CN1393508A - Catalytic conversion process for increasing output of diesel oil and low-carbon olefin - Google Patents
Catalytic conversion process for increasing output of diesel oil and low-carbon olefin Download PDFInfo
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- CN1393508A CN1393508A CN 01119806 CN01119806A CN1393508A CN 1393508 A CN1393508 A CN 1393508A CN 01119806 CN01119806 CN 01119806 CN 01119806 A CN01119806 A CN 01119806A CN 1393508 A CN1393508 A CN 1393508A
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Abstract
A catalytic transform process for increasing the outupt of diesel oil and low-carbon olefin features that the regenerator (20-80 wt.%) comes into internal delivery tube via transition segment, the rest of catalyst is fed in ring cavity via hole of the said transition segment, the gasoline is fed in the said ring cavity containing catalyst for reaction, the mixture from ring cavity, the catalyst from internal delivery tube, and the crude hydrocarbon oil are in contact with each other in upper part of external delivery tube for reaction, the oil-gas is separated, and the catalyst is regenerated. Its advantage is high output rate of targent product.
Description
The invention belongs to the catalysis conversion method of petroleum hydrocarbon under the situation that does not have hydrogen, more particularly, is the catalysis conversion method of a kind of increasing output of diesel oil and liquefied gas.
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.
CN1160746A preferentially contacts it low-quality gasoline fraction injecting lift pipe such as straight-run spirit, coker gasoline bottom with high-temperature regenerated catalyst, and than carrying out catalytic conversion reaction under the exacting terms, with the octane value of raising gasoline fraction.
CN1279270A discloses the catalysis conversion method of a kind of high-yield diesel oil and liquefied gas.This method is straight-run spirit, coker gasoline or catalytic gasoline injecting lift pipe bottom, contacts with regenerated catalyst and reacts, and the finish mixture that is generated is up along riser tube; In the conventional atomizing nozzle injecting lift pipe of catalytically cracked stock, contact with above-mentioned finish mixture by different level; Inject reaction terminating agent at the riser tube outlet section.
USP5846403 has disclosed a kind of method of catalytic cracking volume increase light olefin.This method is the downstream with catalytic cracking petroleum naphtha injecting lift pipe reactor, makes its fully cracking under exacting terms very; And the upstream of conventional catalytically cracked stock injecting lift pipe reactor contacts with finish mixture from the downstream and reacts.
The common ground of above-mentioned background technology is: gasoline fraction carries out catalytic conversion reaction in the riser tube bottom, and its reaction conditions is difficult to physico-chemical property and injection rate flexible thereof according to gasoline fraction.So just can cause detrimentally affect to product distribution and product property inevitably, thereby further have influence on the economic benefit of whole catalytic cracking unit.
The object of the present invention is to provide a kind of new increasing output of diesel oil and the catalysis conversion method of low-carbon alkene.In the method, the reaction conditions of the gasoline fraction of injecting lift pipe reactor bottom can be optimized adjusting, thereby gasoline fraction can comparatively react under the ideal atmosphere, thereby the yield and the quality that improve the purpose product are improved.
The catalysis conversion method of increasing output of diesel oil provided by the invention and low-carbon alkene is such: regenerated catalyst enters the pre-riser tube 1 of the oil solution mixing chamber that is arranged in the riser reactor bottom through tremie pipe 9, and upwards flows under the effect that promotes medium; 20～80 heavy % of above-mentioned regenerated catalyst logistics and continue to quicken upwards to flow under the effect that promotes medium in round table-like transition section 2 enters in the transfer lime 4; The perforate of the catalyzer of rest part on round table-like transition section 2 enter interior transfer lime and outside in the annular cavity between the transfer lime, and under the effect that promotes medium, upwards flow; Gasoline stocks injects annular cavities through nozzle 3, contact with catalyzer in the cavity and react, and reaction oil gas and mixture of catalysts make progress mobile along annular cavity; The top of transfer lime is outside converged from the finish mixture of annular cavity and catalyzer from interior transfer lime; Hydrocarbon oil crude material injects through nozzle 6, contacts, reacts with above-mentioned logistics, and formed finish mixture upwards flows, behind riser reactor 7, the catalyzer of reaction oil gas and carbon deposit is separated, and oil gas is introduced subsequent separation system, and the catalyzer of carbon deposit recycles after stripping, regeneration.
Aforesaid method provided by the present invention is to realize in a catalytic cracking reaction-regeneration system rapidly that contains oil solution mixing chamber.This oil solution mixing chamber 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 the circumferential 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.The Chinese patent application of this oil solution mixing chamber number is 01118430.2.
Further specify method provided by the invention below in conjunction with accompanying drawing.
