CN109423330A - A kind of processing method of catalytic cracked oil pulp - Google Patents
A kind of processing method of catalytic cracked oil pulp Download PDFInfo
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- CN109423330A CN109423330A CN201710766275.XA CN201710766275A CN109423330A CN 109423330 A CN109423330 A CN 109423330A CN 201710766275 A CN201710766275 A CN 201710766275A CN 109423330 A CN109423330 A CN 109423330A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
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Abstract
The present invention relates to a kind of processing method of catalytic cracked oil pulp, this method comprises: a, mixing catalytic cracked oil pulp with catalytic cracking diesel oil, mixed fraction oil is obtained；Wherein, the mixed weight of the catalytic cracked oil pulp and catalytic cracking diesel oil ratio is 1:(0.2-10)；80 DEG C of viscosity of the mixed fraction oil are not higher than 60 millimeters2/ the second；B, gained mixed fraction oil is subjected to separating treatment using catalyst fines separation equipment, obtains clarified separation oil and greasy filth.The processing method provided by the present invention can reduce the viscosity of catalytic cracked oil pulp, improves the separative efficiency of solid particle in slurry oil, ensures the long-term operation of separation equipment.
Description
Technical field
The present invention relates to a kind of processing methods of catalytic cracked oil pulp.
Background technique
The heavy distillat extracted out from catalytic cracking fractionating tower tower bottom is known as slurry oil, and it is thin to have a certain amount of catalyst in slurry oil
Powder, in general, slurry oil are that boiling range is greater than 350 DEG C of (initial boiling point) fractions, have high arene content, and gum level is relatively high,
Sulfur content and the relatively high feature of nitrogen content, are the components that catalytic cracking unit is difficult to convert, although hydrogen content is relatively low,
Still it can achieve 7%~9.5%.Due to containing catalyst fines in catalytic cracked oil pulp, therefore, it is difficult to directly utilize, need
Carrying out catalyst fines removing processing could further utilize.
Chinese patent CN01113134.9 discloses the method for washing sedimentation separation catalyst powder in catalytic cracking oil slurry,
Be into catalytic cracked oil pulp be added 5~10% water and 100~1000PPM surfactant-like compounds make sedimentation help
Agent, and being sufficiently mixed evenly, slurry oil temperature is maintained at 60~90 DEG C in settling tank, and natural subsidence 12~60 hours, then periodically
Discharge falls to the catalyst fines of pot bottom and the mixture of water.
Chinese patent CN201210123869.6 discloses a kind of method for removing catalyst in catalytic cracked oil pulp, the party
Method first settles catalytic cracked oil pulp in settling tank, and the catalyst in slurry oil enters after settling tank sedimentation from tank bottom hole
Send pipeline outside, be pushed into receiving tank using the spiral propeller sent outside in pipeline, then using pump by receiving tank catalyst and
The pureed mixture of oil is squeezed into gravity tank, the catalyst in gravity tank is discharged into squeezer squeezing, by the oil pressure in catalyst
It squeezes out and, catalyst is stayed in squeezer and is discharged, thus can be continuously by the catalyst and slurry oil in catalytic cracked oil pulp
Separation, while the oil content in catalyst can be reduced.
Chinese patent CN201310456765.1 discloses cleaning equipment and the purification side of a kind of purifying and catalytic cracking slurry oil
Catalytic cracked oil pulp is entered settling tank by method, this method by the road, and level-one electrostatic separator is sent into overflow by the road, and underflow is through pipe
Routing is pumped to centrifuge, and settling tank bottom solid phase is discharged through tank bottom sewage pipe, and solid phase is sent by the road to riser, centrifugation after centrifugation
Liquid phase is pumped into level-one electrostatic separator by the road afterwards, and the slurry oil product after electrostatic depuration is sent by pipeline to products pot, level-one
After electrostatic separator filling adsorption saturation, catalytic cracked oil pulp to be clean is introduced from level-one electrostatic separator bottom pair by pipeline
It is backwashed, and for backwash liquid by returning to settling tank by the road at the top of separator, purified slurry oil product is discharged into production by pipeline
Product tank.
