CN105622316B - A kind of method for transformation of Fischer-Tropsch synthesis oil raw material - Google Patents
A kind of method for transformation of Fischer-Tropsch synthesis oil raw material Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P20/584—Recycling of catalysts
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Abstract
The invention discloses a kind of method for transformation of Fischer-Tropsch synthesis oil raw material, this method includes：Fischer-Tropsch synthesis oil raw material is contacted in the reactor of catalytic cracking unit with regenerated catalyst, obtains carbon deposited catalyst；The carbon deposited catalyst is introduced into regenerator after stripping by reclaimable catalyst delivery pipe and regenerated, obtains the regenerated catalyst；The reactor includes the riser reactor and fluidized-bed reactor being connected in series, wherein, the Fischer-Tropsch synthesis oil raw material is introduced into the riser reactor, and introduce fuel oil into the fluidized-bed reactor so that the Fischer-Tropsch synthesis oil raw material carries out described contact with regenerated catalyst in the presence of fuel oil.The above method of the present invention can adjust the technique thermal balance during Fischer-Tropsch synthesis oil producing light olefins through catalytic conversion on the premise of the yield by Fischer-Tropsch synthesis oil raw material production propylene is improved.
Description
Technical field
The present invention relates to a kind of method for transformation of Fischer-Tropsch synthesis oil raw material.
Background technology
Oil is a kind of non-renewable resources, with current petroleum reserves increasingly reduce and consumption increases sharply,
Research about oil product substitute increasingly heats up.Wherein, the research of Fischer-Tropsch (F-T) synthesis oil tech existing more than 80 years,
There are the F- T synthesis technology of its ripe independent development in the companies such as Sasol, Shell, Exxon/Mobil.
Fischer-Tropsch synthesis oil is a kind of material being mainly made up of the alkane and alkene of straight chain, is substantially free of aromatic hydrocarbons.Fischer-Tropsch closes
Each cut into product needs just obtain meeting the fluid product using specification by corresponding processing modification.At present, it is right
Diesel oil and more heavy distillat in Fischer-Tropsch synthesis oil, can use be hydrocracked/isomerization process long chain hydrocarbons therein are cut off or
The positive structure of the good short chain of cryogenic property or isoparaffin are isomerized to, obtains the jet fuel and diesel oil blending component of high quality；
The preferable lube base oil of hydroisomerizing DEWAXING TECHNIQUE synthesising property can also be used.The gasoline fraction alkane of Fischer-Tropsch synthesis oil
Content is higher, octane number is low, is not suitable for as gasoline blend component, can be as steam cracking device after hydrofinishing
Raw material produces ethene.As fully visible, the secondary operation of Fischer-Tropsch synthesis oil is directed to greatly expensive hydrogenation process or energy consumption is higher
High temperature pyrolysis process.
But it can be seen that from document report in recent years and Fischer-Tropsch synthesis oil raw material processed using deep catalytic cracking technology, Fischer-Tropsch closes
Reveal the performance of outstanding production low-carbon alkene into oil meter, but its coke output is low.Therefore, according to existing catalytic cracking unit
Fischer-Tropsch synthesis oil is processed, itself thermal balance can not be met at all by depending merely on the coke combustion heat release being attached on reclaimable catalyst, instead
Should-regenerative system exist very big heat breach, it is necessary to provide heat by other means for system.
A kind of method of additional heat is that fuel oil is injected directly into regenerator, and fuel oil can be that feedstock oil, diesel oil evaporate
Point or other liquid fuels.Can cause local temperature too high in this way, so as to cause device impaired, catalyst inactivation,
The adverse consequences such as catalyst structure avalanche.CN1345911A discloses a kind of regulation catalytic conversion technological reaction-regeneration system heat
The method of balance.This method, which uses, contacts heavy end injection stripping section with reclaimable catalyst, is carried with increasing on catalyst
Amount of coke and oil gas, so as to increase the heat of reaction-regeneration system.Such a method is commonly used concurrent heating side of current refinery
Method, but because Fischer Tropsch synthetic oil in catalytic cracking mode reaction coking rate is low, generally less than 3 weight %, the cracking activity of reclaimable catalyst
It is still very high, therefore be not suitable for directly spraying into fuel oil to stripper.