Fig. 1 is the structural representation of oil solution mixing chamber used in the present invention.
Fig. 2 is the schematic flow sheet of method provided by the present invention.
As shown in Figure 2,650～750 ℃ regenerated catalyst from regenerator enters in the pre-lift pipe 1 through regenerated catalyst tremie pipe 9. Promote medium, for example steam and/or dry gas inject pre-lift pipe bottom through distributor 10, promote regenerated catalyst, make it to accelerate upwards to flow. 20～80 heavy % of above-mentioned regenerated catalyst logistics, preferred 30～70 heavy % enter in the interior carrier pipe 4 through round table-like changeover portion 2. Promote medium, for example steam and/or dry gas, carrier pipe in distributor 8 injects, it is mobile to make catalyst in this pipe continue to accelerate to make progress; 20～80 heavy % of regenerated catalyst logistics, preferred 30～70 heavy %, in the perforate on the round table-like changeover portion 2 enters toroidal cavity between interior carrier pipe and outer carrier pipe, promote medium, for example steam and/or dry gas, inject this toroidal cavity through distributor 11, be beneficial to fluidisation, the conveying of catalyst.
Gasoline stocks injects toroidal cavities through nozzle 3, contacts with catalyst in the cavity and reacts. Described gasoline stocks can be selected from: the mixture of one or more in catalytic gasoline, coker gasoline, direct steaming gasoline, the visbreaking gasoline. Wherein, catalytic gasoline both can be stable gasoline, also can be raw gasoline. Gasoline stocks described here can be selected the hydrocarbon ils cut (true boiling point distillation temperature) of initial boiling point～220 ℃, also can select part narrow fraction wherein. The reaction condition of described gasoline stocks is as follows: reaction temperature is 480～660 ℃, preferred 520～620 ℃; 0.2～2 second reaction time, preferred 0.4～1.2 second; The weight ratio of catalyst and gasoline stocks is 6～40: 1, preferred 15～35: 1. The mass flow of the gasoline stocks that injects through nozzle 3 should be 3～30 heavy % of hydrocarbon oil crude material mass flow, preferred 5～20 heavy %.
The mixture of above-mentioned reaction oil gas and catalyst upwards flows along toroidal cavity. The top of carrier pipe is outside converged from the finish mixture of toroidal cavity and catalyst from interior carrier pipe. Hydrocarbon oil crude material injects through nozzle 6, mixes with above-mentioned logistics, and reacts under the catalytic cracking reaction condition. Described hydrocarbon oil crude material can be selected from: one or more in vacuum gas oil (VGO), deasphalted oil, coker gas oil, reduced crude, decompression residuum or the crude oil. The reaction condition of described hydrocarbon oil crude material is as follows: reaction temperature is 480～550 ℃, preferred 490～530 ℃; 0.5～3 second reaction time, preferred 1～2 second; The weight ratio of catalyst and gasoline stocks is 4～15: 1, preferred 6～10: 1.
In method provided by the invention, hydrocarbon oil crude material can also can be divided into it 2～4 strands fully by in the nozzle 6 injecting lift pipe reactors, is injected by the hydrocarbon ils nozzle that is positioned at riser different level place. The division of hydrocarbon oil crude material is preferably according to its physico-chemical property, and the raw material that makes easy cracking separates charging with the raw material of difficult cracking. Concrete sectional feeding method can be referring to CN1279270A.
Reactant flow continues upwards to flow, enter 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, the beneficial effect that the invention provides method is mainly reflected in the following aspects: 1. in method provided by the invention, the reaction conditions of gasoline stocks can be according to its injection rate and physico-chemical property flexible, thereby make gasoline stocks under optimum reaction conditions, carry out catalytic conversion reaction, to improve the yield of purpose product.2. in method provided by the invention, gasoline fraction is injected by the bottom of annular cavity, with height
Contact of temperature regenerator and reaction.By the mass rate of regulating regenerator in the annular cavity be
Can change the reaction conditions of gasoline stocks; And the accent of regenerator mass rate in the annular cavity
Joint can come real by changing the flow of lifting medium in interior transfer lime and annular cavity
Existing.Therefore, the reaction conditions of gasoline stocks is easy to regulate among the present invention, and should the side
Method is easy to implement on full scale plant.3. in method provided by the invention,, make that the radial distribution of riser tube inner catalyst logistics is more even, thereby can improve reaction environment, the raising reaction preference of hydrocarbon oil crude material because the bottom of riser reactor is provided with oil solution mixing chamber.4. in method provided by the invention, the catalyzer that hydrocarbon oil crude material touched not only has the long-pending catalyzer that a small amount of coke is arranged from annular cavity, also have a large amount of with have high temperature, a highly active regenerated catalyst from interior transfer lime.Therefore, can make hydrocarbon oil crude material obtain more sufficient cracking, and obtain comparatively ideal transformation efficiency.5. in method provided by the invention, gasoline stocks at first contacts, reacts with the high temperature regeneration agent in annular cavity, the reaction oil gas that is generated contacts, reacts with high-temperature regenerated catalyst from interior transfer lime once more in annular cavity enters behind the transfer lime top.This reaction process helps the generation of micro-molecular gas alkene.
