CN100377774C - Reactor for catalytic conversion of hydrocarbon oil - Google Patents
Reactor for catalytic conversion of hydrocarbon oil Download PDFInfo
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- CN100377774C CN100377774C CNB2004100838886A CN200410083888A CN100377774C CN 100377774 C CN100377774 C CN 100377774C CN B2004100838886 A CNB2004100838886 A CN B2004100838886A CN 200410083888 A CN200410083888 A CN 200410083888A CN 100377774 C CN100377774 C CN 100377774C
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Abstract
The present invention relates to catalytic conversion reactor for hydrocarbon oil, which mainly comprises a first reaction zone, a second reaction zone of which the diameter is enlarged, a third reaction zone, a fourth reaction zone of which the diameter is enlarged, an outlet zone and an oil separation zone, wherein the first reaction zone, the second reaction zone, the third reaction zone and the fourth reaction zone are in sequential and coaxial arrangement from bottom to top in a vertical direction; one end of the outlet zone is connected with the fourth reaction zone, and the other end is connected with the oil separation zone. The reactor enables raw hydrocarbon oil with different properties to be injected into different reaction zones, and respectively controls the reaction depth of all the reaction zones; thus, products with high yield and high quality can be obtained.
Description
Technical field
The invention belongs to the catalyticing conversioning equipment of hydrocarbon ils under the situation that does not have hydrogen, in particular, is a kind of reactor for catalytic conversion of hydrocarbon oil.
Background technology
Early stage catalytic cracking process adopts the dense bed reactor, and along with the application of high activity and high selectivity zeolite catalyst, the dense bed reactor is raised pipe reactor gradually and replaces, to reduce the catalyst back-mixing, to improve purpose product yield and quality.
The purpose product of catalytic cracking is high-quality gasoline in early days, along with the requirement on environmental protection increasingly stringent, requires catalytically cracked gasoline further to reduce olefin(e) centent, sulfur content.For this reason, developed catalyst and the auxiliary agent that reduces the catalytic cracking olefin(e) centent.Simultaneously, along with Elementary Chemical Industry raw material ethene, propylene increase in demand, developed with the mink cell focus is the technology of raw material low-carbon olefines high-output, MGG, ARGG, DCC, CPP technology as increasing production of liquid gas, the MGD technology of increasing production of liquid gas and diesel oil, the auxiliary agent of propylene enhancing etc. are so that by industrial chemicals such as heavy oil catalytic cracking process increasing output of ethylene, propylene.
CN1078094C has disclosed a kind of riser reactor that is used for fluidized catalytic conversion, and the suitable hole enlargement in the middle part of this reactor with the increase secondary response time, and can be used for two section feedings.
CN2360148Y improves the pre-lifting zone in the bottom in the catalytic cracking riser reactor, make it become enlarged tube, different and the enlarged tube that owing to interior carrier pipe and lift gas pipe the position is set in enlarged tube all can reach the contact conditions that improves catalyst and feedstock oil with different two kinds of new catalytic cracking riser reactors that obtain of riser type of attachment, improve the yield and the quality of purpose product, improve the operating flexibility of device, and the purpose that cuts down the consumption of energy.
CN2214222Y has introduced a kind of novel two-stage catalytic cracking reactor with up-downgoing reaction tube, and it is the improvement that belongs to existing catalytic cracking riser reactor structure.It is the purpose that realizes improving yield of light oil, reduces gas and coke yield by the catalyst cracker that adopts two-stage structure.It mainly is made up of two sections up-downgoing reaction tube and gas-solid separator.It can be at the intersegmental catalyst of isolating coking, feed new regenerated catalyst to next section simultaneously, oil gas is continuous-flow then, make every section oil gas can both contact selectivity and activity catalyst preferably, can control every section reaction temperature and oil ratio again, carry out condition optimizing, improve the purpose that product distributes, improves the light oil receipts thereby reach.
CN1091393C discloses a kind of catalytic cracking riser reactor, its main reaction section is made up of first conversion zone, second conversion zone, reaction control section, and first conversion zone is a conical pipe, and second conversion zone is a cylindrical tube, establish the water conservancy diversion sleeve pipe in it, the reaction control section is isometrical pipe.This reactor can effectively reduce main reaction section back-mixing, improve the gas-solid contacting efficiency.
