CN1275434A - Catalyst inlet device adaptable to gas-solid cocurrent flow descending bed reactor - Google Patents
Catalyst inlet device adaptable to gas-solid cocurrent flow descending bed reactor Download PDFInfo
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- CN1275434A CN1275434A CN 00106169 CN00106169A CN1275434A CN 1275434 A CN1275434 A CN 1275434A CN 00106169 CN00106169 CN 00106169 CN 00106169 A CN00106169 A CN 00106169A CN 1275434 A CN1275434 A CN 1275434A
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- 239000003054 catalyst Substances 0.000 title claims abstract description 61
- 239000007787 solid Substances 0.000 title claims abstract description 28
- 239000012159 carrier gas Substances 0.000 claims description 28
- 238000009434 installation Methods 0.000 claims description 2
- 239000002245 particle Substances 0.000 abstract description 17
- 238000005299 abrasion Methods 0.000 abstract description 4
- 239000008187 granular material Substances 0.000 description 11
- 230000004048 modification Effects 0.000 description 8
- 238000012986 modification Methods 0.000 description 8
- 239000007789 gas Substances 0.000 description 6
- RZVAJINKPMORJF-UHFFFAOYSA-N Acetaminophen Chemical compound CC(=O)NC1=CC=C(O)C=C1 RZVAJINKPMORJF-UHFFFAOYSA-N 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000004523 catalytic cracking Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 229920005479 Lucite® Polymers 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000004926 polymethyl methacrylate Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000005514 two-phase flow Effects 0.000 description 1
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Abstract
The catlyst inlet device applicable to gas-solid parallel-flow downgoing bed reactor includes external shell of said device and inlet of said downgoing bed reactor main body, the said external shell and reactor main body are co-axially mounted, and the top of said external shell is turbulent mixing zone, and on the periphery of the side wall of said external shell, the gas-carrying inlet pipelines are uniformly distributed, and the side wall of lower portion of gas-carrying inlet is equipped with catalyst conveying pipeline, and the lower portion of annular gap is equipped with loose wind distributor, and the side wall of external shell under the distributor is equipped with loose wind inlet pipeline. Said invented device can implement quick distribution of catalyst particles, and its structure is simple, operation elasticity is large, pressure drop is small, and particles abrasion on equipment is little.
Description
The present invention relates to a kind of catalyst inlet device that is applicable to the gas-solid cocurrent flow descending bed reactor, belong to the catalyst charge equipment technical field in the chemical industry equipment.
Descending-bed reactor utilizes gas-solid along the characteristics that gravitational field moves downward, and can adapt to catalytic cracking/cracking rapid-action requirement.Usually, its gas-solid mixing, the descending haptoreaction of gas-solid two-phase, gas-solid separate total process of three operations fast and finished within 1 second.Owing in the ultrashort time, finish gas-solid contact and reaction, and gas-solid two phase concentrations, velocity radial are evenly distributed in the reactor, and time of staying distribution is approximately laminar flow, and the back-mixing of catalyst and oil gas is little, help the raising of reaction selectivity, reduce catalyst and dry gas output.But because its rapid-action characteristics require catalyst just to be evenly distributed in the porch.Otherwise because the time of staying of descending bed gas-solid two-phase has only hundreds of milliseconds, and it flows and is similar to laminar flow, and catalyst all will be in whole reactor in a kind of state of skewness, and this will reduce the efficient of reactor greatly.
Oil company both domestic and external and scientific research structure have all been launched research to the catalyst inlet structure of descending-bed reactor.The patent (Fig. 1-A, patent No. US4338187) of Stone Webster Engineering Corp. company has adopted the design of multitube jet in its catalyst inlet device.Its advantage is the mixing that can control grain flux effectively, can realize the uniform and gas-solid of particle simultaneously.It is too complicated that but its maximum shortcoming is structure, bring easy to wear, easily stop up and overhaul shortcoming such as difficulty, be difficult to satisfy requirement of actual application.The patent of Texaco Inc. company (Fig. 1-B and Fig. 1-C, patent No. US4514285) utilizes the distribution grid of particle to realize the uniform of particle.Though simplify to some extent on the structure, the droop loss of distribution grid is big, and is difficult for reaching high particle internal circulating load, its wearing and tearing simultaneously are also bigger.By the explanation of above-mentioned existing patent as can be seen, utilize mechanical device, realize the uniform of particle, all can cause structural complexity, cause a series of difficulties in commercial Application as mozzle, distributor.