Chinese patent CN201310334457.1 discloses a kind of coking, catalysis drying gas automatic back blow sweeps filter device.It should
Patent is provided with coking, catalysis drying gas automatic back blow sweeps filter device, including filter element and automatic back blow sweep unit, described
Filter element includes filter housings, filter element and tube sheet, and wherein tube sheet is set to the top of filter housings, under tube sheet
Side is fixed with filter element, and the side wall of tube sheet is equipped with air inlet；It includes that automatic back blow sweeps control that the automatic back blow, which sweeps unit,
Device and surge tank processed, the inlet end that wherein automatic back blow sweeps control device are connected with surge tank, and automatic back blow sweeps control device
Outlet side be connected with the air inlet on tube sheet side wall.
Chinese patent CN201110032024.1 discloses a kind of catalytic cracking unit externally extracting oil filtering of secondary filtration
Device, the device include that concatenated first order filtering is filtered with the second level, which is filtered into one or two filters, should
The second level is filtered at least two filters；The filter core that uses of filter of first order filtering for wedge wire winded filtering core,
The wedge wire winded filtering core is made of the wire winding that section is wedge shape, each circle wire and adjacent wire it
Between gap be fixed, and be continuous infundibulate；The filter of second level filtering uses metal powder sintered filter element.
Chinese patent CN201210274634.7 discloses a kind of catalytic filter system, which includes: filtering container,
The filtering container has fluid inlet and fluid outlet；The inside of the filtering container is arranged in partition wall, the partition wall
In；And multiple filter candles；The inside is divided into raw gas room and purification gas room by the partition wall；The partition wall packet
Include the multiple openings for being designed to hermetically accommodate the multiple filter candle；The fluid inlet be arranged to on the multiple filter candle
The raw gas room of trip is in fluid communication；The fluid outlet is arranged to the purified gas with the multiple filter candle downstream
Body room is in fluid communication；And the filter system includes the first catalytic media being accommodated in the purification gas room, institute
Purification gas room is stated in the filter candle downstream and the fluid outlet upstream.
Chinese patent CN200510122904.2 discloses a kind of for petroleum catalytic cracking experimental provision reaction system mistake
Filter, comprising: filter supporting body, filter body and connector, wherein filter body uses aperture for 50 nanometer -0.2
The ceramic membrane of micron, filter body are fairshaped cylindrical body, and 4~5 millimeters of wall thickness, filter body lower section is equipped with support
There are connector in body, top.Can pass through to make filter bottom and surrounding oil gas, the side of supporter open 4 slots,
Circular hole is opened in bottom, and supporter is connected with reactor outlet pipe using steel connector.Use apparatus of the present invention rear catalyst
Entrainment phenomenon greatly reduces, and loses solid particle substantially in reactor outlet pipe, product receiving flask, ensure that catalytic cracking is tested
Work is gone on smoothly.
Chinese patent CN201110329376.3 discloses a kind of filter method of solid-liquid slurry, this method comprises: by institute
It states solid-liquid slurry injection purpose ceramic-film filter to be filtered, is purified material and concentration material, consolidating for the concentration material contains
Amount is higher than the solid content of the solid-liquid slurry, and the solid content of the purification material is lower than the solid content of the solid-liquid slurry；Wherein,
Before the solid-liquid slurry is injected the purpose ceramic-film filter, by the filter core of the purpose ceramic-film filter with 5-150 DEG C/it is small
When heating rate heating so that the temperature difference of the temperature of the filter core and the solid-liquid slurry is not more than 50 DEG C.
It is above-mentioned in the prior art, sedimentation has the characteristics that equipment is simple, operating cost is low and easy to operate, but due to oil
Catalyst fines are smaller in slurry, and the inhibition by resin and asphalt in slurry oil, and catalyst particle size is less than 20 μm
The more difficult removing of catalyst fines.The method of being separated by filtration can be very good the catalyst fines in removing slurry oil, and key technology is choosing
Select suitable filtering material and effective back-flushing method.Currently, catalytic cracking unit, in order to preferably " eat dry squeeze only "
Raw material, slurry oil density general control is in 1000kg/m3More than, viscosity is higher, and existing separation equipment is difficult to ensure long-term operation.
Summary of the invention
The object of the present invention is to provide a kind of processing method of catalytic cracked oil pulp, the processing method provided by the present invention can
The viscosity of catalytic cracked oil pulp is reduced, the separative efficiency of solid particle in slurry oil is improved, ensures the long-term operation of separation equipment.
