CN102212382B - Catalytic cracking process and device - Google Patents
Catalytic cracking process and device Download PDFInfo
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- CN102212382B CN102212382B CN 201010139860 CN201010139860A CN102212382B CN 102212382 B CN102212382 B CN 102212382B CN 201010139860 CN201010139860 CN 201010139860 CN 201010139860 A CN201010139860 A CN 201010139860A CN 102212382 B CN102212382 B CN 102212382B
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Abstract
The invention discloses a catalytic cracking process and a catalytic cracking device. A main technical scheme is that: a regenerator is placed on the upper part of a reaction precipitator; a regenerated catalyst from the regenerator downwards enters the reaction precipitator to generate forward or backward contact reaction with raw oil entering the reaction precipitator through a feeding nozzle; after the reaction, the spent catalyst and the generated oil gas are subjected to separation and steam stripping; the generated oil gas subjected to separation and steam stripping enters a fractionating system to perform fractionation; the spent catalyst subjected to separation and steam stripping enters a tube type burning device to burn and regenerate; and the semi-regenerated catalyst regenerated by the tube type burning device enters a regenerator again to regenerate and then is recycled. By the catalytic cracking process and the catalytic cracking device, burning capacity can be enhanced and the treating quantity of raw materials is increased. The catalytic cracking process and the catalytic cracking device have the advantages of low contact temperature of the catalyst and the raw oil, short reaction time, big ratio of the catalyst to the oil, low yield of cracked gas and coke, high yield of gasoline and diesel, high product distributivity, simple device structure, operating flexibility, low energy consumption and the like.
Description
Technical field
The invention belongs to the hydrocarbon oil catalytic cracking field, particularly a kind of short distance, efficient catalytic cracking technology and device.
Background technology
At present, each riser reactor top exit of employed single or many riser fluid catalytic crackings is connected with separately settling vessel respectively in the petroleum chemical industry catalytic cracking process, and the bottom is connected with revivifier by inclined tube to be generated and regeneration standpipe separately.In above-mentioned conventional catalytic cracking unit, the problem that following several respects are arranged: first, be that regenerator temperature can't realize flexible control, the regeneration temperature of catalyzer generally all is higher than 650 ℃, make in the riser reactor finish moment contact temperature higher, too high finish contact temperature can add the tool heat cracking reaction, reduce the degree of catalytic cracking reaction, the result is that the product distribution worsens, dry gas and coke yield rise, total liquid yield descends, and (total liquid yield refers to liquefied gas yield, gasoline yield and diesel yield sum), because higher regenerated catalyst temperature, limited by device thermal equilibrium, make the agent-oil ratio of heavy oil riser reactor less relatively, be generally 5～8 (agent-oil ratio of riser reactor is the ratio of weight internal circulating load with the weight rate of heavy oil riser reactor charging of riser reactor inner catalyst); The second, owing to promote the reaction times (generally about 4s) that the length of tubular reactor has determined raw material.The long reaction times has also been aggravated the secondary reaction of raw material cracking resultant when improving the raw material per pass conversion, make the reacted gas gain in yield, thereby has reduced the yield of vapour, diesel oil distillate; The 3rd, owing to being higher than the catalyzer linear speed, the oil gas linear speed in the lifting tubular reactor cause the landing of coking catalyzer to form back-mixing, thus, promoting tubular type reactor feedstocks nozzle top, the catalyzer of coking landing contacts with initial stage cracking resultant again with atomized feed, thereby worsened the product distribution, reduced the product selectivity of catalyzer to the raw material cracking; The 4th, because revivifier carbon-burning capacity and to burn efficient relatively low, make the size of revivifier big and catalyst inventory is higher, cause facility investment relatively large.
The related regenerated catalyst falling temperature technique of Chinese patent ZL200510017751.5 is the technical superiority of utilizing the catalytic cracking double lifting leg, the spent agent that remains with high remaining activity (be equivalent to regenerator activity 90%), low temperature (about 500 ℃) after the lighter hydrocarbons riser tube reaction is partly or entirely returned the mixing tank that heavy oil riser tube bottom arranges, in mixing tank with after regenerated catalyst from revivifier mixes, enter heavy oil riser tube and heavy oil contact reacts.Because the heat exchange action of two strands of catalyzer effectively drops to about 630 ℃ the temperature of mixed catalyst in the mixing tank, enter heavy oil riser tube and heavy feed stock contact reacts, agent-oil ratio is significantly improved, and effectively reduce dry gas, the coke yield of device, liquid yield improves, product distributes and improves, and the economic benefit of refinery improves.But there is following some deficiency in this technology: at first, regenerator temperature can't realize flexible control, and this technical superiority only is embodied in the catalytic cracking unit of two above riser tubes.Secondly, because this technology is traditional lifting tubular type catalytic cracking, shown still that long reaction time, dry gas and coke yield are high relatively, product distribution relative mistake, the revivifier carbon-burning capacity is low and the high deficiency of plant energy consumption.
