CN105586077B - Heavy oil coking equipment - Google Patents
Heavy oil coking equipment Download PDFInfo
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- CN105586077B CN105586077B CN201410562515.0A CN201410562515A CN105586077B CN 105586077 B CN105586077 B CN 105586077B CN 201410562515 A CN201410562515 A CN 201410562515A CN 105586077 B CN105586077 B CN 105586077B
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Abstract
The invention provides heavy oil coking equipment, which includes a heating furnace (a), a coke reactor (b), a spray coking tower (c), a cyclone separator (d) and a fractionating tower (e). A coking raw material is preheated in a heating furnace (a) and then atomized by an atomizing nozzle (c18) of the spray coking tower (c), oxygen-containing high temperature gas from the heating furnace (a) is deoxidized by the coke reactor (b) and then contacts the atomized state coking raw material in the spray coking tower (c) to carry out coking reaction, the coarse coke powder in the coking reaction product is collected from a lower cone collection area (c22), oil gas and coke fine powder in the coking reaction product are separated by the cyclone separator (d), and oil gas is introduced into the fractionating tower e to perform fraction separation. Belonging to direct heating type coking equipment, the heavy oil coking equipment can greatly reduce coking in a heating furnace tube and improve the liquid yield, also the obtained coke powder and the dry gas from the fractionation tower can be burnt to serve as the heat source of the heavy oil coking equipment.
Description
Technical field
The present invention relates to a kind of coking heavy oil equipment.
Background technology
Current crude oil heaviness, in poor quality, higher-priced trend are more and more obvious, need of the whole world to lightweight and clean fuel oil
Rapid growth is sought, along with environmental requirement is increasingly strict so that heavy oil deep processing technology has turned into petroleum refining industry of the world today
The emphasis of development.Particularly inferior heavy oil density is big, viscosity is high, content of beary metal is high, sulfur content is high, nitrogen content is high, colloid and
The features such as asphalt content is high, the processing (the especially secondary operation of heavy oil) to crude oil brings bigger difficulty.Carry at present
Heavy oil conversion level high, the earned value techniques of increase light-end products yield still rely primarily on coking, RFCC and residual oil and add
The techniques such as hydrogen treatment.Wherein, coking is the primary means that the inferior heavy oil (particularly residual oil) based on de- charcoal technique is converted.And
Delay coking process has that de- charcoal is thorough, flow is simple, technology maturation, relatively low plant investment the features such as, it has also become processing of heavy oil
One of important process.
Delayed coking is a kind of heat processing technique of depth thermal cracking, can convert heavy oils into for coking dry gas, liquefied gas,
The products such as coker gasoline, coker gas oil, wax tailings, coke.Generally the yield of coker gasoline, coker gas oil and wax tailings
Sum as delayed coking liquid yield, liquid yield is the most important technical-economic index of coking process.Conventional delay
Coking process main flow is：Heavy oil is rapidly heated in the radiating furnace tube of heating furnace and is warmed up to coking temperature (usually
490-515 DEG C or so) after, enter coke drum from the bottom of coke drum, pyrogenetic reaction is carried out in coke drum, the coke of generation is stayed
In coke drum, the oil gas of generation is escaped into fractionating column from top of coke tower and is fractionated, and obtains cooking gas (including coking
Gasoline), coker gas oil, wax tailings and bottom of towe recycle oil.Wherein, coke drum is generally two, and two coke drums are used in turn,
, full of being devoked after coke, hot logistics switches to another coke drum and carries out pyrogenetic reaction for one of them.Generation in coke drum
Coke be monoblock shape, be broadly divided into economic worth needle coke higher, general sponge coke and poor shot coke, transition
It is burnt.Decoking process mainly include reduce tower in coke temperature it is small steam out, steam out greatly, it is cold Jiao (note cooling water), draining, remove tower
Interior coke unloads top cover and bottom, drills and cuts burnt (using giant), upper top cover and bottom, warm tower (logical steam) etc..
Current processing heavy oil tends to the increase of in poor quality, carbon residue, asphalitine and tenor etc., to delayed coking unit
Operation bring challenge, not only product slates are deteriorated, liquid yield reduction, and coking of the raw material in heating furnace tube enter
One step is aggravated, and directly influences the long-term operation of device.Additionally, the decoking process of delayed coking coke drum belongs to interval behaviour
Make, its program is more, and time-consuming, can also produce large amount of sewage, not only increased the energy consumption and running cost of device, and also environment is made
Into immense pressure.
