CN105586075B - A kind of Grading And Zoning catalytic cracking conversion method of wax tailings - Google Patents
A kind of Grading And Zoning catalytic cracking conversion method of wax tailings Download PDFInfo
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Abstract
The invention provides a kind of method of catalytic cracking wax tailings, this method comprises the following steps：(1) wax tailings are fractionated, using cut of the boiling range more than the first cut-point and below the second cut-point as the first cut, boiling range are less than the cut of the first cut-point and/or boiling range is more than the second cut-point cut as the second cut；(2) the first feedstock oil containing first cut is converted into the first material containing the first primary cracking product；(3) the second feedstock oil containing second cut is converted into the second material containing the second primary cracking product；(4) first material and the second material are contacted in riser reactor, continues catalytic cracking reaction subsequently into stripping sedimentation device and carry out gas solid separation, obtain oil gas product and reclaimable catalyst.Pass through above-mentioned technical proposal, the present invention can mitigate toxic action of the wax tailings to catalyst, enable to conversion ratio to rise, product distribution more preferably with product quality raising, mixes refining ratio so as to improve wax tailings in catalytic cracking.
Description
Technical field
The present invention relates to petrochemical industry, in particular it relates to a kind of Grading And Zoning catalytic cracking conversion of wax tailings
Method.
Background technology
As crude oil heaviness, the aggravation of in poor quality degree and light-end products demand increasingly increase, development heavy oil is efficient
Conversing technology turns into the urgent task of current petroleum refining industry.Delayed coking is one of Main Means of heavy oil lighting, is accounted for
More than the 30 weight % of world's processing of heavy oil ability.In the product distribution of coking, wax tailings (Coker Gas Oil)
Yield be usually 20-30 weight %, the processing and utilization of this part cut, directly affect heavy oil transformation efficiency, turn into restriction
The key issue of heavy oil deep processing.
At present, wax tailings are generally as secondary operation device such as catalytic cracking (Fluid Catalytic
Cracking the raw material), being hydrocracked.Take the process program being hydrocracked in external oil refining enterprise more；Due to by hydrogenation capability,
The restriction of the conditions such as hydrogen inadequate resource, with reference to each refinery facilities it is supporting the characteristics of, China mainly splits wax tailings as catalysis
Change process mixes refining raw material.Production practices show that the reactivity worth of wax tailings is poor, cause under catalytic cracking process conversion ratio
How a series of adverse consequences such as drop, product distribution deteriorate, product quality is deteriorated, therefore, improve catalytic cracking unit to poor quality
The adaptability of raw material, reduction mix refining wax tailings caused by adversely affect, be tackle coking production capacity increase rapidly compel
It is essential and asks.Carried out largely to solve this problem, production unit and researcher in terms of wax tailings processing technology
Work.
For example, CN1891791A discloses a kind of method and apparatus of processing coked waxy oil, it is specifically that riser is anti-
Answer the bottom of device to be divided into the separate reaction zones of two vertical parallels, allow wax tailings to enter with other more high-quality convenient source oil
Enter different reaction zones and carry out catalytic cracking reaction, reacted logistics is in the riser reactor in two reaction zones
Top is converged, i.e., riser reactor bottom is the separate reaction zones that two branch pipes are formed.But the it is demonstrated experimentally that above method
In mix refining wax tailings caused by adverse effect it is still larger, exist conversion ratio decline, product distribution deteriorate and product quality
It is the defects of variation, still relatively low so as to cause wax tailings mixing in catalytic cracking to refine ratio.
The content of the invention
The purpose of the present invention is to mix to adversely affect caused by refining wax tailings in mitigating, and improves wax tailings and is split in catalysis
Refining ratio is mixed in change, there is provided a kind of Grading And Zoning catalytic cracking conversion method of wax tailings.
It was found by the inventors of the present invention that by wax tailings using the arbitrary temp in the range of 390-410 DEG C as the first cut-point,
After being fractionated using the arbitrary temp in the range of 440-460 DEG C as the second cut-point, by obtained boiling range the first cut-point with
Cut and remaining cut below upper and the second cut-point carry out remixing after preliminary catalytic cracking respectively carrying out follow-up urge
Change cracking, it becomes possible to mitigate toxic action of the wax tailings to catalyst, enable to conversion ratio to rise, product distribution is more preferable and
Product quality improves, and mixes refining ratio in catalytic cracking so as to improve wax tailings, resulting in the present invention.