The following examples will be further specified the present invention, but therefore not make the present invention be subjected to any restriction.
Embodiment 1
Present embodiment illustrates that method provided by the invention can make product distribute and improve.
Employed catalyzer is industrial by Qilu Petrochemical company catalyst plant among this embodiment, and trade names are RDG-1, and its main physico-chemical property is listed in table 1.The raw material oil properties is listed in table 2.This test is to carry out on treatment capacity is the catalytic cracking middle-scale device of 0.24t/d, and the schematic flow sheet of this device 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; The regenerated catalyst of 50 heavy % and continues upwards to flow under the effect that promotes steam in 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; Gasoline stocks contacts with regenerator and reacts in nozzle 3 injects annular cavities; The top of transfer lime is outside converged from the finish mixture of annular cavity and catalyzer from interior transfer lime, and hydrocarbon oil crude material 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 revolve 12 and the catalyzer of cyclone separator 13 separating reaction oil gas and reaction back carbon deposit by riser tube outlet, 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 test-results that disclosed method obtains among the CN1279270A.
It is all identical with embodiment 1 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 in the table 3 and Comparative Examples is compared, can draw to draw a conclusion: under stock oil, catalyzer and the main essentially identical prerequisite of operational condition, adopt method provided by the present invention that product is distributed and improve, the yield of high-value product is improved.
Table 1
| The catalyzer title | ????RDG-1 |
| Chemical constitution, heavy % Al 2O 3????RE 2O 3Apparent density, kg/m 3Pore volume, cm 3/ g specific surface, m 2/ g size composition, heavy % 0～40 μ m 40～80 μ m＞80 μ m equilibrium catalyst micro-activities | ? ????48.0 ????2.10 ????830 ????0.24 ????101 ? ????24.7 ????48.9 ????26.4 ????63 |
Table 2
| Material name | Hydrocarbon oil crude material |
| Density (20 ℃), kilogram/rice 3Kinematic viscosity (100 ℃), millimeter 2/ second carbon residue, heavy % condensation point, ℃ elementary composition, heavy % C H S N heavy metal, ppm Fe V Na Cu Ni boiling range, ℃ initial boiling point/5% 10%/30% 50%/70% | ????926.2 ????8.89 ????3.6 ????34 ? ????86.50 ????12.15 ????0.97 ????0.24 ? ????3.4 ????18.1 ????1.6 ????0.1 ????9.3 ? ????328/371 ????404/440 ????485/- |
| Material name density (20 ℃), kilogram/rice 3Octane value RON MON alkene, weigh % inductive phase, the min existent gum, mg/100ml | Gasoline stocks 0.7326 92.8 80.9 41.35 535 2 |
Table 3
| Project | Embodiment 1 | Comparative Examples 1 |
| Gasoline stocks: | ||
| Injection rate (accounting for hydrocarbon oil crude material), heavy % | ????20 | ????20 |
| Temperature of reaction, ℃ | ????648 | ????646 |
| Reaction times, s | ????0.8 | ????0.8 |
| Agent-oil ratio | ????18.5 | ????35.5 |
| Hydrocarbon oil crude material: | ||
| Temperature of reaction, ℃ | ????504 | ????504 |
| Reaction times, s | ????2.3 | ????2.4 |
| Agent-oil ratio | ????7.4 | ????7.1 |
| The regeneration dense phase temperature, ℃ | ????676 | ????678 |
| Product distributes, heavy % | ||
| Dry gas | ????4.83 | ????4.68 |
| Liquefied gas | ????17.36 | ???18.15 |
| Wherein, propylene | ????8.56 | ????5.97 |
| Gasoline | ????32.65 | ????31.53 |
| Diesel oil | ????31.30 | ????30.88 |
| Heavy oil | ????5.43 | ????6.48 |
| Coke | ????8.07 | ????7.85 |
| Yield of light oil, heavy % | ????63.95 | ????62.41 |
| Total lighter hydrocarbons liquid is received, heavy % | ????81.31 | ????80.56 |
| Main products character: | ||
| Gasoline density, g/cm 3 | ???0.7165 | ????0.7158 |
| Gasoline RON | ????93.6 | ????93.8 |
| ??????MON | ????81.5 | ????81.7 |
| Olefin(e) centent, heavy % | ????33.8 | ????34.2 |
| Inductive phase, min | ????662 | ????667 |
| Diesel oil density, g/cm 3 | ??0.8827 | ???0.8841 |
| Condensation point of diesel oil, ℃ | ????-2 | ????-3 |
Claims (10)
