CN104974783A - Catalytic cracking method - Google Patents
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- CN104974783A CN104974783A CN201410147959.8A CN201410147959A CN104974783A CN 104974783 A CN104974783 A CN 104974783A CN 201410147959 A CN201410147959 A CN 201410147959A CN 104974783 A CN104974783 A CN 104974783A
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Abstract
The invention discloses a catalytic cracking method. In the method, a regenerated catalyst from a cooler is divided into two ways, one is fed into a tubular reactor through a first regenerated catalyst transportation tube and is mixed with raw material oil, which is fed through a material feeding nozzle, and is subjected to a contact reaction, and the other one passes through a heat remover and is fed into the tubular reactor through a second regenerated catalyst transportation tube. The distance between the two inlets that the two ways of regenerated catalyst enter the tubular reactor is 1/3-2/3 of the total length of the tubular reactor. The reacted material flow enters a precipitator for performing solid-gas separation, wherein separated oil gas generated in the reaction is subjected to fractionation in a fractionation system. Separated to-be-regenerated catalyst is subjected to burning regeneration through a burner and a tubular burner, wherein the regenerated catalyst can be recycled after being cooled. By means of the method, the content of olefin in gasoline can be reduced by 10-20% by volume and the octane number (RON) of the gasoline can be increased by 0.1-0.5 units.
Description
Technical field
The invention belongs to hydrocarbon oil catalytic cracking field, particularly a kind of catalyst cracking method.
Background technology
The catalytic cracking of conventional lift tubular type is still the Main Means of China's oil secondary processing at present, and occupies extremely important status in oil refining enterprise of China.But, the catalytic cracking of conventional lift tubular type also exists the problem of following several respects: 1. regenerator temperature achieve effective control cannot cause that finish Contact Temperature is high, agent-oil ratio is low (4 ~ 8), and result is that product slates worsens, dry gas and coke yield is high, total liquid yield is low; 2, the reaction times (generally at about 3 ~ 4s) is long, and the long reaction times exacerbates the secondary reaction of crack materials, reacted gas and coke yield is increased, reduces the yield of vapour, diesel oil distillate; 3, in riser reactor, coked catalyst produces landing back-mixing, and thus on gasoline stock raw material nozzles top, the catalyzer of coking landing contacts with initial stage cracking resultant again with atomized feed, be degrading product slates, reduce the product selectivity of catalyzer to crack materials; 4, the main method reducing self gasoline olefin at present in conventional lift tubular type catalytic cracking unit is not the increase in plant energy consumption, compromises the quality of diesel oil exactly.
In addition, catalytic cracking gasoline olefine content is generally between 40 ~ 60v%.And the share of China's catalytically cracked gasoline in China's gasoline products reaches more than 70%, state IV oil quality causing the olefin(e) centent in gasoline product to perform now far above China requires that the olefin(e) centent of gasoline is not more than the standard of 35v%.Although the alkene in gasoline can drop to very low by traditional hydrofining, significantly have lost the octane value of gasoline.Therefore, domestic each research institution develops various technology for reducing content of olefin in gasoline: the GOR catalyst series (" refining of petroleum and chemical industry " 2002 7 phase 5th ~ 8 pages) of the reduction catalytic gasoline olefin(e) centent of Research Institute of Petro-Chemical Engineering of China Petrochemical Industry exploitation, can make FCC gasoline alkene reduce about 10 percentage points; The LAP series auxiliary agent (" oil refining design " phase calendar year 2001 9 23rd ~ 27 pages) of the reduction catalytic gasoline olefin(e) centent of refining institute of Luoyang Petrochemical engineering corporation of China Petrochemical Industry exploitation, when adding the LAP auxiliary agent of 5% in catalyzer, FCC gasoline alkene can be made to reduce about 10 percentage points.In processing method, the MGD technique (" refining of petroleum and chemical industry " 2002 2 phase 19th ~ 22 pages) that the having of Research Institute of Petro-Chemical Engineering of China Petrochemical Industry exploitation reduces content of olefin in gasoline function, take into account the reaction conditions of main riser tube heavy oil fluid catalytic cracking, the amount of gasoline upgrading is limited, and Olefin decrease amplitude is also not ideal.
