CN105985791A - Method for preparing needle coke raw material - Google Patents
Method for preparing needle coke raw material Download PDFInfo
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- CN105985791A CN105985791A CN201510068337.0A CN201510068337A CN105985791A CN 105985791 A CN105985791 A CN 105985791A CN 201510068337 A CN201510068337 A CN 201510068337A CN 105985791 A CN105985791 A CN 105985791A
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Abstract
The invention discloses a method for preparing a needle coke raw material. The method comprises pouring a part of a delayed coking raw material and catalytic cracking oil slurry into the lower part of a coking fractionating tower, feeding the fractionating tower bottom oil containing the part of delayed coking raw material and the catalytic cracking oil slurry into the upper part of a coke tower, heating the other part of the delayed coking raw material through a heating furnace radiation section, feeding the heated delayed coking raw material into the bottom of the coke tower, carrying out delayed coking, carrying out fractionation on the oil gas produced by the delayed coking reaction to obtain a wax oil component, and carrying out steam stripping on the wax oil component to obtain the needle coke raw material, wherein in the delayed coking reaction, cooling oil and/or cooling water is fed into the top of the coke tower through pipes, steam is injected into the bottom of the coke tower, the pipes for feeding the cooling oil and/or cooling water stretch into the coke tower and the cooling oil and/or cooling water contains desulfuration and denitrification catalysts.
Description
Technical field
The present invention relates to a kind of method preparing needle-shape coke raw material.
Background technology
Needle coke is to produce high power, the main raw material(s) of ultra high power graphite electrode.High-quality needle coke valency
Lattice are higher, can be as electric furnace steel making ultra high power graphite electrode, ultracapacitor used for electric vehicle, logical
Interrogate battery li-ion electrode and be widely used.In needle coke produces, the influence factor of most critical is former
Material character, the best needle coke product hierarchy obtained of feedstock property is the highest.General requirement produces needle coke
In raw material, arene content reaches 30%-50%, colloid, asphalitine less than 1%, ash less than 100ug/g,
Sulfur content is less than 0.5%.Catalytic cracked oil pulp rich in a large amount of aromatic components be produce needle coke ideal
Component.Owing to the character limiting most catalytic cracked oil pulp of raw material can not meet above-mentioned requirements, belong to
In slurry oil inferior, impurity is many, colloid is high with asphalt content, and these components and impurity can have a strong impact on pin
The preparation process that shape is burnt, makes the needle coke Quality Down of production will not even generate needle coke.If by upper
Stating component and magazins' layout, catalytic cracked oil pulp inferior is then preferable needle-shape coke raw material.At present, account for
The most slurry oil inferior of catalytic cracked oil pulp yield is mainly used in blended fuel oil or incorporation subtracts slag conduct
The raw material of delayed coking, it is burnt with common that the most substantial amounts of aromatic component becomes fuel oil component
Charcoal, this waste the most greatly.How to utilize existing technique, make catalytic cracked oil pulp inferior meet pin
The requirement of shape Jiao's raw material is problem demanding prompt solution.
CN101724420B discloses one and utilizes delay coking process to process catalytic cracked oil pulp and routine
Coking raw material produces the method for needle-shape coke raw material.Slurry oil feeds from coke drum middle and upper part in the method, often
Rule coking raw material feeds from the bottom of coke drum, and in coke drum, slurry oil contacts with high-temperature oil gas, and it is unfavorable to remove
In the component that needle coke produces, obtain wax tailings by the side line of coking fractional distillation column former as needle coke
Material.In the method owing to slurry oil is without heating furnace radiant section, temperature is relatively low and slurry oil is all therefrom gone up
Portion feeds, and the time of staying is shorter, and this makes part colloid, asphalitine be not sufficiently reacted, will be oily
Gas is carried in wax tailings；If on the other hand the sulfur content in raw material slurry oil is higher, in wax tailings
Sulfur content is difficult to meet requirement, and therefore the application of the method is considerably limited.Additionally, delayed coking
Main reactor be coke drum, in coke drum, raw material is converted into oil gas and coke, conventional delayed coking
In technique, a large amount of aromatic components have little time to leave from coke drum to translate into coke, reduce pin Jiao's raw material
Yield.