To achieve the goals above, the present invention provides a kind of processing method of catalytic cracked oil pulp, this method comprises: a, general
Catalytic cracked oil pulp is mixed with catalytic cracking diesel oil, obtains mixed fraction oil；Wherein, the catalytic cracked oil pulp and catalytic cracking
The mixed weight ratio of diesel oil is 1:(0.2-10)；80 DEG C of viscosity of the mixed fraction oil are not higher than 60 millimeters2/ the second；B, by institute
It obtains mixed fraction oil and separating treatment is carried out using catalyst fines separation equipment, obtain clarified separation oil and greasy filth.
Optionally, the method also includes: gained greasy filth will be sent into catalyst cracker and urge with regenerated in step b
Catalytic cracking reaction is carried out with catalytically cracked stock together after fluidized cracking catalysts mixing；And/or gained greasy filth feeding is urged
Change cracking regenerator to be regenerated.
Optionally, the method also includes: by step b gained greasy filth using catalytic cracking diesel oil carry out carrying out washing treatment,
Obtain clarification washing oil and catalyst fines, wherein the washing weight ratio of the greasy filth and catalytic cracking diesel oil is 1:(0.1-
6)。
Optionally, the method also includes: the catalyst fines are dried.
Optionally, the method also includes: by gained at least partly clarify washing oil as catalytic cracking diesel oil carry out institute
It states carrying out washing treatment and/or is mixed in step a with the catalytic cracked oil pulp.
Optionally, gained clarified separation oil in step b is subjected to hydrofinishing processing, obtains hydrotreated product.
Optionally, it is being catalyzed after gained hydrotreated product being mixed with catalytically cracked stock with catalytic cracking catalyst
It is contacted in cracker and carries out catalytic cracking reaction.
Optionally, using gained hydrotreated product as catalytically cracked material and catalytic cracking catalyst in Catalytic Cracking Unit of Measure
It answers to contact in device and individually carries out catalytic cracking reaction.
Optionally, it is 250-500 DEG C that the condition of the hydrofinishing processing, which includes: temperature, and hydrogen partial pressure is 2-30 megapascal, body
Product air speed is 0.1-30 hours-1。
Optionally, the catalytically cracked stock is selected from reduced crude, decompression residuum, coker gas oil, deasphalted oil
At least one of with hydrotreating residual oil；The catalytic cracking catalyst includes molecular sieve, carrier and binder；The catalysis
The condition of cracking reaction includes 400 DEG C -750 DEG C of temperature, -1.0 megapascal of 0.10 megapascal of reaction pressure, the weight of catalyst and raw material
Than 1-100, the weight ratio 0.02-1.0 of water vapour and raw material；The catalyst cracker is riser reactor and/or stream
Fluidized bed reactor.
Optionally, catalyst fines separation equipment described in step b be selected from sedimentation separation equipment, filtering separation device,
At least one of electrostatic separation equipment and centrifugal separation equipment.
Optionally, it is 10-360 DEG C that the natural subsidence condition, which includes: temperature, and the time is 0.5-240 hours.
Optionally, the filtration treatment preferred filters, filter are metal sintering porous material and/or ceramic porous material
Material, 1.2 micron particles filtering accuracies of filter are 99.9%.Optional catalyst fines separation process is first to carry out nature to sink
Then drop is filtered device filtering.
Optionally, the method also includes: by step b gained clarified separation oil cut in fractionating column, obtain
Diesel oil distillate and slurry oil fraction；Wherein, the cut point of the cutting is 340-380 DEG C.
Optionally, the boiling range initial boiling point of the catalytic cracked oil pulp is greater than 290 DEG C.
Optionally, the catalytic cracking diesel oil boiling range range is 180-380 DEG C.
Optionally, 80 DEG C of viscosity of the mixed fraction oil are not higher than 50 millimeters2/ the second.
