 | ZCM-7 |
| Chemical constitution, m% Al 2O 3Na 2O SO 4 =Fe 2O 3Physical properties: specific surface, m 2/ g pore volume, ml/g apparent density, g/cm 3Abrasion index, %h -1Size composition, m% 0～40 μ m 40～80 μ m 780 μ m | 44.6 0.13 1.40 0.43 232 0.36 0.62 2.5 13.1 54.9 32.0 | 45.4 0.15 1.10 0.45 211 0.34 0.78 3.5 - - - | 44.1～45.2 0.26 0.41 - 204 0.31 0.60 2.3 16.1 54.1 29.8 |
Table 3
| Project | Agent-oil ratio | ||
| 18 | 20 | 32 | |
| Product distribution m% H 2-C 2C 3-C 4The gasoline, diesel coke amounts to | 10.48 27.42 56.27 2.25 3.58 100 | 10.60 30.48 53.97 1.26 3.69 100.00 | 11.24 34.75 48.93 1.29 3.79 100.00 |
| Gasoline octane rating MON RON | 77.0 85.0 | - - | - - |
| Weight space velocity, h -1 | 30.7 | 32.1 | 34.9 |
Table 4
| Project | Agent-oil ratio | ||
| 19 | 22 | 30 | |
| Product distribution m% H 2-C 2C 3-C 4The gasoline, diesel coke amounts to | 10.47 24.09 62.02 0.86 2.56 100.00 | 10.76 26.66 58.63 1.38 2.57 100.00 | 12.12 30.30 53.35 1.63 2.60 100.00 |
| Gasoline octane rating MON RON | 75.0 84.0 | - - | - - |
| Weight space velocity, h -1 | 30.4 | 32.7 | 34.8 |
Table 5
| Project | The present invention | Conventional FCC | Directly blending |
| Charging constitutes, and ten thousand tons of/year intermediate base wax oils are mixed 21% vacuum residuum straight-run spirit catalytic gasoline: straight-run spirit (weight) | 100.00 10.00 | 100.00 - | 52.2∶10.0 |
| Product slate, ten thousand tons of/year dry gas liquefied gas gasoline solar oil slurry oil coke | 4.86 13.23 57.83 16.72 9.95 7.41 | 3.81 10.49 52.20 16.49 9.95 7.06 | |
| Gasoline octane rating MON RON | 80.2 92.6 | 80.5 93.4 | 76.6 87.7 |
Table 6
| Project | The present invention | MGG | Directly blending |
| Charging constitutes long residuum, m% straight-run spirit, m% MGG gasoline: straight-run spirit (weight) | 88.81 11.19 | 100.00 | 33.4∶10.0 |
| Product yield, the loss of m% dry gas liquefied gas gasoline light diesel fuel heavy oil coke | 4.47 23.16 38.25 20.66 5.62 7.32 0.52 | 4.36 22.05 37.37 23.11 4.02 8.42 0.67 | |
| Gasoline octane rating MON RON | 92.4 78.3 | 93.4 79.1 | 88.2 77.2 |
Table 7
| Catalyzer | A | C | ||
| Stock oil | Grand celebration straight-run spirit | The grand celebration coker gasoline | Grand celebration straight-run spirit | The grand celebration coker gasoline |
| Product distributes, m% H 2-C 2C 3-C 4The gasoline, diesel coke amounts to | 15.42 38.34 42.15 0.57 3.92 100.00 | 14.68 87.56 40.68 1.28 5.80 100.00 | 15.93 37.45 41.54 1.08 4.00 100.00 | 15.33 36.64 40.85 0.98 6.20 100.00 |
| Gasoline octane rating MON RON | 58.1 66.1 | 68.5 76.5 | 58.4 66.4 | 68.2 76.2 |
| Weight space velocity, h-1 | 27.9 | 30.4 | 28.1 | 30.7 |
| Agent-oil ratio | 25 | 25 | 28 | 30 |
Table 8
| Stock oil | The defeated straight-run spirit of pipe | The defeated coker gasoline of pipe |
| Product distributes, m% H 2-C 2C 3-C 4The gasoline, diesel coke amounts to | 11.9 27.1 57.0 1.4 2.6 100.0 | 11.6 26.3 56.5 1.6 4.0 100.0 |
| Gasoline octane rating MON RON | 76.5 84.5 | 78 86 |
Table 9
| Stock oil | The defeated gasoline that directly increases of pipe | The defeated coker gasoline of pipe |
| Product distribution m% H 2-C 2C 3-C 4The gasoline, diesel coke amounts to | 10.4 30.7 54.0 1.8 3.1 100.0 | 10.1 30.5 52.8 2.0 4.6 100.0 |
| Gasoline octane rating MON RON | 78 86 | 78.5 88 |
Table 10