The objective of the invention is to design a kind of catalyst inlet device of gas-solid cocurrent flow descending bed reactor, overcome the deficiencies in the prior art, the turbulence mixing with gas-solid two-phase in the two phase flow itself realizes the even distribution of catalyst granules fast.Its biggest advantage is exactly can realize catalyst granules uniform fast.Have both simple in structure, requirement such as operating flexibility is big, pressure drop is little and equipment and abrasion of particles be little simultaneously, be easy in industrial realization.
The catalyst inlet device that is applicable to the gas-solid cocurrent flow descending bed reactor of the present invention design comprises the inlet of crust of the device and descending-bed reactor main body.Crust of the device and the coaxial installation of descending-bed reactor main body form annular space between the two; The ratio D1/Dr of the diameter D1 of shell and the diameter Dr of descending-bed reactor remains between 1.3～2.0.The crust of the device top is that spheroid shape forms gas-solid turbulent flow mixed zone; Vertical range H4 between ellipsoid peak and descending bed entrance face is 1.0～2.0D1; Uniform carrier gas inlet pipeline on the sidewall circumference of shell; The quantity N1 of carrier gas inlet pipeline is 4～8, and diameter D3 is 0.1～0.2D1, with inlet device shell (6) angulation β be 15 °～45 °, and the vertical range H3 between the inlet device lower surface is 1.0～1.5 times of D1; A catalyst transport pipeline is housed on the lower sides of carrier gas inlet, and its diameter D2 is 0.2～0.4D1, must be with inlet device shell (6) angulation α less than 45 °, and the vertical range H1 between the inlet device lower surface is 0.3～0.5D1; Loosening wind distributor is equipped with in described annular space bottom, on the side wall of outer shell of distributor below a loosening wind inlet duct is housed, and its diameter D4 is 25～50mm.
Above-mentioned gas-solid turbulent flow mixed zone can diminish, and the top casing of two-phase turbulent flow mixed zone changes horizontal plate into, and the vertical range H5 between itself and descending bed entrance face is 0.2～0.8D1; Simultaneously at the circumferential edges of horizontal plate angle being arranged is γ, and wide is the chamfering of W, can prevent the formation in dead band.
The top structure of above-mentioned two-phase turbulent flow mixed zone is the saddle-shape structure, vertical range H7 between the circular arc intersection of saddle-shape structure and descending bed entrance face is 0.1～0.3D1, and the vertical range H6 between circular arc peak and descending bed entrance face is 0.2～0.8D1.
Can also there be a undergauge district above-mentioned two-phase turbulent flow mixed zone; The diameter D6 in undergauge district is 0.7～0.9D1
Two-phase turbulent flow mixed zone in the above-mentioned device can add the oblique spout of carrier gas.
Inlet device of the present invention is through supercooled state flow model (diameter 420mm, high 18m) DCO, experiment shows that this inlet device can be realized the uniform fast of catalyst granules, has both simple in structure, requirement such as operating flexibility is big, pressure drop is little and equipment and abrasion of particles be little simultaneously.Experiment proves also simultaneously that in descending-bed reactor through the distance of double diameter (Dr), catalyst granules can be evenly distributed.Owing to there is not orifice, the carrier gas pressure drop of this entrance structure significantly reduces, greatly within 200Pa simultaneously.Experiment is proof also, and under various operating conditions, it is stable that the catalyst flow of this catalyst inlet device can both keep, its fluctuation＜5%.Because this apparatus structure is simple, do not have the sharp wear position of catalyst granules and equipment, so the wearing and tearing of equipment and catalyst also seldom simultaneously.This cold conditions flow model running is after 8 months, and the entrance structure that its lucite is made is still complete.
Description of drawings
Fig. 1-A is the catalyst inlet device that relates among the patent US4338187.
Fig. 1-B is the catalyst inlet device that relates among the patent US4514285.
Fig. 2 is the schematic diagram of gas-solid two-phase movement locus in this catalyst inlet device.
Fig. 3 is the front view of this catalyst inlet device.
Fig. 4 is a kind of modification of catalyst inlet device shown in Fig. 3, and main the variation is that two-phase turbulent flow mixed zone diminishes.
Fig. 5 is a kind of modification of catalyst inlet device shown in Fig. 4, and the top structure that main variation is two-phase turbulent flow mixed zone changes.
Fig. 6 is a kind of modification of catalyst inlet device shown in Fig. 4, and main the variation is the undergauge district that has of two-phase turbulent flow mixed zone.
Fig. 7 is a kind of modification of catalyst inlet device shown in Fig. 4, and main the variation is the oblique spout that two-phase turbulent flow mixed zone adds carrier gas.
