CN102839014A - Reactor and method for reinforcing heavy oil conversion and reducing gasoline olefin - Google Patents
Reactor and method for reinforcing heavy oil conversion and reducing gasoline olefin Download PDFInfo
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- CN102839014A CN102839014A CN2011101709577A CN201110170957A CN102839014A CN 102839014 A CN102839014 A CN 102839014A CN 2011101709577 A CN2011101709577 A CN 2011101709577A CN 201110170957 A CN201110170957 A CN 201110170957A CN 102839014 A CN102839014 A CN 102839014A
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Abstract
The invention relates to a reactor and a method for reinforcing heavy oil conversion and reducing gasoline olefin. According to the method, a novel lift pipe reactor is provided, and is adopted to increase a density of a catalyst and a oil agent contact efficiency in the lift pipe, and a two-section heavy oil conversion rate is increased by controlling operation conditions according to characteristics of the reactor so as to further reduce olefin content in gasoline. According to the present invention, the lift pipe reactor of the present invention is designed into a structure comprising two sections of straight pipes with different diameters, wherein the upper part is thick, the lower part is thin, the middle is connected through a circular table type diameter changing section, and the upper diameter and the lower diameter of the circular table are equal to the diameters of the straight pipes.
Description
Technical field
The present invention relates to a kind of reactor drum and method of strengthening heavy oil conversion and decreasing by gasoline olefin.This method belongs to the process modification of petroleum refining process.
Technical background
Catalytic cracking is important heavy oil lighting technology.Along with the continuous aggravation of crude oil heaviness, poor qualityization, the raw material of catalytic cracking causes transformation efficiency to reduce also worse and worse, and the green coke amount increases.In China, catalytic cracking provides about 80% motor spirit.Catalytic cracking gasoline olefine content is too high, far surpass the requirement of motor spirit standard, and China's hydrogenation ability is obviously not enough, therefore reduces content of olefin in gasoline through catalytic cracking itself and becomes the target that each enterprise is pursued.
The two-stage riser fluid catalytic cracking technology has overcome the drawback of traditional single riser tube technology through segmentation reaction, catalyzer relay etc.; Fresh feed is reacted at one section riser tube; Recycle stock and gasoline react at two sections riser tubes; Avoid long cracking and the competitive adsorption of material of different nature in a riser tube excessively that causes of reaction times, can effectively improve the transformation efficiency of heavy oil, reduce the content of gasoline olefin.Yet in the operating process of reality, there are deficiencies such as agent-oil ratio is lower, the recycle stock transformation efficiency is not high and content of olefin in gasoline is still higher, the gasoline loss is bigger in two sections riser tubes of two-stage riser fluid catalytic cracking technology.And, cause the concentration of heavy constituent in the settling vessel to increase the easy coking of settling vessel because the recycle stock transformation efficiency is on the low side.The agent-oil ratio that decreasing by gasoline olefin need be bigger, lower cracking activity and relatively low agent-oil ratio, and two sections full distillation gasolines of riser tube freshening of existing technology, freshening gasoline is from two sections riser tube bottom feeds; Directly and the high temperature catalyst contact reacts; Activity of such catalysts is too high, and agent-oil ratio is lower again, the large percentage that disadvantageous catalytic cracking and heat cracking reaction account for; Cause gasoline loss bigger, and it is not fully up to expectations to fall the effect of alkene.Recycle stock gets into riser tube at riser tube middle part, the temperature of catalyzer is lower, and activity descends to some extent, and catalyzer flows and be in abundant development section, and the finish contact efficiency is lower, thereby causes the recycle stock transformation efficiency lower.
Therefore; Develop new two sections riser reactors and feeding manner; Recycle stock and gasoline are reacted under adapt circumstance, strengthen recycle stock and transform and decreasing by gasoline olefin, can improve the advantage of two-stage riser fluid catalytic cracking technology aspect the inferior raw material catalyzed conversion.
Summary of the invention
The object of the invention provides a kind of reactor drum method of use of strengthening heavy oil conversion and decreasing by gasoline olefin with regard to being to avoid the weak point of above-mentioned prior art.This technology is that a kind of novel riser reactor both was provided; And utilize this reactor drum can improve density of catalyst and finish contact efficiency in the riser tube; Simultaneously also improve the transformation efficiency of two sections heavy oil, and further reduce the olefin(e) centent of gasoline according to the characteristics red-tape operati condition of this reactor drum.
To achieve these goals, the contriver then is designed to be made up of two sections straight tubes of different diameter to the present invention's novel riser reactor recited above, and is upper coarse and lower fine, and middle the diameter up and down of round platform equals the straight tube diameter by the connection of circular platform type reducer, wherein:
The bus of round platform and the angle of axis are 10～60 °, and be preferred, is 20～50 °.