To achieve these goals, the invention provides a kind of method of catalytic cracking wax tailings, this method to be included such as
Lower step：(1) wax tailings are fractionated, using boiling range more than the first cut-point and the following cut of the second cut-point is as
One cut, boiling range is less than the cut of the first cut-point and/or boiling range is more than the cut of the second cut-point as the second cut, institute
The first cut-point is stated as the arbitrary temp in the range of 390-410 DEG C, second cut-point is any in the range of 440-460 DEG C
Temperature；(2) by the first feedstock oil containing first cut and first cracking catalyst in the first anti-of riser reactor
Answer and the first contact is carried out in area, obtain the first material containing the first primary cracking product；(3) second cut will be contained
Second feedstock oil carries out second in the second reaction zone of the riser reactor with the second Cracking catalyst and contacted, and is contained
There is the second material of the second primary cracking product；(4) by the first material and the second material in the lifting tube reaction
3rd reaction zone of device carries out the 3rd contact, and continuing catalytic cracking reaction promoting the circulation of qi of going forward side by side subsequently into stripping sedimentation device consolidates
Separation, obtains oil gas product and reclaimable catalyst；(5) reclaimable catalyst is transported in fluid bed regenerator and burnt
Regeneration obtains regenerated catalyst, and using at least part of regenerated catalyst as the first cracking catalyst and described the
Two Cracking catalyst are respectively delivered in first reaction zone and the second reaction zone；Wherein, first reaction zone and
The second reaction zone is independently juxtaposed on the lower section of the 3rd reaction zone and met in the 3rd reaction zone.
Pass through above-mentioned technical proposal, the present invention can mitigate deactivation of the wax tailings to catalyst, enable to turn
Rate rises, product distribution is more preferable and product quality improves, and mixes refining ratio in catalytic cracking so as to improve wax tailings.
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 is the schematic diagram of device used in a kind of particularly preferred embodiment of the method for the present invention.
Description of reference numerals
The double distilled subtube of 1 fractionating column 11
12 light fraction pipelines
The reaction zone of 2 riser reactor 21 first
The reaction zone of 22 second reaction zone 23 the 3rd
The 3 stripping strippers of sedimentation device 31
The settler of 32 cyclone separator 33
4 regenerators
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that this place is retouched
The embodiment stated is merely to illustrate and explain the present invention, and is not intended to limit the invention.
In the present invention, in the case where not making opposite explanation, the noun of locality such as " upper and lower, bottom, top " used typically exists
Defined in the case of catalytic cracking unit normal use provided by the invention, specifically refer to the page shown in Fig. 1,
" inside and outside " refers to the inner and outer of respective profile.It should be noted that these nouns of locality are served only for the explanation present invention, it is not used to
The limitation present invention.
The invention provides a kind of method of catalytic cracking wax tailings, this method comprises the following steps：(1) by coking wax
Oil is fractionated, using cut of the boiling range more than the first cut-point and below the second cut-point as the first cut, boiling range is small
It is as the second cut, first cut-point more than the cut of the second cut-point in the cut and/or boiling range of the first cut-point
Arbitrary temp in the range of 390-410 DEG C, second cut-point are the arbitrary temp in the range of 440-460 DEG C；(2) will contain
First feedstock oil of first cut carries out first with first cracking catalyst in the first reaction zone of riser reactor
Contact, obtains the first material containing the first primary cracking product；(3) by the second feedstock oil containing second cut and
Two Cracking catalyst carry out the second contact in the second reaction zone of the riser reactor, obtain primary cracking containing second
The second material of product；(4) by the first material and the second material the riser reactor the 3rd reaction zone
The 3rd contact is carried out, continues catalytic cracking reaction subsequently into stripping sedimentation device and carries out gas solid separation, obtain oil gas
Product and reclaimable catalyst；(5) reclaimable catalyst is transported into progress coke burning regeneration in fluid bed regenerator to be regenerated
Catalyst, and using at least part of regenerated catalyst as the first cracking catalyst and second Cracking catalyst
It is respectively delivered in first reaction zone and the second reaction zone；Wherein, first reaction zone and second reaction
Area is independently juxtaposed on the lower section of the 3rd reaction zone and met in the 3rd reaction zone.