CN1872963A discloses a kind of preprocessing method of raw materials producing needle coke, and raw oil is first through subtracting
Pressure distillation removes wherein undesirable components, and remaining ideal composition contacts with hydrogen, hydrogenation catalyst, adds
Hydrogen reactant flows through isolated and produces the raw material of needle coke.The method needs individually to filter, reduce pressure and steam
Distillation unit, investment is relatively big, and still contains a certain amount of in the needle-shape coke raw material obtained by the method
Colloid, affecting the quality of needle coke, to produce high-grade needle coke product the most difficult.
Summary of the invention
Present invention aim at providing a kind of new method preparing needle-shape coke raw material, by the side of the present invention
Method can prepare the needle-shape coke raw material of high-quality, and can extend the raw material sources of needle coke.
The present invention provides a kind of method preparing needle-shape coke raw material, and the method includes former for section retards coking
Material and catalytic cracked oil pulp inject coking fractional distillation column bottom, and will containing described section retards coking raw material with
The fractionating column base oil of catalytic cracked oil pulp injects coke drum top, is passed through by another part delayed coking raw material
Inject at the bottom of coke drum after the heating of heating furnace radiant section, carry out delayed coking reaction, and by delayed coking reaction
The oil gas produced carries out fractional distillation, obtains wax oil component, and the wax oil component obtained is carried out steam stripping obtains
To needle-shape coke raw material；Wherein, during delayed coking reaction, pass through pipeline at described coke drum top
Inject cooling oil and/or cooling water, inject steam in coke drum bottom, inject cooling oil and/or cooling water
Pipeline stretch in coke drum, and containing desulfurization, denitrification catalyst in described cooling oil and/or cooling water.
In the described preparation method of the present invention, inject cooling oil at the top of described coke drum by pipeline
And/or cooling water, and the pipeline injecting cooling oil and/or cooling water suitably controlling to stretch in coke drum is long
Degree, can reduce coke drum upper temp and advantageously reduce and beneficially produce the aromatic component of needle coke at coke
Reaction in tower.
Inject cooling oil and/or cooling water at the top of described coke drum by pipeline, coke can be reduced
Tower upper temp, thus advantageously reduce the aromatic component producing needle coke reaction in coke drum.
In the described preparation method of the present invention, cooling is oily and/or cools down water by pipeline with water column
Form is injected so that cooling oil and/or cooling water will not directly be carried to big oil with the form of fine droplet
In gas pipeline.
In the described preparation method of the present invention, by injecting steam in coke drum bottom, it is possible to effectively
Keep green coke duct and reduce the time of staying that secondary response component easily occurs.
In the described preparation method of the present invention, colloid in delayed coking raw material and catalytic cracked oil pulp,
Asphalitine by a series of cracking and condensation reaction, is taken off generating the form of distillate and coke
Removing, metal impurities also serve as the component of coke and are removed, and sulfur, nitrogen are because at desulfurization, denitrification catalyst
It is reduced under existence condition.
It addition, in the described preparation method of the present invention, due to asphalitine, colloid can be Jiao with metal
Charcoal tower has been carried out removing, and sulfur, nitrogen also are able to be reduced.Therefore, the preparation method of the present invention
It is particularly well-suited to the poor catalytic cracked oil pulp of character (such as: asphalitine is more than 4 weight % (preferably
4-15 weight %, ash are more than 0.8 weight more than 0.2 weight % (preferably 0.2-1 weight %), sulfur content
Amount % (preferably 0.8-3 weight %)).Additionally, due to the preparation method of the present invention can be applicable to character
Poor catalytic cracked oil pulp, it is possible to extend the raw material sources of needle coke.
Other features and advantages of the present invention will be described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and constitutes the part of description, with
Detailed description below is used for explaining the present invention together, but is not intended that limitation of the present invention.?
In accompanying drawing:
Fig. 1 is the signal of the equipment for implementing the described method preparing needle-shape coke raw material that the present invention provides
Figure.
Detailed description of the invention
Hereinafter the detailed description of the invention of the present invention is described in detail.It should be appreciated that this place is retouched
The detailed description of the invention stated is merely to illustrate and explains the present invention, is not limited to the present invention.
According to the method preparing needle-shape coke raw material of the present invention, its method includes former for section retards coking
Material and catalytic cracked oil pulp inject coking fractional distillation column bottom, and will containing described section retards coking raw material with
The fractionating column base oil of catalytic cracked oil pulp injects coke drum top, is passed through by another part delayed coking raw material
Inject at the bottom of coke drum after the heating of heating furnace radiant section, carry out delayed coking reaction, and by delayed coking reaction
The oil gas produced carries out fractional distillation, obtains wax oil component, and the wax oil component obtained is carried out steam stripping obtains
To needle-shape coke raw material；Wherein, during delayed coking reaction, pass through pipeline at described coke drum top
Inject cooling oil and/or cooling water, inject steam in coke drum bottom, inject cooling oil and/or cooling water
Pipeline stretch in coke drum, and containing desulfurization, denitrification catalyst in described cooling oil and/or cooling water.