In order to improve the liquid yield of delayed coking and extend the on-stream time of delayed coking, petroleum refining researcher research
The technology related to developing.
For example, CN1599784A discloses a kind of delayed coking method for producing anisotropy free-flowing shot coke,
The method includes with oxidant contacting vacuum residuum feed at a temperature of about 150-325 DEG C, subsequently into heating stove heat
Temperature to needed for coking, then generates the shot coke that anisotropy is flowed freely in coke drum.Although the method can be with
Obtain shot coke, and eliminate coke cleaning step, but due to vacuum residuum feed enter heating furnace before need first with
There is oxidation reaction and condensation reaction in oxidising agent, therefore can be further exacerbated by the coking of heating furnace tube, so as to influence
Continuous production, the technique is difficult to industrialize.
CN101619237A and CN101619238A disclose the technique that delayed coking is combined with vacuum distillation process,
The liquid yield of delayed coking unit is improve, the property of weight wax tailings is improved.But, the method still needs will be postponed
Coking raw material is directly heated to coking temperature in heating furnace tube, therefore, the coking of boiler tube is exacerbated, so that can shortening device
On-stream time.
Additionally, the coking in order to slow down delayed coker unit furnace boiler tube, petroleum refining researcher research and develop
Related technology.Research shows, diluent, free radical inhibitors, arene coking are added toward delayed coking raw material
Inhibitor, anti-coking agent etc. can to a certain extent suppress the coking of heating furnace tube, extend on-stream time, but mode of heating
Indirect heating manner (by heating-furnace tube wall heat exchange) is generally belonged to, the thermal efficiency is low, therefore boiler tube green coke problem
Can not be able to effectively solve, and liquid yield is lifted without essence, and coke drum decoking environmental issue is still protruded.
In sum, needing a kind of coking behavior that can either improve heating furnace tube of exploitation badly at present can improve liquid again
The coking heavy oil equipment of body yield.
The content of the invention
The invention aims to overcome the existing delayed coking equipment can not be while realizing improving heating furnace tube
Coking behavior simultaneously improves the defect of liquid yield, and provides a kind of new coking heavy oil equipment.
Specifically, the coking heavy oil equipment that the present invention is provided includes heating furnace, coke gasification reaction device, spraying coking tower, whirlwind
Separator and fractionating column, the spraying coking tower include interconnected top straight tube reaction zone and bottom cone collecting region, set
Put atomizer that is at the top of the top straight tube reaction zone and being connected with the feed(raw material)inlet of the spraying coking tower and side
To outlet；Coking heavy oil raw material is preheated in the radiant heating area of the heating furnace, preheated coking heavy oil raw material warp
It is introduced into the spraying coking tower by the feed(raw material)inlet and is atomized by the atomizer, from the heating furnace
The oxygen-containing high-temperature gas of combustion chamber carries out deoxidation by the coke gasification reaction device, through the deoxidation high-temperature gas after deoxidation by being located at
Hot-wind inlet at the top of the spraying coking tower is introduced into the spraying coking tower and is contacted with the coking heavy oil raw material of atomization state,
So that the coking heavy oil raw material of the atomization state reaches coking temperature and carries out pyrogenetic reaction, the coke in pyrogenetic reaction product is thick
Powder draws from the bottom cone collecting region bottom collection, oil gas and coke fines in coke gasification reaction product from the side outlet
Enter to carry out in the cyclone separator separation of oil gas and coke fines, the oil gas from the cyclone separator introduces fractionating column
In carry out fraction seperation.
By the discovery after further investigation, existing delayed coking equipment generally only includes heating to the present inventor
Stove, coking tower and fractionating column, in actual production process, coking heavy oil raw material is in the radiant heating area of heating furnace through boiler tube pipe
Wall exchanges heat and indirectly heat afterwards again introduces the coking heavy oil raw material of the liquid after heating from coking tower bottom of towe to coking temperature
To carry out pyrogenetic reaction in coking tower, pyrogenetic reaction product is finally carried out into fraction seperation in fractionating column.However, using this
Indirectly heat (being exchanged heat by boiler tube tube wall) mode and directly by coking heavy oil raw material one-time heating to coking temperature and
Coking heavy oil raw material carries out the coking that the mode of coking is not only easily caused in heating furnace tube, and liquid in liquid form
Yield is relatively low.