Compared with the conventional method, major advantage is as follows for method of the invention:
1, it by using the heavy colloid wrapped up on the outside of catalyst fines in catalytic cracking diesel oil dissolution slurry oil, reduced
The viscosity of oil strain slurry, can efficiently separate the catalyst fines in slurry oil, and ensure the long-term operation of separation equipment；
2, filtered low viscosity clarified separation oil carries out catalytic cracking after can carrying out hydrofinishing processing, realizes oil product
Efficient utilization.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
The drawings are intended to provide a further understanding of the invention, and constitutes part of specification, 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 a kind of flow diagram of specific embodiment of the method for the present invention.
Fig. 2 is the flow diagram of the method for the present invention another kind specific embodiment.
Fig. 3 is the slurry oil filtration time of the embodiment of the present invention 1 and comparative example 1 and the variation diagram of flow.
Fig. 4 is feedstock oil 200 DEG C of viscosity (abscissa, the unit: millimeter that the present invention summarizes2/ the second) and nozzle atomization droplet
The linear relationship chart of diameter (ordinate, unit: micron).
Specific embodiment
Below in conjunction with attached drawing, detailed description of the preferred embodiments.It should be understood that this place is retouched
The specific embodiment stated is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
It should be noted that if diesel oil and light cycle oil are a kind of fraction in the present invention without specified otherwise.
As shown in Figure 1, the present invention provides a kind of processing method of catalytic cracked oil pulp, this method comprises: a, catalysis split
Carburetion slurry is mixed with catalytic cracking diesel oil, obtains mixed fraction oil；Wherein, the catalytic cracked oil pulp and catalytic cracking diesel oil
Mixed weight ratio is 1:(0.2-10)；80 DEG C of viscosity of the mixed fraction oil are not higher than 60 millimeters2/ the second；B, gained is mixed
Distillate carries out separating treatment using catalyst fines separation equipment, obtains clarified separation oil and greasy filth.
Catalyst under catalytic cracking unit normal operating conditions, containing -15 grams per liter of 1 grams per liter in catalytic cracked oil pulp
Fine powder, the present inventor research in have been surprisingly found that, the catalyst fines in slurry oil are by the weight with a thickness of 0.1 micron -8 microns
Matter colloid is wrapped up, and the catalyst fines wrapped up by heavy colloid have very strong viscosity, to cause catalyst in slurry oil thin
Powder is difficult to separate and be difficult to ensure separation equipment long-term operation.
Slurry oil processing method of the invention is mixed using catalytic cracking diesel oil with catalytic cracked oil pulp, with catalytic dissolution cracking
The heavy colloid on catalyst fines surface, makes mixed fraction oil be more easier to filter in slurry oil, effectively prevent the stifled of separation equipment
Plug, and improve the operation cycle of the rate of filtration and separation equipment.
According to the present invention, catalyst fines and part heavy colloid are contained in the separating obtained greasy filth of step b, is formed similar
In the higher carbon deposited catalyst of hydrogen content, in order to efficiently use the part greasy filth, the method can also include: will be in step b
Gained greasy filth be sent into catalyst cracker in mixed with regenerated catalytic cracking catalyst after together with catalytically cracked stock
Carry out catalytic cracking reaction；And/or gained greasy filth feeding catalytic cracking regenerator is regenerated.Greasy filth after separation is sent into
Catalyst activity can be reduced in catalyst cracker, prevents heavy oil by overcracking, and reduces green coke.By the oil after separation
Mud, which is sent into catalytic cracking regenerator, can be improved regeneration temperature, to save other fuel.
According to the present invention, since the heavy colloid in greasy filth also has use value, in order to utilize the part heavy glue
Matter, the method can also include: that gained greasy filth in step b is carried out carrying out washing treatment using catalytic cracking diesel oil, be clarified
Washing oil and catalyst fines, wherein the washing weight ratio of the greasy filth and catalytic cracking diesel oil is 1:(0.1-6).The step
Hydro carbons most of in greasy filth can be washed, be increased operation rate, so that catalyst fines be made to be contained only substantially as solvent
Catalytic cracking diesel oil, in order to recycle the part diesel oil, the method can also include: that the catalyst fines are dried
Processing, the temperature of the drying process can also be gradually heated on the boiling range range of diesel oil from the initial boiling point of diesel oil
The end point of distillation of diesel oil, to effectively prevent diesel oil coking.