Involved by Chinese patent ZL200510017751.5, regenerated catalyst falling temperature technique is the technical superiority utilizing catalytic cracking double lifting leg, and effectively reduce the dry gas of device, coke yield, improve liquid yield, product slates improves.Catalytic gasoline is through lighter hydrocarbons riser tube upgrading, and after upgrading, content of olefin in gasoline is down to 10 ~ 25v%, the range of decrease 25 ~ 50 percentage points; Gasoline octane rating (RON) improves 0.1 ~ 2 unit; Content of sulfur in gasoline reduces by 20 ~ 40%.But it is not enough still to there are following several respects in this technology: 1. regenerator temperature cannot realize flexible control, and this technical superiority is only embodied in the catalytic cracking unit of more than two riser tubes.2., due to the lifting tubular type catalytic cracking that this technology is traditional, still show that long reaction time, dry gas and coke yield are relatively high, product slates relative mistake.3. cause the dry gas of device and coke yield to increase further during the independent upgrading of inferior patrol, reformulated gasoline yield reduces, and plant energy consumption rises.
US Patent No. P:5462652 technology achieves the raw material short reaction time in reacting-settler, and high agent-oil ratio operates, and the reacted gas of device, coke yield are declined, and liquid yield improves, and product slates improves.But this technology does not relate to self generates decreasing by gasoline olefin technology.
Therefore, how to control regenerated catalyst temperature, improve the agent-oil ratio of catalytic cracking reaction, Reaction time shorten, reduce total reacted gas (comprising liquefied gas) and coke yield, and under the prerequisite improving petrol and diesel oil cut yield, reduce self generate gasoline olefin(e) centent to raising oil product of gasoline quality, reduce plant energy consumption, increase economic efficiency significant.
Summary of the invention
The object of the present invention is to provide a kind of catalyst cracking method, existing catalytic cracking process regeneration temperature cannot effectively control to solve, regenerated catalyst and the raw material reaction time is long, agent-oil ratio is low, generate the complex art difficulty of the aspects such as content of olefin in gasoline is high.Use catalyst cracking method of the present invention can reduce reacted gas and coke yield, increase substantially gasoline and diesel oil distillate yield, improve gasoline product quality.
The invention provides a kind of catalyst cracking method, it is characterized in that comprising the steps:
A () is divided into two-way from the regenerated catalyst of water cooler: a road enters tubular reactor and the stock oil mixing and contacting reaction entered through feed nozzle through I regenerated catalyst; Another road enters tubular reactor through heat collector by II regenerated catalyst and carries out strengthening reaction, distance between the entry position that two-way regenerated catalyst enters tubular reactor is 1/3 to 2/3 of tubular reactor total length, reacted logistics enters settling vessel and carries out gas solid separation, isolated reaction generation oil gas enters fractionating system and carries out fractionation, and isolated reclaimable catalyst enters step (b);
B () enters settling vessel stripping stage stripping downwards from the reclaimable catalyst of step (a), reclaimable catalyst after stripping enters and burns device and burn, burn the up tubular type that enters again of the semi regeneration catalyzer generated in device to burn device and burn wind and contact to carry out burning and obtain the catalyzer after regenerating, catalyzer after the regeneration cyclonic separator entered in water cooler carries out catalyzer and is separated with flue gas, isolated flue gas is discharged, the isolated external warmer that is regenerated catalyst through cools the catalyzer after regenerating with the cooling air from cooling air grid distributor, cooled regenerated catalyst recycles.
The further technical characteristic of the present invention is: the described regenerated catalyst temperature entering tubular reactor through I regenerated catalyst is 580 ~ 650 DEG C, and the regenerated catalyst temperature entering tubular reactor through II regenerated catalyst is 430 ~ 550 DEG C.
The further technical characteristic of the present invention is: the operational condition of described tubular reactor is, temperature of reaction is 470 ~ 550 DEG C, preferably 480 ~ 540 DEG C, is preferably 490 ~ 520 DEG C, and total reaction time is 0.5 ~ 1.5s; The regenerated catalyst entering tubular reactor through I regenerated catalyst is 0.3 ~ 1.2s with the contact reacts time of the stock oil entered through feed nozzle, and preferably 0.5 ~ 1.0s, is preferably 0.6 ~ 0.8s, and agent-oil ratio is 5 ~ 10; The contact reacts time of the regenerated catalyst and reaction oil gas that enter tubular reactor through II regenerated catalyst is 0.2 ~ 1.0s, and preferably 0.3 ~ 0.8s, is preferably 0.4 ~ 0.6s; Agent-oil ratio is 4 ~ 8.