CN1364854A discloses a kind of improved catalyst cracker.This reactor is made of riser, stripper, the first fluidized bed, second fluid bed and settler from bottom to up.During riser, riser, stripper, the first fluidized bed, second fluid bed and settler are coaxial, and their diameter enlarges successively in adopting; During riser, stripper, the first fluidized bed, second fluid bed and settler are coaxial, and their diameter enlarges successively outside adopting.Adopt this reactor can improve the operating flexibility of catalytic cracking unit, and product distribute, the tool that improves the quality of products has certain effect to improving.
CN1340594A discloses a kind of catalyst cracking method of handling multiple petroleum hydrocarbon simultaneously, be the finish distributor to be set in riser reactor inside, the lower part of riser reactor is divided into is parallel to 2～4 axial reaction zones, and corresponding feed nozzle is set at each reaction zone; High temperature regeneration agent from regenerator evenly distributes in each reaction zone; Pre-upgrading raw material injects wherein in the partial reaction district, contacts with the high temperature regeneration agent and reacts; It is up along riser in reaction zone separately to have neither part nor lot in catalyst for reaction in reaction logistics and other reaction zone, and contacts with main material after steam atomization in the main material porch and react.
CN1259559A discloses a kind of heavy residual oil fluidized catalytic cracking method, comprises the weight resid feed is contacted with adsorbent earlier in riser bottom, removing impurity such as carbon residue in the weight residual oil, heavy metal, and then contacts with catalyst, carries out cracking reaction; In stripper, catalyst is separated with the product hydro carbons with adsorbent, in separator, separate reclaimable catalyst and adsorbent, and they are regenerated respectively.
USP4579716 discloses anti-overladen FCC reactor.This reactor is made up of riser, firsts and seconds cyclone separator and stripper, and they are arranged in the reactor.The one-level cyclone separator is connected by drip valve or other method are arranged with riser, prevents the thermal cracking of the hydro carbons that comes out from riser.
Summary of the invention
The objective of the invention is on the basis of above-mentioned prior art, to provide a kind of novel reactor for catalytic conversion of hydrocarbon oil.
Reactor for catalytic conversion of hydrocarbon oil provided by the invention mainly comprises with the lower part: the 4th reaction zone of second reaction zone of first reaction zone, enlarged-diameter, the 3rd reaction zone, enlarged-diameter, outlet area and finish Disengagement zone, wherein, the vertically coaxial successively from bottom to top setting of first reaction zone to the, four reaction zones, one end of outlet area links to each other with the 4th reaction zone, and the other end links to each other with the finish Disengagement zone; Perhaps do not set out oral region, the finish Disengagement zone is directly linked to each other with the 4th reaction zone.
Compared with prior art, reactor for catalytic conversion of hydrocarbon oil provided by the invention has following characteristics:
1, reactor for catalytic conversion of hydrocarbon oil provided by the invention is to improve to form on the basis of ripe petroleum hydrocarbon catalytic conversion reactor, it is divided into several different reaction zones with petroleum hydrocarbon catalytic conversion reaction process, and make hydrocarbon oil crude material of different nature inject different reaction zones, control the reaction depth of each reaction zone respectively, to obtain high yield, high-quality purpose product.
2, adopt reaction zone provided by the present invention can increase productivity of propylene, improve quality of gasoline, reduce content of sulfur in gasoline, olefin(e) centent, and reduce dry gas yied.
3, reactor provided by the present invention is easy to implement.Can transform existing catalytic cracking reaction device according to the present invention.New device also can reduce construction investment.
4, reactor provided by the present invention reflects oral region, finish separation facilities, collection chamber, oil-gas pipeline etc. by what a series of mutual airtight connections were set, thereby replaced the reactor settler that conventional catalytic cracking unit adopted, the construction investment of equipment is reduced significantly.
5, the present invention has strengthened the cracking of light hydrocarbon oil cut and the cracking of heavy hydrocarbon oil respectively by the meticulous design to structure of reactor, increases the cracking again of a crackate of mink cell focus, thereby increases liquefied gas yield and productivity of propylene.
Description of drawings
Fig. 1 is the structural representation of reactor provided by the present invention.