Since heavy colloid is less in greasy filth, the clarification washing oil after using can continue reuse, for example, institute
The method of stating can also include: gained is at least partly clarified washing oil as catalytic cracking diesel oil carry out the carrying out washing treatment and/
Or it is mixed in step a with the catalytic cracked oil pulp.Clarification washing oil is continued into reuse, catalytic cracking bavin can be improved
The utilization efficiency of oil.
The present inventor is by diligent the study found that raw material oil viscosity and nozzle atomization fogdrop diameter have very well
Linear relationship.As shown in figure 4, Y (fogdrop diameter)=AX (raw material oil viscosity)+B, wherein slope A and constant B are by burner design
It is determined with pressure drop, and catalysis can be substantially reduced after highly viscous catalytically cracked stock is mixed with the distillate of low viscosity and split
Change raw material oil viscosity, improve nozzle atomization effect, reduce coke and dry gas yied, to change tradition mainly by raising feedstock oil
The method that temperature reduces viscosity overcomes resin and asphalt in the excessively high caused feedstock oil of fuel oil preheating temperature that coking is precipitated
The shortcomings that.Based on above-mentioned discovery, the method for the present invention can also include: that gained clarified separation oil in step b is carried out hydrofinishing
Processing (can make at least partly aromatic hydrocarbons saturation in clarified separation oil), obtain hydrotreated product；Gained hydrofinishing is produced
Object contacts in catalyst cracker with catalytic cracking catalyst after mixing with catalytically cracked stock and carries out catalytic cracking
Reaction, alternatively, using gained hydrotreated product as catalytically cracked material and catalytic cracking catalyst in catalyst cracker
Middle contact individually carries out catalytic cracking reaction.The hydrotreated product is rich in cycloalkane and/or is rich in mononuclear aromatics, not only can be with
The viscosity of catalytically cracked stock is reduced, and since catalytically cracked stock negative hydrogen ion generated can be passed to effectively
Hydrotreated product generates non-classical carbonium ion and causes dry gas and coke yield when hydrotreated product being avoided individually to react
The problem of increase, to may be implemented in terms of reducing dry gas and coke yield than individually reacting better effect.
Hydrofinishing is used to make the part aromatic hydrocarbons saturation in clarified separation oil, and reaction condition and reactor are this fields
Known to technical staff, for example, the hydrofinishing processing condition include: temperature be 250-500 DEG C, hydrogen partial pressure 2-30
Megapascal, volume space velocity 1-30h-1, reactor is fixed bed reactors, fluidized bed reactor, paste state bed reactor.Catalytic cracking
Be it is well-known to those skilled in the art, the catalytically cracked stock can be for selected from reduced crude, decompression residuum, coking watt
At least one of this oil, deasphalted oil and hydrotreating residual oil；The condition of the catalytic cracking reaction may include: temperature
400 DEG C -750 DEG C, -1.0 megapascal of 0.10 megapascal of reaction pressure, the weight ratio 1-100 of catalyst and raw material, water vapour and raw material
Weight ratio 0.02-1.0；The catalyst cracker can be riser reactor and/or fluidized-bed reactor.This field skill
Art personnel also can according to need using other reaction conditions and reactor, and the present invention repeats no more.
According to the present invention, catalyst fines separation equipment is well-known to those skilled in the art, for example, can for selected from
At least one of sedimentation separation equipment, filtering separation device, electrostatic separation equipment and centrifugal separation equipment, preferably filtering point
From equipment.
According to the present invention, solid particulate matter is few in clarified separation oil, may be further processed, for example, such as Fig. 2 institute
Show, the method also includes: gained clarified separation oil in step b is cut in fractionating column, obtains diesel oil distillate and oil
Starch fraction；Wherein, the cut point of the cutting is 340-380 DEG C.It can be by cutting gained diesel oil distillate and slurry oil fraction
One step carries out subsequent processing, to improve fraction utilization rate.
According to the present invention, catalytic cracked oil pulp is phosphorus content and the highest product of boiling range in catalytic cracking production, for example, institute
The boiling range initial boiling point for stating catalytic cracked oil pulp can be greater than 290 DEG C, preferably greater than 300 DEG C, further preferably greater than 330 DEG C.It urges
Changing cracked diesel oil is product of the boiling range between gasoline and slurry oil, such as the catalytic cracking diesel oil boiling range may range from
180-380 DEG C, preferably 190 DEG C -380 DEG C, further preferably 250 DEG C -370 DEG C.In the present invention, gasoline boiling range is used
ASTMD86 standard is distilled, and the high boiling fractions such as diesel oil and slurry oil are distilled using ASTM D1160 standard.