The content of the invention
The purpose of the present invention is the defects of overcoming prior art, is being improved by the yield of Fischer-Tropsch synthesis oil raw material production propylene
On the premise of, there is provided one kind regulation Fischer-Tropsch synthesis oil catalyzed conversion produces the thermally equilibrated side of technique in low carbon olefin hydrocarbon in high yield
Method.
To achieve these goals, the present invention provides a kind of method for transformation of Fischer-Tropsch synthesis oil raw material, and this method includes：Will
Fischer-Tropsch synthesis oil raw material contacts with regenerated catalyst in the reactor of catalytic cracking unit, obtains carbon deposited catalyst；By described in
Carbon deposited catalyst is introduced into regenerator after stripping by reclaimable catalyst delivery pipe to be regenerated, and obtains the regeneration catalyzing
Agent；The reactor includes the riser reactor and fluidized-bed reactor being connected in series, wherein, the Fischer-Tropsch synthesis oil is former
Material is introduced into the riser reactor, and introduces fuel oil into the fluidized-bed reactor so that the Fischer-Tropsch synthesis oil
Raw material carries out described contact with regenerated catalyst in the presence of fuel oil.
When being converted by using the above method of the present invention by Fischer-Tropsch synthesis oil raw material, it can efficiently supplement and be used for
Heat needed for the reaction-regeneration system of Fischer-Tropsch synthesis oil raw material conversion；Fuel oil is split in a fluidized bed reactor simultaneously
Change reaction generating portion liquefied gas and gasoline etc., improve the economic benefit of plant running.Moreover, the above method energy of the present invention
It is enough to suppress the yield that Fischer-Tropsch synthesis oil raw material production low-carbon alkene is improved while conversion again of propylene, butylene.
Further, the method that the present invention is can be seen that by the result of embodiments of the invention can obtain high third
Alkene yield, moreover, by adjusting process operating condition, the yield of propylene is enabled to reach more preferably.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Accompanying drawing is for providing a further understanding of the present invention, and a part for constitution instruction, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 be the method according to the invention a kind of preferred embodiment used by process flow diagram.
Embodiment
The embodiment of the present invention is described in detail below.It is it should be appreciated that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The invention provides a kind of method for transformation of Fischer-Tropsch synthesis oil raw material, this method includes：By Fischer-Tropsch synthesis oil raw material
Contacted with regenerated catalyst in the reactor of catalytic cracking unit, obtain carbon deposited catalyst；By the carbon deposited catalyst through vapour
It is introduced into regenerator and is regenerated by reclaimable catalyst delivery pipe after carrying, obtains the regenerated catalyst；The reactor bag
The riser reactor and fluidized-bed reactor being connected in series are included, wherein, the Fischer-Tropsch synthesis oil raw material is introduced into the lifting
In pipe reactor, and fuel oil is introduced into the fluidized-bed reactor so that the Fischer-Tropsch synthesis oil raw material and regeneration catalyzing
Agent carries out the contact in the presence of fuel oil.
In the present invention, the fuel oil can include the slurry oil of catalytic cracking, the heavy end of coking, the weight of thermal cracking
At least one of matter cut, the heavy end of visbreaking, straight run reduced pressure distillate and straight asphalt.
In the present invention, the boiling range of the fuel oil can be more than 300 DEG C, and carbon residue can be not less than 5 weight %.It is preferred that
In the case of, the carbon residue of the fuel oil is more than 10 weight %.
The temperature of the preferably regenerated catalyst of the invention is higher than 600 DEG C.
In method of the present invention, the bottom of preferably described fluidized-bed reactor is connected with settler.It will can flow
Logistics after being contacted in fluidized bed reactor with regenerated catalyst, which is introduced into settler, to be separated, and obtains reaction oil gas and carbon deposit is urged
Agent.The carbon deposited catalyst can be incorporated into regenerator to be regenerated by using conventional method in the art to be made with circulating
With the present invention is preferably incorporated into regenerator by reclaimable catalyst delivery pipe to be regenerated；The reaction oil gas can be carried out
Fractionation etc. is operated to obtain product.In the present invention, it is necessary to which special instruction, the carbon deposited catalyst are this area routine
Described reclaimable catalyst, the present invention use " carbon deposited catalyst " description " reclaimable catalyst " to express clearly and facilitate.
