CN1141361C - Catalytic cracking process for reducing content of olefin in gasoline - Google Patents
Catalytic cracking process for reducing content of olefin in gasoline Download PDFInfo
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- CN1141361C CN1141361C CNB001341197A CN00134119A CN1141361C CN 1141361 C CN1141361 C CN 1141361C CN B001341197 A CNB001341197 A CN B001341197A CN 00134119 A CN00134119 A CN 00134119A CN 1141361 C CN1141361 C CN 1141361C
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Abstract
The present invention relates to a catalytic cracking process for reducing olefinic content in gasoline. The condensed oil of a rich gas compressor and/or a light gasoline fraction extracted from the upper part of a stabilizer are/is injected into a riser reactor from the upper reaches of a raw oil feed nozzle or injected into the riser reactor along with raw oil from the raw oil feed nozzle, and are/is in contact with and react/reacts with a regenerated catalyst; the flow of a reactant ascends along a riser, and enables reaction oil gas to rapidly separate from the catalyst at the outlet of the riser, and reaction products are recycled for recycling use after a spent catalyst is stripped and regenerated; by adopting the process, the olefinic content of the gasoline can decrease by 10 to 20v%.
Description
Technical field
The invention belongs to the catalyst cracking method of petroleum hydrocarbon, more particularly, is a kind of catalyst cracking method that reduces olefin(e) centent in the product gasoline.
Background technology
In the last few years, the environmental regulation of countries in the world had all proposed the requirement of increasingly stringent to the quality of vapour, diesel oil, and was especially more and more harsher to the requirement of indexs such as the olefin(e) centent of gasoline, sulphur content, benzene content.Therefore, become the main impellent that promotes that every oil Refining Technologies further advances from the requirement of environmental protection aspect, and comparatively traditional catalytic cracking technology stands in the breach especially.
As everyone knows, the olefin(e) centent of catalytically cracked gasoline is 35～65 heavy %, is a kind of more representational gasoline fraction that is rich in alkene.Though this gasoline has higher octane value, its poor heat stability easily forms colloid; Also can increase the quantity of toxic substance such as active hydro carbons thing and polyenoid in the discharge after the burning, unsuitable direct blend component as commercial gasoline.
CN1244569A has disclosed a kind of catalysis conversion method that reduces alkene and sulphur in the gasoline, nitrogen content.This method is that the light gasoline fraction after the preheating is entered in riser tube or the fluidized-bed reactor, contacts and reacts with being cooled to regenerated catalyst about 300 ℃, and the weight ratio of catalyzer and light gasoline fraction is 6, weight hourly space velocity is 4h
-1Returning reactor recycles through stripping, regeneration and after suitably cooling off for reaction product isolated, reclaimable catalyst.Light gasoline fraction mainly carries out isomerization reaction and hydrogen transfer reactions above-mentioned under than the demulcent condition, and making the conversion of olefines in the gasoline is isoparaffin and aromatic hydrocarbons, and part sulphur and nitrogen are removed.Fall the alkene effect preferably though this method has, the olefin(e) centent of gasoline is reduced to below the 20 heavy %, the enforcement of this method is had relatively high expectations to equipment.Implement to need to adopt the complete catalytic cracking unit of a cover separately; Then need original device is carried out bigger transformation with the catalytic cracking unit Joint Implementation of routine, and flow process complexity, operation easier are big.
The disclosed method of USP5846403 be with in the catalytically cracked gasoline＜140 ℃ lighting end injects the upstream of stock oil feed nozzle, utilize high temperature and highly active regenerated catalyst to make above-mentioned gasoline fraction generation catalytic conversion reaction, temperature of reaction is 620～775 ℃, agent-oil ratio is 75～150, and the reaction times was less than 0.1 second.This method can improve the productive rate of propylene and butylene, and the octane value of gasoline is increased.
In catalytic cracking process, after the separation column fractionation, the mixture of gasoline and rich gas enters the oil-gas separator at separation column top from the reaction oil gas of reactive moieties.After separating, rich gas enters rich gas compressor and boosts, and cools off and isolates compression rich gas and condensed oil.The compression rich gas enters the bottom on absorption tower, is absorbed as absorption agent by stable gasoline and raw gasline.Absorbed C
3, C
4And portion C
2Rich absorbent oil enter the top of desorption tower with above-mentioned condensed oil, the heat that utilizes tower bottom reboiler to provide makes C
2Component and a considerable amount of C
3, C
4Component is by desorb, and stripping gas is discharged by the desorption tower top, and the gasoline fraction that removes behind the stripping gas is drawn by the desorption tower bottom as deethanizing gasoline, and sends into follow-up stabilizer tower and make with extra care.