The specific embodiment
As shown in Figure 1, reactor for catalytic conversion of hydrocarbon oil provided by the invention mainly comprises with the lower part: the 4th reaction zone 4, outlet area 5 and the finish Disengagement zone 6 of second reaction zone 2 of first reaction zone 1, enlarged-diameter, the 3rd reaction zone 3, enlarged-diameter.The vertically coaxial successively from bottom to top setting of first reaction zone to the, four reaction zones, fixing and airtight connection between above-mentioned each reaction zone.One end of outlet area 5 links to each other with the 4th reaction zone, and the other end links to each other with finish Disengagement zone 6.
The bottom conversion zone of first reaction zone of the present invention and conventional FCC riser reactor is basic identical, this reaction zone is not only fixedly connected with regenerated catalyst pipeline 13 and be connected, but also petroleum hydrocarbon feed nozzle 15, atomizing steam should be set and promote dielectric distribution device etc. in advance.The height of described first reaction zone accounts for the 5-20% of this total reactor height, preferred 8-15%.The pre lift zone of the diameter of described first reaction zone and conventional FCC riser reactor is basic identical, and for example, its diameter can be 0.2-5 rice.
The diameter ratio of the diameter of second reaction zone of the present invention and first reaction zone is 1.2-8: 1, and preferred 1.5-5: 1.The height of second reaction zone accounts for the 10-40% of this total reactor height, preferred 20-35%.First and second reaction zone binding site is a truncated cone-shaped, and the apex angle of its vertical section isosceles trapezoid is 30-80 °.
The diameter ratio of the diameter of the 3rd reaction zone of the present invention and first reaction zone is 0.8-1.2: 1, and preferred 0.9-1.1: 1.The height of the 3rd reaction zone accounts for the 5-20% of this total reactor height, preferred 8-15%.Second and third reaction zone binding site is a truncated cone-shaped, and the base angle β of its vertical section isosceles trapezoid is 30-80 °.The 3rd reaction zone is provided with petroleum hydrocarbon feed nozzle 17 and corresponding atomizing steam injection device.
The diameter ratio of the diameter of the 4th reaction zone of the present invention and first reaction zone is 1.2-8: 1, and preferred 1.5-5: 1.The height of the 4th reaction zone accounts for the 10-40% of this total reactor height, preferred 20-35%.Third and fourth reaction zone binding site is a truncated cone-shaped, and the drift angle γ of its vertical section isosceles trapezoid is 30-80 °.Described the 4th reaction zone links to each other with catalyst stripping equipment 9 by catalyst transport pipeline 10, and the catalyst in the 4th reaction zone can be delivered in the stripper 9 through pipeline 10.In addition, the 4th reaction zone links to each other with the top of stripper 9 by pipeline 8, and the reaction oil gas that stripping medium and institute's stripping are come out can return the dilute phase section of the 4th reaction zone through pipeline 8.
The diameter ratio of the diameter of outlet area of the present invention and first reaction zone is 0.8-1.2: 1, and preferred 0.9-1.1: 1.The height of outlet area accounts for the 0-20% of this total reactor height, preferred 5-15%.The binding site of the 4th reaction zone and outlet area is a truncated cone-shaped, and the base angle δ of its vertical section isosceles trapezoid is 30-80 °.One end of outlet area 5 links to each other with the 4th reaction zone, and the other end links to each other with finish Disengagement zone 6.When this reactor did not set out oral region, promptly to account for the ratio of this total reactor height be 0 o'clock to the height of outlet area, the suction line of finish Disengagement zone 6 directly linked to each other with the outlet of the 4th reaction zone get final product.
Finish of the present invention Disengagement zone 6 adopts this areas equipment that reaction oil gas and catalyst are separated commonly used to get final product, for example, and cyclone separator etc., and described finish separation equipment can adopt one-level, also can adopt multistage.The catalyst granules that described finish separation equipment is separated returns in the 4th reaction zone by pipeline 19, and the reaction oil gas of being separated is delivered to collection chamber 20 and compiled, and delivers to subsequent separation system through oil-gas pipeline 7 then and further is separated into various products.