The related high efficiency regenerating technology for molecular sieve catalyst technology of Chinese patent ZL97106088.6 mainly comprises: 1. reclaimable catalyst enters the external cyclone water-separator group after the regeneration of the first root regeneration pipe, enters the second root regeneration pipe through dipleg.2. the second root regeneration pipe external cyclone water-separator group dipleg directly enters external warmer, and inclined tube enters riser reactor through the bottom.Technology was burnt the time in 10 seconds, burnt intensity (per hour, the burning carbon amount of catalyzer per ton) and be about 10 times of prior art.But also there are following 2 deficiencies in this technology: 1. employing promotes tubular reactor and can't realize the raw material short reaction time.2. technological process and complicated operation are difficult to carry out on the engineering.
The related a kind of catalytic cracking riser coke burning regeneration device technical characterstic of Chinese patent ZL93242428.7 is: riser regenerator is provided with the multistage air inlet and carries out reclaimable catalyst regeneration, strengthened the coke burning regeneration process of reclaimable catalyst, it is simple in structure, and is easy to operate.But there is the lifting tubular reactor in this technology and can't realizes the operation of raw material short reaction time.
The related technology features of US Patent No. P:5462652 is: 1. reacting-settler top arranges the catalyst mix jar, and mixing tank adopts water vapor to carry out the even mixing of catalyzer; The reacting-settler top arranges the mixed catalyst chamber, and catalyzer enters reacting-settler by mixed catalyst chamber central opening.2. the stripping of the reaction of catalyzer and raw material and reclaimable catalyst all carries out in reacting-settler, and catalyzer flows and is directed downwards, and the raw material injection direction of nozzle becomes 90 ° of angles, the plug-in cyclonic separator of reacting-settler with the mobile direction of catalyzer.3. a part of reclaimable catalyst is promoted to revivifier by first air-lift tube and carries out coke burning regeneration, another part reclaimable catalyst is promoted to the catalyst mix jar by second air-lift tube, and the catalyzer after the regeneration is promoted to the catalyst mix jar by the 3rd air-lift tube and mixes to reduce the mixed catalyst temperature that enters reacting-settler with reclaimable catalyst.Because above feature, US Patent No. P:5462652 technology realize the raw material short reaction time in reacting-settler, low finish contact temperature, the high agent-oil ratio operation descends the dry gas of device, coke yield, and liquid yield improves, and product distributes and improves.But still there is following some deficiency in this technology: 1. adopt conventional catalytic cracking regenerator, its carbon-burning capacity is low.2. participate in catalyst for reaction and be the catalyzer after regenerating and the mixture of reclaimable catalyst, this mixed catalyst must be affected to the cracking activity of raw material, also certainly will distribute to product and bring disadvantageous effect.3. technological process and complicated operation.
Therefore, reduce and control the temperature of regenerated catalyst, the agent-oil ratio of raising catalytic cracking reaction, shorten the reaction times and adopt tubular type to burn to improve and regenerate carbon-burning capacity and burn efficient, reduce dry gas (even comprising liquefied gas) and coke yield to the catalyst inventory of the product distribution that improves heavy oil fluid catalytic cracking and product property, reduction plant energy consumption, reduction revivifier, dwindle the revivifier size and reduce facility investment and have important effect.
Summary of the invention
Technical problem to be solved by this invention is: a kind of short distance is provided, efficient catalytic cracking technology and device, this technology and device have been realized implementing reclaimable catalyst tubular type coke burning regeneration and controlling the catalyst temperature (between 580～650 ℃) of revivifier in catalytic cracking unit, adopt the short reaction time (reaction times is between 0.01～1.0s), high agent-oil ratio (5～30) is operated, reach and reduce reacted gas (comprising dry gas and liquefied gas) and coke yield, significantly improve the process goal of gasoline and diesel oil distillate yield, and overcome the catalyst temperature that existing catalytic cracking process is in revivifier under the existing catalytic cracking process superiority condition and can't control flexibly keeping, regenerated catalyst and raw material contact the temperature height, long reaction time, the low complex art difficulty that reaches aspects such as the device carbon-burning capacity is low of agent-oil ratio.
The invention provides a kind of catalytic cracking process, its technical scheme is:
(a) regenerated catalyst in the revivifier enters reacting-settler downwards, with the stock oil that enters reacting-settler through feed nozzle in the same way or reverse contact reacts, reaction back logistics separates, isolated reaction generation oil gas enters fractionating system and carries out fractionation, and isolated reclaimable catalyst enters step (b);
(b) entering tubular type from the reclaimable catalyst of step (a) behind the water vapour stripping burns device and carries out coke burning regeneration, enter revivifier afterwards, carrying out catalyzer through cyclonic separator separates with flue gas, flue gas after the separation is discharged revivifier, half regenerated catalyst after the separation carries out coke burning regeneration at the regenerated catalyst dense bed, and the regenerated catalyst after the regeneration recycles.
Catalytic cracking process of the present invention is further characterized in that: the regenerated catalyst temperature that enters in the reacting-settler is 580～650 ℃, and the contact reacts time of stock oil and regenerated catalyst is 0.01～1.0s; Temperature of reaction is 480～580 ℃, and agent-oil ratio (being the weight ratio of catalyzer and stock oil) is 5～30, and the reaction absolute pressure is 0.15～0.40MPa.