And the coking heavy oil equipment that the present invention is provided is by increasing the coke gasification reaction device, spraying coking tower and cyclonic separation newly
Device, can not only reduce the coking in heating furnace tube, but also can improve liquid yield.Concrete principle is as follows：On the one hand,
When the coking heavy oil equipment that the present invention is provided is reacted for coking heavy oil, heating furnace only serves the work of preheating coking heavy oil raw material
With without coking heavy oil raw material is heated into coking temperature (generally the heating furnace as existing coking heavy oil equipment
It is 490-515 DEG C), the thermal source of pyrogenetic reaction is carried along into by high-temperature gas, and the high-temperature gas is straight in coking tower of spraying
Connect and contact and reach coking temperature with the coking heavy oil raw material after preheating, therefore, it is possible to significantly reduce the coking of heating furnace tube；
On the other hand, the atomizer for being set in the spraying coking tower can be by coking heavy oil stock dispersion into fine oil droplets, significantly
Increase unit volume coking heavy oil raw material and high-temperature gas between contact area, and spraying coking tower can with negative-pressure operation,
So as to cause that the heat-transfer capability of whole pyrogenetic reaction process greatly strengthens, green coke amount is reduced, liquid yield increases, and
And generation coke be with certain particle size distribution can fluidized particles, easily fluidisation conveying, eliminate coke cleaning step, saved expense
With and time cost, production process do not devoke waste water, reduces the process step and intractability of follow-up waste water.Additionally, institute
State the oxygen content that coke gasification reaction device can be reduced in high-temperature gas as early as possible, prevent spray coking tower occur burning, blast can
Energy property, it is ensured that the security for using.
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 to constitute the part of specification, with following tool
Body implementation method is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
The structural representation of the coking heavy oil equipment that Fig. 1 is provided for a kind of specific embodiment of the invention；
The structural representation of the spraying coking tower that Fig. 2 is provided for a kind of specific embodiment of the invention；
The structural representation of the coke gasification reaction device that Fig. 3 is provided for a kind of specific embodiment of the invention；
The part-structure schematic diagram of the coking heavy oil equipment that Fig. 4 is provided for a kind of specific embodiment of the invention.
Description of reference numerals
A- heating furnaces；B- coke gasification reaction devices；B27- gas distributors；B28- fluidizes state solid；B29- solids add mouth；
B31- solid outlets；C- spraying coking towers；C18- atomizers；C19- side outlets；C20- chev(e)ron baffles；C21- tops
Straight tube reaction zone；C22- bottoms cone collecting region；C24- hot-wind inlets；C25- feed(raw material)inlets；C30- gas distribution grids；D- whirlwind
Separator；E- fractionating columns；E1- raw materials oil-in；E11- coking dry gas are exported；E12- liquefied gas is exported；E13- coker gasolines go out
Mouthful；E14- coker gas oils are exported；E15- wax tailings are exported；N- pipe networks；K- coke meal collecting tanks；M- coke fines are collected
Tank；G- pumps；F- air blowers；H- air-introduced machines；2- preheated coking heavy oil raw material；The oxygen-containing high-temperature gases of 3-；4- deoxidation High Temperature Gas
Body；The mixture of 6- oil gas and coke fines；The stripped vapors of 7- first；The stripped vapors of 9- second；10- oil gas；16- bottom of towe flows back
Oil；17- coking raw materials.
Specific embodiment
Specific embodiment of the invention is described in detail below.It should be appreciated that described herein specific
Implementation method 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 opposite explanation is not made, the noun of locality for using such as " upper and lower, left and right " is typically referred to
Coking heavy oil equipment of the invention direction under operating conditions, that is, the direction shown in accompanying drawing.
As depicted in figs. 1 and 2, the coking heavy oil equipment that the present invention is provided includes that heating furnace a, coke gasification reaction device b, spraying are burnt
Changing tower c, cyclone separator d and fractionating column e, the spraying coking tower c includes interconnected top straight tube reaction zone c21 with
Portion cone collecting region c22, be arranged at the top of the top straight tube reaction zone c21 and enter with the raw material of the spraying coking tower c
The atomizer c18 and side outlet c19 of mouth c25 connections；Coking heavy oil raw material is in the radiant heating area of the heating furnace a
In preheated, preheated coking heavy oil raw material 2 is introduced into the spraying coking tower c and leads to via the feed(raw material)inlet c25
Cross the atomizer c18 to be atomized, the oxygen-containing high-temperature gas 3 of the combustion chamber from the heating furnace a passes through the coke
Reactor b carries out deoxidation, through the deoxidation high-temperature gas 4 after deoxidation by the hot-wind inlet at the top of the spraying coking tower c
C24 is introduced into the spraying coking tower c and is contacted with the coking heavy oil raw material of atomization state, so that the coking heavy oil of the atomization state
Raw material reaches coking temperature and carries out pyrogenetic reaction, and the coke meal in pyrogenetic reaction product is from the bottom cone collecting region
C22 bottom collections, the mixture 6 of oil gas and coke fines in coke gasification reaction product introduces described from the side outlet c19
The separation of oil gas and coke fines is carried out in cyclone separator d, the oil gas 10 from the cyclone separator d introduces the fractionation
Fraction seperation is carried out in tower e.