According to the present invention, after catalytic cracking diesel oil is mixed with catalytic cracked oil pulp, the viscosity of slurry oil can be reduced, to make
It is appropriate for catalytic cracking, for example, 80 DEG C of viscosity of mixed fraction oil can be not higher than 60 millimeters2It is/the second, preferably not high
In 50 millimeters2/ the second is further preferably not higher than 40 millimeters2/ the second is still more preferably not higher than 30 millimeters2/ the second.
The present invention will be further illustrated by embodiment below, but the present invention is not therefore subject to any restriction.
Hydrogenation protecting agent, hydrodemetallization agent employed in embodiment and comparative example, hydrofinishing agent and hydro-upgrading
The trade names of agent are respectively RG-10B, RDM-2, RN-32V and RIC-1, are catalyzed by Sinopec catalyst branch Chang Ling
The production of agent factory.
The trade names CGP-1 and ASC-4 of catalytic cracking catalyst employed in embodiment and comparative example, by Chinese stone
Change the production of catalyst branch Chang Ling catalyst plant.
The cut point of gasoline and light cycle oil is 201 DEG C in the embodiment of the present invention and comparative example, light cycle oil and slurry oil
Cut point is 365 DEG C.
Embodiment 1
As shown in Figure 1, catalytic cracked oil pulp A and catalytic cracking diesel oil B are mixed in blending tank according to weight ratio 1:1,
Obtain mixed fraction oil C.Using the catalyst fines in suction method separation mixed fraction oil C, wherein the aperture of filter membrane is 0.22
Micron, vacuum degree are 0.085 megapascal.The property of catalytic cracked oil pulp A, catalytic cracking diesel oil B and mixed fraction oil C such as 1 institute of table
Show, catalytic cracked oil pulp and catalytic cracking diesel oil pick up from Sinopec Yanshan Mountain branch company, and filter membrane changes in flow rate becomes in separation process
Gesture is shown in Fig. 3.
Comparative example 1
It is essentially identical with the method for embodiment 1, the difference is that: slurry oil is separately separated, is filtered in separation process
Film changes in flow rate trend is shown in Fig. 3.
From figure 3, it can be seen that embodiment 1 still can be protected using method of the invention with the increase of filtration time
Very high flow is held, and 1 filtration time of comparative example is more than to begin within 3 minutes flow decline occur, especially filtration time is super
It crosses after ten minutes, flow declines faster, illustrates that the operation cycle of filter plant can be improved in method of the invention.
Embodiment 2
As shown in Figure 1, the method according to the invention, by the self-produced diesel oil J of the kitty cracker of property shown in table 4 and
Self-produced slurry oil K carries out sedimentation separation after mixing according to weight ratio 1:1.29, obtains sedimentation mixed fraction oil M, settles mixed fraction
The property of oily M is shown in Table 4, sedimentation separation condition and the results are shown in Table 5.
Comparative example 2
Using separation method same as Example 2, the difference is that: slurry oil is separately separated.
As can be seen from Table 5, compared with comparative example 2, embodiment 1 carries out processing slurry oil using method of the invention, settles
Slurry oil solid content reduces by 23 micro- gram grams from 71 micro- gram grams after separation, and reduction amplitude is 67.6 weight %.
Embodiment 3
Sedimentation mixed fraction oil M in embodiment 2 is sent into hydrogenation plant to contact and added with Hydrobon catalyst
Then hydrogen refinement treatment returns to catalytically cracked stock B shown in kitty cracker and table 2 according to weight ratio 1:2.28
Mixing is used as catalytic cracking feeds, and the trade mark of catalytic cracking catalyst is ASC-4, and specific nature and composition are shown in Table 3, concrete operations
Condition and product distribution are shown in Table 6.
Comparative example 3
It is essentially identical with comparative example 3, the difference is that catalytically cracked stock B is individually subjected to catalytic cracking reaction,
Concrete operations condition and product distribution are shown in Table 6.