Preferably, the pipeline injecting cooling oil and/or cooling water extends vertically in coke drum.
Preferably, the length of described coke drum top feed entrance point distance cylinder lower end accounts for whole barrel lenght
5/10～9/10；The length of feed entrance point distance cylinder lower end, the most described coke drum top accounts for whole
The 7/10～9/10 of barrel lenght.Here, the length of described cylinder refers to that cylinder is with coke drum upper cover even
Connect the vertical dimension between portion and cylinder and bottom cone connecting portion；Described coke drum top feed entrance point away from
Length from cylinder lower end refers to the feed entrance point vertical dimension to cylinder Yu bottom cone connecting portion.
Top of coke tower can use the end socket of routine, such as, can be dome head or ellipsoidal head.When
When top of coke tower uses dome head, stretch into the pipeline injecting cooling oil and/or cooling water in coke drum long
Degree is the 1-45%, preferably 20-35% of coke drum diameter.When top of coke tower uses ellipsoidal head,
Inject cooling oil and/or the 1-22% that length of pipeline is coke drum diameter, preferably 12-20% of cooling water.
In the present invention, in order to ensure that the cooling oil and/or the cooling water that are injected by pipeline will not directly be taken
Taking in main oil gas piping, the opening diameter of the pipeline injecting cooling oil and/or cooling water is preferably 10-50
Millimeter, more preferably 20-30 millimeter.
In the present invention, in order to remain with the aromatic component beneficially producing needle coke further, preferably in institute
Cooling oil and cooling water are injected by pipeline in the top stating coke drum.In this case, cool down oily and cold
But water can be injected by pipeline respectively, it is also possible to is injected as a mixture by same pipeline,
Preferably the two is injected by pipeline respectively.
When at the top of described coke drum by pipeline inject cooling oil and cooling water time, described cooling oil with
The weight ratio of the injection rate of described cooling water can be 0.01-1:1, preferably 0.1-0.3:1.
The weight ratio of the consumption that total consumption of the oily and described cooling water of described cooling feeds with described coke drum
Can be 0.01-0.25:1, preferably 0.01-0.10:1, more preferably 0.03-0.05:1..For institute
State the total consumption cooling down oily and described cooling water, if only injecting described cooling oil and being not injected into described cooling
Water, the most described total consumption list refers to the injection rate of described cooling oil；If only injecting described cooling water and not noting
Entering described cooling oil, the most described total consumption list refers to the injection rate of described cooling water；If being injected simultaneously into described
Cooling down oily and described cooling water, the most described total consumption refers to the injection rate sum of the two.
In the present invention, to described desulfurization, the kind of denitrification catalyst and consumption, there is no particular limitation,
The desulfurization of this area routine, denitrification catalyst can be used with conventional amount used.As such catalyst example
As being the catalyst with nickel-molybdenum, molybdenum-cobalt, nickel-cobalt, nickel-molybdenum-cobalt etc. as active component.
Preferably, on the basis of the consumption that described coke drum feeds, described desulfurization, the use of denitrification catalyst
Amount is 100-10000ppm (more preferably 500-2000ppm).It is to say, in the present invention, with
On the basis of the injection rate (i.e. weight) of described coke drum charging, described desulfurization, the injection of denitrification catalyst
Amount is preferably 100-10000ppm (more preferably 500-2000ppm).
In the present invention, described cooling oil can be various quench oils commonly used in the art.Preferably
In the case of, described cooling oil is the petroleum distillate of 100-450 DEG C for boiling range, and more preferably boiling range is
The petroleum distillate of 250-380 DEG C.
In the present invention, described cooling water can be fresh water, softening water, demineralized water, deaerated water and coagulate
At least one in bearing water, preferably demineralized water.
In the present invention, described another part delayed coking raw material is permissible before injecting at the bottom of described coke drum
It is heated to 490-515 DEG C, preferably 500-505 DEG C.
