CN1191325C - Oil Solution mixing chamber for catalytic cracking riser reactor - Google Patents
Oil Solution mixing chamber for catalytic cracking riser reactor Download PDFInfo
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- CN1191325C CN1191325C CNB011184302A CN01118430A CN1191325C CN 1191325 C CN1191325 C CN 1191325C CN B011184302 A CNB011184302 A CN B011184302A CN 01118430 A CN01118430 A CN 01118430A CN 1191325 C CN1191325 C CN 1191325C
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- transfer lime
- riser tube
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Abstract
The present invention relates to an oil solution mixing chamber for a catalytic cracking riser reactor, which comprises a pre-riser 1, an inner conveying pipe 4, an outer conveying pipe 5, risen medium distributors 8, 10 and 11, chemkleen distributors 3 and 6, wherein the pre-riser and the inner conveying pipe are arranged coaxially from bottom to top, a circular transition section 2 is arranged between the pre-riser and the inner conveying pipe, the outer conveying pipe is positioned on the outer side of the inner conveying pipe, and the outer conveying pipe and the inner conveying pipe are coaxial; the upper part of the outer conveying pipe is connected with a riser 7 after diameter reduction, while the lower part of the outer conveying pipe is connected with the circular transition section 2 afterdiameter reduction; the chemkleen distributors 3 and 6 are respectively positioned on the lower part and the upper part of the outer conveying pipe; the present invention has the advantage of good mixing effect of oil solutions.
Description
Technical field
The invention belongs to hydrocarbon oil catalytic cracking equipment, more particularly, is a kind of oil solution mixing chamber that is used for catalytic cracking riser reactor.
Background technology
The rise of crude oil price is had a strong impact on the survival and development of oil refining enterprise in the world wide, and the oil refining industry can only rely on scale and benefit and technical progress seeking development.From long-range viewpoint, catalytic cracking will be to produce one of main means of Fuel Petroleum, and for diesel oil and industrial chemicals, also will promote the development of catalytic cracking process process as the demand of gas alkene, aromatic hydrocarbons etc.
Riser tube is as the history in existing 50 years of catalyst cracker.In these 50 years, the progress of riser reactor aspect process engineering is mainly reflected in following aspect: the design of hydrocarbon ils atomizing nozzle, hydrocarbon ils are along riser tube sectional feeding, Quench technology and riser tube outlet finish sharp separation technology etc.; And be not a lot of about the report of the initial contact segment texture improvement of riser tube bottom finish.
USP4820493 discloses a kind of improved oil solution mixing chamber.This mixing section is arranged on the bottom of riser reactor, and the mixing section internal diameter is slightly larger than the riser tube internal diameter; In mixing section, be provided with from bottom to up vertically and promote transfer lime in medium ingress pipe and the catalyzer; Promote between medium ingress pipe, the interior transfer lime of catalyzer and the mixing section and form an annular space, the regenerated catalyst of close phase is full of the bottom of this annular space; Regenerated catalyst enters transfer lime in the catalyzer in the slit under the effect of annular space upper pressure and catalyst bed stressor layer, in promoting medium ingress pipe and catalyzer between the transfer lime, and sends into riser tube under the effect that promotes medium.Though the design of this oil solution mixing chamber can improve the flow state of riser tube inner catalyst to a certain extent, but because the gaseous pressure on mixing section top not only directly influences the internal circulating load of catalyzer, but also can influence the blanking amount of regenerator sloped tube, cause the operation fluctuation of device.
The structure of the disclosed oil solution mixing chamber of CN1174094A is similar to USP4820493, just the tremie pipe with regenerated catalyst is immersed in the catalyzer dense-phase bed, thereby avoided of the direct influence of the interior gaseous pressure of mixing section, mainly by line of pipes velocity modulation joint catalyst recirculation amount in changing to regenerated catalyst blanking amount.This design can produce detrimentally affect to the flow condition of riser tube inner catalyst inevitably, makes the radial distribution of catalyzer more inhomogeneous.