Catalytic cracking process of the present invention is further characterized in that: the temperature of burning that tubular type is burnt in the device is 600～720 ℃, and the air linear speed is 1.0～5m/s, and burning intensity is 300～1000kg.t
-1.h
-1, burn time 8～40s.
Catalytic cracking process of the present invention is further characterized in that: revivifier catalyzer dense bed temperature is 580～650 ℃.
The present invention also provides a kind of catalytic cracking unit, it is characterized in that: this device comprises revivifier, reacting-settler and tubular type are burnt device, revivifier comprises cyclonic separator and distributor pipe of cardinal wind, reacting-settler comprises cyclonic separator and reacting-settler stripping stage, the bottom of reacting-settler is the reacting-settler stripping stage, tubular type is burnt device and is comprised and burn the wind distribution pipe, revivifier is connected with settling vessel by regenerated catalyst, the regenerated catalyst flowrate control valve is set on the regenerated catalyst, reacting-settler stripping stage bottom is burnt the device bottom by inclined tube to be generated and tubular type and is connected, inclined tube to be generated middle part arranges the reclaimable catalyst flowrate control valve, and tubular type is burnt the interior cyclonic separator of device top exit and revivifier and is connected.
Catalytic cracking unit of the present invention is further characterized in that: revivifier is arranged on the reacting-settler top, but revivifier and reacting-settler coaxial arrangement, but also disalignment is arranged.
Catalytic cracking unit of the present invention is further characterized in that: the regenerated catalyst entrance is arranged on the revivifier catalyzer dense bed top of revivifier, outlet is arranged on the inside of reacting-settler, and the vertical height L at the reclaimable catalyst dense bed interface in outlet position and the settling vessel is 2～6M.
Catalytic cracking unit of the present invention is further characterized in that: regenerated catalyst adopts cross section to be circular metal tube, Φ 200～3000mm, and the position can be arranged in revivifier and the settling vessel any position radially.
Catalytic cracking unit of the present invention is further characterized in that: the mobile direction of the feed nozzle Way out in the reacting-settler and regenerated catalyst arranges in the same way, its position is arranged on the medullary ray of regenerated catalyst outlet in the reacting-settler, feed nozzle exit end and regenerated catalyst outlet are in same level height, and feed nozzle meets the general feature of conventional catalytic cracking unit feed nozzle.
Catalytic cracking unit of the present invention is further characterized in that: the reverse setting of direction of flowing of the feed nozzle Way out in the reacting-settler and regenerated catalyst, its position is arranged on the medullary ray of regenerated catalyst outlet in the reacting-settler, the feed nozzle outlet is 2～6M with regenerated catalyst exit separation H, and is positioned at reacting-settler reclaimable catalyst dense bed top.
Catalytic cracking unit of the present invention is further characterized in that: described tubular type is burnt the device middle and upper part can arrange heat collector.
Catalytic cracking unit of the present invention is further characterized in that: described revivifier can arrange external warmer.
The present invention compared with prior art has following beneficial effect:
1. burn in the device in tubular type, burning air flow quantity can adjust flexibly, and the reclaimable catalyst amount of unit time enters tubular type and burns device bottom and contact and strengthened the carbon-burning capacity that tubular type is burnt device with the oxygen containing fresh air that burns capacity, rich all the time, make tubular type burn device and burn the intensity increase, improved the efficient of burning that tubular type is burnt device.But tubular type is burnt on the device burning-off reclaimable catalyst 70～80% coke.Tubular type is burnt device, and to burn temperature be that 600～720 ℃, air linear speed are 1.0～5m/s, burn time 8～40s; Tubular type is burnt device, and to burn intensity (per hour, the burning carbon amount of catalyzer per ton) be 300～1000kg.t
-1.h
-1, tubular type is burnt device and is compared with conventional catalytic cracking unit regeneration and have stronger carbon-burning capacity and turndown ratio more flexibly.
2. heavy oil fluid catalytic cracking finish contact temperature is high can aggravate the heat cracking reaction of raw material, the degree of reduction catalytic cracking reaction, the result is that the product distribution worsens, and dry gas and coke yield rise, total liquid yield descends (total liquid yield refers to liquefied gas yield, gasoline yield and diesel yield sum).Adopt revivifier main air cooling regenerated catalyst technology, can effectively control regenerated catalyst temperature between 580～650 ℃, thereby reduce the temperature that contacts of regenerated catalyst and raw material, reach the dry gas, the coke yield that reduce device, improve liquid yield, improve product and distribute, improve the purpose of the economic benefit of refinery.
3. in catalytic cracking process, the long reaction times has also been aggravated the secondary reaction of raw material cracking resultant when improving the raw material per pass conversion, make the reacted gas gain in yield, thereby has reduced the yield of vapour, diesel oil distillate; The high agent-oil ratio operation can remedy the raw material per pass conversion dampening factor that brings owing to the short reaction time.Adopt short contact reaction times (reaction times is between 0.01～1.0s), high agent-oil ratio 5～30 operations of regenerated catalyst and raw material, can reduce reacted gas (comprising dry gas and the liquefied gas) productive rate of device, make the yield of vapour, diesel oil distillate obtain increasing, improved the utilization ratio of petroleum resources.