According to method of the present invention, relative to the Fischer-Tropsch synthesis oil raw material of 100 parts by weight, the dosage of the fuel oil
Can be 10-30 parts by weight；Preferably 12-25 parts by weight.
According to method of the present invention, relative to the Fischer-Tropsch synthesis oil raw material of 100 parts by weight, the carbon deposited catalyst
Coke content can be 5-10 parts by weight.
In method of the present invention, the fuel oil can be introduced to the middle and upper part of the fluidized-bed reactor.
, preferably can be apart from institute relative to the total length of the fluidized-bed reactor in method of the present invention
State and introduce the fuel oil at the top of fluidized-bed reactor at 1/8-1/2.In the present invention, it is necessary to especially explain, the stream
Fluidized bed reactor can be cylinder, and the introducing position of the fuel oil can be 1/ at the top of the fluidized-bed reactor
8 any places sentenced down in the region more than at the top of the fluidized-bed reactor 1/2 introduce, moreover, of the invention
Method to the number of point that introduces the fuel oil, also there is no particular limitation, those skilled in the art are understanding the present invention
Technical scheme after can be selected to introduce the number of the point of the fuel oil according to actual conditions.
In the case of more preferably, in method of the present invention, relative to the total length of the fluidized-bed reactor,
The fuel oil can be being introduced at 1/3-1/2 at the top of the fluidized-bed reactor.
According to method of the present invention, fuel oil is introduced into the fluidized-bed reactor, under preferable case so that institute
It is downward to state the penetrating direction of fuel oil, and axial angle α is 30 ° -60 °.In the present invention, it is necessary to special instruction, the axle
Refer to the angle value of the acute angle of the side wall formation for spraying into direction and the fluidized-bed reactor of fuel oil to angle α.
In method of the present invention, the reaction condition in the riser reactor and fluidized-bed reactor can phase
It is same or different.
In method of the present invention, the reaction condition in preferably described fluidized-bed reactor includes：Reaction temperature is
480-700 DEG C, preferably 500-620 DEG C.
In method of the present invention, the reaction condition in preferably described fluidized-bed reactor includes：When oil gas stops
Between be 0.5-20 seconds, preferably 2-10 seconds.
In method of the present invention, the reaction condition in preferably described fluidized-bed reactor includes：The regeneration is urged
Agent and the weight ratio of the Fischer-Tropsch synthesis oil raw material and the summation of the fuel oil are 6-40：1, preferably 10-30：1.
In method of the present invention, the reaction condition in preferably described riser reactor includes：Reaction temperature is
480-700 DEG C, preferably 500-650 DEG C.
In method of the present invention, the reaction condition in preferably described riser reactor includes：When oil gas stops
Between be 0.5-10 seconds, preferably 0.5-6 seconds.
In method of the present invention, the reaction condition in preferably described riser reactor includes：The regeneration is urged
Agent and the weight ratio of the Fischer-Tropsch synthesis oil raw material are 5-40：1, preferably 10-20：1.
In the present invention, the oil gas residence time refers to that the oil phase material of unit portion and the mixture of gaseous phase materials exist
Residence time in reactor.
In the present invention, it is preferred to it is described by Fischer-Tropsch synthesis oil raw material and regenerated catalyst catalytic cracking unit reactor
The method of middle contact includes：The Fischer-Tropsch synthesis oil raw material and the regenerated catalyst are first introduced into the riser reactor,
Then the logistics in the riser reactor is introduced into the fluidized-bed reactor.