1, the catalysis conversion method of a kind of increasing output of diesel oil and low-carbon alkene is characterized in that regenerated catalyst enters the pre-riser tube 1 of the oil solution mixing chamber that is arranged in the riser reactor bottom through tremie pipe 9, and upwards flows under the effect that promotes medium; 20～80 heavy % of above-mentioned regenerated catalyst logistics and continue to quicken upwards to flow under the effect that promotes medium in round table-like transition section 2 enters in the transfer lime 4; The perforate of the catalyzer of rest part on round table-like transition section 2 enter interior transfer lime and outside in the annular cavity between the transfer lime, and under the effect that promotes medium, upwards flow; Gasoline stocks injects annular cavities through nozzle 3, contact with catalyzer in the cavity and react, and reaction oil gas and mixture of catalysts make progress mobile along annular cavity; The top of transfer lime is outside converged from the finish mixture of annular cavity and catalyzer from interior transfer lime; Hydrocarbon oil crude material injects through nozzle 6, contacts, reacts with above-mentioned logistics, and formed finish mixture upwards flows, behind riser reactor 7, the catalyzer of reaction oil gas and carbon deposit is separated, and oil gas is introduced subsequent separation system, and the catalyzer of carbon deposit recycles after stripping, regeneration.
2, according to the method for claim 1, it is characterized in that described oil solution mixing chamber 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 the circumferential 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.
3, according to the method for claim 1,30～70 heavy % that it is characterized in that the regenerated catalyst logistics in round table-like transition section 2 enters in the transfer lime 4, the perforate of the regenerated catalyst logistics of remaining 30～70 heavy % on round table-like transition section 2 enter interior transfer lime and outside in the annular cavity between the transfer lime.
4, according to the method for claim 1, it is characterized in that described gasoline stocks is selected from: the mixture of one or more in catalytic gasoline, coker gasoline, straight-run spirit, the viscosity breaking gasoline, and described gasoline stocks can be selected the hydrocarbon ils cut of initial boiling point～220 ℃ for use, also can select part narrow fraction wherein for use.
5, according to the method for claim 1, it is characterized in that the reaction conditions of described gasoline stocks is as follows: temperature of reaction is 480～660 ℃, and in 0.2～2 second reaction times, the weight ratio of catalyzer and gasoline stocks is 6～40: 1.
6, according to the method for claim 5, it is characterized in that the reaction conditions of described gasoline stocks is as follows: temperature of reaction is 520～620 ℃, and in 0.4～1.2 second reaction times, the weight ratio of catalyzer and gasoline stocks is 15～35: 1.
7,, it is characterized in that described hydrocarbon oil crude material is selected from: one or more in vacuum gas oil, deasphalted oil, coker gas oil, long residuum, vacuum residuum or the crude oil according to the method for claim 1.
8, according to the method for claim 1, it is characterized in that the reaction conditions of described hydrocarbon oil crude material is as follows: temperature of reaction is 480～550 ℃, and in 0.5～3 second reaction times, the weight ratio of catalyzer and gasoline stocks is 4～15: 1.
9, according to the method for claim 8, it is characterized in that the reaction conditions of described hydrocarbon oil crude material is as follows: temperature of reaction is 490～530 ℃, and in 1～2 second reaction times, the weight ratio of catalyzer and gasoline stocks is 6～10: 1.
10,, it is characterized in that the mass rate of the described gasoline stocks that injects through nozzle 3 accounts for 3～30 heavy % of hydrocarbon oil crude material mass rate according to the method for claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011198060A CN1173008C (en) | 2001-06-29 | 2001-06-29 | Catalytic conversion process for increasing output of diesel oil and low-carbon olefin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011198060A CN1173008C (en) | 2001-06-29 | 2001-06-29 | Catalytic conversion process for increasing output of diesel oil and low-carbon olefin |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1393508A true CN1393508A (en) | 2003-01-29 |
| CN1173008C CN1173008C (en) | 2004-10-27 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011198060A Expired - Fee Related CN1173008C (en) | 2001-06-29 | 2001-06-29 | Catalytic conversion process for increasing output of diesel oil and low-carbon olefin |
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| Country | Link |
|---|---|
| CN (1) | CN1173008C (en) |
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| CN1173008C (en) | 2004-10-27 |
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Granted publication date: 20041027 Termination date: 20110629 |