4. device dry gas, coke yield descend, and the energy consumption of device is reduced.Tubular type is burnt device and is burnt the catalyst inventory that the intensity burning carbon amount of catalyzer per ton (per hour) can reduce revivifier greatly, and the size of revivifier is dwindled, and plant investment descends.
The present invention is applicable to the catalyzed cracking processing of long residuum, vacuum residuum, straight-run gas oil, wax tailings, deasphalted oil, hydrogenation tail oil, recycle stock, slurry oil, crude oil, shale oil, synthetic oil and the various hydro carbons heavy oil of coal tar wet goods.
The present invention is further detailed explanation below in conjunction with accompanying drawing, embodiment and embodiment.But do not limit the scope of protection of present invention.
Accompanying drawing and description of drawings
Fig. 1 is a kind of catalytic cracking unit synoptic diagram of the present invention.
Fig. 2 is the another kind of catalytic cracking unit synoptic diagram of the present invention.
Reference numeral shown in the figure is:
1,14, the 19-cyclonic separator, 2-revivifier, 3-regenerated catalyst dense bed, the 4-regenerated catalyst, 5-distributor pipe of cardinal wind, 6-regenerated catalyst flowrate control valve, 7-stock oil, 8-reacting-settler, 9-reclaimable catalyst dense bed, 10-reacting-settler stripping stage, 11-inclined tube to be generated, 12-flue gas, 13-regenerated flue gas collection chamber, the 15-tubular type is burnt device, 16-main air, 17-oil gas collection chamber, the 18-reaction generates oil gas, the 20-feed nozzle, 21-water vapor, 22-reclaimable catalyst flowrate control valve, 23-burns wind, 24-burns the wind distribution pipe, 26-heat collector, 27-external warmer.
Embodiment
A kind of short distance of the present invention, efficient catalytic cracking unit as shown in Figure 1, this device comprise that revivifier 2, reacting-settler 8, tubular type burn device 15 three parts and form.Press the flow process of device inner catalyst, be provided with revivifier 2, regenerated catalyst 4, regenerated catalyst flowrate control valve 6 successively; Reacting-settler 8, reacting-settler stripping stage 10 and tubular type are burnt device 15.Revivifier 2 is connected with reacting-settler 8 by regenerated catalyst 4, on the regenerated catalyst 4 between revivifier 2 and the reacting-settler 8 regenerated catalyst flowrate control valve 6 is set, the bottom of reacting-settler 8 is reacting-settler stripping stage 10, and reacting-settler stripping stage 10 bottoms of reacting-settler 8 are burnt device 15 bottoms by inclined tube 11 to be generated and tubular type and are connected.Inclined tube to be generated 11 middle parts arrange reclaimable catalyst flowrate control valve 22, and the cyclonic separator 14 that tubular type is burnt in device 15 top exits and the revivifier 2 is connected.The dipleg of cyclonic separator 14 enters in the regenerated catalyst dense bed 3.
Described revivifier 2 comprises cyclonic separator 14 and cyclonic separator 1, and the size of cyclonic separator 14 and cyclonic separator 1 and structure determine to meet the conventional general feature that promotes tubular type catalytic cracking unit revivifier.It is circular metal tube that the pipeline of regenerated catalyst 4 adopts cross section, and internal diameter is Φ 200～2000mm, and its diameter is determined according to the stream pipe method of calculation of flooding that routine promotes in the tubular type catalytic cracking unit revivifier.
Described regenerated catalyst flowrate control valve 6 is located on the regenerated catalyst 4 that links to each other between revivifier 2 and the reacting-settler 8, can adopt various flowrate control valves commonly used (as adopting guiding valve), to regulate the regenerated catalyst flow, realize the temperature of reaction control to reacting-settler 8.
Described regenerated catalyst 4 entrances are arranged on below, regenerated catalyst dense bed 3 interfaces, and its set-up mode and position can be determined with reference to the stream pipe that floods in the conventional catalytic cracking unit revivifier.Outlet is arranged on the inside of reacting-settler 8, and the spacing L at reclaimable catalyst dense bed 9 interfaces in outlet position and the reacting-settler 8 is 2～6M.
Described reacting-settler 8 comprises cyclonic separator 19 and reacting-settler stripping stage 10, and its size and structure determine to meet the conventional general calculated characteristics that promotes tubular type catalytic cracking unit settling vessel.
The mobile direction of feed nozzle 20 Way outs in the described reacting-settler 8 and regenerated catalyst arranges in the same way, its position is arranged on the medullary ray that is arranged in 4 outlets of reacting-settler 8 regenerated catalyst, feed nozzle 20 outlet ports and regenerated catalyst 4 outlets are in same level height, and feed nozzle 20 meets the general feature of conventional catalytic cracking unit feed nozzle.