According to a kind of preferred embodiment of the present invention, method of the invention can include：By Fischer-Tropsch synthesis oil
Raw material contacts in the riser reactor and fluidized-bed reactor of catalytic cracking unit successively with regenerated catalyst, and to institute
State and the fuel oil is introduced in fluidized-bed reactor so that the Fischer-Tropsch synthesis oil raw material is with regenerated catalyst in fluidized-bed reaction
Contact in device is carried out in the presence of fuel oil；Then by the Fischer-Tropsch synthesis oil raw material and fuel oil and the regenerated catalyst
Logistics after contact introduces settler, reaction oil gas and carbon deposited catalyst is separated, so as to obtain the carbon deposited catalyst；By described in
Reaction oil gas introduces fractionating system, and the carbon deposited catalyst is sent into regenerator by reclaimable catalyst delivery pipe after stripping and carried out
Regeneration, the carbon deposited catalyst are recycled in Returning reactor after regeneration.
There is no particular limitation for method and condition of the method for the present invention to the fractionation, and the method and bar of the fractionation
Part is known to those skilled in the art, and the present invention will not be repeated here.
There is no particular limitation to property of the Fischer-Tropsch synthesis oil raw material etc. for the method for the present invention, under preferable case, institute
State Fischer-Tropsch synthesis oil raw material selected from Fischer-Tropsch synthetic mid-boiling point scope be 23 DEG C into the part cut or full cut of the end point of distillation
One or more of mixtures.
According to another preferred embodiment of the present invention, method of the invention is using the technological process signal shown in Fig. 1
Figure is carried out, and specifically, is carried out with the following method：By Fischer-Tropsch synthesis oil raw material by pipeline 1 with being conveyed from regenerated catalyst
The regenerated catalyst of pipe 12 contacts in the riser reactor 2 and fluidized-bed reactor 3 of catalytic cracking unit successively, and to
The fuel oil is introduced by pipeline 13 in the fluidized-bed reactor so that the Fischer-Tropsch synthesis oil raw material and regenerated catalyst
Contact in a fluidized bed reactor is carried out in the presence of fuel oil；Then by the Fischer-Tropsch synthesis oil raw material and fuel oil and institute
State the logistics after regenerated catalyst contact and introduce settler 4, reaction oil gas and carbon deposited catalyst are separated, so as to obtain the carbon deposit
Catalyst；The reaction oil gas is introduced into follow-up fractionating system through pipeline 5, the carbon deposited catalyst enters stripper 6, and leads to
Cross pipeline 7 and introduce stripping fluid into the stripper, the carbon deposited catalyst is sent by reclaimable catalyst delivery pipe 8 after stripping
Enter and regenerated in regenerator 10, in regenerative process, oxygen-containing gas etc. enters the regenerator through pipeline 9, and regenerated flue gas passes through
Pipeline 11 is discharged, and the carbon deposited catalyst in the Returning reactor of regenerated catalyst 12 after regeneration by recycling.
It will be understood by those skilled in the art that in the present invention, the kind of the regenerated catalyst and reclaimable catalyst
Class is identical, and both are only the different conditions for representing same catalyst, therefore, in the present invention, describes for convenience, hereinafter
Also the regenerated catalyst and reclaimable catalyst are referred to as catalyst.
In method of the present invention, the catalyst can be that active component is selected from the Y for containing or not contain rare earth
Or HY types zeolite, the ultrastable for containing or not contain rare earth, ZSM-5 series zeolites or the high silicon with five-membered ring structure
One or more catalyst or amorphous silicon aluminium catalyst in zeolite and β zeolites.
In the present invention, to the regeneration and the condition regenerated, there is no particular limitation, and those skilled in the art can
Regenerated with the condition using various regenerations commonly used in the art and regeneration, for example, example in embodiments of the invention
Property regenerated by the way of CO completely burneds, those skilled in the art by this should not be construed as to the present invention technical side
The limitation of case.
The above-mentioned technical proposal of the present invention has advantages below：
1st, method provided by the invention can efficiently supplement the heat needed for reaction-regeneration system；
2nd, method provided by the invention can make fuel oil cracking generating portion liquefied gas and gasoline etc., improve plant running
Economic benefit；
3rd, method provided by the invention can suppress propylene, butylene converts again, improve Fischer-Tropsch synthesis oil production low-carbon
The selectivity of alkene.