As can be seen from Table 6, it although catalytically cracked stock B density height, carbon residue are high, is individually carried out with feedstock oil anti-
It should compare, using method of the invention, gasoline yield is up to 62.90% in product, total liquid yield (liquefied gas yield+gasoline
Yield+diesel yield, abbreviation total liquid yield) it is up to 86.95%.
Table 1
| Distillate number | Slurry oil A | Diesel oil B | Mixed fraction oil C |
| Density (20 DEG C)/(kilogram-meter-3) | 1059.8 | 957.2 | 1008.5 |
| Particle content/(gram liter-1) | 5.3 | 0.0 | 2.5 |
| Viscosity (80 DEG C)/(millimeter2Second-1) | 77.96 | 1.23 | 39.6 |
| Boiling range/DEG C | |||
| IBP | 304.9 | 185.9 | / |
| 5 weight % | 316.8 | 232.6 | / |
| 10 weight % | 386.8 | 240.3 | / |
| 30 weight % | 432.9 | 262.4 | / |
| 95 weight % | / | 366.9 | / |
| FBP | / | 377.2 | / |
Table 2
| Catalytically cracked stock number | B |
| Density (20 DEG C)/(kilogram-meter-3) | 952.8 |
| Carbon residue/weight % | 13.2 |
| Freezing point/DEG C | 42 |
| Viscosity (80 DEG C)/(millimeter2·s-1) | 784 |
| Tenor/(microgram gram-1) | |
| Fe | 30 |
| Ni | 44 |
| V | 0.6 |
| Element quality composition/weight % | |
| H | 11.86 |
| S | 0.51 |
| N | 0.62 |
| Hydrocarbon system's quality composition/weight % | |
| Saturated hydrocarbons | 24.3 |
| Aromatic hydrocarbons | 35.2 |
| Colloid | 40.1 |
| Asphalitine | 0.4 |
| Boiling range/DEG C | |
| IBP | >440 |
| 5 weight % | / |
| 10 weight % | / |
| 30 weight % | / |
| FBP | / |
Table 3
| The catalyst trade mark | ASC-4 |
| Chemical composition/weight % | |
| Al2O3 | 53.0 |
| Na2O | 0.21 |
| SiO2 | 37.1 |
| P2O5 | 0.352 |
| SO3 | 0.173 |
| K2O | 0.367 |
| TiO2 | 0.164 |
| Physical property | |
| Total specific surface area/(rice2Gram-1) | 92 |
| Matrix specific surface area/(rice2Gram-1) | 44 |
| Micropore specific area/(rice2Gram-1) | 48 |
| Total pore volume/(milliliter gram-1) | 0.148 |
| Micro pore volume/(milliliter gram-1) | 0.029 |
| Screening quality composition/% | |
| 0~20 micron | 0 |
| 0~40 micron | 10.2 |
| 0~80 micron | 69.7 |
| 0~105 micron | 86.3 |
| 0~149 micron | 98.5 |
Table 4
| Distillate number | Diesel oil J | Slurry oil K | Settle mixed fraction oil M |
| Density/(kilogram-meter-3) | 928.3 | 980.2 | 957.6 |
| Solid content/(gram liter-1) | 0 | 6.1 | 4.0 |
| Viscosity (80 DEG C)/(millimeter2/ the second) | 1.21 | 25.4 | 16.1 |
| Hydrogen content/weight % | 11.01 | 10.42 | 10.68 |
| Boiling range/DEG C | |||
| IBP | 223 | 345 | 222 |
| 5 weight % | 234 | 379 | / |
| 10 weight % | 239 | 382 | 244 |
| 30 weight % | 253 | 399 | 300 |
| 50 weight % | 274 | 421 | 358 |
| 70 weight % | 299 | 441 | 414 |
| 90 weight % | 325 | 482 | 469 |
| FBP | 339 | / | / |
Table 5
| Embodiment | Embodiment 2 | Comparative example 2 |
| Sedimentation time/hour | 24 | 24 |
| Settling temperature/DEG C | 85 | 85 |
| Solid particulate matter content/(microgram gram in slurry oil after sedimentation-1) | 23 | 71 |
Table 6
* on the basis of fresh feed oil.