In the present invention, described fractionating column base oil contains described section retards coking raw material and cycle oil
Slurry is as main component.In addition to containing above-mentioned two kinds of compositions, described fractionating column base oil is possibly together with fractional distillation
During in fractionating column, condense liquid phase (namely non-catalytic cracking slurry oil described later, the delayed coking of formation
Raw material components).In described fractionating column base oil, contain in described liquid phase and described fractionating column base oil urges
The weight ratio changing cracking slurry oil and delayed coking raw material components sum can be 0.05-0.8:1, is preferably
0.1-0.3:1。
It addition, in the present invention, in order to delayed coking can preferably be carried out, described part is preferably comprised
The fractionating column base oil of delayed coking raw material and catalytic cracked oil pulp is being injected into the temperature before coke drum top
Degree is 310-360 DEG C, preferably 340-360 DEG C.
In the present invention, in order to keep green coke duct and reduce the stop that secondary response component easily occurs time
Between, this method selects to inject steam in coke drum bottom, simultaneously in order to reduce after steam injects catalyst
Impact, the injection rate of steam needs to be controlled.The weight ratio of the consumption of steam and coke drum charging can
Think 0.02-0.1:1, preferably 0.04-0.06:1.
Injecting steam in coke drum bottom to be carried out by pipeline, the opening diameter of described pipeline does not has spy
Other restriction, such as, can be 10-50 millimeter, preferably 20-30 millimeter.
Due to less demanding, therefore from catalytic cracking fractionating tower tower to catalytic cracked oil pulp character of the present invention
The catalytic cracked oil pulp that the end obtains can directly use, and without carrying out other place before the use
Reason.As from the catalytic cracked oil pulp obtained at the bottom of catalytic cracking fractionating tower tower, its fragrance point content is the highest
In 50 weight %.
Described delayed coking raw material can be various conventional delayed coking raw material commonly used in the art,
Can be such as decompression residuum, reduced crude, visbroken resids, heavy deasphalted oil, viscous crude, plug
At least one in crude oil, shale oil and liquefied coal coil.Described viscous crude refers to asphalitine and gum level relatively
High and that viscosity is bigger crude oil.
In order to make described another part delayed coking raw material can be heated before injecting described coke drum
To above-mentioned temperature range, the outlet temperature of the most described heating furnace radiant section is 490-515 DEG C；More excellent
Elect 500-505 DEG C as.
In the present invention, the condition of described delayed coking reaction includes: coke drum pressure is
0.05-0.25MPa, coking cycle is 18-36h；Preferably coke drum pressure is 0.12-0.17MPa, coking
Cycle is 24-36h.
In the present invention, pressure refers to gauge pressure.
In the present invention, a part and the catalytic cracked oil pulp of described delayed coking raw material is injected into coking
Fractionating column bottom, and form described fractionating column base oil with after described liquid-phase mixing bottom coking fractional distillation column,
And it is injected into coke drum top by the way of described fractionating column base oil；Meanwhile, another part delay coke
Change raw material to be injected directly at the bottom of coke drum after heating through heating furnace radiant section, and thus in coke drum
Carry out delayed coking reaction.
It is to say, in the present invention, the charging in described coke drum of the described delayed coking raw material is with same
The two ways of Shi Jinhang is carried out, that is, a part is injected into coke drum top along with fractionating column base oil,
Another part is directly injected at the bottom of coke drum.For the delay coke fed by above two feeding manner
The ratio changing raw material can change in wide scope.With the combined feed weight of described delayed coking raw material it is
Benchmark, injects the described another part delayed coking at the bottom of coke drum preferably through heating furnace radiant section after heating
The consumption of raw material is 60-99 weight %, preferably 90-99 weight %, more preferably 90-95 weight %.
Additionally, the scope of the feed weight ratio of described catalytic cracked oil pulp and described delayed coking raw material is permissible
Change in wide scope.The most described catalytic cracked oil pulp and the feed weight of described delayed coking raw material
Ratio is 0.1:99.9～99.9:0.1, more preferably 20:80～50:50.
In the present invention, described catalytic cracked oil pulp is as fractionating column base oil and is injected on coke drum
Portion, thus carry out delayed coking reaction with described delayed coking raw material.The charging of described catalytic cracked oil pulp
As long as weight meets above-mentioned scope.
Additionally, in the present invention, there is no particular limitation for described coke drum, can be that this area routine makes
Various coke drums.
In the present invention, carry out fractional distillation by the coke drum tower top oil gas produced by delayed coking reaction,
To wax oil component.Described fractional distillation can be carried out in fractionating column, and the condition of described fractional distillation includes: fractionating column
Tower top temperature 100～145 DEG C, fractionation column pressure on top surface 0.13～0.17MPa, fractionating column column bottom temperature
310～360 DEG C.