The method according to the invention, wherein it is preferred to, first cut-point is any temperature in the range of 395-405 DEG C
Degree, second cut-point is the arbitrary temp in the range of 445-455 DEG C, it is highly preferred that first cut-point is 398-402
Arbitrary temp in the range of DEG C, second cut-point are the arbitrary temp in the range of 448-452 DEG C, particularly preferably, it is described
First cut-point is 400 DEG C, and second cut-point is 450 DEG C；Under the preferable case, catalytic cracking can be further improved
Efficiency.
The method according to the invention, wherein, the catalyst in the 3rd reaction may come from first reaction zone
With the second reaction zone, it is preferable that this method also includes：The 3rd cracking catalysis are added into the 3rd reaction zone
Agent, the 3rd Cracking catalyst come from Regenerated cracking catalyst.
Wherein it is preferred to the weight for the 3rd Cracking catalyst added causes the catalysis in the 3rd reaction zone
The gross weight of agent and the ratio of first feedstock oil and the gross weight of the second feedstock oil are (5-9)：1.
Wherein, the mode that first reaction zone and the second reaction zone are formed in the riser reactor can be with
With a variety of changes, for example, first reaction zone and the second reaction zone in the riser reactor bottom by setting
The mode for putting the longitudinal baffle in pipe, sleeve pipe or branched pipe is formed.
The method according to the invention, wherein, the condition of the first contact conducted in first reaction zone can be normal
The condition of riser reactor used in the catalytic cracking of rule, for example, conducted in first reaction zone first contact
Condition includes：Temperature can be 375-515 DEG C, and preferably 400-500 DEG C, it can be 3-6, preferably 4-5 that oil ratio, which is, react
Time can be 0.6-2.4s, preferably 1-2s；The outlet pressure of first reaction zone can be 0.1-0.4MPa, preferably 0.2-
0.3MPa。
The method according to the invention, wherein, the condition of the second contact conducted in the second reaction zone can be normal
The condition of riser reactor used in the catalytic cracking of rule, for example, conducted in the second reaction zone second contact
Condition can include：Temperature can be 480-550 DEG C, and preferably 490-530 DEG C, oil ratio can be 3-8, preferably 5-7, instead
Can be 0.6-3s, preferably 1-2s between seasonable；The outlet pressure of second reaction zone can be 0.1-0.4MPa, preferably 0.2-
0.3MPa。
The method according to the invention, wherein, the condition of the 3rd contact conducted in the 3rd reaction zone can be normal
The condition of riser reactor used in the catalytic cracking of rule, for example, conducted in the 3rd reaction zone the 3rd contact
Condition can include：Temperature is 450-550 DEG C, and preferably 495-525 DEG C, the reaction time can be 0.6-3s, preferably 1-2s.
The method according to the invention, wherein, the weight ratio of first feedstock oil and second feedstock oil can compared with
Change in a wide range of, for example, the weight ratio of first feedstock oil and second feedstock oil can be (0.01-0.4)：1, it is excellent
Elect as (0.05-0.3)：1.
The method according to the invention, wherein, first feedstock oil can also contain other catalytically cracked stock, example
Such as, first feedstock oil is also higher than 0.2 weight % other catalytically cracked materials containing nitrogen content.Preferably, the nitrogen contains
Other catalytically cracked materials of the amount higher than 0.2 weight % are shale oil；In first feedstock oil, first cut with it is described
The weight ratio of other catalytically cracked materials of the nitrogen content higher than 0.2 weight % can be (0.01-100):1, it is preferably (0.1-
10):1。
The method according to the invention, wherein, second feedstock oil can also contain other catalytically cracked materials, for example,
Second feedstock oil is also less than 0.2 weight % other catalytically cracked materials containing nitrogen content；Second cut with it is described
The weight ratio of other catalytically cracked materials can be (0.01-100)：1, be preferably (0.05-0.8)：1；More preferably (0.1-
0.4)：1.Wherein, other catalytically cracked materials can include but is not limited to straight-run gas oil, solvent-deasphalted oils and decompression slag
At least one of oil.
The method according to the invention, wherein, first cracking catalyst and second Cracking catalyst can come from fresh
Cracking catalyst, can be from Regenerated cracking catalyst；For being carried out continuously for reaction, regenerated cracking catalyst is preferred from
Agent.
The method according to the invention, wherein, in order to save regenerated catalyst, it is preferable that by a part of catalysis to be generated
Agent and a part of regenerated catalyst are together as the first cracking catalyst transport into first reaction zone.