Claims (13)
1. a kind of processing method of catalytic cracked oil pulp, this method comprises:
A, catalytic cracked oil pulp is mixed with catalytic cracking diesel oil, obtains mixed fraction oil；Wherein, the catalytic cracked oil pulp with
The mixed weight ratio of catalytic cracking diesel oil is 1:(0.2-10)；80 DEG C of viscosity of the mixed fraction oil are not higher than 60 millimeters2/
Second；
B, gained mixed fraction oil is subjected to separating treatment using catalyst fines separation equipment, obtains clarified separation oil and oil
Mud.
2. according to the method described in claim 1, the method also includes: by step b gained greasy filth be sent into Catalytic Cracking Unit of Measure
It answers and carries out catalytic cracking reaction with catalytically cracked stock together after mixing in device with regenerated catalytic cracking catalyst；And/or
Gained greasy filth feeding catalytic cracking regenerator is regenerated.
3. according to the method described in claim 1, the method also includes: by step b gained greasy filth use catalytic cracking bavin
Oil carries out carrying out washing treatment, obtains clarification washing oil and catalyst fines, wherein the washing weight of the greasy filth and catalytic cracking diesel oil
Amount is than being 1:(0.1-6).
4. according to the method described in claim 3, the method also includes: the catalyst fines are dried.
5. according to the method described in claim 3, the method also includes: by gained at least partly clarify washing oil as catalysis
Cracked diesel oil carries out the carrying out washing treatment and/or mixes in step a with the catalytic cracked oil pulp.
6. according to the method described in claim 1, wherein, gained clarified separation oil in step b being carried out hydrofinishing processing, is obtained
To hydrotreated product；
With catalytic cracking catalyst in catalyst cracker after gained hydrotreated product is mixed with catalytically cracked stock
Middle contact simultaneously carries out catalytic cracking reaction, alternatively, urging using gained hydrotreated product as catalytically cracked material and catalytic cracking
Agent contacts in catalyst cracker individually carries out catalytic cracking reaction.
7. according to the method described in claim 6, wherein, it is 250-500 that the condition of the hydrofinishing processing, which includes: temperature,
DEG C, hydrogen partial pressure is 2-30 megapascal, and volume space velocity is 0.1-30 hours-1。
8. the method according to claim 2 or 6, wherein the catalytically cracked stock is selected from reduced crude, decompression slag
At least one of oil, coker gas oil, deasphalted oil and hydrotreating residual oil；
The catalytic cracking catalyst includes molecular sieve, carrier and binder；
The condition of the catalytic cracking reaction includes: 400 DEG C -750 DEG C of temperature, -1.0 megapascal of 0.10 megapascal of reaction pressure, catalysis
The weight ratio 0.02-1.0 of the weight ratio 1-100 of agent and raw material, water vapour and raw material；
The catalyst cracker is riser reactor and/or fluidized-bed reactor.
9. according to the method described in claim 1, wherein, catalyst fines separation equipment described in step b is selected from sedimentation point
From at least one of equipment, filtering separation device, electrostatic separation equipment and centrifugal separation equipment.
10. according to the method described in claim 1, the method also includes: by step b gained clarified separation oil in fractionating column
In cut, obtain diesel oil distillate and slurry oil fraction；Wherein, the cut point of the cutting is 340-380 DEG C.
11. according to the method described in claim 1, wherein, the boiling range initial boiling point of the catalytic cracked oil pulp is greater than 290 DEG C.
12. according to the method described in claim 1, wherein, the catalytic cracking diesel oil boiling range range is 180-380 DEG C.
13. according to the method described in claim 1, wherein, 80 DEG C of viscosity of the mixed fraction oil are not higher than 50 millimeters2/ the second.
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| CN1262306A (en) * | 1999-01-28 | 2000-08-09 | 中国石油化工集团公司 | Hydrogenation and catalystic cracking combined process for residual oil |
| CN102732312A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking deeply-combined method for residuum |
| CN102732313A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking deeply-combined method for residuum |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1262306A (en) * | 1999-01-28 | 2000-08-09 | 中国石油化工集团公司 | Hydrogenation and catalystic cracking combined process for residual oil |
| CN102732312A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking deeply-combined method for residuum |
| CN102732313A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking deeply-combined method for residuum |
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| CN115785998A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Method and system for removing catalyst powder in catalytic cracking slurry oil |
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