The heating furnace a primarily serves two effects, and one is to preheat coking heavy oil raw material in its radiant heating area, two be
Its combustion chamber provides oxygen-containing high-temperature gas.The effect of preheating coking heavy oil raw material is only served due to the boiler tube of heating furnace a, without
The coking heavy oil raw material is heated to cracking reaction temperature, therefore, coking speed energy of the coking heavy oil raw material in boiler tube
Enough it is able to substantially reduce, the operation cycle can be obviously prolonged.As a rule, the heated stove a of the coking heavy oil raw material is pre-
Temperature after heat can be 50-400 DEG C, preferably 300-400 DEG C.The concrete structure of the heating furnace a can be with prior art
Same or similar, therefore not to repeat here.Additionally, the burning in order to promote fuel in heating furnace a, and cause to be produced in heating furnace a
Raw oxygen-containing high-temperature gas can smoothly supplied to coke gasification reaction device b and spraying coking tower c can be set and the heating furnace a
Combustion chamber air blower f.Additionally, when coking heavy oil raw material (such as coming from the coking raw material of fractionating column e bottom of towe)
When temperature has reached preheating temperature, the coking heavy oil raw material can also be heated without the heating furnace a, and directly burnt to spraying
Change tower c chargings.
According to the coking heavy oil equipment that the present invention is provided, the oxygen-containing high-temperature gas is taken off in coke gasification reaction device b
The purpose of oxygen is the possibility in order to prevent coking heavy oil raw material from burning, blast occurring in coking, so as to ensure to use
Security.The oxygen-containing high-temperature gas can be the existing various gases produced by heating furnace a burnings, for example, can be
The flue gas produced by coke powder and/or coking dry gas burning.Additionally, the oxygen content in the deoxidation high-temperature gas for example can be
Below 2 volume %, preferably 0.03-2 volumes %.
The deoxidation high-temperature gas primarily serves the effect of thermal medium, by the coking heavy oil raw material of the atomization state and deoxidation
After high-temperature gas contact, the temperature of the coking heavy oil raw material can be increased to by coking temperature by heat exchange action.Cause
This, as long as the temperature and consumption of the deoxidation high-temperature gas enable to the temperature of the coking heavy oil raw material of the atomization state to rise to
Coking temperature (usually 490-515 DEG C).For example, typically 490-950 DEG C of the temperature of the deoxidation high-temperature gas,
Preferably 550-850 DEG C.
The present invention is not particularly limited to the concrete structure of the coke gasification reaction device b, as long as can be by oxygen-containing High Temperature Gas
Oxygen in body is removed substantially.For example, the coke gasification reaction device b can be gas-solid fluidized bed reactor.As shown in figure 3,
Be filled with the coke gasification reaction device b fluidisation state solid b28, its can be the coke meal and/or coke fines, it is described to contain
Oxygen high-temperature gas 3 is introduced into the coke gasification reaction device b from the bottom of the coke gasification reaction device b and is connect with the fluidisation state solid b28
Touch to carry out redox reaction (oxygen and coke gasification reaction generation CO or CO2And a small amount of water), it is reacted after deoxidation high temperature
Base top contact of the gas 4 from the coke gasification reaction device b.Wherein, the condition of the redox reaction includes that reaction temperature can be with
It it is 450-750 DEG C, reaction pressure can be 0-0.15MPa, and the reaction time can be 0.1-5min.In the present invention, the pressure
Power refers both to gauge pressure.Being seated in coke meal and/or coke fines in the coke gasification reaction device b can be respectively from the spraying
Coking tower c bottoms and/or the cyclone separator d bottoms.Specifically, the coke meal and/or coke fines can be led to
The solid for crossing the coke gasification reaction device b adds mouth b29 to be introduced into the coke gasification reaction device b, the oxygen-containing high-temperature gas and this portion
The effect deoxidation of point coke blacking, while the fugitive constituent in coke blacking enters gas phase, it is reacted after coke meal and/or coke fines
Can be drawn by the solid outlet b31 of the coke gasification reaction device b, it is also possible to continue to stay in coke gasification reaction device b and react.More
Preferably, the coke gasification reaction device b also includes being arranged on below the coke gasification reaction device b and connecting with oxygen-containing high-temperature gas entrance
Logical gas distributor b27, so can not only cause that oxygen-containing high-temperature gas is realized more uniformly being distributed, so as to by oxygen therein
Gas content is down to lower level, but also can consolidate in the fluidisation state during the initial stage of going into operation plays the support coke gasification reaction device b
The effect of body b28.The gas distributor b27 can for it is existing it is various can realize gas it is equally distributed charging distribution
Device, concrete structure is known to the skilled person, and therefore not to repeat here.