The method according to the invention, wherein, by boiling range be less than the first cut-point cut can separately as the second cut,
Boiling range can also can also be less than evaporating for the first cut-point by the cut that boiling range is more than the second cut-point separately as the second cut
Divide after being more than the cut merging of the second cut-point with boiling range and be used as the second cut；Preferably, boiling range is less than the first cut-point
The cut that cut and boiling range are more than the second cut-point is incorporated as the second cut.
The method according to the invention, wherein, the structure and the method for operation of the stripping sedimentation device can be catalytic cracking
Conventional use of structure and the method for operation in field, the technical staff in catalytic cracking field is to known to this, and the present invention is herein no longer
Repeat.Wherein, the device for carrying out gas solid separation can be cyclone separator, and the cyclone separator can be including one cyclonic point
From device and secondary cyclone.
The method according to the invention, wherein, the reclaimable catalyst, which can import, carries out coke burning regeneration in regenerator.It is described
The structure and the method for operation of regenerator can be conventional use of structure and the method for operation in catalytic cracking field, and catalytic cracking is led
The technical staff in domain is to known to this, the present invention will not be repeated here.
Using the device with reference to shown in figure 1, particularly preferred embodiment of the invention includes：(1) wax tailings are led
Enter and be fractionated in fractionator 1, using cut of the boiling range more than the first cut-point and below the second cut-point as the first cut,
Boiling range is less than the cut of the first cut-point and/or boiling range is more than the second cut-point cut as the second cut, described first point
Cutpoint is the arbitrary temp in the range of 390-410 DEG C, and second cut-point is the arbitrary temp in the range of 440-460 DEG C；The
One cut is discharged through double distilled subtube 11, and the second cut is discharged through light fraction pipeline 12；(2) using first cut as first
Feedstock oil；Using the regenerated catalyst that regenerator 4 is discharged as first cracking catalyst, by first feedstock oil and described first
Cracking catalyst carries out the first contact in the first reaction zone 21 of riser reactor 2, obtains containing the first primary cracking production
The first material of thing；Condition in first reaction zone 21 includes：Temperature can be 375-515 DEG C, preferably 400-500 DEG C, agent
Oil is than for that can be 3-6, preferably 4-5, the reaction time can be 0.6-2.4s, preferably 1-2s；The outlet of first reaction zone
Pressure can be 0.1-0.4MPa, preferably 0.2-0.3MPa；(3) second cut is mixed as second with straight-run gas oil
Feedstock oil, using the regenerated catalyst that regenerator 4 is discharged as the second Cracking catalyst, by second feedstock oil and the second cracking
Catalyst carries out the second contact in the second reaction zone 22 of the riser reactor 2, obtains containing the second primary cracking production
The second material of thing；The condition of the second contact conducted in second reaction zone includes：Temperature can be 480-550 DEG C, preferably
For 490-530 DEG C, oil ratio can be 3-8, preferably 5-7, and the reaction time can be 0.6-3.0s, preferably 1-2s；Second
The outlet pressure of reaction zone can be 0.1-0.4MPa, preferably 0.2-0.3MPa：(4) by the first material and described second
Material carries out the 3rd contact in the 3rd reaction zone 23 of the riser reactor 2, and the material that then the 3rd contact obtains enters
Stripping sedimentation device 4 continues catalytic cracking reaction and carries out gas solid separation, obtains oil gas product and reclaimable catalyst；It will treat
Raw catalyst is sent into regenerator 4 and carries out coke burning regeneration.Wherein, the weight of the first feedstock oil and the second feedstock oil ratio is (0.05-
0.4)：1；The condition of 3rd contact includes：Temperature is 450-550 DEG C, and preferably 400-500 DEG C, the reaction time can be 0.6-
3s, preferably 1-2s.Wherein, the 3rd Cracking catalyst is added into the 3rd reaction zone；The 3rd cracking added is urged
The weight of agent causes the gross weight of the catalyst in the 3rd reaction zone and first feedstock oil and the second feedstock oil
The ratio of gross weight is (5-9)：1.
The present invention is further described by the following examples.