The further technical characteristic of the present invention is: described in the temperature of burning of burning in device be 600 ~ 750 DEG C, preferably 620 ~ 720 DEG C, be preferably 660 ~ 700 DEG C; Air linear speed is 0.7 ~ 1.5m/s, and the reclaimable catalyst residence time is 3 ~ 20min, preferably 5 ~ 15min, is preferably 7 ~ 10min.
The further technical characteristic of the present invention is: the temperature of burning that described tubular type is burnt in device is 600 ~ 750 DEG C, and tubular type is burnt bottom device and supplemented fresh Air for burning coke, and its total air linear speed is 3.0 ~ 20m/s, char length 1.0 ~ 10s.
The present invention compared with prior art, has following beneficial effect:
1) the present invention arranges and burns device and tubular type and burn device and carry out compound and burn, and reclaimable catalyst completes the regeneration of catalyzer in compound burning process; Regenerated catalyst is cooled to 580 ~ 650 DEG C by the synergy of external warmer and air by the water cooler arranged, thus realizes catalytic cracking short reaction time, high agent-oil ratio operation.Reach the technique object reducing catalytic cracking reacted gas and coke yield, significantly raising gasoline and diesel oil distillate yield.The complex art difficulty of the aspects such as the Contact Temperature overcoming existing catalytic cracking process regenerated catalyst and raw material is high, long reaction time, agent-oil ratio are low, product slates difference.
2) be divided into two-way from the regenerated catalyst of water cooler and enter tubular reactor respectively: a road enters tubular reactor and the stock oil mixing and contacting reaction entering tubular reactor through feed nozzle, and the temperature that regenerated catalyst enters tubular reactor is 580 ~ 650 DEG C; Another road through heat collector and by regenerated catalyst enter tubular reactor apart from feed entrance point 1/3 to 2/3 place with generate oil gas and carry out strengthening and react, the transformation efficiency of raw material can be improved on the one hand, Olefin decrease reaction can be carried out to the gasoline generated on the other hand.It is 0.3 ~ 0.7 second that regenerated catalyst temperature (430 ~ 550 DEG C) from heat collector to enter in the middle part of tubular reactor with the duration of contact of reaction oil gas, and agent-oil ratio is 4 ~ 8.In tubular reactor, regenerated catalyst and raw material total contact reacts time are 0.5 ~ 1.5s, the average linear speed 5 ~ 20m/s of reaction oil gas, tubular reactor temperature out is 470 ~ 550 DEG C, and total agent-oil ratio is 5 ~ 20, and the absolute pressure of tubular reactor is 0.15 ~ 0.40MPa.
The present invention passes through aforesaid method, make self to generate gasoline olefin(e) centent reduces 10 ~ 20 volume percentage points, gasoline octane rating (RON) improves 0.1 ~ 0.5 unit, the problem that the plant energy consumption caused when solving the self-produced gasoline of catalytic cracking upgrading rises.
3) the present invention's reacted gas productive rate decline compared with Conventional catalytic makes reaction heat reduce, and gasoline generates and obtains upgrading in same tubular reactor, and these factors can make employing energy consumption of the present invention decline, and economic benefit improves.
The present invention is applicable to the catalyzed cracking processing of the various hydro carbons heavy oil of long residuum, vacuum residuum, straight-run gas oil, wax tailings, deasphalted oil, hydrogenation tail oil, recycle stock, slurry oil, shale oil, synthetic oil and coal tar wet goods.
Below in conjunction with accompanying drawing, embodiment and embodiment, the present invention is further detailed explanation.But do not limit the scope of protection of present invention.
Accompanying drawing explanation
Fig. 1 is the device schematic diagram of a kind of catalyst cracking method of the present invention.