In the present invention, described wax oil component refers to that boiling range is at the distillate of about 350-450 DEG C.
In the present invention, also include that the wax oil component obtained is carried out steam stripping obtains needle-shape coke raw material.
The wax oil component obtained carries out steam stripping preferably carry out in knockout drum, its concrete condition bag
Including: operation pressure is 0.1-0.15MPa, operation temperature is 300-330 DEG C, the quantity of steam of injection and entrance
The weight ratio of the wax oil group component of knockout drum is 0.05-0.1:1.
In one embodiment, the described group technology of the present invention is implemented in equipment as shown in Figure 1,
Specifically, described equipment specifically includes that delay coking heating furnace, delayed coker fractionator 18, delay coke
Change coke drum 6 and knockout drum 19.Delayed coking raw material 1 optionally with coker gas oil, wax tailings,
After coking wax slop heat exchange, (not marking in Fig. 1) is divided into two-way, and a road passes sequentially through heating furnace convection section
4, radiant section 5 heats, subsequently into coke drum bottom；Meanwhile, separately lead up to pipeline 23 with
By the partially catalyzed cracking slurry oil 9 of pipeline 24 (optionally with coker gas oil, wax tailings, Jiao
After changing wax slop heat exchange, Fig. 1 does not marks) mix the upper feeding collectively as fractionating column 18, another
Partially catalyzed cracking slurry oil 9 separately as the lower charging of coking fractional distillation column 18, upper feeding and lower charging with
Mixing high-temperature oil gas 22 and fractionating column upper feeding, coking wax slop from coke drum 6 and knockout drum 19
The liquid phase stream formed after 17 heat exchange is mixed to form fractionating column base oil 8, fractionating column base oil at fractionation column base
It is sent to coke drum 6 top after 8 extractions and carries out coking reaction, inject steam by pipeline 7 simultaneously；Coke
The top of tower 6 is provided with cooling oil supply pipeline 10 and/or cooling water supplying pipe line 11, in the mistake of green coke
Journey injects cooling oil and/or cooling by cooling oil supply pipeline 10 and/or cooling water supplying pipe line 11
Water, wherein, containing desulfurization, denitrification catalyst in described cooling oil and/or cooling water；The coke generated stays
In coke drum 6, the high-temperature oil gas of generation is transported in fractionating column 18 separate by pipeline 12,
Obtain rich tail gas of coking plant 13, coker gasoline 14, coker gas oil 15 and wax tailings 16；Wax tailings 16
By pipeline to knockout drum 19, knockout drum 19 is passed through steam (not marking in figure) to wax tailings
16 strip, and obtain needle-shape coke raw material in separation tank bottom, and needle-shape coke raw material is sent into by pipeline 21
Subsequent handling.
In the above-described embodiment, non-catalytic cracking slurry oil, delayed coking raw material group in fractionating column base oil
Divide the catalytic cracked oil pulp and delay coke contained in (the most above-mentioned liquid phase component) and described fractionating column base oil
The weight ratio changing raw material components sum can be 0.05-0.8:1, preferably 0.1-0.3:1.
In the present invention, wax tailings (the most described wax oil component) refers to that boiling range is at about 350-450 DEG C
Distillate；Coking wax slop refers to that initial boiling point is higher than the heavy wax oil of 430 DEG C.
The invention will be further described by the following examples.
Embodiment 1
The preparation method of the described needle-shape coke raw material that the present embodiment provides for the present invention is described.
The present embodiment uses the flow process shown in Fig. 1.(i.e. delayed coking raw material, it is correlated with decompression residuum 1
Parameter is as shown in table 1) it is 75:25 with the ratio of catalytic cracked oil pulp 9 (relevant parameter is as shown in table 1)；
It addition, on the basis of the gross weight of decompression residuum 1, pass sequentially through heating furnace convection section 4, radiant section 5
Heating, the consumption subsequently into the decompression residuum 1 of coke drum bottom is 90 weight %.