In following examples, the straight-run gas oil and wax tailings property used detected according to national standard after numerical value such as table
Shown in 1.The Cracking catalyst property used includes：On the basis of total catalyst weight, used catalyst contains 40 weight %'s
ZRP-1 zeolites, 20 weight % DASY zeolites, 20 weight % kaolin and 20 weight % alumina binder；Wherein
ZRP-1 zeolites, DASY zeolites are sinopec catalyst asphalt in Shenli Refinery product；The micro-activity of the catalyst is 75, surface
Product is 144m2/ g, pore volume 0.19cm3/ g, density 0.98g/cm3, Ni contents are 2155 μ g/g, and V content is 1419 μ g/
g：Na contents are 2487 μ g/g, and size distribution is 0-40 μm and accounts for 12.0 weight %, and 40-80 μm accounts for 45.8 weight %, more than 80 μm
For 42.2 weight %.
Table 1
Embodiment 1
Wax tailings shown in table 1 are imported in fractionator 1 and are fractionated, by boiling range more than the first cut-point and second
As the first cut, the cut that boiling range is less than to the first cut-point evaporates cut below cut-point with boiling range more than the second cut-point
Divide and be incorporated as the second cut, first cut-point is 400 DEG C, and second cut-point is 450 DEG C；First cut is through double distilled
Subtube 11 is discharged, and the second cut is discharged through light fraction pipeline 12；The first cut and the second cut of wax tailings shown in table 1
Weight ratio be 0.4:1.
Using first cut as the first feedstock oil；The regenerated catalyst that regenerator 4 is discharged is urged as first cracking
Agent, first feedstock oil is carried out in the first reaction zone 21 of riser reactor 2 with the first cracking catalyst
First contact, obtains the first material containing the first primary cracking product；Condition in first reaction zone 21 includes：Temperature is
470 DEG C, oil ratio 4, reaction time 1.3s；The outlet pressure of first reaction zone is 0.2MPa.
Second cut mixes to (ratio that the second cut and straight-run gas oil mix is classified as with the straight-run gas oil in table 1
0.3：1, the weight ratio of the first feedstock oil and the second feedstock oil is about 0.1：1 so that the weight of wax tailings and straight-run gas oil ratio
For 3:7) the second feedstock oil is used as, it is former by described second using the regenerated catalyst that regenerator 4 is discharged as the second Cracking catalyst
Material oil carries out second in the second reaction zone 22 of the riser reactor 2 with the second Cracking catalyst and contacted, and is contained
The second material of second primary cracking product；The condition of the second contact conducted in second reaction zone includes：Temperature is 500
DEG C, oil ratio 7, reaction time 2s；The outlet pressure of second reaction zone is 0.2MPa.
The first material and the second material are carried out the 3rd in the 3rd reaction zone 23 of the riser reactor 2
Contact, then the 3rd obtained material of contact enters stripping sedimentation device 4 and continues catalytic cracking reaction promoting the circulation of qi of going forward side by side divides admittedly
From obtaining oil gas product and reclaimable catalyst；Reclaimable catalyst feeding regenerator 4 is subjected to coke burning regeneration.Article of 3rd contact
Part includes：Temperature is 500 DEG C, and oil ratio is that 9 (oil ratio is the gross weight and described first of the catalyst in the 3rd reaction zone
The ratio of the gross weight of feedstock oil and the second feedstock oil), reaction time 1s.
Embodiment 2
Using embodiment 1 method carry out catalytic cracking, unlike, first cut-point be 395 DEG C, described second
Cut-point is 445 DEG C.
Embodiment 3
Using embodiment 1 method carry out catalytic cracking, unlike, first cut-point be 405 DEG C, described second
Cut-point is 455 DEG C.
Embodiment 4
Using embodiment 1 method carry out catalytic cracking, unlike, first cut-point be 390 DEG C, described second
Cut-point is 440 DEG C.
Embodiment 5
Using embodiment 1 method carry out catalytic cracking, unlike, first cut-point be 410 DEG C, described second
Cut-point is 460 DEG C.
Embodiment 6
Catalytic cracking is carried out using the method for embodiment 1, unlike, the ratio of the second cut and straight-run gas oil mixing is
0.18：1, the weight ratio of the first feedstock oil and the second feedstock oil is about 0.06：1 so that the weight of wax tailings and straight-run gas oil
Than for 2:8.