USP5318691 discloses a kind of structure design of improving intake zone finish contact effect.This design makes regenerated catalyst enter deceleration area behind an annular space, increases suddenly because the deceleration area cross-section of pipeline is long-pending, causes the density of catalyst increase and is vortex flow; Hydrocarbon ils is through cone shape feed distributor, inject above-mentioned catalyzer deceleration area with lower linear speed.In this design, distribute mutually because the catalyzer that hydrocarbon oil crude material touched is close, thereby can obtain comparatively ideal atomizing effect; Can strengthen finish contact effect to a certain extent though catalyzer is vortex flow, can cause the catalyzer back-mixing inevitably, the fresh hydrocarbon oil crude material of part is contacted with the catalyzer of carbon deposit, product selectivity is caused detrimentally affect.
CN1217366A improves the agent oil contact efficiency of mentioned nozzle area, and adopts the necking down structure to prevent the axial landing of limit wall catalyzer by dwindling riser diameter, setting up a method of tangential second lift wind.But because tangential number of nozzle and tangentially promote distinguished and admirable quantitative limitation, can only play certain mitigation to the flow condition of " Bian Binong, center rare " in the riser tube, the problem of riser tube catalyzer radial distribution inequality still is not resolved.
In sum, in the prior art structure of the initial contact segment of disclosed riser tube finish do not make the riser tube inner catalyst flow state be improved significantly, the texture improvement that has even can cause detrimentally affect to the reactivity worth of riser tube.
Summary of the invention
The object of the present invention is to provide a kind of novel oil solution mixing chamber that is used for catalytic cracking riser reactor, this oil solution mixing chamber can make that hydrocarbon ils and the catalyzer flow state in riser tube improves, the reactivity worth of riser tube is optimized.
The mixing section that is used for catalytic cracking riser reactor provided by the present invention comprises with lower member: pre-riser tube 1, interior transfer lime 4, outer transfer lime 5, lifting dielectric distribution device 8,10 and 11, hydrocarbon oil distribution device 3 and 6; Wherein, pre-riser tube 1 and the coaxial from bottom to up setting of interior transfer lime 4 are round table-like transition section 2 between the two, and along the even perforate of rotation sidewall direction of this round platform; Outer transfer lime is positioned at the outside of transfer lime, and coaxial with interior transfer lime, and they form annular cavity between the two; Link to each other with riser tube 7 behind the top undergauge of outer transfer lime, and behind the undergauge of its underpart with pre-riser tube and interior transfer lime between round table-like transition section 2 link to each other; Promote that dielectric distribution device 8,10 and 11 is arranged at interior transfer lime, pre-riser tube respectively and by the bottom of the formed annular cavity of inside and outside transfer lime; Hydrocarbon oil distribution device 3 and 6 is arranged at the bottom and the top of outer transfer lime respectively.
Description of drawings
Fig. 1 is the structural representation of oil solution mixing chamber provided by the present invention.
Fig. 2 is the position view of oil solution mixing chamber provided by the present invention in catalytic cracking unit.
Embodiment
Describe the structure of oil solution mixing chamber provided by the present invention below in detail.
As shown in Figure 1, the bottom of oil solution mixing chamber provided by the present invention is columned pre-riser tube 1, and its height is 1: 3～20 with the ratio of riser tube useful length, and the ratio of its diameter and riser tube mean diameter is 1: 0.5～2.Pre-riser tube 1 links to each other with regenerated catalyst tremie pipe 9, and angle between the two is 20～60 °.The lower end sealing of pre-riser tube, its upper end links to each other with interior transfer lime 4 by round table-like transition section 2.With promote the bottom that lifting dielectric distribution device 10 that the medium supply line links to each other is positioned at pre-riser tube, this sparger can adopt any sparger that disperses the lifting medium that is applicable to, for example, distribution rings, nozzle, the seedpod of the lotus are first-class.
The upper end of pre-riser tube 1 links to each other with a round table-like transition section 2.The upper end diameter of this transition section is identical with the lower end diameter of interior transfer lime, and its lower end diameter is identical with the diameter of pre-riser tube, and the reducing taper angle theta is 15～75 °.This transition section is along the even perforate of rotation sidewall direction, and the ratio of perforated area and this transition section outer surface area is 1: 2～10.The present invention to the shape of above-mentioned perforate without limits, circular hole, square hole, oblong aperture etc. all can.