Thick straight tube is 2/1～1/4 with the length ratio of thin straight tube, and is preferred, is 1/1～1/2.
Thick straight tube is definite according to the amount of freshening gasoline with the diameter beguine of thin straight tube, but will guarantee that the superficial gas velocity in the thick straight tube is not less than 4m/s, and is preferred, is not less than 7m/s.
The charging endless tube is installed in bottom at the thick straight tube of above-mentioned riser tube, arranges a plurality of nozzles on the endless tube.
The direction of charging endless tube upper spray nozzle can with the axis coplane, also can be, but general direction keeps up along the rotation of the tangential direction of endless tube.
With the angle of the coplanar nozzle of axis be-45～+ 45 °, preferred, be-30～+ 30 °.
Preferably along the nozzle of endless tube tangential direction rotation, nozzle and endless tube planar angle are 5～85 ° in the present invention, and be preferred, is 20～75 °, preferred, is 45～75 °.
The lower disposed heavy oil nozzle of thin straight tube in above-mentioned riser tube.
With existing reducing riser tube compared with techniques; The present invention not merely is the reducing that carries out riser tube; But adopt the thickness two-stage riser; The charging endless tube that relies on thick straight tube bottom to install realizes that the high-density of thick straight tube inner catalyst and the efficient of finish contact, and oil gas and catalyzer can not underspeed greatly because of caliber becomes, and influence normal fluidisation.
Heavy oil of the present invention is recycle stock or recycle stock and slurry oil mixture, and described gasoline is petroleum naphtha, and boiling range is IBP～100 ℃, and is preferred, and boiling range is IBP～70 ℃.The used catalyzer of the present invention is conventional catalytic cracking catalyst.
Adopting reactor drum provided by the present invention, the process design that the contriver then will strengthen the novel method of two sections heavy oil conversion and decreasing by gasoline olefin is:
Fresh catalytically cracked material gets into one section riser tube and reacts after preheating, carry out getting into separation column with two sections oil gas after finish separates through settling vessel; The isolated heavy oil heat exchange of separation column is after the heavy oil nozzle of two sections riser tube bottoms gets into riser tube, and with the high temperature catalyst contact reacts, the catalyzer of reacted oil gas and part coking makes progress along riser tube, gets into thick straight-tube portion; The isolated light gasoline fraction of separation column gets into riser tube through the charging endless tube of thick straight tube bottom in two sections riser tubes and reacts, and reacted finish oil gas after separating advances separation column, and catalyzer gets into the revivifier coke burning regeneration behind stripping.
The drawing explanation
Accompanying drawing 1 is the schematic flow sheet of two sections heavy oil conversion of reinforcement of the present invention and decreasing by gasoline olefin.
Accompanying drawing 2 is the synoptic diagram of riser reactor of the present invention.
Accompanying drawing 3 is a charging endless tube synoptic diagram of the present invention.
Wherein,
The 1-revivifier; 2-burns jar; The 3-settling vessel; The 4-separation column; One section riser tube of 5-;
Two sections riser tubes of 6-; The 7-flue gas; The 8-air; The 9-stripped vapor; 10-fcc raw material feed nozzle;
The 11-reaction oil gas; 12-petroleum naphtha charging endless tube; 13-recycle stock feed nozzle;
The 14-rich gas; The 15-raw gasline; The 16-catalytic diesel oil; The 17-catalytic slurry
Embodiment
To combine accompanying drawing and specific embodiment to come enumeration technical characterstic of the present invention below:
Embodiment 1
The charging endless tube is installed in thick straight tube bottom at riser tube, arranges a plurality of nozzles on the endless tube.The direction of charging endless tube upper spray nozzle can with the axis coplane, also can be, but general direction keeps up along the rotation of the tangential direction of endless tube.With the angle of the coplanar nozzle of axis be-45～+ 45 °, preferred-30～+ 30 °.Preferably along the nozzle of endless tube tangential direction rotation, nozzle and endless tube planar angle are 5～85 °, preferred 20～75 °, and more preferably 45～75 °.
The heavy oil nozzle is arranged on bottom, regenerator sloped tube top at the thin straight tube of riser tube, and recycle stock and slurry oil are by this nozzle entering riser tube.
The form of present embodiment simulation charging endless tube is to the influence of riser tube inner catalyst density.