Reference numeral shown in figure is:
1-water cooler collection chamber, 2, 3, 18, 19,-water cooler cyclonic separator, 4-water cooler, 5-water cooler dense bed, 6A-I baffle plate, 6B-II baffle plate, 7-cooling air, 8-stripped vapor, 9A-I regenerated catalyst, 9B-II regenerated catalyst, 10-feed nozzle, 11-tubular type burns device, 12-tubular reactor, 13-burns wind distribution rings, 14-reclaimable catalyst flowrate control valve, 15-burns device, 16-main air, 17-mixed flue gas, 20-heat collector, 21-cooling air grid distributor, 22A-I regenerated catalyst flowrate control valve, 22B-II regenerated catalyst flowrate control valve, 23-reaction oil gas (going fractionating system), 24-oil gas collection chamber, 25, 26, 28, 29-settling vessel cyclonic separator, 27-settling vessel, 30-settling vessel stripping stage, 31-regeneration standpipe, 32-inclined tube to be generated, 33-distributor pipe of cardinal wind, 34-stock oil, 35-external warmer.
Embodiment
A kind of catalyst cracking method of the present invention is as follows as shown in Figure 1:
A () is divided into two-way from the regenerated catalyst of water cooler 4: enter tubular reactor 12 and stock oil 34 mixing and contacting reaction entering tubular reactor 12 through feed nozzle 10 through I regenerated catalyst 9A and I regenerated catalyst flowrate control valve 22A under a road direction; Another road is through heat collector 20 heat-obtaining, pass downwardly through II regenerated catalyst 9B and II regenerated catalyst flowrate control valve 22B afterwards to enter tubular reactor 12 and carry out strengthening reaction, the distance between the entry position that described two-way regenerated catalyst enters tubular reactor is 1/3 to 2/3 of tubular reactor total length.Reacted logistics enters settling vessel 27 and carries out gas solid separation through settling vessel cyclonic separator 29 and settling vessel cyclonic separator 25, isolated reaction generation oil gas 23 enters fractionating system through settling vessel collection chamber 24 and carries out fractionation, and isolated reclaimable catalyst enters step (b);
B () enters settling vessel stripping stage 30 downwards from the reclaimable catalyst of step (a) and carries out water vapour 8 stripping.The oil gas be separated with settling vessel cyclonic separator 26 through the settling vessel cyclonic separator 28 of settling vessel 27 and water stripping steam enter fractionating system through settling vessel collection chamber 24 and carry out fractionation; Reclaimable catalyst after settling vessel stripping stage 30 stripping is entered by regeneration standpipe 31 and inclined tube to be generated 32, reclaimable catalyst flowrate control valve 14 and burns device 15 and burn.Enter the reclaimable catalyst burning device 15 to contact with from the main air 16 burning device 15 distributor pipe of cardinal wind 33 and burn, burn the semi regeneration agent generated in device 15 common with flue gas on be advanced into tubular type and burn device 11 and again contact the regeneration of having burnt catalyzer with by burning the supplementary wind that burns entered of wind distribution rings 13.Complete the regenerated catalyst the burnt water cooler cyclonic separator 3 entered in water cooler 4 to carry out catalyzer with water cooler cyclonic separator 2 and be separated with flue gas, isolated mixed flue gas 17 is discharged through water cooler collection chamber 1; Isolated regenerated catalyst enters water cooler 4.In water cooler, by external warmer 35 and the acting in conjunction from the cooling air 7 of cooling air grid distributor 21, regenerator is cooled; Cooling air 7 after intensification and flue gas to be separated with water cooler cyclonic separator 18 through water cooler cyclonic separator 19 and to enter water cooler 4 collection chamber 1 and discharge.The cooled regenerated catalyst of water cooler 4 divides two-way to enter tubular reactor 12 downwards to recycle.
The present invention effectively can control regenerated catalyst temperature, realizes regenerated catalyst and stock oil high agent-oil ratio, short reaction time operation under the operational condition of routine.Reach and significantly reduce reacted gas dry gas and liquefied gas and productive rate, improve gasoline and diesel yield, improve the object generating quality of gasoline. reduce plant energy consumption simultaneously, significantly add the economic benefit of catalytic cracking list covering device..
Water cooler 4 regenerated catalyst temperature control objectives of the present invention is 580 ~ 650 DEG C, and absolute operating pressures is 0.15 ~ 0.40MPa, and dilute phase air linear speed is 0.3 ~ 0.7m/s; The residence time 3 ~ the 5min of regenerated catalyst in water cooler.The cooling air 7 of water cooler 4 is pressurized air, and the Main Function of this cooling air is cooling regenerated catalyst, and cooling air 7 air quantity is determined by heat calculation according to the catalyst inventory of water cooler 4 and control target temperature.