Rich gas compressor is one of nucleus equipment of catalytic cracking unit, and its model generally is to select according to rich gas flow and absorption tower working pressure.But the heavy metal contamination degree of reaction conditions, feedstock property, catalyzer etc. all can influence the flow of rich gas.For these reasons, consider the device needs of capacity expansion revamping from now on simultaneously, when selecting the model of rich gas compressor, often leave certain surplus.In this case, can run well, just the rich gas after the part compression need be circulated to the inlet of rich gas compressor, to satisfy the requirement of its inlet flow rate in order to make rich gas compressor.This operating method does not only make the processing power of rich gas compressor be fully utilized, but also can increase plant energy consumption.
In sum, reducing the technical elements of catalytic cracking gasoline olefine content, at present easy feasible technological without comparison also in the prior art; And the scheme that effectively utilizes the surplus of catalytic cracking rich gas compressor is also never appeared in the newspapers.
Summary of the invention
The objective of the invention is to provide on the basis of above-mentioned prior art a kind of simple processing method that reduces catalytic cracking gasoline olefine content, purpose of the present invention is to effectively utilize the rich gas compressor that surplus is arranged in the catalytic cracking unit simultaneously.
Method provided by the invention is the light gasoline fraction extracted out with the condensed oil of rich gas compressor and/or by the stabilizer tower top upstream injecting lift pipe reactor by the stock oil feed nozzle, perhaps with stock oil by stock oil feed nozzle injecting lift pipe reactor, make it to contact with regenerated catalyst and react, reactant flow is up along riser tube, make reaction oil gas and catalyzer sharp separation in the riser tube exit, reclaim reaction product, reclaimable catalyst recycles after stripping and regeneration.
The beneficial effect that the invention provides method is mainly reflected in the following aspects:
(1) in the gasoline product of China, be that olefin(e) centent is than higher catalytically cracked gasoline more than the 70 heavy %.
In order to satisfy the requirement of new environmental regulation, the olefin(e) centent that makes gasoline must fall less than 35%
The olefin(e) centent of low catalytically cracked gasoline.According to the practical situation of China, catalytically cracked gasoline all
Carry out hydrogenation etc. again treating processes be unpractical, tooling cost also can further improve.Therefore,
Must be based on catalytic cracking unit itself, solve catalysis by technical progress and plant modification and split
Change the high problem of content of olefin in gasoline.The present invention is a kind of so suitable China's national situation easy just
And effective processing method.
(2) this method is easy to implement on catalytic cracking unit, and can obviously reduce olefin(e) centent in the gasoline.
By the process pipeline and the corresponding flow control system of setting up the petroleum naphtha freshening, can implement this
The method that invention provides makes the olefin(e) centent of gasoline reduce by 10～20v%.
(3) because the present invention has selected suitable reaction conditions for light gasoline fraction, make the alkene head in the gasoline
Carry out the selective cracking reaction earlier, and then further upgrading is isoparaffin and aromatic hydrocarbons.Though
Variation has taken place in the group composition of gasoline, and olefin(e) centent obviously reduces, but to the influence of gasoline yield
Less, the reduction amplitude of gasoline yield is less than 5 percentage points.In addition, in above-mentioned reaction process
In, by main technologic parameters such as conditioned reaction temperature, reaction times, agent-oil ratios, strictly
Control reaction severity remains unchanged the productive rate of dry gas and coke substantially.Thereby the present invention carries
The enforcement of supplier's method can not influence the treatment capacity of device.
(4) method of reduction catalytic cracking gasoline olefine content provided by the invention has certain handiness,
Can select different feed solutions for use according to the load of rich gas compressor in the catalytic cracking unit.
Especially when the load of rich gas compressor has surplus, adopt and improve the condensation of fractionator overhead oil gas
Cooling temperature, increase the method for the mass rate of condensed oil, not only can make the quality of condensed oil
Flow satisfies requirement of the present invention, and the load of rich gas compressor is utilized effectively,
Reduce the energy expenditure of device.
Description of drawings
Fig. 1 is the schematic flow sheet of method provided by the present invention.