The workflow of reactor of the present invention is as follows: after the preheating or enter the bottom of first reaction zone 1 through pipeline 14 or 15 without the gasoline stocks of preheating, contact with regenerated catalyst from regenerator sloped tube 13, and react at first reaction zone, formed reaction logistics is up, enter enlarged-diameter second reaction zone 2 in.Reaction oil gas continues to contact, react with catalyst in second reaction zone, further increases the cracking of light petrol, increases yield of light olefin.The reaction logistics of second reaction zone of flowing through continues upwards to flow, and enters the 3rd reaction zone 3 that has dwindled than second reaction zone diameter.In the 3rd reaction zone, heavy raw oil after the preheating injects through pipeline 17, contact, react with reaction logistics in this reaction zone, and formed reaction logistics continues to make progress mobile, enter the 4th reaction zone 4 of hole enlargement, the further cracking of the intermediate product that heavy raw oil is generated.The reaction logistics is flowed through behind the 4th reaction zone, enters outlet area 5, because outlet area has apparent in view undergauge design than the 4th reaction zone, the flowing velocity of the reaction logistics that enters outlet area is improved, and enters finish Disengagement zone 6 through this outlet area.In the finish Disengagement zone, by means of separation facilities such as cyclone separators reaction oil gas and catalyst are separated, the reaction oil gas of separating is delivered to collection chamber 20 earlier and is compiled, and sends into subsequent separation system by oil-gas pipeline 7 then, further is separated into various products.And be back in the beds of the 4th reaction zone by pipeline 19 through the catalyst that cyclone separator separates.Catalyst controlling level by in 18 controls of the guiding valve on catalyst line 10 and this pipeline the 4th reaction zone is delivered to the interior successive ground warp pipeline 10 of catalyst of the 4th reaction zone and carries out stripping in the stripper 9.The reaction oil gas that institute's stripping comes out in stripper returns the top dilute phase section of the 4th reaction zone by pipeline 8, catalyst behind the stripping is delivered to regenerator 12 coke burning regenerations through pipeline 11 to be generated, and first reaction zone that the catalyst after the regeneration returns this reactor recycles.
Following main operating condition is adopted in reactor suggestion of the present invention: the gasoline stocks after the preheating enters first reaction zone and contacts with catalyst, and reaction temperature is 200-700 ℃, is preferably 400-650 ℃; Reaction pressure is 130-450 kPa, is preferably 250-400 kPa; The gross weight air speed is 1-120 hour
-1, be preferably 2-100 hour
-1The weight ratio of catalyst and gasoline stocks is 2-15: 1, be preferably 3-10: 1; The weight ratio of water vapour and gasoline stocks is 0-0.1: 1, be preferably 0.01-0.05: 1; The reaction condition of heavy hydrocarbon oil raw material is in the 3rd reaction zone and the 4th reaction zone: reaction temperature is 200-650 ℃, is preferably 400-600 ℃; Reaction pressure is 130-450 kPa, is preferably 250-400 kPa; The gross weight air speed is 1-120 hour
-1, be preferably 2-100 hour
-1The weight ratio of catalyst and heavy hydrocarbon oil raw material is 2-15: 1, be preferably 4-10: 1; The weight ratio of water vapour and heavy hydrocarbon oil raw material is 0-0.1: 1, be preferably 0.01-0.05: 1.
The following examples will give further instruction to the present invention, but therefore the present invention is not subjected to any restriction.The character of employed catalyst of embodiment and raw material hydrocarbon is listed in table 1 and table 2 respectively, and the catalyst in the table 1 is by Sinopec Shandong catalyst plant industrial production.
Embodiment 1
Present embodiment explanation: adopt reactor of the present invention to carry out the catalyzed conversion test, product distribution and product quality are improved.
With mink cell focus in the table 2 and the light gasoline fraction in the table 3 is raw material, uses the listed catalyst of table 1, tests on the kitty cracker that adopts reactor of the present invention, and the structure of reactor as shown in Figure 1.Wherein, the total height of reactor is 12 meters, 1.5 meters of first reaction zones, 4 meters of second reaction zones, 1.5 meters of the 3rd reaction zones, 4 meters of the 4th reaction zones, 1 meter of outlet area, and the diameter ratio of each reaction zone was followed successively by 1: 2: 1: 2: 1.The binding site of each reaction interval is truncated cone-shaped, and the drift angle of its vertical section isosceles trapezoid or base angle are 40 °.