The interior bore of the atomizer c18 is preferably 0.5-50mm, so enables to coking heavy oil raw material through atomization
The droplet of size suitable (droplet size is about 20-500 μm) is obtained afterwards, so as to significantly improve the coking heavy oil of unit volume
Contact area between raw material and thermal medium high-temperature gas, increases heat and mass ability, and further improve liquid yield.It is described
The quantity of atomizer c18 can be carried out rationally according to the volume of the spraying coking tower c and the disposal ability of unit interval
Ground selection, for example, when the volume of the spraying coking tower c is bigger, disposal ability of the unit interval is stronger, the atomizer
The quantity of c18 can accordingly increase；When the volume of the spraying coking tower c is smaller, disposal ability of the unit interval is weaker, institute
The quantity for stating atomizer c18 can be reduced accordingly.As a rule, the quantity of the atomizer c18 can be 4-12.It is many
Individual atomizer c18 is preferably evenly distributed through the top of the top straight tube reaction zone c21.Additionally, the atomizer c18 can
To set vertically downward, it is also possible to set diagonally downward, and the acute angle between the axial line and horizontal plane of the atomizer c18
Angle can be 10-90 DEG C.The concrete structure of the atomizer c18 is known to the skilled person, and therefore not to repeat here.
According to the coking heavy oil equipment that the present invention is provided, it is preferable that the spraying coking tower c also includes being located at being arranged on institute
State gas distribution grid c30, the gas distribution grid c30 at the top of straight tube reaction zone c21 and connected with the hot-wind inlet c24
For carrying out gas distribution before the deoxidation high-temperature gas 4 is introduced into the spraying coking tower c, so enable to described de-
Oxygen high-temperature gas 4 is uniformly distributed in the spraying coking tower c, so as to further increase and the coking heavy oil raw material of atomization between
Contact area, and improve liquid yield.The concrete structure of the gas distribution grid c30 can with the coking reactor b in
Gas distributor b27 it is identical, and can be this area conventional selection, therefore not to repeat here.
According to the coking heavy oil equipment that the present invention is provided, it is preferable that the spraying coking tower c also includes being arranged on the side
To the chev(e)ron baffle c20 directly over outlet c19, and the chev(e)ron baffle c20's is opening down, is so prevented from generation
Coke granule be deposited on the induced duct of side outlet c19.The present invention does not have to the angle and length of the chev(e)ron baffle c20
Have and especially limit, as long as the coke granule for being prevented from generation is deposited on the induced duct of side outlet c19.For example,
The angle β of the chev(e)ron baffle c20 can be 10-150 °, preferably 30-100 °.The angle of the chev(e)ron baffle c20 sets
Put angle of repose of the angle between baffle surface to be caused and horizontal plane less than coke meal.Additionally, the side outlet c19 and
Chev(e)ron baffle c20 can be arranged on the junction of the top straight tube reaction zone c21 and bottom cone collecting region c22.
The present invention is not particularly limited to the size of the coking heavy oil equipment.For example, the spraying coking tower c's is upper
The ratio of height to diameter of portion straight tube reaction zone c21 can be 2-10:1, preferably 2-8:1.The cone angle of the bottom cone collecting region c22
It can be 10-150 °, preferably 70-120 °.Additionally, the hot-wind inlet c24 and side outlet c19 diameters can be ability
The conventional selection in domain, therefore not to repeat here.
Additionally, the spraying coking tower c's and cyclone separator d has been respectively arranged below coke meal collecting tank k and Jiao
Charcoal fines collection tank m, coke meal collecting tank k is fallen into from the spraying coking tower c by the coke meal that self gravitation is settled
In, and pass through the coke fines that cyclone separator d isolates and fall into coke fines collecting tank m.Additionally, being received to improve liquid
Rate, it is preferable that the first stripped vapor 7 and second can be each led into coke meal collecting tank k and coke fines collecting tank m
Stripped vapor 9, can so purge to the coke granule for generating, and the oil gas for being adsorbed is stripped off, Jiao after stripping
Charcoal meal and a coke fines part are transported to conduct fluidisation state solid b28, remainder equipment leading out in coke gasification reaction device b
Or as the fuel of heating furnace a.