Be provided with and promote the lifting dielectric distribution device 8 that the medium supply line links to each other in interior transfer lime inside, the distance of the lower edge of this sparger to interior transfer lime bottom is 0.2～1.5: 1 with the ratio of interior transfer lime lower end diameter.This sparger can adopt any sparger that disperse to promote medium that is applicable to, for example, distribution rings, nozzle, the seedpod of the lotus are first-class.
The outside of transfer lime 4 in outer transfer lime 5 is located at, and with the coaxial setting of interior transfer lime.The ratio of the diameter of outer transfer lime 5 and interior transfer lime mean diameter is 1.3～5: 1, preferred 1.5～3: 1; Outer transfer lime is 1.1～3: 1 with the ratio of the height of interior transfer lime, preferred 1.2～1.5: 1.The diameter of outer transfer lime is 1.5～4: 1 with the ratio of the mean diameter of riser reactor 7, preferred 1.5～3: 1.Form an annular cavity between interior transfer lime 4 and the outer transfer lime 5.The top of outer transfer lime links to each other with riser tube 7 by round table-like undergauge section 5a, and the reducing cone angle is 30～50 °.The bottom of outer transfer lime links to each other with round table-like transition section 2 between pre-riser tube 1 and the interior transfer lime 4 by round table-like undergauge section 5b, and the reducing cone angle beta is 30～50 °.
Be provided with in the bottom of interior transfer lime 4 and outer transfer lime 5 formed annular cavities and promote dielectric distribution device 11, this sparger links to each other with lifting medium supply line.This sparger can adopt any sparger that disperse to promote medium that is applicable to, for example, distribution rings, nozzle, the seedpod of the lotus are first-class.
Hydrocarbon oil distribution device 3 is positioned at the bottom of outer transfer lime 5.This sparger should be arranged on the top that promotes dielectric distribution device 11, its upper end to the vertical range that promotes dielectric distribution device 11 with outside the ratio of internal diameter of delivery hose be 0.05～0.5, preferred 0.08～0.15.Hydrocarbon oil distribution device 3 can be made up of 3～20 along the circumferential direction equally distributed hydrocarbon ils atomizing nozzles, also can select the sparger of patterns such as the distribution rings that is suitable for disperseing hydrocarbon ils, shower nozzle, sieve plate for use.
The top, the below of undergauge section 5a of transfer lime 4 in hydrocarbon ils nozzle 6 is arranged at, the angle γ of itself and vertical direction is 30～50 °, preferred 40～50 °.Hydrocarbon oil distribution device 6 can be made up of 3～20 nozzles that along the circumferential direction evenly are provided with, and this sparger can be selected the high-efficient atomizing nozzle of any pattern for use, for example, and LPC type nozzle, KH type nozzle etc.
Further specify the mode of operation of oil solution mixing chamber provided by the invention below in conjunction with accompanying drawing 2.
As shown in Figure 2, enter in the pre-riser tube 1 through regenerated catalyst tremie pipe 9 from the high-temperature regenerated catalyst of revivifier, promote medium, for example steam and/or dry gas inject pre-riser tube bottom through sparger 10, promote regenerated catalyst, making it to quicken upwards to flow.Part regenerated catalyst in the transfer lime 4, promotes medium transfer lime in sparger 8 injects in round table-like transition section 2 enters, make the catalyzer in this pipe continue to quicken upwards to flow; The perforate of another part catalyzer on round table-like transition section 2 enters in the annular cavity, promotes medium and injects this annular cavity through sparger 11, is beneficial to fluidisation, the conveying of catalyzer.Hydrocarbon oil crude material injects annular cavities through nozzle 3, contact with catalyzer in the cavity, and reacts under the catalytic cracking reaction condition, and reaction oil gas and mixture of catalysts are upwards mobile along annular cavity.Hydrocarbon oil distribution device 3 can be selected to inject hydrocarbon oil crude material of different nature according to the requirement of production decision, also can only inject an amount of protection steam, and not inject hydrocarbon oil crude material.The top of transfer lime is outside converged from the finish mixture of annular cavity and catalyzer from interior transfer lime; Meanwhile, hydrocarbon oil crude material injects through nozzle 6, mixes with above-mentioned logistics, and reacts under the catalytic cracking reaction condition.Reactant flow continues upwards to flow, and enters in the riser reactor 7.Reactant flow is flowed through behind the riser reactor, slightly revolves 12 and the catalyzer of cyclone separator 13 separating reaction oil gas and reaction back carbon deposit by the riser tube outlet, and oil gas is introduced subsequent separation system, further is separated into various products.The catalyzer of carbon deposit enters stripper 14, behind the water vapor stripping, sends into the revivifier coke burning regeneration by pipeline 15 to be generated, and the catalyzer after the regeneration returns pre-riser tube 1 through tremie pipe 9 and recycles.