Test procedure is summarized as follows: the light petrol raw material enters the bottom of first reaction zone 1 through pipeline 14, contacts, reacts with regenerated catalyst, and formed reaction logistics is up, enter second reaction zone continues reaction.The reaction logistics of second reaction zone of flowing through continues upwards to flow, and enters the 3rd reaction zone 3.In the 3rd reaction zone, heavy raw oil after the preheating injects through pipeline 17, contact, react with reaction logistics in this reaction zone, and formed reaction logistics continues to make progress mobile, enter the 4th reaction zone 4, the further cracking of the intermediate product that heavy raw oil is generated.The reaction logistics is flowed through behind the 4th reaction zone, enters outlet area 5, and enters finish Disengagement zone 6 through this outlet area.In the finish Disengagement zone reaction oil gas and catalyst are separated, the reaction oil gas of separating is delivered to collection chamber earlier and is compiled, and sends into subsequent separation system by oil-gas pipeline 7 then.And be back in the 4th reaction zone by pipeline 19 through the catalyst that cyclone separator separates.The interior successive ground warp pipeline 10 of catalyst of the 4th reaction zone is delivered to carries out stripping in the stripper 9.Catalyst behind the stripping returns first reaction zone and recycles after regeneration.Main operating condition, product distribute and major product character sees Table 5.
Comparative Examples 1
Explanation in this contrast: adopt the resulting result of the test of the described reactor of CN1078094C.
With mink cell focus in the table 2 and the light gasoline fraction in the table 3 is raw material, uses the listed catalyst of table 1, tests on the kitty cracker that adopts the described reactor of CN1078094C.Wherein, the total height of reactor is 12 meters, 2 meters of pre lift zones, 2 meters of first reaction zones, 6 meters of second reaction zones, 2 meters of outlet areas, and the diameter ratio of each reaction zone was followed successively by 1: 1: 2: 1.The binding site of each reaction interval is truncated cone-shaped, and the drift angle of its vertical section isosceles trapezoid or base angle are 40 °.Test procedure is substantially the same manner as Example 1, and gasoline stocks and heavy oil feedstock be injecting reactor respectively, and resulting result of the test is referring to table 5.
Embodiment 2
Present embodiment explanation: adopt the reactor of the present invention of successive reaction-regenerative operation to carry out the catalyzed conversion test, product distribution and product quality are improved.
With mink cell focus in the table 2 and the C 4 fraction in the table 4 is raw material, uses the listed catalyst of table 1, tests on the kitty cracker that adopts reactor of the present invention, and the structure of reactor as shown in Figure 1.Wherein, the total height of reactor is 12 meters, 1.5 meters of first reaction zones, 4 meters of second reaction zones, 1.5 meters of the 3rd reaction zones, 4 meters of the 4th reaction zones, 1 meter of outlet area, and the diameter ratio of each reaction zone was followed successively by 1: 2: 1: 2: 1.The binding site of each reaction interval is truncated cone-shaped, and the drift angle of its vertical section isosceles trapezoid or base angle are 40 °.
Test procedure is summarized as follows: C 4 fraction enters the bottom of first reaction zone 1 through pipeline 14, contacts, reacts with regenerated catalyst, and formed reaction logistics is up, enter second reaction zone continues reaction.The reaction logistics of second reaction zone of flowing through continues upwards to flow, and enters the 3rd reaction zone 3.In the 3rd reaction zone, heavy raw oil after the preheating injects through pipeline 17, contact, react with reaction logistics in this reaction zone, and formed reaction logistics continues to make progress mobile, enter the 4th reaction zone 4, the further cracking of the intermediate product that heavy raw oil is generated.The reaction logistics is flowed through behind the 4th reaction zone, enters outlet area 5, and enters finish Disengagement zone 6 through this outlet area.In the finish Disengagement zone reaction oil gas and catalyst are separated, the reaction oil gas of separating is delivered to collection chamber earlier and is compiled, and sends into subsequent separation system by oil-gas pipeline 7 then.And be back in the 4th reaction zone by pipeline 19 through the catalyst that cyclone separator separates.The interior successive ground warp pipeline 10 of catalyst of the 4th reaction zone is delivered to carries out stripping in the stripper 9.Catalyst behind the stripping returns first reaction zone and recycles after regeneration.Main operating condition, product distribute and major product character sees Table 5.