The operational condition of tubular reactor 12 of the present invention is: temperature of reaction is 470 ~ 550 DEG C, preferably 480 ~ 540 DEG C, is preferably 490 ~ 520 DEG C, and total reaction time is 0.5 ~ 1.5s; First via regenerated catalyst and stock oil 34 are 0.3 ~ 1.2s, preferably 0.5 ~ 1.0s by feed nozzle 10 and the contact reacts time of regenerated catalyst, are preferably 0.6 ~ 0.8s; Agent-oil ratio is 5 ~ 10; The contact reacts time of the second road regenerated catalyst and reaction oil gas is 0.2 ~ 1.0s, preferably 0.3 ~ 0.8s, is preferably 0.4 ~ 0.6s; Agent-oil ratio is 4 ~ 8; Described agent-oil ratio is determined by the heat calculation of material each when reacting; Tubular reactor reaction absolute pressure is 0.15 ~ 0.40MPa;
The stripping conditions of settling vessel stripping stage 30 of the present invention is conventional, and stripping fluid is water vapor, and stripping temperature is 480 ~ 520 DEG C.
Device 15 operational condition of burning of the present invention is: burning temperature is 600 ~ 750 DEG C, preferably 620 ~ 720 DEG C, is preferably 660 ~ 700 DEG C; Air linear speed is 0.7 ~ 1.5m/s; The reclaimable catalyst residence time is 3 ~ 20min, preferably 5 ~ 15min, is preferably 7 ~ 10min, burns the device reclaimable catalyst residence time to determine its equipment size.The coke more than 95% of reclaimable catalyst completes wherein and burns, and the main air amount of burning of burning in device 15 can be carried out calculating according to the regeneration required air quantity of spent catalytic cracking catalyst and be determined.
The semi regeneration catalyzer burnt through burning device 15 burns device 11 entrance with generation flue gas in tubular type and contacts with by burning the supplementary wind that burns entered of wind distribution rings 13 and burn the residual coke on device 11 up burning-off semi regeneration catalyzer along tubular type.Tubular type is burnt device 11 and is burnt temperature and to burn device substantially identical, and the air linear speed that tubular type burns device is 3.0 ~ 20m/s, preferably 5.0 ~ 15m/s, is preferably 8 ~ 10m/s; Char length 1.0 ~ 10s, can select tubular type to burn the char length of device according to device height.
Of the present invention burn that device and tubular type burn that device and water cooler adopt burn wind and cooling air is pressurized air, this pressurized air meets the compressed-air actuated general feature of Conventional catalytic cracking device, and its flow can be multiplied by the required air quantity calculating when burning of unit weight coke according to feed material time green coke amount to be determined.
Stock oil 11 of the present invention meets the ingredient requirement of conventional lift tubular type catalytic cracking unit.
What a kind of catalyst cracking method of the present invention adopted is conventional lift tubular type catalytic cracking catalyst.
Concrete operations condition of the present invention and control process, the those of ordinary skill for catalytic cracking field all can be selected according to concrete operations situation.
Comparative example
Test raw material adopts Lip river refining mixed gatch, and catalyzer adopts Lip river refining catalytic cracking industry equilibrium catalyst, and micro-activity is 62.
Catalytic cracking scheme is tested on catalytic cracking riser pilot plant.The regeneration temperature of revivifier inner catalyst is 700 DEG C, and the carbon content of regenerated catalyst is 0.05w%, and micro-activity is 62.The stripping fluid of reacting-settler stripping stage is water vapor, and stripping temperature is 500 DEG C.
Catalytic cracking feeds character is in table 1, and the operational condition of riser catalytic cracking reaction, product slates is in table 2.
Embodiment 1
Test raw material adopts Lip river refining mixed gatch, and catalyzer adopts Lip river refining catalytic cracking industry equilibrium catalyst, and the micro-activity of catalyzer is 62.
Catalytic cracking scheme: carry out on short reaction time catalytic cracking pilot plant, as shown in Figure 1, reclaimable catalyst adopts and burns device and burn to burn after device burns with tubular type and enter water cooler tubular reactor pattern, and micro-activity is 62.The stripping fluid of settling vessel stripping stage is water vapor, and stripping temperature is 500 DEG C.