Compared with prior art, beneficial effect of the present invention is mainly reflected in the following aspects:
1. the present invention can improve finish contact effect, be the good initial reaction condition of catalytic cracking reaction creation of hydrocarbon ils.In the present invention, the diameter of interior transfer lime increases from bottom to top gradually, makes that the linear gas velocity in this pipe exit reduces, catalyst density improves; In addition, the catalyzer in the annular cavity with higher flow velocity transfer lime top outside the limit wall enters, can prevent that catalyzer in this zone is along the axial landing of limit wall under the effect that promotes medium.Owing to there is the influence of above-mentioned two aspects, by outer transfer lime top inject hydrocarbon oil crude material touched is the higher catalyst stream of density of avoiding axial landing, so both helped the atomizing of hydrocarbon oil crude material, reaction preference is improved.
2. the present invention can make the radial distribution of riser tube inner catalyst logistics more even.Because the present invention is at the suitable undergauge in the exit of oil solution mixing chamber, and then link to each other with riser reactor.This design can improve riser tube inlet linear speed, and prevents the axial landing of catalyzer to a certain extent, makes the radial distribution of riser tube inner catalyst more even.
3. oil solution mixing chamber provided by the invention can be adjusted operating method flexibly according to the requirement of production decision, thereby improves the yield and the quality thereof of purpose product.
4. oil solution mixing chamber provided by the invention is simple in structure, is easy to make, and is convenient to operation.
The following examples will be further specified the present invention, but therefore not make the present invention be subjected to any restriction.
Present embodiment is to use the resulting test-results of oil solution mixing chamber provided by the present invention on the catalytic cracking middle-scale device.
Employed catalyzer is industrial by Qilu Petrochemical company catalyst plant among this embodiment, and trade names are DVR-1, and its main physico-chemical property is listed in table 1.Stock oil is grand celebration vacuum residuum, and its character is listed in table 2.In treatment capacity is on the catalytic cracking middle-scale device of 0.24t/d, adopts oil solution mixing chamber research experiment provided by the present invention, and the structural representation of reactive moieties is referring to accompanying drawing 2.Main testing sequence is as follows: the high-temperature regenerated catalyst from revivifier enters in the pre-riser tube 1 through regenerated catalyst tremie pipe 9, quickens upwards to flow under the effect of pre-lifting steam; Part regenerated catalyst and continues upwards mobile under the effect that promotes medium through round table-like transition section 2 enters in the transfer lime 4; The perforate of the regenerated catalyst of rest part on round table-like transition section 2 enters in the annular cavity, and upwards flows at the effect lower edge annular cavity that promotes steam; The top of transfer lime is outside converged from the catalyzer of annular cavity and catalyzer from interior transfer lime, and stock oil injects through nozzle 6, contacts with catalyzer and reacts under the catalytic cracking reaction condition; Reactant flow continues upwards to flow, and enters in the riser reactor 7; Reactant flow is flowed through behind the riser reactor, slightly revolves 12 and the catalyzer of cyclone separator 13 separating reaction oil gas and reaction back carbon deposit by the riser tube outlet, and oil gas is introduced subsequent separation system, further is separated into various products, and they are measured respectively, analyze; The catalyzer of carbon deposit enters settling vessel 14, behind the water vapor stripping, sends into the revivifier coke burning regeneration by pipeline 15 to be generated, and the catalyzer after the regeneration returns pre-riser tube 1 through tremie pipe 9 and recycles.Main operational condition, test-results and main products character see Table 3.