Embodiment
We find by a large amount of tests, and the alkene in catalytically cracked gasoline more than the 60 heavy % concentrates in the light gasoline fraction of carbon below six.By the compositional analysis data of catalytically cracked gasoline cited in the table 1 as can be seen, the gasoline that has even the above alkene of 70 heavy % is arranged is to concentrate in the light gasoline fraction of carbon below six.Therefore, the olefin(e) centent that reduces in the light gasoline fraction has vital role to the quality that improves catalytically cracked gasoline.
Method provided by the invention is so concrete enforcement: rich gas compressor condensed oil or the light gasoline fraction of being extracted out by stabilizer tower top or their mixture are through preheating or without preheating in the direct injecting lift pipe reactor.Above-mentioned logistics promptly can be by the upstream injecting lift pipe reactor of stock oil feed nozzle, also can be with stock oil by stock oil feed nozzle injecting lift pipe reactor.When above-mentioned logistics during, can adopt following two kinds of injection modes by the upstream injecting lift pipe reactor of stock oil feed nozzle:
(1) inject by the bottom of riser reactor, and instead of part or whole pre-lifting media;
(2) by the position injecting lift tube reaction more than the riser tube Y type section, below the fresh feed feed nozzle
Device.
Rich gas compressor condensed oil of the present invention is meant that this condensed oil is mainly less than C by the rich gas compressor one-level condensed oil that liquid/gas separator extracts out of working off one's feeling vent one's spleen
6Cut.Because the fractionation cat head oil gas condensation cooling temperature of conventional FCC apparatus is 40 ℃, only weigh % and the mass rate of rich gas compressor one-level outlet condensed oil is general for 3～8 of fresh feed amount, can not satisfy the processing requirement of the present invention to petroleum naphtha freshening amount, so need to improve the condensation cooling temperature of fractionation cat head oil gas, for example, this temperature can be brought up to about 50 ℃, so that increase the mass rate of condensed oil.But the condensation cooling temperature that improves fractionation cat head oil gas will make the load of rich gas compressor increase, and be applicable to that rich gas compressor has the catalytic cracking unit of surplus so improve the method for fractionation cat head oil gas condensation cooling temperature.
The final boiling point of the light gasoline fraction of being extracted out by stabilizer tower top of the present invention is less than 130 ℃.In order to guarantee the extraction of this cut, need to set up light gasoline fraction and extract side line out on stabilizer tower top, and draw-off pan and which floor contiguous tower tray thereof carried out necessary transformation, for example adjust spacing, the percentage of open area of extracting near several tower trays plate out, and increase liquid collecting equipment.
The present invention also can mix the condensed oil of rich gas compressor one-level outlet with the light gasoline fraction that extract out on stabilizer tower top, carry out catalytic reforming in the injecting lift pipe reactor reacts.This feeding manner is applicable to the rich gas compressor full load operation, and the less catalytic cracking unit of the mass rate of condensed oil.
Owing to mainly contain carbon three, carbon four and light gasoline fraction in the rich gas compressor condensed oil, so in the present invention rich gas compressor condensed oil and the light gasoline fraction extracted out by stabilizer tower top are referred to as light gasoline fraction.