Table 1
| Trade names | GOR-2 |
| Zeolite type | REHY+MOY |
| Chemical composition, heavy % | |
| Aluminium oxide | 52.4 |
| Sodium oxide molybdena | 0.10 |
| Iron oxide | 0.17 |
| Bulk density, kilogram/rice 3 | 710 |
| Pore volume, milliliter/gram | 0.36 |
| Specific area, rice 2/ gram | 265 |
| Abrasion index is when weighing % -1 | 2.0 |
| Size consist, heavy % | |
| The 0-40 micron | 14.7 |
| The 40-80 micron | 55.1 |
| ＞80 microns | 29.7 |
Table 2
| Project | ||
| Density, Kgm -3(20℃) | 898.5 | |
| Carbon residue, m% | 5.22 | |
| Refraction coefficient | 1.4881 | |
| Freezing point, ℃ | 44.0 | |
| Sulfur content, heavy % | 0.49 | |
| Boiling range/℃ | HK | 278 |
| 10％ | 367 | |
| 30％ | 424 | |
| 50％ | 470 | |
| 67.6％ | 544 | |
| Tenor/ppm | Fe | 2.6 |
| Ni | 6.8 | |
| V | 1.1 | |
| Fe | 3.1 | |
| Na | 0.8 | |
| Viscosity/mm 2·s -1 | 80℃ | 23.85 |
| 100℃ | 13.96 | |
| Composition/the m% of hydrocarbon system | Alkane | 66.4 |
| Aromatic hydrocarbons | 19.4 | |
| Colloid | 12.8 | |
| Asphalitine | 1.4 | |
Table 3
| Gasoline stocks character: | |
| Density (20 ℃), g/cm 3 | 0.7217 |
| Induction period, min | 375 |
| Vapour pressure, KPa | 74 |
| Initial boiling point/do, ℃ | 29/182 |
| MON | 78.4 |
| RON | 91.0 |
Table 4
| Form | C 4 fraction, wt% |
| C 3 0 | 0.44 |
| C 3 ＝ | 0.70 |
| iC 4 0 | 15.02 |
| nC 4 0 | 8.55 |
| nC 4 ＝ | 14.11 |
| iC 4 ＝ | 28.70 |
| tC 4 ＝ | 14.08 |
| cC 4 ＝ | 19.03 |
Table 5
| Embodiment 1 | Embodiment 2 | Comparative Examples 1 | |
| Lightweight material: reaction temperature, ℃ | 600 | 598 | 600 |
| Oil ratio | 30 | 30 | 30 |
| Water-oil factor | 0.3 | 0.3 | 0.3 |
| Heavy charge: reaction temperature, ℃ | 495 | 496 | 495 |
| Oil ratio | 6.0 | 6.0 | 6.0 |
| Water-oil factor | 0.06 | 0.06 | 0.06 |
| Product distributes, heavy % | |||
| H 2-C 2 | 1.78 | 1.69 | 1.95 |
| Liquefied gas | 14.77 | 14.62 | 13.86 |
| Propylene wherein | 5.12 | 4.75 | 4.27 |
| C 5 +Gasoline | 45.07 | 47.90 | 47.45 |
| Diesel oil | 21.53 | 18.96 | 19.62 |
| Heavy oil | 9.04 | 9.02 | 9.15 |
| Coke | 7.81 | 7.81 | 7.97 |
| Gasoline products: initial boiling point/50% | 43/119 | 50/122 | 46/121 |
| 90%/do | 176/201 | 178/205 | 175/203 |
| MON/RON | 79.3/90.7 | 79.0/90.4 | 78.7/90.2 |
| Alkene, v% | 27.5 | 28.7 | 31.8 |
| Sulfur content, wt% | 0.087 | 0.089 | 0.096 |
| Diesel product: initial boiling point/50% | 196/267 | 198/268 | 198/268 |
| 90%/do | 324/353 | 326/354 | 324/352 |
| Condensation point, ℃ | -4 | -3 | -1 |
| Cetane number | 38 | 35 | 34 |
Claims (8)
1. reactor for catalytic conversion of hydrocarbon oil, it is characterized in that this reactor mainly comprises with the lower part: the 4th reaction zone (4) of second reaction zone (2) of first reaction zone (1), enlarged-diameter, the 3rd reaction zone (3), enlarged-diameter, outlet area (5) and finish Disengagement zone (6), wherein, first reaction zone (1) is to the 4th reaction (4) the vertically coaxial successively from bottom to top setting in district, one end of outlet area (5) links to each other with the 4th reaction zone (4), and the other end links to each other with finish Disengagement zone (6); Perhaps do not set out oral region (5), make finish Disengagement zone (6) directly link to each other (4) with the 4th reaction zone, the height of described first reaction zone (1) accounts for the 5-20% of this total reactor height, the height of second reaction zone (2) accounts for the 10-40% of this total reactor height, the height of the 3rd reaction zone (3) accounts for the 5-20% of this total reactor height, the height of the 4th reaction zone (4) accounts for the 10-40% of this total reactor height, and the height of outlet area (5) accounts for the 0-20% of this total reactor height.