Comparative Examples 1
This Comparative Examples is to adopt the resulting test-results of finish mixed structure shown in the accompanying drawing 1 among the USP5318691 on the catalytic cracking middle-scale device.
It is all identical with embodiment to test used stock oil, catalyzer, main operational condition and testing sequence, and product distributes and main products character sees Table 3.
The test-results of embodiment and Comparative Examples in the comparison sheet 3, as can be seen, under stock oil, catalyzer and the main essentially identical prerequisite of operational condition, adopt oil solution mixing chamber provided by the present invention that product is distributed and improve, the yield of high-value product is improved.Illustrate that oil solution mixing chamber provided by the present invention has comparatively ideal finish contact effect, can create good initial reaction condition for the catalytic cracking of hydrocarbon ils.
Table 1
| The catalyzer title | DVR-1 |
| Chemical constitution, heavy % Na 2O Al 2O 3Fe 2Q 3Tap density, kg/m 3Pore volume, cm 3/ g specific surface, m 2/ g size consist; Heavy % 0～20 μ m 20～40 μ m 40～80 μ m 80～100 μ m＞100 μ m catalyst micro-activities (800 ℃, 4h) | 0.14 48.5 0.29 670 0.41 296 1.5 17.2 55.6 15.9 9.8 75 |
Table 2
| Density (20 ℃), kilogram/rice 3Kinematic viscosity (100 ℃), millimeter 2/ second carbon residue, heavy % condensation point, ℃ elementary composition, heavy % C H S heavy metal, ppm Fe V Na Cu Ni boiling range, ℃ initial boiling point distillates rate, V% for 10% 500 ℃ | 910.2 51.16 7.5 37 88.81 11.08 0.11 5.0 0.1 2.2 0.1 6.9 378 420 21 |
Table 3
| | Embodiment | 1 | Comparative Examples 1 |
| Main operational condition: | |||
| Temperature of reaction, ℃ | 510 | 512 | |
| Reaction pressure (gauge pressure), kPa | 0.131 | 0.132 | |
| Raw material preheating temperature, ℃ | 220 | 220 | |
| The regenerator temperature, ℃ | 668 | 665 | |
| Agent-oil ratio | 7.4 | 6.5 | |
| Reaction times, s | 2.6 | 3.1 | |
| Product distributes, heavy % | |||
| Dry gas | 5.21 | 5.10 | |
| Liquefied gas | 12.97 | 13.98 | |
| Gasoline | 42.93 | 41.92 | |
| Diesel oil | 24.09 | 22.97 | |
| Heavy oil | 5.53 | 5.64 | |
| Coke | 8.9 | 10.08 | |
| Loss | 0.37 | 0.31 | |
| Transformation efficiency, heavy % | 70.38 | 71.39 | |
| Yield of light oil, heavy % | 67.02 | 64.89 | |
| Main products character: | |||
| Gasoline density, g/cm 3 | 0.7221 | 0.7224 | |
| Gasoline RON | 90.4 | 90.6 | |
| MON | 78.6 | 78.7 | |
| Diesel oil density, g/cm 3 | 0.8745 | 0.8703 | |
| Condensation point of diesel oil, ℃ | -3 | -1 |
Claims (3)
1, a kind of oil solution mixing chamber that is used for catalytic cracking riser reactor is characterized in that this mixing section comprises with lower member: pre-riser tube (1), interior transfer lime (4), outer transfer lime (5), lifting dielectric distribution device (8,10,11), hydrocarbon oil distribution device (3,6), regenerated catalyst tremie pipe (9); Wherein, pre-riser tube (1) and the coaxial from bottom to up setting of interior transfer lime (4) they are round table-like transition section (2) between the two, and along the even perforate of rotation sidewall direction of this round platform; Outer transfer lime is positioned at the outside of transfer lime, and coaxial with interior transfer lime, and they form annular cavity between the two; Link to each other with riser tube (7) behind the top undergauge of outer transfer lime, and behind the undergauge of its underpart with pre-riser tube and interior transfer lime between round table-like transition section (2) link to each other; Promote that dielectric distribution device (8,10,11) is arranged at interior transfer lime, pre-riser tube respectively and by the bottom of the formed annular cavity of inside and outside transfer lime; Hydrocarbon oil distribution device (3,6) is arranged at the bottom and the top of outer transfer lime respectively;
Described pre-riser tube (1) is cylindric, and the ratio of its diameter and riser tube mean diameter is 1: 0.5～2, and its height is 1: 3～20 with the ratio of riser tube useful length; This pipe links to each other with regenerated catalyst tremie pipe (9), and angle between the two is 20～60 °;