Below in conjunction with accompanying drawing, introduce in detail content of the present invention.
Among Fig. 1-Fig. 7,1 is two-phase turbulent flow mixed zone. 2 is the carrier gas inlet pipeline. 3 for catalyst granules defeated Send pipeline. 4 are loosening wind distributor. 5 is the descending-bed reactor main body. 6 be the catalyst inlet device outside Shell. 7 for being positioned at the intersubjective annular space of shell and descending-bed reactor. 8 are loosening wind inlet duct. 9 is two-phase Top enclosure after the turbulent flow mixed zone dwindles. 10 is the another kind of its top enclosure after two-phase turbulent flow mixed zone dwindles Configuration. 11 is the crust of the device behind the undergauge. 12 is the oblique spout of the carrier gas of two-phase turbulent flow mixed zone. 13 is two sections Formula riser regenerating unit. 14 is down-flow fluidized bed using ECT catalyst inlet device. 15 is the feedstock oil entrance. 16 is down-flow fluidized bed using ECT Reactor body. 17 is catalyst and the fast separation device that reacts rear oil gas. 18 is cyclone separation system. 19 Be the catalyst stripping device.
Size label wherein is: Dr is the diameter of descending-bed reactor main body. D1 is outside the catalyst inlet device The diameter of shell. D2 is the diameter of catalyst transport pipeline. D3 is the diameter of carrier gas inlet pipeline (Fig. 3). D4 is the diameter of loosening wind inlet duct. D5 is the diameter in undergauge district, two-phase turbulent flow mixed zone. H1 is catalyst Vertical range between conveyance conduit and inlet device lower surface. H2 is inlet of downer end face and inlet device lower end Vertical range between face. H3 is the vertical range between carrier gas inlet pipeline and inlet device lower surface. H4 is two Vertical range between phase turbulent flow mixed zone peak (Fig. 3) and inlet of downer end face. H5 is mixed for the two-phase turbulent flow Close and distinguish the vertical range of dwindling between rear (Fig. 5) its top enclosure and inlet of downer end face. H6 is another kind of top Vertical range between section's shell (Fig. 6) circular arc peak and inlet of downer end face. H7 is outside the another kind of top Vertical range between shell (Fig. 6) circular arc intersection and inlet of downer end face. W is the contracting of two-phase turbulent flow mixed zone The chamfering width of (Fig. 5) its top enclosure after little. N1 is the quantity of carrier gas inlet pipeline. α is that catalyst is defeated Send pipeline and inlet device housing angulation. β is the angle that the carrier gas inlet pipeline becomes with the inlet device housing Degree. γ is the chamfer angle of (Fig. 5) its top enclosure after two-phase turbulent flow mixed zone dwindles.
Introduce workflow of the present invention below in conjunction with Fig. 2, Fig. 3. Catalyst leaves the riser regeneration of catalyst Behind the device (14), entered by inlet device shell (6) and down-flow fluidized bed using ECT by catalyst granules conveyance conduit (3) In the annular space (7) that reactor body (5) forms. Under loosening wind action, be close mutually upwards motion. When It moves near the carrier gas inlet pipeline (2) because the high velocity jet effect of carrier gas, catalyst granules begin into Row mixes with the violent turbulence of carrier gas. Two-phase turbulent flow mixed zone has guaranteed fully mixing of catalyst and carrier gas. Urge Change the agent particle after fully the mixing of two-phase turbulent flow mixed zone and carrier gas, enter descending-bed reactor main body and oil gas Begin reaction.
As shown in Figure 3, this down-flow fluidized bed using ECT catalyst inlet structure is mainly entered by catalyst transport pipeline (3), carrier gas Mouth pipeline (2), two-phase turbulent flow mixed zone, descending-bed reactor entrance (5) and loosening wind apparatus (4,8) Form. The characteristic size of inlet device is the diameter D1 of its shell. The diameter Dr's of D1 and descending-bed reactor Ratio D1/Dr remains between 1.3～2.0.
Particle transport pipeline (3) is to connect catalyst regeneration device (14) and down-flow fluidized bed using ECT catalyst inlet device (15) pipeline. Its diameter D2 is 0.2～0.4D1, and angulation α is necessary with inlet device shell (6) Less than 45 °, and the vertical range H1 between the inlet device lower surface is 0.3～0.5D1.