It is circular metal tube that described inclined tube to be generated 11, pipeline adopt cross section, and liner insulating and wearing-resistant lining, internal diameter are Φ 300～2000mm, and its diameter promotes tubular type catalytic cracking unit inclined tube method of calculation to be generated according to routine and determines.The stripping stage 10 that reclaimable catalyst flowrate control valve 22 is located at reacting-settler 8 burns on the inclined tube to be generated 11 that links to each other between the device 15 with tubular type, can adopt various flowrate control valves commonly used (as adopting guiding valve), to regulate the reclaimable catalyst flow.
Described tubular type is burnt device 15 and is adopted cross section to be circular metal tube, the liner insulating and wearing-resistant lining, and length is 20～40M, Φ 400～2500mm; Tubular type is burnt device 15 bottoms distribution pipe 24 is set, and the size of distribution pipe 24 is determined according to the distribution pipe method of calculation that routine promotes the tubular type catalytic cracking unit.The concrete diameter that tubular type is burnt device 15 determines according to burning the operating linear velocity that wind 23 burns device 15 in tubular type, and tubular type is burnt device 15 length and determined according to the total height of revivifier 2 and reacting-settler 8.
The another kind of short distance of the present invention, efficient catalytic cracking unit as shown in Figure 2, the difference of itself and Fig. 1 is: described tubular type is burnt device 15 middle and upper parts heat collector 26 is set; Described revivifier arranges external warmer 27.Described feed nozzle 20 and the mobile reverse setting of direction of regenerated catalyst, the position is arranged on the medullary ray of regenerated catalyst 4 outlets in the reacting-settler 8, feed nozzle 20 outlets are 2～6M with regenerated catalyst 4 exit separation H, and are positioned at top, reacting-settler 8 reclaimable catalyst dense beds 9 interfaces.
A kind of short distance of the present invention, efficient catalytic cracking method are as follows as shown in Figure 1: the regenerated catalyst from revivifier 2 enters reacting-settler 8 by regenerated catalyst 4 and regenerated catalyst flowrate control valve 6.Stock oil 7 enters reacting-settler 8 by feed nozzle 20, and stock oil 7 contacts in the same way with the regenerated catalyst short period of time that enters reacting-settler 8 and reacts.After reaction finished, reactant flow was separated with the cyclonic separator 19 of stripped vapor water vapor 21 in reacting-settler 8, isolated reaction and generated oil gas 18 and reclaimable catalyst.The oil gas collection chamber 17 of isolated reaction generation oil gas 18 in reacting-settler 8 enters fractionating system and carries out fractionation; Isolated reclaimable catalyst enters tubular type by inclined tube 11 to be generated and reclaimable catalyst flowrate control valve 22 at the reacting-settler stripping stage 10 of reacting-settler 8 and burns device 15 bottoms and burn from distribution pipe 24 that wind 23 contacts and burn the device 15 up reclaimable catalyst coke burning regenerations that carry out along tubular type behind water vapor 21 strippings.Burning half regenerated catalyst after device 15 regeneration by tubular type enters cyclonic separator 14 in the revivifier 2 and carries out catalyzer and separate with flue gas.Half regenerated catalyst after the separation enters in the regenerated catalyst dense bed 3 of revivifier 2 through the dipleg of cyclonic separator 14, main air 16 enters revivifier 2 by distribution pipe 5 bottom contacts the residual coke on burning-off half regenerated catalyst and cools off regenerated catalyst with half regenerated catalyst, the regeneration rear catalyst enters regenerated catalyst 4 and recycles.The flue gas 12 that generates is discharged revivifier 2 by regenerated flue gas collection chamber 13 again after cyclonic separator 1 separates.Above-mentioned operating process circulation is continuously carried out.
The present invention adopts tubular type to burn and revivifier main air cooling, can effectively control regenerated catalyst temperature, thereby reduces the temperature that contacts of regenerated catalyst and raw material, reach the dry gas, the coke yield that reduce device, improve liquid yield, improve product and distribute, improve the economic benefit of refinery; Adopt the short reaction time, the high agent-oil ratio operation has reduced reacted gas (comprising dry gas and the liquefied gas) productive rate of device, makes the yield of vapour, diesel oil distillate obtain increasing, and has improved the utilization ratio of petroleum resources; Adopt tubular type to burn device and improved the carbon-burning capacity of device and burnt efficient, reduced the catalyst inventory of revivifier, dwindled the size of revivifier, the appliance arrangement investment is descended.Device dry gas, coke yield descend, and the energy consumption of device is reduced
Regenerated catalyst temperature is 580～650 ℃ in the described revivifier 2, and absolute regeneration pressure is 0.15～0.40MPa, the catalyzer residence time 3～6min.Other operating parameterss meet the general feature of conventional catalytic cracking unit revivifier.
The main air 16 of described revivifier 2 is pressurized air, residual coke on main effect burning-off half regenerated catalyst of this main air 16 also cools off the temperature of the regenerated catalyst dense bed 3 of revivifier 2, and regenerated catalyst dense bed 3 temperature that reach control revivifier 2 are 580～650 ℃ purpose.The air quantity of main air 16 is determined by heat calculation according to catalyst inventory and the control target temperature of revivifier 2.