In riser reactor, above-mentioned light gasoline fraction contacts with regenerated catalyst, vaporizes rapidly and reacts, and temperature of reaction is 600～700 ℃, and preferred 630～670 ℃, the weight ratio of regenerated catalyst and light gasoline fraction is 30～75, and preferred 40～65.When being injected by the bottom of riser reactor when the rich gas compressor condensed oil and/or by the light gasoline fraction that extract out on stabilizer tower top, its reaction times is 0.3～0.6 second, preferred 0.3～0.5 second; More than above-mentioned light gasoline fraction is by riser tube Y type section, when injecting below the fresh feed feed nozzle, its reaction times is 0.2～0.5 second, preferred 0.3～0.5 second; When light gasoline fraction with stock oil during by stock oil feed nozzle injecting lift pipe, the reaction times of light gasoline fraction is identical with the reaction times of stock oil.In order to obtain to reduce preferably the effect of content of olefin in gasoline, preferably light gasoline fraction is by stock oil feed nozzle upstream injecting lift pipe reactor.Table 1
| 1,000,000 tons of/year FCC full scale plants | 800,000 tons of/year FCC full scale plants | |||||||
| Alkane | Alkene | Naphthenic hydrocarbon | Aromatic hydrocarbons | Alkane | Alkene | Naphthenic hydrocarbon | Aromatic hydrocarbons | |
| C 4 | 1.8 | 4.6 | - | - | 0.99 | 3.08 | - | - |
| C 5 | 5.37 | 10.54 | 0.12 | - | 6.31 | 10.63 | - | - |
| C 6 | 4.82 | 9.79 | 1.53 | 0.63 | 6.58 | 7.52 | 1.28 | 1.4 |
| C 7 | 3.88 | 7.59 | 2.57 | 3.16 | 4.8 | 7.15 | 1.74 | 1.77 |
| C 8 | 3.79 | 4.77 | 2.24 | 7 | 5.32 | 3.27 | 3.02 | 4.68 |
| C 9 | 2.45 | 2.44 | 1.56 | 8.69 | 5.02 | 1.76 | 1.28 | 6.37 |
| C 10 | 2.18 | 1.02 | 0.39 | 4.8 | 2.48 | 0.38 | 1.3 | 6.04 |
| C 11 | 1.28 | 0.25 | 0.04 | 0.29 | 2.25 | - | - | 1.79 |
| C 12 | 0.35 | 0.04 | - | - | 1.61 | - | - | 0.18 |
| Full cut adds up to | 25.92 | 41.04 | 8.45 | 24.57 | 35.36 | 33.79 | 8.62 | 22.23 |
| ＜C 6Add up to | 11.99 | 24.93 | 1.65 | 0.63 | 13.88 | 21.23 | 1.28 | 1.4 |
| ＜C 6Account for full cut, m% | 46.26 | 60.75 | 19.53 | 2.56 | 39.25 | 62.83 | 14.85 | 6.30 |
| 120,000 tons of/year FCC full scale plants | 400,000 tons of/year FCC full scale plants | |||||||
| Alkane | Alkene | Naphthenic hydrocarbon | Aromatic hydrocarbons | Alkane | Alkene | Naphthenic hydrocarbon | Aromatic hydrocarbons | |
| C 4 | 0.01 | 0.17 | - | - | 0.71 | 2.18 | - | - |
| C 5 | 6.41 | 16.14 | - | - | 14.53 | 10.47 | - | - |
| C 6 | 8.29 | 13.18 | 1.00 | 0.48 | 10.50 | 5.84 | 2.00 | 0.72 |
| C 7 | 5.00 | 7.11 | 1.71 | 2.23 | 5.29 | 4.10 | 2.67 | 4.54 |
| C 8 | 3.95 | 3.98 | 1.31 | 5.43 | 3.49 | 1.44 | 1.42 | 9.76 |
| C 9 | 2.37 | 2.08 | 1.94 | 5.87 | 1.39 | 0.60 | 0.48 | 8.62 |
| C 10 | 2.75 | 0.46 | 0.55 | 3.55 | 1.35 | 0.32 | 0.11 | 3.69 |
| C 11 | 1.54 | - | 0.57 | 1.13 | 1.36 | - | 0.42 | 1.44 |
| C 12 | 0.14 | - | - | - | 0.55 | - | - | - |
| Full cut adds up to | 30.46 | 43.12 | 7.08 | 18.69 | 39.17 | 24.95 | 7.10 | 28.77 |
| ＜C 6Add up to | 14.71 | 29.49 | 1.00 | 0.48 | 25.74 | 18.49 | 2.00 | 0.72 |
| ＜C 6Account for full cut, m% | 48.29 | 68.39 | 14.12 | 2.57 | 65.71 | 74.11 | 28.17 | 2.50 |
The reaction product of light gasoline fraction and the reaction product of stock oil are converged in riser reactor and are up along riser tube.In the riser tube exit, the catalyzer sharp separation of carbon deposit after reaction oil gas and the reaction, reclaimable catalyst recycles after stripping and regeneration.
Method provided by the invention does not have special requirement to catalyzer and stock oil, and any catalyzer in catalytic cracking field or stock oil of being applicable to all can be used for the present invention.Described catalyzer can contain one or more zeolites, and described zeolite can be selected from: X type zeolite, REY type zeolite, REHY type zeolite, USY type zeolite, ZSM-5 zeolite, other has supersiliceous zeolite of five-membered ring structure etc.Described stock oil can be selected from: the mixture of decompressed wax oil, vacuum residuum, long residuum, wax tailings, deasphalted oil, hydrogenation tail oil or two or more above-mentioned hydrocarbon ils.