The present invention is not particularly limited to the condition of the pyrogenetic reaction, for example, the condition of the pyrogenetic reaction is usual
It can be 490-515 DEG C, preferably 495-505 DEG C including coking temperature；Coking pressure can for -0.01MPa to 0.1MPa, it is excellent
Elect -0.01MPa to 0MPa as；Scorch time can be 0.01-20min, preferably 0.1-5min.Additionally, the spraying coking
The negative-pressure operation of tower c is conducive to the raising of product liquid yield.Wherein, the internal pressure of the spraying coking tower c can pass through
The rotating speed of the air-introduced machine h being arranged on the pipeline of connection cyclone separator d and fractionating column e is adjusted.
According to the coking heavy oil equipment that the present invention is provided, in order to by the preheated smooth delivery of power of coking heavy oil raw material 2 to position
Feed(raw material)inlet c25 at the top of the spraying coking tower c, can connect the pipe between the heating furnace a and spraying coking tower c
Pump g is set on line.
The present invention is not particularly limited to the species of the cyclone separator d, as long as can be by coke fines and oil gas
Separated, so as to obtain coke fines in the bottom of the cyclone separator d, top obtains oil gas, specially ability
Known in field technique personnel, therefore not to repeat here.
A kind of specific embodiment of the invention, as shown in figure 4, the coke gasification reaction device b, spraying coking tower c and
Cyclone separator d is of coupled connections, and now, the coke gasification reaction device b is gas-solid fluidized bed reactor.Come self-spray coking tower c and
Coke granule after being stripped respectively through the first stripped vapor 7 and the second stripped vapor 9 of cyclone separator d bottoms is introduced directly into
In the coke gasification reaction device b as fluidisation state solid b28, oxygen-containing high-temperature gas 3 from coke gasification reaction device b bottoms introduce and with it is described
The b28 contacts of fluidisation state solid are drawn through the deoxidation high-temperature gas after deoxidation with carrying out deoxidation from the top of the coke gasification reaction device b
Go out, and exchanged heat with preheated coking heavy oil raw material 2 in entrance spraying coking tower c.
Main theing improvement is that of the invention has increased the coke gasification reaction device b and cyclone separator d newly and to coking tower c
Internal structure improved, and the fractionating column e structurally and operationally can be with same as the prior art.For example, such as Fig. 1 institutes
Show, the oil gas 10 from the cyclone separator d is fractionated into coking dry gas, liquefied gas, coker gasoline, coking in fractionating column e
Diesel oil and wax tailings, i.e. be correspondingly provided with coking dry gas outlet e11, liquefied gas outlet e12, Jiao on the fractionating column e respectively
Change fuel dispensing outlet e13, coker gas oil outlet e14 and wax tailings outlet e15.The coking dry gas can be as heating furnace a's
Fuel and be back in the combustion chamber of heating furnace a, also can outward arrange and be incorporated in pipe network n.
According to the coking heavy oil equipment that the present invention is provided, it is preferable that the fractionating column e also includes being arranged on the fractionating column
The reactor outer circulation pipeline of e bottoms, for recycle column bottom withdrawing oil 16, can so play during wash-out is introduced into the oil gas of fractionating column e and press from both sides
The effect of the coke fines do not isolated by cyclone separator d of band.It is highly preferred that be additionally provided with the reactor outer circulation pipeline changing
Hot device.
According to the coking heavy oil equipment that the present invention is provided, it is preferable that the side-lower of the fractionating column e is provided with feedstock oil and enters
Mouthful e1, and the bottom of the fractionating column e connects with the radiant heating area of the heating furnace a, coking heavy oil raw material is from the raw material
After oil-in e1 is introduced into and is contacted with bottom of towe withdrawing oil 16 and coking oil gas to capture the coke fines remained in oil gas, as
Coking raw material 17 drawn from the bottom of the fractionating column e and into being preheated in the radiant heating area of the heating furnace a (if
The temperature of coking raw material 17 has reached preheating temperature, then can directly enter the coking raw material 17 to spraying coking tower c
Material), the accumulation of coke fines in fractionating column e can not only be so prevented, but also the thermal source in fractionating column can be made full use of
Coking raw material is heated, great prospects for commercial application.