The present invention will be described in detail by way of examples below.Catalyst used in embodiment and comparative example by
Catalyst asphalt in Shenli Refinery of Sinopec Group industrial production, product designation MMC-2.The catalyst contains
Ultrastable and average pore size are less than 0.7 nanometer of ZSP zeolites, are satisfied using preceding at a temperature of 800 DEG C through 100 weight %
With steam hydrothermal aging 14 hours, the main physico-chemical property of the catalyst was shown in Table 1.Raw material cost used in embodiment and comparative example
The property of support artificial oil is shown in Table 2.Used fuel oil is the slurry oil for picking up from Conventional catalytic cracking device, the property of the fuel oil
It is shown in Table 3.Used device is the middle- scale device of successive reaction-regenerative operation, and reactor is the compound of riser and fluid bed
Reactor, riser reactor more than outlet are fluidized-bed reactor.The temperature control of the middle- scale device comes from electrical heating.
In the following Examples and Comparative Examples, the oil ratio is catalyst and feedstock oil (including Fischer-Tropsch synthesis oil raw material and fuel
Oil) weight ratio.
Table 1
| Catalyst | MMC-2 |
| Zeolite | |
| Y contents/weight % | 16 |
| ZSP contents/weight % | 12 |
| Physical property | |
| Than surface/(m2/g) | 143 |
| Pore volume/(cm3/g) | 0.186 |
| Apparent density/(g/cm3) | 0.85 |
| Screening | |
| 0-20 μm/weight % | 0.8 |
| 0-40 μm/weight % | 10.4 |
| 0-80 μm/weight % | 70.8 |
| 0-110 μm/weight % | 88.5 |
| 0-149 μm/weight % | 97.8 |
| >149 μm/weight % | 2.2 |
| Micro-activity | 66 |
Table 2
| Project | Raw material |
| Density (20 DEG C)/gcm-3 | 0.806 |
| Freezing point/DEG C | 76 |
| Element composition/weight % | |
| C | 85.18 |
| H | 14.47 |
| O | 0.35 |
| S/μg·g-1 | 1.6 |
| N/μg·g-1 | 5 |
| Boiling range/DEG C | |
| Initial boiling point | 268 |
| 10 volume % | 391 |
| 30 volume % | 465 |
| 50 volume % | 521 |
| 70 volume % | 584 |
| 90 volume % | 652 |
| The end point of distillation | 710 |
Table 3
| Project | Fuel oil |
| Density (20 DEG C)/(gcm-3) | 1.016 |
| Carbon residue/weight % | 11.63 |
| Element composition/weight % | |
| C | 91.1 |
| H | 7.3 |
| Boiling range/DEG C | |
| Initial boiling point | 301 |
| 10 volume % | 321 |
| 50 volume % | 403 |
| The end point of distillation | 601 |
| Four components/weight % | |
| Saturated hydrocarbons | 35.10 |
| Aromatic hydrocarbons | 49.90 |
| Colloid | 10.67 |
| Asphalitine | 4.03 |
Embodiment 1
The present embodiment is carried out using process chart as shown in Figure 1, is in particular：
Fischer-Tropsch synthesis oil raw material shown in table 2 is passed through into pipeline 1 and the regeneration catalyzing from regenerated catalyst 12
Agent (property is as shown in table 1) contacts in the riser reactor 2 and fluidized-bed reactor 3 of catalytic cracking unit successively, and
The fuel oil of property shown in table 3 is introduced by pipeline 13 into the fluidized-bed reactor so that the Fischer-Tropsch synthesis oil raw material
Carried out with the contact of regenerated catalyst in a fluidized bed reactor in the presence of fuel oil；Then by the Fischer-Tropsch synthesis oil raw material
Logistics after being contacted with fuel oil with the regenerated catalyst introduces settler 4, separates reaction oil gas and carbon deposited catalyst, so as to
Obtain the carbon deposited catalyst；The reaction oil gas is introduced into follow-up fractionating system through pipeline 5, the carbon deposited catalyst enters
Stripper 6, and stripping fluid is introduced into the stripper by pipeline 7, the carbon deposited catalyst is urged by be generated after stripping
Agent delivery pipe 8, which is sent into regenerator 10, to be regenerated, and in regenerative process, oxygen-containing gas etc. enters the regenerator through pipeline 9,
And regenerated flue gas is discharged through pipeline 11, the carbon deposited catalyst passes through the Returning reactor of regenerated catalyst 12 after regeneration
Middle recycling.