Further specify the method for reduction content of olefin in gasoline provided by the invention below in conjunction with accompanying drawing, but not thereby limiting the invention.
As shown in Figure 1, light gasoline fraction after the preheating enters riser reactor 2 bottoms through pipeline 1, contact with regenerated catalyst and react from regenerator sloped tube 17, reaction oil gas that is generated and mixture of catalysts are up along riser tube, converge with the stock oil that sprays at stock oil feed nozzle 3 places and continue along riser tube up.In the riser tube exit, reaction oil gas and catalyzer sharp separation.Reaction oil gas and water vapor through settling vessel 7, enter follow-up system by pipeline 8 and carry out product separation.The reclaimable catalyst of finishing above-mentioned reaction process enters in the stripper 9, behind the water vapor stripping from pipeline 10, enters revivifier 13 coke burning regenerations through inclined tube 5 to be generated.The oxygen-containing gas of regeneration usefulness is introduced revivifier 13 through pipeline 14, and regenerated flue gas is drawn by pipeline 12.High temperature regeneration agent after the regeneration is returned riser reactor 2 through regenerator sloped tube 17 and is recycled.
Except above-mentioned feeding manner, light gasoline fraction also can by be positioned at more than the riser tube Y type section, the feed nozzle 4 injecting lift pipes of stock oil feed nozzle below 3; Perhaps with petroleum naphtha with after stock oil mixes, by stock oil feed nozzle 3 injecting lift pipes.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
Present embodiment explanation: method provided by the invention can obviously reduce the olefin(e) centent of catalytically cracked gasoline, and the influence that the treatment capacity and the product of device distributed is less.
On the riser fluid catalytic cracking of 1,000,000 tons/year in a cover, mixing residual oil with the import wax oil shown in the table 2 is raw material, and the mixture of the Ramcat catalyzer of the LV-23 catalyzer of employing Lanzhou oil-refining chemical head factory catalyst plant production and the production of GraceDavison company, its character sees Table 3, the invention provides the commerical test of method.The final boiling point that used light gasoline fraction is extracted out for stabilizer tower top is less than 130 ℃ cut, and its character sees Table 4.Main operational condition in the process of the test sees Table 5, and the product distribution situation sees Table 6.The character of gasoline products sees Table 7.For the purpose of contrasting, will implement before the present invention, the character of the main operational condition of this catalytic cracking unit, product distribution situation and gasoline products is listed in table 5～7 in the lump.
By the product distributed data in the table 6 and the gasoline products character data in the table 7 as can be seen, adopt method provided by the invention can make the olefin(e) centent of gasoline products reduce by 11.6 percentage points, and the treatment capacity of device is not had influence substantially, therefore the economic benefit of device is suffered a loss.
Table 2
| Material name | The import wax oil is mixed residual oil | The grand celebration long residuum |
| Density (20 ℃), g/cm 3 | 0.9167 | 0.8889 |
| Carbon residue, heavy % | 3.7 | 4.1 |
| Basic nitrogen, ppm | 943 | 837 |
| Hydrogen richness, heavy % | 12.21 | 13.15 |
| Group composition, V% | ||
| Stable hydrocarbon | 58.2 | 54.0 |
| Aromatic hydrocarbons | 29.4 | 28.4 |
| Colloid | 11.8 | 17.1 |
| Bituminous matter | 0.6 | 0.5 |
Table 3
Table 4
Table 5
Table 6
Table 7
| The catalyzer title | LV-23+Ramcat | RAG |
| Chemical constitution, heavy % | ||