According to the coking heavy oil equipment that the present invention is provided, it is preferable that be provided with coking dry gas at the top of the fractionating column e and go out
Mouth e11, and the coking dry gas export the combustion chamber of the e11 and heating furnace a, the coking dry gas that will be isolated are used as institute
State the fuel of heating furnace a combustion chambers and generate the oxygen-containing high-temperature gas, can so realize effective utilization of raw material.
The coking heavy oil raw material can be various coking heavy oil raw materials commonly used in the art, for example, can be decompression
Residual oil, reduced crude, heavy crude, de-oiled asphalt, residual hydrogenation heavy oil, thermal cracking heavy oil, the tapped oil of lube oil finishing, urge
In recycle oil and clarified oil, the tar of cracking of ethylene, coal tar, shale oil, oil-sand heavy oil, bitumen of change cracking etc. extremely
Few one kind.
The fine particle coke of the spraying coking tower c outputs is mainly the coke of spheroidal, the diameter one of coke granule
As be 0.001-1mm.The mobility of these spheroidal coke preferably, can be easier and rapidly from spraying coking tower c rows
Go out.Wherein, the particle diameter of the coke meal that can be deposited on the spraying coking tower c bottoms by self gravitation can be 0.01-
1mm, preferably 0.02-1mm；And need can be with the particle diameter of the coke fines of Oil-gas Separation by cyclone separator d
0.001-0.1mm, preferably 0.001-0.05mm.It is possible to be stained with a small amount of coke on the inwall of the spraying coking tower c
Particle adhesion thing, can be removed in shut-down (breakdown) mainteance using conventional hydraulic decoking method.
Below will the present invention will be described in detail by embodiment.
Coking heavy oil equipment used in following examples as Figure 1-3, including：Heating furnace a, coke gasification reaction device b, spray
Mist coking tower c, cyclone separator d and fractionating column e；The coke gasification reaction device b is gas-solid fluidized bed reactor, wherein the stream for loading
Change the mixture that state solid b28 is coke meal and coke fines；The spraying coking tower c includes interconnected top straight tube
Reaction zone c21 and bottom cone collecting region c22, be arranged at the top of the top straight tube reaction zone c21 and with spraying coking tower c
Feed(raw material)inlet c25 connection set vertically downward atomizer c18 (in nozzle bore be 1mm, quantity be 6, described
Be uniformly arranged at the top of top straight tube reaction zone c21), be arranged at the top of the straight tube reaction zone c21 and with spraying coking tower c
Hot-wind inlet c24 connections gas distribution grid c30, be arranged on top straight tube reaction zone c21 and cone collecting region c22 in bottom connects
The side outlet c19 at the place of connecing and it is arranged on directly over side outlet c19 and downward opening chev(e)ron baffle c20 (angle β
It is 90 °), the ratio of height to diameter of the top straight tube reaction zone c21 of the spraying coking tower c is 5:1 (being highly 10m, internal diameter is 2m), under
The cone angle of portion cone collecting region c22 is 60 °, a diameter of 400mm of hot-wind inlet c24, and side outlet c19's is a diameter of
300mm；Coking dry gas outlet e11 is provided with the top of the fractionating column e, bottom is provided with reactor outer circulation pipeline, and side-lower is set
There is raw material oil-in e1, and the bottom of the fractionating column e connects with the radiant heating area of the heating furnace a, coking dry gas outlet
The combustion chamber of e11 and heating furnace a.
In following examples and comparative example：
Feedstock oil is same residual oil (its property is shown in Table 1), and inlet amount is 25kg/h；It is in fractionating column e that bottom of towe is normal
The cut that more than 460 DEG C of pressure boiling point is extracted out as bottom of towe withdrawing oil；Recycle ratio refers to the non-fresh feedstock oil portion in fractionating column base oil
Divide the weight ratio with fresh feed oil part；Collecting tank below spraying coking tower c and cyclone separator d is passed through stripped vapor
STRENGTH ON COKE particle purged after discharging again.
Embodiment 1-3
Embodiment 1-3 is used to illustrate the method that the coking heavy oil equipment provided using the present invention carries out coking heavy oil.