Catalyst granules enters into by inlet device shell (6) and descending-bed reactor from grain conveyance conduit (3) In the annular space (7) that main body (5) forms. Below annular space, be provided with loosening wind distributor (4) and loosening wind entrance Pipeline (8). The diameter D4 of loosening wind inlet duct is 25～50mm. Loosening wind action is to carry particle Form with close phase moves upward. Loosening wind energy enough make catalyst granules stable in annular space (7), equably to Upper flowing is for guaranteeing that stable grain flux is most important. The flow of loosening wind be 10% of carrier gas air quantity～30%.
Carrier gas inlet pipeline (2) evenly distributes along shell (6) circumference of inlet device, to reach the even distribution of gas-solid two-phase.Its quantity N1 is 4～8, and diameter D3 is 0.1～0.2D1, with inlet device shell (6) angulation β be 15 °～45 °, and the vertical range H3 between the inlet device lower surface is 1.0～1.5 times of D1.
Two-phase turbulent flow mixed zone is the semiellipse type, is become by two-phase turbulent flow mixed zone shell (1) encirclement.Vertical range H4 between its peak and descending bed entrance face is 1.0～2.0 times of D1.
Particle with after carrier gas mixes rapidly, evenly enters descending-bed reactor (5) inlet in two-phase turbulent flow mixed zone.Vertical range H3 between descending bed entrance face and inlet device lower surface is 1.2～1.6D1.
Embodiments of the invention are:
Embodiment 1: Fig. 4 is a kind of modification of catalyst inlet device shown in Fig. 3, and main the variation is that two-phase turbulent flow mixed zone diminishes.The top casing of two-phase turbulent flow mixed zone changes horizontal plate (9) into, and the vertical range H5 between itself and descending bed entrance face is 0.2～0.8D1.Simultaneously at its circumferential edges angle being arranged is γ, and wide is the chamfering of W, can prevent the formation in dead band.
Embodiment 2: Fig. 5 is a kind of modification of catalyst inlet device shown in Fig. 4, and the top structure that main variation is two-phase turbulent flow mixed zone changes.Top casing becomes saddle-shape (10) structure by the horizontal plate (9) of Fig. 4.This helps particle to flow to descending bed porch.From Fig. 5, its axial cross section of crossing the center is two crossing circular arcs.Vertical range H7 between circular arc intersection and descending bed entrance face is 0.1～0.3D1, and the vertical range H6 between circular arc peak and descending bed entrance face is 0.2～0.8D1.
Embodiment 3: Fig. 6 is a kind of modification of catalyst inlet device shown in Fig. 4, and main the variation is that two-phase turbulent flow mixed zone has a undergauge district.The diameter D5 in undergauge district is 0.7～0.9D1.The movement velocity of particle can improve in the undergauge district, and the quickening carrier gas mixes with catalyst, reduces the time of staying of particle in inlet device.
Embodiment 4: Fig. 7 is a kind of modification of catalyst inlet device shown in Fig. 4, and main the variation is the oblique spout (12) that two-phase turbulent flow mixed zone adds carrier gas.The oblique spout of carrier gas helps to eliminate the dead band of two-phase turbulent flow mixed zone.
Descending-bed reactor utilizes gas-solid along the characteristics that gravitational field moves downward, and can adapt to catalytic cracking/cracking rapid-action requirement.Usually, its gas-solid mixing, the descending haptoreaction of gas-solid two-phase, gas-solid separate total process of three operations fast and finished within 1 second.Owing in the ultrashort time, finish gas-solid contact and reaction, and gas-solid two phase concentrations, velocity radial are evenly distributed in the reactor, and time of staying distribution is approximately laminar flow, and the back-mixing of catalyst and oil gas is little, help the raising of reaction selectivity, reduce catalyst and dry gas output.This entrance structure can be fast, equably at descending bed porch distribution catalyst granules, adapt to descending-bed reactor fast reaction and the mobile characteristics of approximate laminar flow.Simultaneously it has both requirements such as simple in structure, that operating flexibility is big, pressure drop is little and equipment and abrasion of particles be little, is easy in industrial realization.