The present embodiment uses the total length relative to the fluidized-bed reactor, at the top of the fluidized-bed reactor
The fuel oil is introduced at 1/2, and axial angle α is 45 °.
The process conditions and result of the present embodiment are as shown in table 4.
Comparative example 1
This comparative example is carried out using method similar to Example 1, except that：
Fuel oil is not introduced into the fluidized-bed reactor.Remaining is same as Example 1.
Prevailing operating conditions and result are listed in table 4.
Comparative example 2
This comparative example is carried out using method similar to Example 1, except that：
The fuel oil is incorporated into riser reactor, and intake apart from the outlet of the riser reactor about
10cm.Remaining is same as Example 1.
Prevailing operating conditions and result are listed in table 4.
Comparative example 3
This comparative example is carried out using method similar to Example 1, except that：
Fuel oil is introduced into the stripper.Remaining is same as Example 1.
Prevailing operating conditions and result are listed in table 4.
Embodiment 2
The present embodiment is carried out using method similar to Example 1, except that：
The present embodiment uses the total length relative to the fluidized-bed reactor, at the top of the fluidized-bed reactor
The fuel oil is introduced at 2/5, and axial angle α is 40 °, technological parameter condition is different from embodiment 1, specifically such as institute in table 5
Show.
The process conditions and result of the present embodiment are as shown in table 5.
Embodiment 3
The present embodiment is carried out using method similar to Example 1, except that：
The present embodiment uses the total length relative to the fluidized-bed reactor, at the top of the fluidized-bed reactor
The fuel oil is introduced at 1/3, and axial angle α is 50 °, technological parameter condition is different from embodiment 1, specifically such as institute in table 5
Show.
The process conditions and result of the present embodiment are as shown in table 5.
Embodiment 4
The present embodiment is carried out using method similar to Example 1, except that：
The fuel oil is introduced from the top of fluidized-bed reactor.Remaining is same as Example 1.
Prevailing operating conditions and result are listed in table 5.
Embodiment 5
The present embodiment is carried out using method similar to Example 2, except that：
Relative to the Fischer-Tropsch synthesis oil raw material of 100 parts by weight, the dosage of the fuel oil is 30 parts by weight.Remaining with reality
It is identical to apply example 2.
Prevailing operating conditions and result are listed in table 5.
Embodiment 6
The present embodiment is carried out using method similar to Example 5, except that：
Relative to the Fischer-Tropsch synthesis oil raw material of 100 parts by weight, the dosage of the fuel oil is 5 parts by weight.Remaining with reality
It is identical to apply example 5.
Prevailing operating conditions and result are listed in table 5.
Table 4
| Project | Embodiment 1 | Comparative example 1 | Comparative example 2 | Comparative example 3 |
| Feed throughput/(kg/h) | 1 | 1 | 1 | 1 |
| Injection burning oil mass/(kg/h) | 0.14 | 0 | 0.14 | 0.14 |
| Riser reactor | ||||
| Reaction temperature/DEG C | 620 | 620 | 620 | 620 |
| The oil gas residence time/s | 2.5 | 2.5 | 2.5 | 2.5 |
| Fluidized-bed reactor | ||||
| Reaction temperature/DEG C | 580 | 580 | 580 | 580 |
| The oil gas residence time/s | 5 | 5 | 5 | 5 |
| Settler pressure/(105Pa) | 1.8 | 1.8 | 1.8 | 1.8 |
| Regeneration | CO completely burneds | CO completely burneds | CO completely burneds | CO completely burneds |
| Regeneration temperature/DEG C | 680 | 680 | 680 | 680 |
| Product yield/(kg/h) | ||||
| Dry gas | 0.076 | 0.071 | 0.085 | 0.072 |
| Liquefied gas | 0.51 | 0.495 | 0.487 | 0.498 |
| Gasoline | 0.395 | 0.369 | 0.304 | 0.373 |
| Diesel oil | 0.061 | 0.041 | 0.083 | 0.045 |
| Heavy oil | 0.010 | 0 | 0.061 | 0 |
| Coke | 0.088 | 0.024 | 0.12 | 0.152 |
| Amount to | 1.14 | 1 | 1.14 | 1.14 |
| Propene yield/(kg/h) | 0.294 | 0.261 | 0.233 | 0.262 |
Table 5
The preferred embodiment of the present invention described in detail above, still, the present invention are not limited in above-mentioned embodiment
Detail, in the range of the technology design of the present invention, a variety of simple variants can be carried out to technical scheme, this
A little simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy no longer separately illustrates.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should equally be considered as content disclosed in this invention.