The operational condition of the present embodiment, product slates and portioned product character are in table 3.
Embodiment 2
By embodiment 1, difference is that the temperature of regenerated catalyst from water cooler, temperature of reaction, raw material are at the agent-oil ratio, reaction times etc. of tubular reactor.The operational condition of the present embodiment device, product slates and portioned product character are in table 4.
Embodiment 3
By embodiment 1, difference is that the temperature of regenerated catalyst from water cooler, temperature of reaction, raw material are at the agent-oil ratio, reaction times etc. of tubular reactor.The operational condition of the present embodiment device, product slates and portioned product character are in table 5.
Embodiment 4
By embodiment 1, difference is that the temperature of regenerated catalyst from water cooler, temperature of reaction, raw material are at the agent-oil ratio, reaction times etc. of tubular reactor.The operational condition of the present embodiment device, product slates and portioned product character are in table 6.
Table 1 catalytic cracking feeds character (comparative example)
| Catalytic cracking feeds charging | Lip river refining mixed gatch |
| Density (20 DEG C), kgm -3 | 901.2 |
| Carbon residue, w% | 0.32 |
| Group composition, w% | |
| Stable hydrocarbon | 57.5 |
| Aromatic hydrocarbons | 39.8 |
| Colloid+bituminous matter | 2.7 |
| Sulphur content, μ gg -1 | 1700 |
| Nitrogen content, w% | 0.2706 |
| Ni，μg·g -1 | 2.6 |
| V，μg·g -1 | 0.2 |
The operational condition of table 2 Conventional riser catalytic cracking, product slates and portioned product character (comparative example)
The operational condition of the catalytic cracking of table 3 Conventional riser and embodiment 1, product slates and portioned product character
| Project | Riser tube | Tubular reactor |
| Tubular reactor temperature out, DEG C | 480 | 480 |
| One period of reaction times, s | 3.9 | 1.0 |
| One section of agent-oil ratio | 4.2 | 6.3 |
| The second-stage reaction time, s | 0.3 | |
| Two sections of agent-oil ratios | 4.1 | |
| Reaction absolute pressure, MPa | 0.22 | 0.25 |
| Regenerator temperature, DEG C | 705 | |
| Water cooler catalyzer dense phase temperature, DEG C | 620 | |
| The close phase linear speed of water cooler, m/s | 0.5 | |
| Water cooler catalyst residence times, min | 3.0 | |
| Heat collector outlet catalyst temperature, DEG C | 480 | |
| Burn device char length, min | / | 20.0 |
| Burn device and burn linear speed, m/s | / | 0.7 |
| Burn device and burn temperature, DEG C | / | 630 |
| Tubular type burns device temperature out, DEG C | / | 630 |
| Tubular type burns device char length, s | / | 10 |
| Tubular type burns device linear speed, m/s | / | 3.5 |
| Product slates, w% | ||
| Dry gas | 3.70 | 1.83 |
| Liquefied gas | 11.61 | 7.11 |
| Gasoline (< 204 DEG C) | 46.61 | 48.7 |
| Diesel oil (< 360 DEG C) | 33.70 | 38.06 |
| Coke | 3.95 | 3.90 |
| Loss | 0.43 | 0.40 |
| Add up to | 100 | 100 |
| Gasoline+diesel yield, w% | 80.31 | 86.76 |
| Gasoline RON | 90.3 | 90.5 |
| Diesel cetane-number | 30 | 33 |
| Generate content of olefin in gasoline, v% | 47 | 35 |
The operational condition of the catalytic cracking of table 4 Conventional riser and embodiment 2, product slates and portioned product character
| Project | Riser tube | Tubular reactor |
| Tubular reactor temperature out, DEG C | 510 | 510 |
| One period of reaction times, s | 3.5 | 0.7 |
| One section of agent-oil ratio | 5.9 | 9.5 |
| The second-stage reaction time, s | 0.5 | |
| Two sections of agent-oil ratios | 5.5 | |
| Reaction absolute pressure, MPa | 0.23 | 0.25 |
| Regenerator temperature, DEG C | 707 | |
| Chiller temperature, DEG C | 600 | |
| The close phase linear speed of water cooler, m/s | 0.6 | |
| Water cooler catalyst residence times, min | 4.0 | |
| Heat collector outlet catalyst temperature, DEG C | 510 | |