| Stock oil | The defeated straight-run spirit of pipe | The defeated coker gasoline of pipe |
| Product distributes, m% H 2-C 2C 3-C 4The gasoline, diesel coke amounts to | 14.6 35.2 45.0 2.0 3.2 100.0 | 14.3 34.6 44.2 2.2 4.7 100.0 |
| Gasoline octane rating MON RON | 79 87 | 79.5 88.5 |
Claims (8)
1. catalysis conversion method that improves low-quality gasoline fraction octane value comprises the RS Regenerator Section of riser tube conversion zone, catalyst separating section and catalyzer it is characterized in that the riser tube conversion zone adopts the mode of two section feedings, and concrete steps comprise:
A. low-quality gasoline fraction contacts with high temperature catalyst from revivifier at first conversion zone of riser reactor, the gasoline upgrading reaction takes place under the condition of 600～730 ℃ of temperature of reaction, weight space velocity 1～180, agent-oil ratio 6～180, generates first and has catalyzer and the reaction oil gas logistics that contains micro-charcoal;
B. (a) goes on foot upwards lifting of first logistics, and the cracking stock that injects with second conversion zone contacts, and second of reaction generation has the charcoal of containing reclaimable catalyst and reaction oil gas logistics under cracking conditions;
C. second logistics that (b) step is generated is input to segregation section, and reclaimable catalyst is separated with reaction oil gas, and reaction oil gas goes fractionation, absorption, stable system.Reclaimable catalyst goes revivifier regeneration, the catalyzer after the regeneration to return (a) step to recycle.
2. in accordance with the method for claim 1, the decanting point that it is characterized in that low-quality gasoline fraction of described (a) step is the following any position of the second conversion zone cracking stock feed points.
3. in accordance with the method for claim 1, it is characterized in that the feed entrance point of the described second conversion zone feed points for conventional riser reactor cracking stock.
4. in accordance with the method for claim 1, it is characterized in that described (a) step reaction conditions is: 660～720 ℃ of temperature, agent-oil ratio 36～80, weight space velocity 10～100 o'clock
-1
5. in accordance with the method for claim 1, it is characterized in that low-quality gasoline of described (a) step comprises any in straight-run spirit, coker gasoline, visbreaking gasoline, hydrofined gasoline, hydrocracking gasoline, the reforming raffinate oil or the mixing oil that they are two or more.
6. in accordance with the method for claim 1, it is characterized in that the cracking stock that described (b) goes on foot comprises any of solar oil, vacuum gas oil, vacuum residuum, long residuum, coker gas oil, deasphalted oil and crude oil or its mixing oil.
7. in accordance with the method for claim 1, it is characterized in that described catalyzer comprises ZSM-5, contains rare-earth five-membered ring supersiliceous zeolite and REY, a kind of or its mixture in the high-silicon Y-Zeolite is the solid acid catalyst of active ingredient.
8. in accordance with the method for claim 1, it is characterized in that first conversion zone can adopt than second conversion zone reaction tubes of large diameter more, the average linear speed that guarantees first logistics is greater than 0.1 meter per second.