The operational condition of described reacting-settler 8 is: temperature of reaction is 480～580 ℃, is preferably 500～560 ℃, is preferably 530～550 ℃; Stock oil 7 is 0.01～1.0s by the reaction times that contacts of feed nozzle 20 and regenerated catalyst, is preferably 0.05～0.5s, is preferably 0.1～0.3s; Agent-oil ratio is 5～30, and agent-oil ratio is determined by the heat calculation in when reaction; The reaction absolute pressure is 0.15～0.40MPa;
The stripping condition of the reacting-settler stripping stage 10 of described reacting-settler 8 is conventional, and the stripping medium is water vapor, and the stripping temperature is 480～520 ℃.
Described reclaimable catalyst burns device 15 bottoms and burns that wind 23 contacts and burn on the device 15 up burning-off reclaimable catalysts 70～80% coke along tubular type in tubular type.Tubular type is burnt device 15, and to burn temperature be 600～720 ℃, and the air linear speed that tubular type is burnt device 15 is 1.0～5m/s, and tubular type is burnt device, and to burn the intensity burning carbon amount of catalyzer per ton (per hour) be 300～1000kg/ (t.h), burns time 8～40s.Burn wind 23 and be pressurized air, this pressurized air meets the compressed-air actuated general feature of conventional catalytic cracking unit, and its flow can multiply by unit weight coke required air quantity when burning according to total green coke amount of raw material unit time and calculate to determine.
Described stock oil 7 meets the conventional ingredient requirement that promotes the tubular type catalytic cracking unit.
The described catalyst cracking method of the present invention of Fig. 2 and difference shown in Figure 1 are: behind external warmer 27 heat-obtainings, enter reacting-settler 8 by regenerated catalyst 4 and regenerated catalyst flowrate control valve 6 from the regenerated catalyst of revivifier 2.Reclaimable catalyst burns the superfluous heat that produces when device 15 is up to carry out the reclaimable catalyst coke burning regeneration along tubular type to be taken away by heat collector 26, and half regenerated catalyst behind the regeneration heat-obtaining enters cyclonic separator 14 in the revivifier 2 to carry out catalyzer and separate with flue gas.
What a kind of short distance of the present invention, efficient catalytic cracking method adopted is the conventional tubular type catalytic cracking catalyst that promotes.
The concrete operations of catalytic cracking of the present invention and control process, the those of ordinary skill in catalytic cracking field can be selected for use according to the concrete operations situation.W% among the present invention is weight percentage.
Comparative Examples and embodiment
Comparative Examples
Test raw material adopts the grand celebration long residuum, and catalyzer adopts commercially available CC-20 catalytic cracking industry equilibrium catalyst, and micro-activity is 65.
Catalytic cracking is tested at the catalytic cracking riser pilot plant.The pilot plant riser reactor is simulated full freshening operation, and the regeneration temperature of revivifier inner catalyst is 700 ℃, and the carbon content of regenerated catalyst is 0.03w%, and micro-activity is 65.The stripping medium of reacting-settler stripping stage is water vapor, and the stripping temperature is 500 ℃.
The catalytic cracking feed properties sees Table 1, and the operational condition of catalytic cracking reaction, product distribute and see Table 2.
Test raw material adopts the grand celebration long residuum, and catalyzer adopts commercially available CC-20 catalytic cracking industry equilibrium catalyst, and micro-activity is 65.
Short distance, efficient catalytic cracking scheme are carried out in the laboratory scale fluidized bed equipment, and reclaimable catalyst enters in the revivifier after adopting tubular type to burn, and micro-activity is 65.The stripping medium of reacting-settler stripping stage is water vapor, and the stripping temperature is 500 ℃.The operational condition of present embodiment short distance, efficient catalytic cracking unit, product distribute and portioned product character sees Table 3.