| Aluminum oxide | 45.7 | 44.6 |
| Sodium oxide | 0.56 | 0.21 |
| Apparent density, kilogram/rice 3 | 780 | 790 |
| Pore volume, milliliter/gram | 0.27 | 0.28 |
| Specific surface area, rice 2/ gram | 102 | 112 |
| Abrasion index, %/hour | 2.3 | 2.1 |
| Size composition, heavy % | ||
| ＜20 microns | 0.1 | 0.7 |
| 20～40 microns | 3.19 | 20.7 |
| 40～80 microns | 52.89 | 50.7 |
| 80～110 microns | 22.31 | 14.5 |
| ＞110 microns | 21.51 | 9.5 |
| Micro-activity | 61 | 66 |
| The character of light gasoline fraction | The petroleum naphtha that extract out on stabilizer tower top | The rich gas compressor condensed oil |
| Density (20 ℃), kilogram/rice 3 | 657 | 645 |
| Group composition, heavy % | ||
| Alkane | 21.04 | 19.17 |
| Alkene | 64.56 | 67.96 |
| Naphthenic hydrocarbon | 8.56 | 7.05 |
| Aromatic hydrocarbon | 5.84 | 5.82 |
| Boiling range, ℃ | ||
| Initial boiling point | 41 | / |
| 10％ | 52 | 49 |
| 50％ | 65 | 67 |
| 90％ | 116 | 119 |
| Do | 128 | 133 |
| Operation scheme | FCC | The present invention |
| Petroleum naphtha freshening amount accounts for fresh feed, heavy % | / | 16.9 |
| The petroleum naphtha feed entrance point | / | The riser tube bottom |
| Reaction pressure (cutting off), MPa | 0.286 | 0.304 |
| Regeneration pressure (cutting off), MPa | 0.303 | 0.305 |
| Temperature of reaction, ℃ | 515 | 515 |
| Agent-oil ratio | 6.2 | 6.5 |
| Reaction times, s | 3.6 | 3.0 |
| The gasoline reaction times, s | / | 0.46 |
| The regeneration dense phase temperature, ℃ | 696 | 690 |
| Operation scheme | FCC | The present invention |
| The fresh feed inlet amount, t/h | 123 | 118 |
| Product distributes, heavy % | ||
| Dry gas | 3.31 | 3.96 |
| Liquefied gas | 9.14 | 11.04 |
| Gasoline | 45.41 | 40.65 |
| Diesel oil | 28.16 | 30.17 |
| Slurry oil | 6.26 | 6.31 |
| Coke | 7.20 | 7.36 |
| Loss | 0.52 | 0.51 |
| Add up to | 100.0 | 100.0 |
| The character of gasoline products | FCC | The present invention |
| Density (20 ℃), kilogram/rice 3 | 0.7307 | 0.7391 |
| RON/MON | 92.6/80.6 | 93.0/81.5 |
| Inductive phase, minute | 570 | 440 |
| Existent gum, milligram/100 | 7 | 4 |
| Sulphur content, ppm | 951 | 659 |
| Nitrogen content, ppm | 29 | 28 |
| Group composition (fluorescent method), V% | ||
| Stable hydrocarbon | 38.9 | 45.2 |
| Alkene | 43.8 | 32.2 |
| Aromatic hydrocarbon | 17.3 | 22.6 |
| Boiling range, ℃ | ||
| Initial boiling point/10% | 37/53 | 40/53 |
| 50％/90％ | 98/161 | 96/163 |
| Do | 196 | 199 |
Present embodiment explanation: method provided by the invention can obviously reduce the olefin(e) centent of catalytically cracked gasoline, and the influence that the treatment capacity and the product of device distributed is less.
In a cover treatment capacity is on the riser fluid catalytic cracking of 16t/h, is raw material with the grand celebration long residuum shown in the table 2, and adopt shown in the table 3 by the industrial RAG catalyzer of Qilu Petrochemical company catalyst plant, the invention provides the commerical test of method.Used light gasoline fraction is the condensed oil of rich gas compressor, and its character sees Table 4.Main operational condition in the process of the test sees Table 8, and the product distribution situation sees Table 9.The character of gasoline products sees Table 10.For the purpose of contrasting, will implement before the present invention, the character of the main operational condition of this catalytic cracking unit, product distribution situation and gasoline products is listed in table 8～10 in the lump.
By the product distributed data in the table 9 and the gasoline products character data in the table 10 as can be seen, adopt method provided by the invention can make the olefin(e) centent of gasoline products reduce by 13.04 percentage points, also smaller to the influence of the treatment capacity of device and economic benefit.