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| Application Number | Priority Date | Filing Date | Title |
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| CN96103408A CN1043782C (en) | 1996-03-21 | 1996-03-21 | Gasoline octane number-raising catalytic conversion method |
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|---|---|---|---|
| CN96103408A CN1043782C (en) | 1996-03-21 | 1996-03-21 | Gasoline octane number-raising catalytic conversion method |
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| CN1160746A CN1160746A (en) | 1997-10-01 |
| CN1043782C true CN1043782C (en) | 1999-06-23 |
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| CN96103408A Expired - Lifetime CN1043782C (en) | 1996-03-21 | 1996-03-21 | Gasoline octane number-raising catalytic conversion method |
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Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1076751C (en) * | 1999-04-23 | 2001-12-26 | 中国石油化工集团公司 | Method for catalytic conversion to prepare isobutane and isoalkane-enriched gasoline |
| WO2001000750A1 (en) * | 1999-06-23 | 2001-01-04 | China Petrochemical Corporation | Catalytic converting process for producing prolifically diesel oil and liquefied gas |
| CN1081220C (en) * | 1999-06-23 | 2002-03-20 | 中国石油化工集团公司 | Catalytic conversion process for modifying gasoline |
| CN1100116C (en) * | 1999-06-23 | 2003-01-29 | 中国石油化工集团公司 | Catalytic transform process for preparing diesel oil and liquified gas with higher outputs |
| CN1100117C (en) * | 2000-01-21 | 2003-01-29 | 中国石油化工集团公司 | Method for increasing liquefied gas yield and gasoline octane number |
| CN1100118C (en) * | 2000-02-22 | 2003-01-29 | 中国石油化工集团公司 | Petroleum hydrocarbon catalytic cracking process of producing diesel oil and high-octane number gasoline |
| CN1100120C (en) * | 2000-08-30 | 2003-01-29 | 中国石油化工股份有限公司 | Catalytic process for modifying light petroleum hydrocarbon |
| CN101993726B (en) * | 2009-08-31 | 2013-11-27 | 中国石油化工股份有限公司 | Method for preparing high-quality fuel oil from inferior crude oil |
| US10266778B2 (en) | 2015-02-04 | 2019-04-23 | China University Of Petroleum-Beijing | Method for upgrading fluid catalytic cracking gasoline |
| CN110857396B (en) * | 2018-08-24 | 2021-11-16 | 中国石油化工股份有限公司 | Method and system for processing coking gasoline and heavy raw oil |
| CN110857395B (en) * | 2018-08-24 | 2021-11-16 | 中国石油化工股份有限公司 | Method and system for processing coking gasoline and heavy raw oil |
| CN110857403B (en) * | 2018-08-24 | 2021-11-16 | 中国石油化工股份有限公司 | Method and system for processing coker gasoline and heavy raw oil by using variable-diameter riser |
| CN110857400B (en) * | 2018-08-24 | 2021-11-16 | 中国石油化工股份有限公司 | Method and system for processing coker gasoline by using double lifting pipes |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4569807A (en) * | 1982-07-16 | 1986-02-11 | Essilor International Cie Generale D'optique | Method and apparatus for molding optical components |
| CN1067258A (en) * | 1991-03-08 | 1992-12-23 | 切夫里昂研究和技术公司 | Low-sulfur reforming processes |
| CN1080313A (en) * | 1992-03-05 | 1994-01-05 | 中国石化洛阳石油化工工程公司 | Catalytic upgrading-aromatization process of poor gasoline |
| US5405525A (en) * | 1993-01-04 | 1995-04-11 | Chevron Research And Technology Company | Treating and desulfiding sulfided steels in low-sulfur reforming processes |
| US5413700A (en) * | 1993-01-04 | 1995-05-09 | Chevron Research And Technology Company | Treating oxidized steels in low-sulfur reforming processes |
-
1996
- 1996-03-21 CN CN96103408A patent/CN1043782C/en not_active Expired - Lifetime
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4569807A (en) * | 1982-07-16 | 1986-02-11 | Essilor International Cie Generale D'optique | Method and apparatus for molding optical components |
| CN1067258A (en) * | 1991-03-08 | 1992-12-23 | 切夫里昂研究和技术公司 | Low-sulfur reforming processes |
| CN1080313A (en) * | 1992-03-05 | 1994-01-05 | 中国石化洛阳石油化工工程公司 | Catalytic upgrading-aromatization process of poor gasoline |
| US5405525A (en) * | 1993-01-04 | 1995-04-11 | Chevron Research And Technology Company | Treating and desulfiding sulfided steels in low-sulfur reforming processes |
| US5413700A (en) * | 1993-01-04 | 1995-05-09 | Chevron Research And Technology Company | Treating oxidized steels in low-sulfur reforming processes |
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| CN1160746A (en) | 1997-10-01 |
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