After delayed coking raw material 1 and coker gas oil, wax tailings, coking wax slop heat exchange (in Fig. 1 not
Mark) it is divided into two-way, a road passes sequentially through heating furnace convection section 4, radiant section 5 carries out being heated to 500 DEG C
After, enter coke drum bottom；Meanwhile, separately lead up to pipeline 23 with by the partially catalyzed of pipeline 24
Cracking slurry oil 9 (after coker gas oil, wax tailings, coking wax slop heat exchange, do not mark in Fig. 1)
Mixing the upper feeding collectively as fractionating column 18, another part catalytic cracked oil pulp 9 is separately as coking
The lower charging of fractionating column 18, upper feeding and lower charging are high with the mixing of knockout drum 19 with from coke drum 6
Temperature oil gas 22 and fractionating column upper feeding, coking wax slop 17 heat exchange after formed liquid phase stream at fractionating column
Bottom is mixed to form fractionating column base oil 8, and fractionating column base oil 8 (temperature is 350 DEG C) is sent to tower top after extracting out
For the top of coke drum 6 of dome head and carry out coking reaction, non-catalytic cracking in fractionating column base oil
The catalytic cracked oil pulp contained in slurry oil, delayed coking raw material components and described fractionating column base oil and delay coke
The weight ratio changing raw material components sum is 0.2:1, and coke drum pressure is 0.15MPa, simultaneously at coke drum
Steam is injected by pipeline 7 in the end；The length of coke drum upper feeding positional distance cylinder lower end accounts for whole cylinder
The 7/10 of length, meanwhile, tower top injects the coking stage casing oil as cooling oil by pipeline 10 and (is derived from
Fractionating column 18, boiling range is 250～380 DEG C) and inject the demineralized water (temperature as cooling water by pipeline 11
Degree is 30 DEG C), in the cooling oil of pipeline 10, add catalyst simultaneously, pipeline 10 and pipeline 11 stretch into
In coke drum, pipeline 10 is 20mm with the opening diameter of pipeline 11, and pipeline 10 and pipeline 11 are stretched
Entering the length in coke drum and be respectively the 30% of coke drum diameter, cooling oil with the weight ratio of demineralized water is
0.1:1, cooling oil and the total injection of demineralized water are 0.04 with the weight ratio of coke drum combined feed injection rate:
1, and, containing desulfurization, denitrification catalyst (containing the catalyst of nickel-molybdenum-cobalt active component) in cooling oil,
On the basis of the injection rate of combined feed, the injection rate with the catalyst of cooling oil injection is 500ppm；Burnt
Charcoal tower bottom steam is by pipeline 7 (opening diameter is that 20mm injects), the injection rate of steam and combined feed
The weight ratio of injection rate is 0.04:1；Coke drum green coke cycle 24h, the coke of generation is stayed in coke drum,
The high-temperature oil gas generated enters in fractionating column 18 and carries out separating that (separation condition is fractionation column pressure on top surface
0.15MPa, fractionating column column bottom temperature 332 DEG C, fractionator overhead temperature 126 DEG C), obtain rich tail gas of coking plant
13, coker gasoline 14, coker gas oil 15 and wax tailings 16, wax tailings goes to knockout drum 19,
The quantity of steam (not marking in Fig. 1) of knockout drum injection and the weight ratio of the wax tailings amount entering knockout drum
Be 0.05, temperature be 300 DEG C, pressure be to strip under conditions of 0.12MPa, obtain pin tank bottoms
Shape Jiao's raw material.The product slates finally obtained and the character of the needle-shape coke raw material of gained are as shown in table 2.
Comparative example 1
Carry out according to the method for embodiment 1, the most in described coke drum 6 inject cooling oil and
Cooling water, the product slates finally obtained and the character of the needle-shape coke raw material of gained are as shown in table 2.
Comparative example 2
Carry out according to the method for embodiment 1, in described coke drum 6, the most do not inject steam,
After the character of needle-shape coke raw material of the product slates that obtains and gained as shown in table 2.
Embodiment 2
The preparation method of the described needle-shape coke raw material that the present embodiment provides for the present invention is described.
The method using embodiment 1 is carried out, except for the difference that: decompression residuum and the ratio of catalytic cracked oil pulp
For 70:30；Pass sequentially through heating furnace convection section 4, the temperature of the heated decompression residuum of radiant section 51 is
501℃；Coke drum pressure is 0.16MPa；Non-catalytic cracking slurry oil, delay coke in fractionating column base oil
Change the catalytic cracked oil pulp and delayed coking raw material components contained in raw material components and described fractionating column base oil
The weight ratio of sum is 0.25:1；The length of coke drum upper feeding positional distance cylinder lower end accounts for whole cylinder
The 9/10 of body length；Described cooling oil (this same amount of cooling water is replaced with same amount of described cooling water
In containing same amount of desulfurization oily with described cooling, denitrification catalyst), make the total injection of cooling water with
It is 0.03:1 that coke drum feeds the weight ratio of injection rate up and down.The product slates finally obtained and gained
The character of needle-shape coke raw material as shown in table 2.