Comparative example 1
Using the wax tailings in table 1 as the first feedstock oil；The regenerated catalyst that regenerator 4 is discharged is as first cracking
Catalyst, first feedstock oil is entered in the first reaction zone 21 of riser reactor 2 with the first cracking catalyst
Row first contacts, and obtains the first material containing the first primary cracking product；Condition in first reaction zone 21 includes：Temperature is
470 DEG C, oil ratio 4, reaction time 1.3s；The outlet pressure of first reaction zone is 0.2MPa.
Using the straight-run gas oil in table 1 as the second feedstock oil, using the regenerated catalyst that regenerator 4 is discharged as the second cracking
Catalyst, second feedstock oil is entered in the second reaction zone 22 of the riser reactor 2 with the second Cracking catalyst
Row second contacts, and obtains the second material containing the second primary cracking product；Conducted in second reaction zone second contact
Condition includes：Temperature is 500 DEG C, oil ratio 7, reaction time 2s；The outlet pressure of second reaction zone is 0.2MPa.
The first material and the second material are carried out the 3rd in the 3rd reaction zone 23 of the riser reactor 2
Contact, then the 3rd obtained material of contact enters stripping sedimentation device 4 and continues catalytic cracking reaction promoting the circulation of qi of going forward side by side divides admittedly
From obtaining oil gas product and reclaimable catalyst；Reclaimable catalyst feeding regenerator 4 is subjected to coke burning regeneration.Wherein, the first raw material
The weight ratio of oil and the second feedstock oil is 3：7；The condition of 3rd contact includes：Temperature is 500 DEG C, and oil ratio is 9 (oil ratios
It is the gross weight and first feedstock oil and the ratio of the gross weight of the second feedstock oil of the catalyst in the 3rd reaction zone), instead
It is 1s between seasonable.
Comparative example 2
Catalytic cracking is carried out using the method for comparative example 1, unlike, the weight ratio of the first feedstock oil and the second feedstock oil
For 2:8.
Testing example 1
According to the method for national oil product professional standard, the catalytic cracking that embodiment 1-2 and comparative example 1-2 is obtained is determined
Product distribution in product (including drippolene, pyrolysis gas oil, slurry oil, liquefied gas, oil refinery dry gas and coke)；As a result such as table 2
It is shown.
Table 2
Visible according to the data of table 1, wax tailings are fractionated by the present invention, can mitigate wax tailings to catalyst
Toxic action, conversion ratio is enabled to rise, product distribution more preferably with product quality raising, is being urged so as to improve wax tailings
Change in cracking and mix refining ratio.Also, in the case where the cut-point of limited fractionation is 395-405 DEG C and 445-455 DEG C, Neng Gouqu
Obtain more preferable effect.The reason for its is possible is：It is more than the first cut-point and rich less than the wax tailings cut of the second cut-point
Containing condensed-nuclei aromatics and nitrogen, there is toxic action to Cracking catalyst, if be fractionated and with partial catalyst it is prior in
With, it becomes possible to toxic action is limited in partial catalyst, and enables remaining catalyst to play dynamical catalysis
Effect, which thereby enhance the efficiency of catalytic cracking.
The preferred embodiment of the present invention is described in detail above in association with accompanying drawing, still, the present invention is not limited to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the present invention, a variety of letters can be carried out to technical scheme
Monotropic type, these 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 (14)
- A kind of 1. method of catalytic cracking wax tailings, it is characterised in that：This method comprises the following steps：(1) wax tailings are fractionated, using cut of the boiling range more than the first cut-point and below the second cut-point as One cut, boiling range is less than the cut of the first cut-point and/or boiling range is more than the cut of the second cut-point as the second cut, institute The first cut-point is stated as the arbitrary temp in the range of 390-410 DEG C, second cut-point is any in the range of 440-460 DEG C Temperature；(2) the first feedstock oil containing first cut and first cracking catalyst are reacted the first of riser reactor The first contact is carried out in area, obtains the first material containing the first primary cracking product；(3) by the second feedstock oil containing second cut and the second Cracking catalyst the second of the riser reactor The second contact is carried out in reaction zone, obtains the second material containing the second primary cracking product；(4) first material and the second material are carried out into the 3rd in the 3rd reaction zone of the riser reactor to connect Touch, subsequently into stripping sedimentation device and carry out gas solid separation, obtain oil gas product and reclaimable catalyst；(5) reclaimable catalyst is transported to progress coke burning regeneration in fluid bed regenerator and obtains regenerated catalyst, and it is near The least a portion of regenerated catalyst is respectively delivered to institute as the first cracking catalyst and second Cracking catalyst State in the first reaction zone and the second reaction zone；Wherein, first reaction zone and the second reaction zone are independently juxtaposed on the lower section of the 3rd reaction zone simultaneously And meet in the 3rd reaction zone.