Table 1 catalytic cracking feed properties (Comparative Examples)
| Catalytic cracking charging charging | The grand celebration long residuum |
| Density (20 ℃), kgm -3 | 908.2 |
| Carbon residue, w% | 4.2 |
| Group composition, w% | |
| Stable hydrocarbon | 62.3 |
| Aromatic hydrocarbons | 25.6 |
| Colloid+bituminous matter | 12.1 |
| Sulphur content, μ gg -1 | 1180 |
| Ni，μg·g -1 | 4.3 |
| V，μg·g -1 | 0.2 |
The operational condition of the conventional riser catalytic cracking of table 2, product distribute and portioned product character (Comparative Examples)
The operational condition of the conventional riser catalytic cracking of table 3 and catalytic cracking of the present invention, product distribute and portioned product character
The operational condition of the conventional riser catalytic cracking of table 4 and catalytic cracking of the present invention, product distribute and portioned product character
The operational condition of the conventional riser catalytic cracking of table 5 and catalytic cracking of the present invention, product distribute and portioned product character
The operational condition of table 6 catalytic cracking of the present invention, product distribute and portioned product character
| Project | Reacting-settler |
| Temperature of reaction, ℃ | 530 |
| Reaction times, s | 0.03 |
| Catalyzer | Catalyzer (CC-20) |
| Raw material preheating temperature, ℃ | 220 |
| Agent-oil ratio | 19.0 |
| The reaction absolute pressure, MPa | 0.25 |
| The regenerator temperature, ℃ | 600 |
| Tubular type is burnt device and is burnt intensity, kg/ (t.h) | 820 |
| Tubular type is burnt device and is burnt the time, s | 15 |
| Tubular type is burnt device linear speed, m/s | 3.0 |
| Recycle ratio (weight ratio) | 0.24 |
| Product distributes, w% | |
| Dry gas | 1.86 |
| Liquefied gas | 8.28 |
| Gasoline (＜180 ℃) | 49.06 |
| Diesel oil (＜360 ℃) | 34.26 |
| Coke | 6.15 |
| Loss | 0.39 |
| Add up to | 100 |
| Total liquid yield, w% | 91.60 |
| Gasoline+diesel yield, w% | 83.32 |
| Gasoline RON | 89.7 |
| Gasoline endpoint, ℃ | 197 |
| Diesel cetane-number | 32.5 |
The operational condition of table 7 catalytic cracking of the present invention, product distribute and portioned product character
| Project | Reacting-settler |
| Temperature of reaction, ℃ | 565 |
| Reaction times, s | 0.08 |
| Catalyzer | Catalyzer (CC-20) |
| Raw material preheating temperature, ℃ | 220 |
| Agent-oil ratio | 23.0 |
| The reaction absolute pressure, MPa | 0.25 |
| The regenerator temperature, ℃ | 630 |
| Tubular type is burnt device and is burnt intensity, kg/ (t.h) | 900 |
| Tubular type is burnt device and is burnt the time, s | 13 |
| Tubular type is burnt device linear speed, m/s | 3.4 |
| Recycle ratio (weight ratio) | 0.18 |
| Product distributes, w% | |
| Dry gas | 3.05 |
| Liquefied gas | 14.51 |
| Gasoline (＜180 ℃) | 48.82 |
| Diesel oil (＜360 ℃) | 25.05 |
| Coke | 8.17 |
| Loss | 0.40 |
| Add up to | 100 |
| Total liquid yield, w% | 88.02 |
| Gasoline+diesel yield, w% | 73.51 |
| Gasoline RON | 90.4 |
| Gasoline endpoint, ℃ | 201 |
| Diesel cetane-number | 26.5 |
The operational condition of table 8 catalytic cracking of the present invention, product distribute and portioned product character
| Project | Reacting-settler |
| Temperature of reaction, ℃ | 520 |
| Reaction times, s | 0.20 |
| Catalyzer | Catalyzer (CC-20) |
| Raw material preheating temperature, ℃ | 220 |
| Agent- |
18 |
| The reaction absolute pressure, MPa | 0.25 |
| The regenerator temperature, ℃ | 590 |
| Tubular type is burnt device and is burnt intensity, kg/ (t.h) | 930 |
| Tubular type is burnt device and is burnt the time, s | 10 |
| Tubular type is burnt device linear speed, m/s | 4.7 |
| Recycle ratio (weight ratio) | 0.19 |
| Product distributes, w% | |
| Dry gas | 1.81 |
| Liquefied gas | 7.93 |
| Gasoline (＜180 ℃) | 50.25 |
| Diesel oil (＜360 ℃) | 32.62 |
| Coke | 7.01 |
| Loss | 0.38 |
| Add up to | 100 |
| Total liquid yield, w% | 90.8 |
| Gasoline+diesel yield, w% | 80.87 |
| Gasoline RON | 90 |
| Gasoline endpoint, ℃ | 199 |
| Diesel cetane-number | 32 |
Claims (12)
1. a catalytic cracking process is characterized in that comprising the steps:
(a) regenerated catalyst in the revivifier (2) enters reacting-settler (8) downwards, with the stock oil (7) that enters reacting-settler (8) through feed nozzle (20) in the same way or reverse contact reacts, reaction back logistics separates, isolated reaction generation oil gas (18) enters fractionating system and carries out fractionation, and isolated reclaimable catalyst enters step (b);
(b) entering tubular type from the reclaimable catalyst of step (a) behind water vapour (21) stripping burns device (15) and carries out coke burning regeneration, enter revivifier (2) afterwards, carrying out catalyzer through II cyclonic separator (14) separates with flue gas, flue gas after the separation (12) is discharged revivifier (2), half regenerated catalyst after the separation carries out coke burning regeneration at regenerated catalyst dense bed (3), and the regenerated catalyst after the regeneration recycles;
The described regenerated catalyst temperature that enters in the reacting-settler (8) is 580～650 ℃, and stock oil (7) is 0.01～1.0s with the contact reacts time of regenerated catalyst; Temperature of reaction is 480～580 ℃, and agent-oil ratio is 5～30, and the reaction absolute pressure is 0.15～0.40MPa; The temperature of burning that tubular type is burnt in the device (15) is 600～720 ℃, and the air linear speed is 1.0～5m/s, and burning intensity is 300～1000kg.t
-1.h
-1, burn time 8～40s.
2. catalytic cracking process according to claim 1 is characterized in that: the regenerated catalyst in the revivifier (2) enters reacting-settler (8) downwards behind heat-obtaining.