| Burn device char length, min | / | 15.0 |
| Burn device and burn linear speed, m/s | / | 1.0 |
| Burn device and burn temperature, DEG C | / | 660 |
| Tubular type burns device temperature out, DEG C | / | 660 |
| Tubular type burns device char length, s | / | 5.0 |
| Tubular type burns device linear speed, m/s | / | 7.0 |
| Product slates, w% | ||
| Dry gas | 4.16 | 2.13 |
| Liquefied gas | 16.71 | 11.91 |
| Gasoline (< 204 DEG C) | 47.51 | 50.14 |
| Diesel oil (< 360 DEG C) | 27.60 | 31.56 |
| Coke | 3.60 | 3.56 |
| Loss | 0.42 | 0.40 |
| Add up to | 100 | 100 |
| Gasoline+diesel yield, w% | 75.11 | 81.70 |
| Gasoline RON | 90.7 | 91.1 |
| Diesel cetane-number | 29.0 | 31 |
| Generate content of olefin in gasoline, v% | 45 | 33 |
The operational condition of the catalytic cracking of table 5 Conventional riser and embodiment 3, product slates and portioned product character
| Project | Riser tube | Tubular reactor |
| Tubular reactor temperature out, DEG C | 530 | 530 |
| One period of reaction times, s | 3.2 | 0.43 |
| One section of agent-oil ratio | 7.6 | 10.0 |
| The second-stage reaction time, s | 0.6 | |
| Two sections of agent-oil ratios | 6.0 | |
| Reaction absolute pressure, MPa | 0.23 | 0.25 |
| Regenerator temperature, DEG C | 704 | |
| Chiller temperature, DEG C | / | 650 |
| The close phase linear speed of water cooler, m/s | / | 0.7 |
| Water cooler catalyst residence times, min | / | 3.0 |
| Heat collector outlet catalyst temperature, DEG C | 530 | |
| Burn device char length, min | / | 5.0 |
| Burn device and burn linear speed, m/s | / | 1.3 |
| Burn device and burn temperature, DEG C | / | 680 |
| Tubular type burns device temperature out, DEG C | / | 680 |
| Tubular type burns device char length, s | / | 2.0 |
| Tubular type burns device linear speed, m/s | / | 15 |
| Product slates, w% | ||
| Dry gas | 5.61 | 2.42 |
| Liquefied gas | 20.72 | 12.76 |
| Gasoline (< 204 DEG C) | 49.80 | 55.76 |
| Diesel oil (< 360 DEG C) | 20.05 | 25.35 |
| Coke | 3.35 | 3.29 |
| Loss | 0.40 | 0.42 |
| Add up to | 100 | 100 |
| Gasoline+diesel yield, w% | 69.85 | 81.11 |
| Gasoline RON | 92.1 | 92.4 |
| Diesel cetane-number | 27.4 | 30 |
| Generate content of olefin in gasoline, v% | 44 | 32 |
The operational condition of table 6 embodiment 4, product slates and portioned product character
| Project | Tubular reactor |
| Tubular reactor temperature out, DEG C | 530 |
| One period of reaction times, s | 0.35 |
| One section of agent-oil ratio | 9.5 |
| The second-stage reaction time, s | 0.7 |
| Two sections of agent-oil ratios | 6.3 |
| Reaction absolute pressure, MPa | 0.24 |
| Chiller temperature, DEG C | 580 |
| The close phase linear speed of water cooler, m/s | 0.6 |
| Water cooler catalyst residence times, min | 4.0 |
| Heat collector outlet catalyst temperature, DEG C | 530 |
| Burn device char length, min | 10 |
| Burn device and burn linear speed, m/s | 0.7 |
| Burn device and burn temperature, DEG C | 620 |
| Tubular type burns device temperature out, DEG C | 620 |
| Tubular type burns device char length, s | 3.2 |
| Tubular type burns device linear speed, m/s | 8.0 |
| Product slates, w% | |
| Dry gas | 2.67 |
| Liquefied gas | 10.72 |
| Gasoline (< 204 DEG C) | 49.45 |
| Diesel oil (< 360 DEG C) | 33.12 |
| Coke | 3.59 |
| Loss | 0.45 |
| Add up to | 100 |
| Gasoline+diesel yield, w% | 81.57 |
| Gasoline RON | 92.6 |
| Diesel cetane-number | 32 |
| Generate content of olefin in gasoline, v% | 26 |
Claims (9)
1. a catalyst cracking method, is characterized in that comprising the steps:
A () is divided into two-way from the regenerated catalyst of water cooler: a road enters tubular reactor and the stock oil mixing and contacting reaction entered through feed nozzle through I regenerated catalyst; Another road enters tubular reactor through heat collector by II regenerated catalyst, distance between the entry position that two-way regenerated catalyst enters tubular reactor is 1/3 to 2/3 of tubular reactor total length, reacted logistics enters settling vessel and carries out gas solid separation, isolated reaction generation oil gas enters fractionating system and carries out fractionation, and isolated reclaimable catalyst enters step (b);