Claims (5)
1, a kind of catalyst inlet device that is applicable to the gas-solid cocurrent flow descending bed reactor is characterized in that this device comprises the inlet of crust of the device and descending-bed reactor main body; Described crust of the device and the coaxial installation of descending-bed reactor main body form annular space between the two; The ratio D1/Dr of the diameter D1 of shell and the diameter Dr of descending-bed reactor remains between 1.3～2.0; Described crust of the device top is that spheroid shape forms gas-solid turbulent flow mixed zone; Vertical range H4 between ellipsoid peak and descending bed entrance face is 1.0～2.0D1; Be evenly equipped with the carrier gas inlet pipeline on the sidewall circumference of shell; The quantity N1 of carrier gas inlet pipeline is 4～8, and diameter D3 is 0.1～0.2D1, with inlet device shell angulation β be 15 °～45 °, and the vertical range H3 between the inlet device lower surface is 1.0～1.5 times of D1; A catalyst transport pipeline is housed on the lower sides of carrier gas inlet, and its diameter D2 is 0.2～0.4D1, with inlet device shell angulation α less than 45 °, and the vertical range H1 between the inlet device lower surface is 0.3～0.5D1; Loosening wind distributor is equipped with in described annular space bottom, on the side wall of outer shell of distributor below a loosening wind inlet duct is housed, and its diameter D4 is 25～50mm.
2, install according to claim 1, it is characterized in that the top casing of described gas-solid turbulent flow mixed zone is a horizontal plate, the vertical range H5 between this horizontal plate and descending bed entrance face is 0.2～0.8D1; At its circumferential edges angle being arranged is γ, and wide is the chamfering of W.
3, as device as described in claims 2, it is characterized in that the top of two-phase turbulent flow mixed zone is the saddle-shape structure; Vertical range H7 between the circular arc intersection of saddle-shape structure and descending bed entrance face is 0.1～0.3D1, and the vertical range H6 between circular arc peak and descending bed entrance face is 0.2～0.8D1.
4, as device as described in claims 2, it is characterized in that there is a undergauge district two-phase turbulent flow mixed zone; The diameter D6 in undergauge district is 0.7～0.9D1
5, as device as described in claims 2, it is characterized in that two-phase turbulent flow mixed zone is provided with the oblique spout of carrier gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00106169A CN1090530C (en) | 2000-04-28 | 2000-04-28 | Catalyst inlet device adaptable to gas-solid cocurrent flow descending bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00106169A CN1090530C (en) | 2000-04-28 | 2000-04-28 | Catalyst inlet device adaptable to gas-solid cocurrent flow descending bed reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1275434A true CN1275434A (en) | 2000-12-06 |
| CN1090530C CN1090530C (en) | 2002-09-11 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN00106169A Expired - Lifetime CN1090530C (en) | 2000-04-28 | 2000-04-28 | Catalyst inlet device adaptable to gas-solid cocurrent flow descending bed reactor |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2003090918A1 (en) * | 2002-04-26 | 2003-11-06 | China Petroleum & Chemical Corporation | Downflow catalytic cracking reactor and use thereof |
| CN109847656A (en) * | 2019-04-12 | 2019-06-07 | 辽宁加宝石化设备有限公司 | Gas-solid short contact separator, gas-solid short contact system and application method |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4364905A (en) * | 1979-11-23 | 1982-12-21 | Standard Oil Company (Indiana) | Fluid catalytic cracking apparatus having riser reactor and improved means associated with the riser reactor for separating cracked product and entrained particulate catalyst |
| US4514285A (en) * | 1983-03-23 | 1985-04-30 | Texaco Inc. | Catalytic cracking system |
| CN1009659B (en) * | 1985-06-24 | 1990-09-19 | 法国石油公司 | Process and equipment for fluidized bed catalytic cracking |
| FR2584732B1 (en) * | 1985-07-10 | 1988-08-19 | Raffinage Cie Francaise | PROCESS AND DEVICE FOR THE CATALYTIC CRACKING OF HYDROCARBON CHARGES, WITH CONTROL OF THE REACTION TEMPERATURE |
| US5296131A (en) * | 1992-12-02 | 1994-03-22 | Mobil Oil Corporation | Process for short contact time cracking |
-
2000
- 2000-04-28 CN CN00106169A patent/CN1090530C/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2003090918A1 (en) * | 2002-04-26 | 2003-11-06 | China Petroleum & Chemical Corporation | Downflow catalytic cracking reactor and use thereof |
| GB2403434A (en) * | 2002-04-26 | 2005-01-05 | China Petroleum & Chemical | Downflow catalytic cracking reactor and use thereof |
| GB2403434B (en) * | 2002-04-26 | 2005-09-14 | China Petroleum & Chemical | A downflow catalytic cracking reactor and its application |
| CN109847656A (en) * | 2019-04-12 | 2019-06-07 | 辽宁加宝石化设备有限公司 | Gas-solid short contact separator, gas-solid short contact system and application method |
| CN109847656B (en) * | 2019-04-12 | 2024-05-14 | 辽宁加宝石化设备有限公司 | Gas-solid contact separation device, gas-solid contact separation system and application method |
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| CN1090530C (en) | 2002-09-11 |
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