Claims (12)
1. a kind of method for transformation of Fischer-Tropsch synthesis oil raw material, this method include：Fischer-Tropsch synthesis oil raw material and regenerated catalyst are existed
Contacted in the reactor of catalytic cracking unit, obtain carbon deposited catalyst；The carbon deposited catalyst is urged after stripping by be generated
Agent delivery pipe, which is introduced into regenerator, to be regenerated, and obtains the regenerated catalyst；Characterized in that, the reactor includes string
Join the riser reactor and fluidized-bed reactor of connection, wherein, it is anti-that the Fischer-Tropsch synthesis oil raw material is introduced into the riser
Answer in device, and fuel oil is introduced into the fluidized-bed reactor so that the Fischer-Tropsch synthesis oil raw material exists with regenerated catalyst
The contact is carried out in the presence of fuel oil.
2. the method according to claim 11, wherein, relative to the Fischer-Tropsch synthesis oil raw material of 100 parts by weight, the fuel oil
Dosage be 10-30 parts by weight.
3. the method according to claim 11, wherein, relative to the Fischer-Tropsch synthesis oil raw material of 100 parts by weight, the fuel oil
Dosage be 12-25 parts by weight.
4. according to the method for claim 1, wherein, relative to the Fischer-Tropsch synthesis oil raw material of 100 parts by weight, the carbon deposit is urged
The coke content of agent is 5-10 parts by weight.
5. according to the method described in any one in claim 1-4, wherein, relative to the overall length of the fluidized-bed reactor
Degree, the fuel oil is being introduced at 1/8-1/2 at the top of the fluidized-bed reactor.
6. the method according to claim 11, wherein, relative to the total length of the fluidized-bed reactor, described in distance
The fuel oil is introduced at the top of fluidized-bed reactor at 1/3-1/2.
7. according to the method for claim 1, wherein, introduce fuel oil into the fluidized-bed reactor so that the combustion
Expect that the penetrating direction of oil is downward, and axial angle α is 30 ° -60 °.
8. according to the method for claim 1, wherein, slurry oil, the heavy of coking that the fuel oil includes catalytic cracking evaporate
Point, at least one of the heavy end of thermal cracking, the heavy end of visbreaking, straight run reduced pressure distillate and straight asphalt.
9. according to the method for claim 1, wherein, the reaction condition in the fluidized-bed reactor includes：Reaction temperature
For 480-700 DEG C；The oil gas residence time is the 0.5-20 seconds；The regenerated catalyst and the Fischer-Tropsch synthesis oil raw material and the combustion
The weight ratio for expecting the summation of oil is 6-40：1.
10. according to the method for claim 8, wherein, the reaction condition in the fluidized-bed reactor includes：Reaction temperature
For 500-620 DEG C；The oil gas residence time is the 2-10 seconds；The regenerated catalyst and the Fischer-Tropsch synthesis oil raw material and the fuel
The weight ratio of the summation of oil is 10-30：1.
11. according to the method for claim 1, wherein, the reaction condition in the riser reactor includes：Reaction temperature
For 480-700 DEG C；The oil gas residence time is the 0.5-10 seconds；The regenerated catalyst and the weight ratio of the Fischer-Tropsch synthesis oil raw material
For 5-40：1.
12. according to the method for claim 11, wherein, the reaction condition in the riser reactor includes：Reaction temperature
Spend for 500-650 DEG C；The oil gas residence time is the 0.5-6 seconds；The regenerated catalyst and the weight of the Fischer-Tropsch synthesis oil raw material
Than for 10-20：1.
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