Embodiment 3
The preparation method of the described needle-shape coke raw material that the present embodiment provides for the present invention is described.
The method with embodiment 1 is used to carry out, except for the difference that: decompression residuum and the ratio of catalytic cracked oil pulp
Example is 65:35；Pass sequentially through heating furnace convection section 4, the temperature of the heated decompression residuum of radiant section 51
It it is 502 DEG C；Coke drum pressure is 0.17MPa；Non-catalytic cracking slurry oil, delay in fractionating column base oil
The catalytic cracked oil pulp contained in coking raw material component and described fractionating column base oil and delayed coking raw material group
The weight ratio of/sum is 0.3:1；The length of coke drum upper feeding positional distance cylinder lower end accounts for whole cylinder
The 8/10 of body length；Replacing described cooling water with same amount of described cooling oil, the injection making cooling oil is total
It is 0.03:1 that amount and coke drum feed the weight ratio of injection rate up and down., and with the injection rate of combined feed as base
Standard, the injection rate with the catalyst of cooling oil injection is 2000ppm.The product slates that finally obtains and
The character of the needle-shape coke raw material of gained is as shown in table 2.
Embodiment 4
The preparation method of the described needle-shape coke raw material that the present embodiment provides for the present invention is described.
Carry out, except for the difference that according to the method for embodiment 1: pass sequentially through heating furnace convection section 4, radiation
The temperature of section 5 heated decompression residuum 1 is 503 DEG C；Coke drum pressure is 0.17MPa；In fractional distillation
Contain in non-catalytic cracking slurry oil in tower base oil, delayed coking raw material components and described fractionating column base oil urges
The weight ratio changing cracking slurry oil and delayed coking raw material components sum is 0.15:1；Cooling oil and demineralized water
Total injection and coke drum to feed the weight ratio of injection rate up and down be 0.05:1..The product finally obtained
The character of the needle-shape coke raw material of distribution and gained is as shown in table 2.
Embodiment 5
The preparation method of the described needle-shape coke raw material that the present embodiment provides for the present invention is described.
Carry out, except for the difference that according to the method for embodiment 3: pass sequentially through heating furnace convection section 4, radiation
The temperature of section 5 heated decompression residuum 1 is 505 DEG C；In fractionating column base oil non-catalytic cracking slurry oil,
The catalytic cracked oil pulp and the delayed coking that contain in delayed coking raw material components and described fractionating column base oil are former
The weight ratio of material component sum is 0.2:1.The product slates finally obtained and the needle-shape coke raw material of gained
Character as shown in table 2.
Embodiment 6
The preparation method of the described needle-shape coke raw material that the present embodiment provides for the present invention is described.
Carry out according to the method for embodiment 3, long in except for the difference that pipeline 10 and pipeline 11 stretch into coke drum
Degree is respectively the 20% of coke drum diameter.The product slates that finally obtains and the needle-shape coke raw material of gained
Character is as shown in table 3.
Embodiment 7
The preparation method of the described needle-shape coke raw material that the present embodiment provides for the present invention is described.
Carrying out according to the method for embodiment 3, except for the difference that top of coke tower uses ellipsoidal head, and pipeline
10 and pipeline 11 stretch into coke drum in length be respectively the 12% of coke drum diameter.The product finally obtained
The character of the needle-shape coke raw material of distribution and gained is as shown in table 3.
Embodiment 8
The preparation method of the described needle-shape coke raw material that the present embodiment provides for the present invention is described.
Carrying out according to the method for embodiment 3, except for the difference that, top of coke tower uses ellipsoidal head, and pipe
In line 10 and pipeline 11 stretch into coke drum, length is respectively the 20% of coke drum diameter.The product finally obtained
The character of the needle-shape coke raw material of product distribution and gained is as shown in table 3.
Embodiment 9
Carry out according to the method for embodiment 3, long in except for the difference that pipeline 10 and pipeline 11 stretch into coke drum
Degree is respectively the 5% of coke drum diameter.The product slates that finally obtains and the needle-shape coke raw material of gained
Character is as shown in table 3.
Embodiment 10
Carry out, except for the difference that according to the method for embodiment 1: cooling oil is 0.3 with the weight ratio of demineralized water:
1, cooling oil and the total injection of demineralized water are 0.1:1 with the weight ratio of coke drum combined feed injection rate；
The injection rate of coke tower bottom steam is 0.06:1 with the weight ratio of coke drum combined feed injection rate.Finally obtain
Product slates and the character of needle-shape coke raw material of gained as shown in table 3.