B () enters settling vessel stripping stage stripping downwards from the reclaimable catalyst of step (a), reclaimable catalyst after stripping enters and burns device and burn, burn the up tubular type that enters again of the semi regeneration catalyzer generated in device to burn device and burn wind and contact to carry out burning and obtain the catalyzer after regenerating, catalyzer after the regeneration cyclonic separator entered in water cooler carries out catalyzer and is separated with flue gas, isolated flue gas is discharged, the isolated external warmer that is regenerated catalyst through cools the catalyzer after regenerating with the cooling air from cooling air grid distributor, cooled regenerated catalyst recycles.
2. cracking method according to claim 1, it is characterized in that: the described regenerated catalyst temperature entering tubular reactor through I regenerated catalyst is 580 ~ 650 DEG C, and the regenerated catalyst temperature entering tubular reactor through II regenerated catalyst is 430 ~ 550 DEG C.
3. cracking method according to claim 1, is characterized in that: the operational condition of described tubular reactor is, temperature of reaction is 470 ~ 550 DEG C, and total reaction time is 0.5 ~ 1.5s; The regenerated catalyst entering tubular reactor through I regenerated catalyst is 0.3 ~ 1.2s with the contact reacts time of the stock oil entered through feed nozzle, and agent-oil ratio is 5 ~ 10; The contact reacts time of the regenerated catalyst and reaction oil gas that enter tubular reactor through II regenerated catalyst is 0.2 ~ 1.0s; Agent-oil ratio is 4 ~ 8.
4. cracking method according to claim 3, it is characterized in that: the temperature of reaction of described tubular reactor is 480 ~ 540 DEG C, the regenerated catalyst entering tubular reactor through I regenerated catalyst is 0.5 ~ 1.0s with the contact reacts time of the stock oil entered through feed nozzle, and the contact reacts time of the regenerated catalyst and reaction oil gas that enter tubular reactor through II regenerated catalyst is 0.3 ~ 0.8s.
5. cracking method according to claim 4, it is characterized in that: the temperature of reaction of described tubular reactor is 490 ~ 520 DEG C, through contact reacts time of I the regenerated catalyst regenerated catalyst entering tubular reactor and the stock oil entered through feed nozzle for being 0.6 ~ 0.8s, the contact reacts time of the regenerated catalyst and reaction oil gas that enter tubular reactor through II regenerated catalyst is 0.4 ~ 0.6s.
6. cracking method according to claim 1, is characterized in that: described in the temperature of burning of burning in device be 600 ~ 750 DEG C, air linear speed is 0.7 ~ 1.5m/s, and the reclaimable catalyst residence time is 3 ~ 20min.
7. cracking method according to claim 6, is characterized in that: described in the temperature of burning of burning in device be 620 ~ 720 DEG C, the reclaimable catalyst residence time is 5 ~ 15min.
8. cracking method according to claim 7, is characterized in that: described in the temperature of burning of burning in device be 660 ~ 700 DEG C; The reclaimable catalyst residence time is 7 ~ 10min.
9. cracking method according to claim 1, is characterized in that: the temperature of burning that described tubular type is burnt in device is 600 ~ 750 DEG C, and tubular type is burnt bottom device and supplemented fresh Air for burning coke, and its total air linear speed is 3.0 ~ 20m/s, char length 1.0 ~ 10s.
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| CN110624481A (en) * | 2018-06-22 | 2019-12-31 | 中国石油化工股份有限公司 | Catalytic reaction equipment and method |
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