- 2. according to the method for claim 1, it is characterised in that：First cut-point is appointing in the range of 395-405 DEG C Meaning temperature, second cut-point are the arbitrary temp in the range of 445-455 DEG C.
- 3. according to the method for claim 1, it is characterised in that：This method also includes：Added into the 3rd reaction zone 3rd Cracking catalyst, the 3rd Cracking catalyst come from Regenerated cracking catalyst.
- 4. according to the method for claim 3, it is characterised in that：The weight for the 3rd Cracking catalyst added causes institute The gross weight and the ratio of first feedstock oil and the gross weight of the second feedstock oil for stating the catalyst in the 3rd reaction zone are (5- 9)：1.
- 5. according to the method for claim 1, it is characterised in that：First reaction zone and the second reaction zone by The mode of longitudinal baffle, sleeve pipe or branched pipe in the riser reactor bottom setting pipe is formed.
- 6. according to the method described in any one in claim 1-5, it is characterised in that：Conducted in first reaction zone The condition of first contact includes：Temperature is 400-500 DEG C, oil ratio 4-5, reaction time 1-2s；First reaction zone goes out Mouth pressure is 0.2-0.3MPa.
- 7. according to the method described in any one in claim 1-5, it is characterised in that：Conducted in the second reaction zone The condition of second contact includes：Temperature is 490-530 DEG C, oil ratio 5-7, reaction time 1-2s；Second reaction zone goes out Mouth pressure is 0.2-0.3MPa.
- 8. according to the method described in any one in claim 1-5, it is characterised in that：Conducted in 3rd reaction zone The condition of 3rd contact includes：Temperature is 495-525 DEG C, reaction time 1-2s.
- 9. according to the method described in any one in claim 1-5, it is characterised in that：First feedstock oil and described second The weight ratio of feedstock oil is (0.01-0.4)：1.
- 10. according to the method described in any one in claim 1-5, it is characterised in that：First feedstock oil also contains nitrogen Content is higher than 0.2 weight % other catalytically cracked materials.
- 11. according to the method for claim 10, it is characterised in that：The nitrogen content is higher than 0.2 weight % other catalysis Cracked stock is shale oil；In first feedstock oil, first cut is other higher than 0.2 weight % with the nitrogen content The weight ratio of catalytically cracked material is (0.1-10):1.
- 12. according to the method described in any one in claim 1-5, it is characterised in that：Second feedstock oil also contains nitrogen Content is less than 0.2 weight % other catalytically cracked materials；The weight of second cut and other catalytically cracked materials Than for (0.01-100)：1.
- 13. according to the method for claim 12, it is characterised in that：The nitrogen content is less than 0.2 weight % other catalysis Cracked stock includes at least one of straight-run gas oil, solvent-deasphalted oils and decompression residuum.
- 14. according to the method described in any one in claim 1-5, it is characterised in that：By a part of reclaimable catalyst With a part of regenerated catalyst together as the first cracking catalyst transport into first reaction zone.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1279270A (en) * | 1999-06-23 | 2001-01-10 | 中国石油化工集团公司 | Catalytic transform process for preparing diesel oil and liquified gas with higher outputs |
| CN1690174A (en) * | 2004-04-29 | 2005-11-02 | 中国石油化工股份有限公司 | Catalytic conversion process for petroleum hydrocarbons |
| CN102071054A (en) * | 2009-10-30 | 2011-05-25 | 中国石油化工股份有限公司 | Catalytic cracking method |
| CN103540359A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Inferior heavy oil catalytic conversion process for improving yield of low-carbon olefin and gasoline |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1279270A (en) * | 1999-06-23 | 2001-01-10 | 中国石油化工集团公司 | Catalytic transform process for preparing diesel oil and liquified gas with higher outputs |
| CN1690174A (en) * | 2004-04-29 | 2005-11-02 | 中国石油化工股份有限公司 | Catalytic conversion process for petroleum hydrocarbons |
| CN102071054A (en) * | 2009-10-30 | 2011-05-25 | 中国石油化工股份有限公司 | Catalytic cracking method |
| CN103540359A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Inferior heavy oil catalytic conversion process for improving yield of low-carbon olefin and gasoline |
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