Table 1
Table 2
Table 3
The preferred embodiment of the present invention described in detail above, but, the present invention is not limited to above-mentioned reality
Execute the detail in mode, in the technology concept of the present invention, can be to the technical side of the present invention
Case carries out multiple simple variant, and these simple variant belong to protection scope of the present invention.
It is further to note that each the concrete technology described in above-mentioned detailed description of the invention is special
Levy, in the case of reconcilable, can be combined by any suitable means, in order to avoid need not
The repetition wanted, various possible compound modes are illustrated by the present invention the most separately.
Additionally, combination in any can also be carried out between the various different embodiment of the present invention, as long as its
Without prejudice to the thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (16)
1. the method preparing needle-shape coke raw material, it is characterised in that the method includes section retards
Coking raw material and catalytic cracked oil pulp inject coking fractional distillation column bottom, and will be containing described section retards coking
The fractionating column base oil of raw material and catalytic cracked oil pulp injects coke drum top, by former for another part delayed coking
Expect to inject at the bottom of coke drum after heating furnace radiant section heats, carry out delayed coking reaction, and by delay coke
The oil gas changing reaction generation carries out fractional distillation, obtains wax oil component, and the wax oil component obtained is carried out steam
Stripping obtains needle-shape coke raw material；Wherein, during delayed coking reaction, lead at described coke drum top
Cross pipeline inject cooling oil and/or cooling water, coke drum bottom inject steam, inject cooling oil and/or
The pipeline of cooling water stretches in coke drum, and described cooling is oily and/or urges containing desulfurization, denitrogenation in cooling water
Agent.
Method the most according to claim 1, wherein, when top of coke tower uses dome head,
Stretch into injecting cooling oil and/or cooling down the 1-45% that length of pipeline is coke drum diameter of water in coke drum.
Method the most according to claim 1, wherein, when top of coke tower uses ellipsoidal head,
Inject cooling oil and/or the 1-22% that length of pipeline is coke drum diameter of cooling water.
Method the most according to claim 1, wherein, in described coke drum combined feed, described in urge
The weight ratio changing cracking slurry oil and delayed coking raw material is 0.1:99.9～99.9:0.1.
Method the most according to claim 1, wherein, described coke drum top feed entrance point distance
The length of cylinder lower end accounts for the 7/10～9/10 of whole barrel lenght.
6. according to the method described in any one in claim 1-5, wherein, inject cooling oil and/or
The opening diameter of the pipeline of cooling water is 10-50 millimeter.
Method the most according to claim 1, wherein, passes through pipeline at the top of described coke drum
Injection cooling oil and cooling water, and described cooling is oily and described cooling water weight ratio is 0.01-1:1.
8. according to the method described in claim 1 or 7, wherein, the oily and described cooling water of described cooling
The weight ratio of total consumption and described coke drum charging be 0.01-0.25:1.
Method the most according to claim 1, wherein, on the basis of the amount that described coke drum feeds,
Described desulfurization, the consumption of denitrification catalyst are 100-10000ppm.
10. according to the method described in claim 1 or 7, wherein, described cooling oil for boiling range is
The petroleum distillate of 100-450 DEG C.
11. according to the method described in claim 1 or 7, and wherein, described cooling water is fresh water, soft
Change at least one in water, demineralized water, deaerated water and condensation water.
12. methods according to claim 1, wherein, described another part delayed coking raw material exists
It is heated to 490-515 DEG C before injecting described coke drum bottom.
13. according to the method described in claim 1 or 12, wherein, containing described section retards coking
The fractionating column base oil of raw material and catalytic cracked oil pulp is injected into the temperature before coke drum top
310-360℃。
14. methods according to claim 1, wherein, the steam of coke drum bottom injection and coke
The weight ratio of tower combined feed consumption is 0.02-0.1:1.
15. according to the method described in any one in claim 1,4 and 12, wherein, described delay
Coking raw material is reduced crude, decompression residuum, visbroken resids, heavy deasphalted oil, viscous crude, plug
One or more in crude oil, shale oil and liquefied coal coil.
16. according to the method described in any one in claim 1-7 and 12, wherein, described delay
The condition of pyrogenetic reaction includes: coke drum pressure is 0.1-0.25MPa, coking cycle 18-36h.
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