3. catalytic cracking process according to claim 1, it is characterized in that: reclaimable catalyst burns device (15) in tubular type and carries out coke burning regeneration and heat-obtaining, enters revivifier (2) afterwards.
4. catalytic cracking process according to claim 1, it is characterized in that: regenerated catalyst dense bed (3) temperature is 580～650 ℃.
5. the device that is used for the described catalytic cracking process of claim 1, it is characterized in that: this device comprises revivifier (2), reacting-settler (8) and tubular type are burnt device (15), revivifier (2) comprises II cyclonic separator (14) and I cyclonic separator (1) and distributor pipe of cardinal wind (5), reacting-settler (8) comprises III cyclonic separator (19) and reacting-settler stripping stage (10), the bottom of reacting-settler (8) is reacting-settler stripping stage (10), tubular type is burnt device (15) and is comprised and burn wind distribution pipe (24), revivifier (2) is connected with reacting-settler (8) by regenerated catalyst (4), regenerated catalyst flowrate control valve (6) is set on the regenerated catalyst (4), reacting-settler stripping stage (10) bottom is burnt device (15) bottom by inclined tube to be generated (11) and tubular type and is connected, inclined tube to be generated (11) middle part arranges reclaimable catalyst flowrate control valve (22), and tubular type is burnt the interior II cyclonic separator (14) of device (15) top exit and revivifier (2) and is connected.
6. the device of catalytic cracking process according to claim 5 is characterized in that: revivifier (2) is arranged on reacting-settler (8) top, revivifier (2) and reacting-settler (8) coaxial arrangement or disalignment layout.
7. the device of catalytic cracking process according to claim 5, it is characterized in that: regenerated catalyst (4) entrance is arranged on regenerated catalyst dense bed (3) top of revivifier (2), outlet is arranged on the inside of reacting-settler (8), and the vertical height L at reclaimable catalyst dense bed (9) interface in outlet position and the reacting-settler (8) is 2～6M.
8. according to the device of claim 5 or 7 described catalytic cracking process, it is characterized in that: regenerated catalyst (4) adopts cross section to be circular metal tube, Φ 200～3000mm, the position is arranged in revivifier (2) and the reacting-settler (8) any position radially.
9. the device of catalytic cracking process according to claim 5, it is characterized in that: the mobile direction of feed nozzle (20) Way out in the reacting-settler (8) and regenerated catalyst arranges in the same way, its position is arranged on the medullary ray that is arranged in reacting-settler (8) regenerated catalyst (4) outlet, feed nozzle (20) exit end and regenerated catalyst (4) outlet are in same level height, and feed nozzle (20) meets the general feature of conventional catalytic cracking unit feed nozzle.
10. the device of catalytic cracking process according to claim 5, it is characterized in that: the reverse setting of direction of flowing of feed nozzle (20) Way out in the reacting-settler (8) and regenerated catalyst, its position is arranged on the medullary ray of regenerated catalyst (4) outlet in the reacting-settler (8), feed nozzle (20) outlet is 2～6M with regenerated catalyst (4) exit separation H, and is positioned at reacting-settler (8) reclaimable catalyst dense bed (9) top.
11. the device of catalytic cracking process according to claim 5 is characterized in that: described tubular type is burnt device (15) middle and upper part heat collector (26) is set.
12. the device of catalytic cracking process according to claim 5 is characterized in that: described revivifier (2) arranges external warmer (27).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010139860 CN102212382B (en) | 2010-04-07 | 2010-04-07 | Catalytic cracking process and device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010139860 CN102212382B (en) | 2010-04-07 | 2010-04-07 | Catalytic cracking process and device |
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| Publication Number | Publication Date |
|---|---|
| CN102212382A CN102212382A (en) | 2011-10-12 |
| CN102212382B true CN102212382B (en) | 2013-10-02 |
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|---|---|---|---|
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103540346B (en) * | 2012-07-09 | 2016-04-13 | 中国石油化工集团公司 | A kind of Desending catalytic cracking device |
| CN104513670B (en) * | 2013-09-29 | 2016-06-08 | 中石化洛阳工程有限公司 | A kind of catalyst cracking method and device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3907663A (en) * | 1973-10-01 | 1975-09-23 | Mobil Oil Corp | Conversion of hydrocarbons |
| CN1154400A (en) * | 1996-01-11 | 1997-07-16 | 中国石油化工总公司 | Method for catalytic conversion of petroleum hydrocarbon |
-
2010
- 2010-04-07 CN CN 201010139860 patent/CN102212382B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3907663A (en) * | 1973-10-01 | 1975-09-23 | Mobil Oil Corp | Conversion of hydrocarbons |
| CN1154400A (en) * | 1996-01-11 | 1997-07-16 | 中国石油化工总公司 | Method for catalytic conversion of petroleum hydrocarbon |
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|---|---|
| CN102212382A (en) | 2011-10-12 |
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Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant after: China Petrochemical Group Corp. Co-applicant after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant before: China Petrochemical Group Corp. Co-applicant before: Luoyang Petrochemical Engineering Co., China Petrochemical Group |
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