Adopt cold conditions circulating fluidized bed experimental installation, fluidizing medium is an air, and particle is common catalytic cracking poiser, and the structure of riser tube such as embodiment 1 are said.The thin straight tube segment length 4m of riser tube, diameter 0.1m, thick straight tube segment length 6m, diameter 0.14m.Superficial gas velocity is 12m/s in the riser tube, and the endless tube air input is 50% of a nozzle air input.0.37m establishes gauge hatch on endless tube, the catalyzer solid holdup in cross section when pressing the multi-form endless tube of equal-area method measurement employing with PC6D granule density survey meter.The endless tube nozzle is along the rotation of endless tube tangential direction, 70 ° of nozzle and endless tube plane included angles.Experimental result is seen table 1.
Comparative Examples 1
Adopt the method identical with embodiment 1, charging endless tube nozzle direction change into part straight up, partly to centroclinal, the angle of angled nozzle and axis is 30 °.Vertical nozzle and angled nozzle staggered arrangement.Experimental result is seen table 1.
Comparative Examples 2
Adopt the method identical with embodiment 1, charging endless tube nozzle direction change into part straight up, part rotates 70 ° of angled nozzle and endless tube plane included angles along the endless tube tangential direction.Vertical nozzle and angled nozzle staggered arrangement.Experimental result is seen table 1.
Table 1
| r/R | Embodiment 1 | Comparative Examples 1 | Comparative Examples 2 |
| 0 | 0.053 | 0.050 | 0.061 |
| 0.158 | 0.054 | 0.047 | 0.062 |
| 0.382 | 0.067 | 0.045 | 0.056 |
| 0.500 | 0.086 | 0.053 | 0.066 |
| 0.590 | 0.361 | 0.055 | 0.077 |
| 0.670 | 0.408 | 0.080 | 0.063 |
| 0.741 | 0.462 | 0.075 | 0.084 |
| 0.806 | 0.431 | 0.090 | 0.077 |
| 0.866 | 0.366 | 0.090 | 0.083 |
| 0.922 | 0.544 | 0.292 | 0.365 |
| 0.974 | 0.499 | 0.319 | 0.373 |
Embodiment 3
Present embodiment adopts the riser reactor of embodiment 1 to carry out heavy oil conversion and decreasing by gasoline olefin at the circulating fluidized bed reaction-regeneration system.
Petroleum naphtha, recycle stock are sprayed in the riser reactor through charging endless tube nozzle and heavy oil atomizing nozzle respectively, and petroleum naphtha accounts for 50% of recycle stock weight, is normal temperature during the petroleum naphtha charging; Be preheated to 300 ℃ during the recycle stock charging, promote on average gas speed 5.0m/s of inner axial tube, 500 ℃ of riser tube temperature outs; In this transfer line fluid cat cracking reaction-regeneration system; The high-temperature regenerated catalyst of coming from revivifier upwards flows along riser tube promoting in advance under the effect of steam, earlier with the raw materials mix that sprays into from nozzle after the atomizing after; In continuing flow process upwards cracking reaction takes place, then with the petroleum naphtha hybrid reaction that sprays into from charging endless tube nozzle.Products distribution and gasoline family form sees table 2.
Table 2
| Products distribution/wt% | |
| Dry gas | 1.39 |
| Liquefied gas | 14.71 |
| Gasoline | 43.96 |
| Diesel oil | 8.83 |
| Heavy oil | 26.18 |
| Coke | 4.93 |
| Composition/the wt% of gasoline family | |
| Normal paraffin | 4.47 |
| Isoparaffin | 23.35 |
| Naphthenic hydrocarbon | 6.66 |
| Aromatic hydrocarbons | 29.18 |
| Alkene | 36.34 |
Reactor drum provided by the present invention and method and original compared with techniques have following advantage:
1. heavy oil directly contacts with high-temperature regenerated catalyst, and principal reaction occurs in the accelerating sections of catalyzer, has both guaranteed high temperature of reaction, can guarantee high density of catalyst again, and the reaction times is shorter, avoids cracking when having realized that heavy oil is efficient and transform.
2. freshening petroleum naphtha rather than full distillation gasoline can improve the relative concentration of alkene, can avoid more macromolecular cracking reaction in the gasoline again, reduce the gasoline loss.
3. the part coked catalyst contact reacts that petroleum naphtha and temperature are lower makes alkene that hydrogen transfer reactions take place as far as possible, reduces cracking reaction, further reduces the gasoline loss.
4. petroleum naphtha is broken the ring-nuclear structure of riser tube inner catalyst through the endless tube charging, improves local density of catalyst, and petroleum naphtha is fully contacted with catalyzer, promotes catalyzed reaction.