Table 8
Table 9
Table 10
| Operation scheme | FCC | The present invention |
| Petroleum naphtha freshening amount accounts for fresh feed, heavy % | / | 12.5 |
| The petroleum naphtha feed entrance point | / | Y type section top |
| Reaction pressure (cutting off), MPa | 0.25 | 0.25 |
| Regeneration pressure (cutting off), MPa | 0.26 | 0.26 |
| Temperature of reaction, ℃ | 530 | 530 |
| Agent-oil ratio | 8.1 | 8.3 |
| Reaction times, s | 3.8 | 3.3 |
| The gasoline reaction times, s | / | 0.32 |
| The regeneration dense phase temperature, ℃ | 700 | 692 |
| Operation scheme | FCC | The present invention |
| The fresh feed inlet amount, t/h | 16 | 16 |
| Product distributes, heavy % | ||
| Dry gas | 4.10 | 4.30 |
| Liquefied gas | 30.56 | 31.90 |
| Gasoline | 44.98 | 42.00 |
| Diesel oil | 11.23 | 12.60 |
| Slurry oil | / | / |
| Coke | 8.60 | 8.70 |
| Loss | 0.53 | 0.50 |
| Add up to | 100.00 | 100.00 |
| The character of gasoline products | FCC | The present invention |
| Density (20 ℃), kilogram/rice 3 | 0.7062 | 0.7122 |
| RON/MON | 94.1/81.0 | 94.0/80.8 |
| Inductive phase, minute | 392 | 498 |
| Existent gum, milligram/100 milliliters | 1.6 | 2 |
| Sulphur content, ppm | 102 | 93 |
| Nitrogen content, ppm | 40 | 29 |
| Group composition (fluorescent method), V% | ||
| Stable hydrocarbon | 33.29 | 42.81 |
| Alkene | 43.13 | 30.09 |
| Aromatic hydrocarbon | 16.96 | 21.03 |
| Boiling range, ℃ | ||
| Initial boiling point/10% | 35/42 | 40/52 |
| 50％/90％ | 72/152 | 83/156 |
| Do | 185 | 187 |
Claims (4)
1, a kind of catalyst cracking method that reduces content of olefin in gasoline may further comprise the steps: reaction, regeneration, fractionation, absorption and stable, it is characterized in that the light gasoline fraction extracted out with the condensed oil of rich gas compressor and/or by stabilizer tower top upstream injecting lift pipe reactor by the stock oil feed nozzle, perhaps with stock oil by stock oil feed nozzle injecting lift pipe reactor, make it to contact with regenerated catalyst and react, temperature of reaction is the weight ratio 30～75 of 600～700 ℃, regenerated catalyst and light gasoline fraction; When being injected by the bottom of riser reactor when the rich gas compressor condensed oil and/or by the light gasoline fraction that extract out on stabilizer tower top, its reaction times is 0.3～0.6 second; More than above-mentioned light gasoline fraction is by riser tube Y type section, when injecting below the fresh feed feed nozzle, its reaction times is 0.2～0.5 second; Reactant flow is up along riser tube, makes reaction oil gas and catalyzer sharp separation in the riser tube exit, reclaims reaction product, and reclaimable catalyst recycles after stripping and regeneration.
2, in accordance with the method for claim 1, it is characterized in that described rich gas compressor condensed oil and/or the final boiling point of the light gasoline fraction extracted out by stabilizer tower top less than 130 ℃.
3, in accordance with the method for claim 1, it is characterized in that described reaction conditions is the weight ratio 40～65 of 630～670 ℃ of temperature of reaction, regenerated catalyst and light gasoline fraction.
4, in accordance with the method for claim 1, when it is characterized in that being injected by the bottom of riser reactor when the rich gas compressor condensed oil and/or by the light gasoline fraction that extract out on stabilizer tower top, its reaction times is 0.3～0.5 second; More than above-mentioned light gasoline fraction is by riser tube Y type section, when injecting below the fresh feed feed nozzle, its reaction times is 0.3～0.5 second.
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| CN100529025C (en) * | 2005-01-31 | 2009-08-19 | 中国科学院大连化学物理研究所 | Catalytic convertion method of liquified petroleum gas and gasoline feeding at same time |
| CN103361105A (en) * | 2012-04-05 | 2013-10-23 | 中国石油天然气股份有限公司 | Simple separation method for separating catalytic cracking gasoline into heavy gasoline and light gasoline |
| CN104650962B (en) * | 2013-11-19 | 2017-02-15 | 中国石油天然气股份有限公司 | Improved catalytic cracking technology method |
| CN114958420B (en) * | 2022-02-21 | 2023-09-05 | 洛阳瑞铭石化技术有限公司 | Processing technology for cracking light oil |
-
2000
- 2000-12-05 CN CNB001341197A patent/CN1141361C/en not_active Expired - Lifetime
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| CN1356372A (en) | 2002-07-03 |
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