The upper end diameter of described round table-like transition section (2) is identical with the lower end diameter of interior transfer lime, and its lower end diameter is identical with the diameter of pre-riser tube, and the reducing taper angle theta is 15～75 °; The ratio of perforated area and this transition section outer surface area is 1: 2～10;
The diameter of transfer lime (4) enlarges from bottom to top gradually in described, and the ratio of its lower end diameter and upper end diameter is 1: 1.2～2; The ratio of the height of interior transfer lime and riser tube useful length is 1: 3～40;
The diameter of described outer transfer lime (5) and the ratio of interior transfer lime mean diameter are 1.3～5: 1, and the ratio of their height is 1.1～3: 1; The ratio of the mean diameter of the diameter of outer transfer lime and riser reactor (7) is 1.5～4: 1;
The top of described outer transfer lime (5) links to each other with riser tube (7) by round table-like undergauge section (5a), and the reducing cone angle is 30～50 °; Its underpart links to each other with round table-like transition section (2) by round table-like undergauge section (5b), and the reducing cone angle beta is 30～50 °;
The described hydrocarbon oil distribution device (3) that is positioned at outer transfer lime bottom is set in place in the top of the lifting dielectric distribution device (11) bottom the formed annular cavity of inside and outside transfer lime, its upper end to the vertical range that promotes dielectric distribution device (11) with outside the ratio of internal diameter of delivery hose be 0.05～0.5, and the hydrocarbon oil distribution device (6) that is arranged on the top of outer transfer lime is positioned at the top of transfer lime (4), the below of undergauge section (5a), and the angle γ of itself and vertical direction is 30～50 °;
The distance of the lower edge of the lifting dielectric distribution device (8) of transfer lime bottom to interior transfer lime bottom is 0.2～1.5: 1 with the ratio of interior transfer lime lower end diameter in described being arranged at.
2,, it is characterized in that described hydrocarbon oil distribution device (3,6) is by 3～20 nozzles compositions that along the circumferential direction evenly are provided with according to the oil solution mixing chamber of claim 1.
3,, it is characterized in that the described hydrocarbon oil distribution device (3) that is positioned at outer transfer lime bottom is selected from distribution rings, shower nozzle or sieve plate according to the oil solution mixing chamber of claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011184302A CN1191325C (en) | 2001-05-30 | 2001-05-30 | Oil Solution mixing chamber for catalytic cracking riser reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011184302A CN1191325C (en) | 2001-05-30 | 2001-05-30 | Oil Solution mixing chamber for catalytic cracking riser reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1388212A CN1388212A (en) | 2003-01-01 |
| CN1191325C true CN1191325C (en) | 2005-03-02 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011184302A Expired - Lifetime CN1191325C (en) | 2001-05-30 | 2001-05-30 | Oil Solution mixing chamber for catalytic cracking riser reactor |
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| CN (1) | CN1191325C (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100443567C (en) * | 2005-08-31 | 2008-12-17 | 中国石油化工股份有限公司 | Inner-component for enhancing air-solid contact of catalytic cracking reaction system |
| CN101850226B (en) * | 2010-01-21 | 2012-12-12 | 中国石油天然气股份有限公司 | Riser reactor for fluidized catalytic conversion by dense phase section feeding |
| CN102059080B (en) * | 2010-11-19 | 2013-05-29 | 洛阳森德石化工程有限公司 | Catalytic cracking riser tube feeding mixing section structure for inhibiting back-mixing of catalyst |
| CN102120165B (en) * | 2010-11-19 | 2013-12-18 | 洛阳森德石化工程有限公司 | Catalytic cracking lifting pipe feeding and mixing section structure for inhibiting catalyst backmixing |
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2001
- 2001-05-30 CN CNB011184302A patent/CN1191325C/en not_active Expired - Lifetime
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