2. according to the reactor of claim 1, it is characterized in that the height of described first reaction zone (1) accounts for the 8-15% of this total reactor height, the height of second reaction zone (2) accounts for the 20-35% of this total reactor height, the height of the 3rd reaction zone (3) accounts for the 8-15% of this total reactor height, the height of the 4th reaction zone (4) accounts for the 20-35% of this total reactor height, and the height of outlet area (5) accounts for the 5-15% of this total reactor height.
3. according to the reactor of claim 1, it is characterized in that the diameter of described second reaction zone (2) and the diameter ratio of first reaction zone (1) are 1.5-8: 1, the diameter ratio of the diameter of the 3rd reaction zone (3) and first reaction zone (1) is 0.8-1.2: 1, the diameter ratio of the diameter of the 4th reaction zone (4) and first reaction zone (1) is 1.5-8: 1, and the diameter ratio of the diameter of outlet area (5) and first reaction zone (1) is 0.8-1.2: 1.
4. according to the reactor of claim 3, it is characterized in that the diameter of described second reaction zone (2) and the diameter ratio of first reaction zone (1) are 1.5-5: 1, the diameter ratio of the diameter of the 3rd reaction zone (3) and first reaction zone (1) is 0.9-1.1: 1, the diameter ratio of the diameter of the 4th reaction zone (4) and first reaction zone (1) is 1.5-5: 1, and the diameter ratio of the diameter of outlet area (5) and first reaction zone (1) is 0.9-1.1: 1.
5. according to the reactor of claim 1, it is characterized in that described first reaction zone (1) and binding site, second reaction zone (2) of second reaction zone (2) are truncated cone-shaped with binding site, the 4th reaction zone (4) of the 4th reaction zone (4) with the binding site of outlet area (5) with binding site, the 3rd reaction zone (3) of the 3rd reaction zone (3), its vertical section is an isosceles trapezoid, and the drift angle of isosceles trapezoid or base angle are 30-80 °.
6. according to the reactor of claim 1, it is characterized in that described the 4th reaction zone (4) links to each other with catalyst stripping equipment (9) by catalyst transport pipeline (10), the catalyst in the 4th reaction zone (4) is delivered in the stripper through pipeline (10); And the 4th reaction zone (4) links to each other with the top of stripper (9) by pipeline (8), and the reaction oil gas that stripping medium and institute's stripping are come out returns the dilute phase section of the 4th reaction zone (4) through pipeline (8).
7. according to the reactor of claim 1, it is characterized in that described finish Disengagement zone (6) adopts one or more levels cyclone separator of airtight connection each other, and the catalyst granules that cyclone separator is separated returns in the 4th reaction zone (4) by pipeline (19), the reaction oil gas of being separated is delivered to collection chamber (20) and is compiled, and sends through oil-gas pipeline (7) then.
8. according to the reactor of claim 1, it is characterized in that this reactor is not provided with settler.
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| CN1030878A (en) * | 1987-07-03 | 1989-02-08 | 阿莫尼·卡萨尔公司 | Heterogeneous synthetic improving one's methods and reactor |
| JPH01151943A (en) * | 1987-09-22 | 1989-06-14 | Mobil Oil Corp | Method and apparatus for regenerating fluidized cracking catalyst having coke bonded thereto |
| US5622677A (en) * | 1991-10-28 | 1997-04-22 | Shell Oil Company | Venturi riser reactor and process for catalytic cracking |
| US5306418A (en) * | 1991-12-13 | 1994-04-26 | Mobil Oil Corporation | Heavy hydrocarbon feed atomization |
| CN1237477A (en) * | 1999-04-23 | 1999-12-08 | 中国石油化工集团公司 | Lift pipe reactor for fluidized catalytic conversion |
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| CN1763154A (en) | 2006-04-26 |
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