5. endless tube nozzle and the thicker upper semisection riser reactor of rotation force catalyzer to center flow, improve the gas-solid contact efficiency, for reactions such as the hydrogen transference of petroleum naphtha, aromizing provide time enough.
Claims (4)
1. reactor drum of strengthening heavy oil conversion and decreasing by gasoline olefin; This reactor drum is that the employing two-stage riser is an infrastructure device; It is characterized in that the reactor design of riser tube is become to be made up of two sections straight tubes of different diameter, upper coarse and lower fine, the centre is connected by the circular platform type reducer; The diameter up and down of round platform equals the straight tube diameter, and its concrete design requirements is:
1) angle of the bus of round platform and axis is 20～50 °;
2) thick straight tube is 1/1～1/2 with the length ratio of thin straight tube;
3) thick straight tube is confirmed according to the amount of freshening gasoline with the diameter beguine of thin straight tube, and requires the superficial gas velocity in the thick straight tube to be lower than 7m/s;
4) the charging endless tube is installed in the bottom of thick straight tube, arranges a plurality of nozzles on the endless tube, and the direction of charging endless tube upper spray nozzle keeps up, and rotates along the tangential direction of endless tube, and it is along the nozzle of endless tube tangential direction rotation, and nozzle and endless tube planar angle are 45～75 °;
2. a kind of reactor drum of strengthening heavy oil conversion and decreasing by gasoline olefin according to claim 1; The charging endless tube is installed in the bottom that it is characterized in that described thick straight tube; Arrange a plurality of nozzles on the endless tube; The direction of charging endless tube upper spray nozzle keeps up, and with the axis coplane, the angle of its nozzle is-30～+ 30 °.
3. a kind of reactor drum of strengthening heavy oil conversion and decreasing by gasoline olefin according to claim 1 is characterized in that described heavy oil is recycle stock or recycle stock and slurry oil mixture, and described gasoline is petroleum naphtha, and boiling range is for being IBP～70 ℃.Described catalyzer is conventional catalytic cracking catalyst.
4. method of strengthening two sections heavy oil conversion and decreasing by gasoline olefin, this method is the described reactor drum of employing claim 1, it is characterized in that process conditions is following:
Fresh catalytically cracked material gets into one section riser tube and reacts after preheating, carry out getting into separation column with two sections oil gas after finish separates through settling vessel; The isolated heavy oil heat exchange of separation column is after the heavy oil nozzle of two sections riser tube bottoms gets into riser tube, and with the high temperature catalyst contact reacts, the catalyzer of reacted oil gas and part coking makes progress along riser tube, gets into thick straight-tube portion; The isolated light gasoline fraction of separation column gets into riser tube through the charging endless tube of thick straight tube bottom in two sections riser tubes and reacts, and reacted finish oil gas after separating advances separation column, and catalyzer gets into the revivifier coke burning regeneration behind stripping.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011101709577A CN102839014A (en) | 2011-06-23 | 2011-06-23 | Reactor and method for reinforcing heavy oil conversion and reducing gasoline olefin |
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| CN2011101709577A CN102839014A (en) | 2011-06-23 | 2011-06-23 | Reactor and method for reinforcing heavy oil conversion and reducing gasoline olefin |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103834430A (en) * | 2013-01-23 | 2014-06-04 | 洛阳瑞泽石化工程有限公司 | Design method of feed nozzle of catalytic cracking device |
| CN111097337A (en) * | 2018-10-25 | 2020-05-05 | 中国石油化工股份有限公司 | Zoned fluidized bed reaction-regeneration device and process for preparing aromatic hydrocarbon through methanol conversion |
| CN113457584A (en) * | 2021-07-07 | 2021-10-01 | 中国石油大学(华东) | Reactor for reinforcing mixing of feeding oil agent |
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| 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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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103834430A (en) * | 2013-01-23 | 2014-06-04 | 洛阳瑞泽石化工程有限公司 | Design method of feed nozzle of catalytic cracking device |
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| CN111097337A (en) * | 2018-10-25 | 2020-05-05 | 中国石油化工股份有限公司 | Zoned fluidized bed reaction-regeneration device and process for preparing aromatic hydrocarbon through methanol conversion |
| CN111097337B (en) * | 2018-10-25 | 2022-04-05 | 中国石油化工股份有限公司 | Zoned fluidized bed reaction-regeneration device and process for preparing aromatic hydrocarbon through methanol conversion |
| CN113457584A (en) * | 2021-07-07 | 2021-10-01 | 中国石油大学(华东) | Reactor for reinforcing mixing of feeding oil agent |
| CN113457584B (en) * | 2021-07-07 | 2024-04-12 | 中国石油大学(华东) | Reactor for strengthening feed oil mixing |
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