Feedstock oil is introduced into fractionating column e from the raw material oil-in e1 of fractionating column e, and and then from the tower of the fractionating column e
Bottom is preheated in being introduced into the radiant heating area of heating furnace a, and preheated feedstock oil introduces the spraying via feed(raw material)inlet c25
It is atomized in coking tower c and by atomizer c18, is obtained 20-500 μm of atomization state droplet, the combustion from heating furnace a
The oxygen-containing high-temperature gas 3 obtained through the coking dry gas that burn for burning room carries out deoxidation by coke gasification reaction device b, through the deoxidation after deoxidation
High-temperature gas 4 (wherein oxygen content is 0.1 volume %) introduces spray by being located at the hot-wind inlet c24 at the top of spraying coking tower c
Contacted in mist coking tower c and with above-mentioned atomization state droplet, so that the atomization state droplet reaches coking temperature and carries out Jiao
Change reaction, the coke meal (particle diameter is 0.02-1mm) in pyrogenetic reaction product is by settlement from bottom cone collecting region
C22 bottom collections, the mixture 6 of oil gas and coke fines (particle diameter is 0.001-0.05mm) in coke gasification reaction product is from lateral
Outlet c19 is introduced into cyclone separator d the separation for carrying out oil gas and coke fines, and the oil gas 10 from cyclone separator d is introduced
Fraction seperation is carried out in fractionating column e, the coking dry gas that tower top is isolated are used as the fuel of heating furnace a combustion chambers and generate oxygen-containing
High-temperature gas 3, in fractionating column e bottoms, carrys out the oil gas 10 of self-spray coking tower c with bottom of towe withdrawing oil 16 and from raw material oil-in
Coking raw material 17 is formed after the feedstock oil heat exchange of e1, the coking raw material 17 is circulated as coking heavy oil raw material from the fractionating column e
Bottom of towe be introduced into the radiant heating area of heating furnace a in preheated.Wherein, reaction condition is as shown in table 2, as a result as shown in table 3.
Comparative example 1
The comparative example is used for the method for illustrating to carry out delayed coking using existing delayed coking equipment.
Delayed coking equipment used by the comparative example includes：Heating furnace, coking tower and fractionating column；The inside of the coking tower
It is hollow structure；The bottom of fractionating column is provided with reactor outer circulation pipeline, and side-lower is provided with raw material oil-in, and the fractionating column
Bottom connects with the heating furnace.Feedstock oil is introduced into fractionating column from the raw material oil-in of fractionating column, and and then from described point
Evaporate tower bottom of towe be introduced into the radiant heating area of heating furnace in be heated to coking temperature, be introduced into coking tower that to carry out coking anti-afterwards
Should, pyrogenetic reaction product is then carried out into fraction seperation in fractionating column.In fractionation column base, oil gas and tower from coking tower
Coking raw material is formed after bottom withdrawing oil and the heat exchange of the feedstock oil from raw material oil-in, the coking raw material is circulated as coking heavy oil
Raw material is used for pyrogenetic reaction.Wherein, reaction condition is as shown in table 2, as a result as shown in table 3.
Table 1
| Project name | Index |
| Density (20 DEG C), kg/m3 | 1009 |
| Sulfur content, weight % | 3 |
| Carbon residue content, weight % | 20.0 |
| Pour point, DEG C | >50℃ |
| Composition, w% | |
| Saturated hydrocarbon content, weight % | 17.0 |
| Arene content, weight % | 55.1 |
| Resin and asphalt total content, weight % | 27.6 |
| Content of beary metal, μ g/g | |
| Ni | 57.1 |
| V | 601 |
Table 2
| Project name | Embodiment 1 | Embodiment 2 | Embodiment 3 | Comparative example 1 |
| Furnace outlet raw material oil temperature, DEG C | 300 | 400 | 350 | 491 |
| Furnace outlet gas temperature, DEG C | 830 | 620 | 650 | - |
| Recycle ratio | 0.13 | 0.13 | 0.13 | 0.19 |
| Spraying coking tower enters gas flow, m3/min | 30 | 20 | 25 | - |
| Spraying coking tower oil inlet quantity, kg/min | 0.41 | 0.41 | 0.41 | - |
| Spraying coking tower hot-wind inlet temperature, DEG C | 829 | 618 | 649 | - |
| Coking temperature, DEG C | 505 | 490 | 491 | 491 |
| Spraying coking tower tower top pressure, MPa | -0.01 | 0.02 | -0.005 | - |
| Coke drum tower top pressure in comparative example, MPa | - | - | - | 0.13 |
| Residence time of the coking raw material in coking tower | 120s | 120s | 120s | 15.9h |
Table 3
Note：In table 3, liquid yield is the total recovery of coker gasoline, coker gas oil and wax tailings.
As can be seen from the above results, the coking heavy oil equipment that the present invention is provided can not only be reduced in heating furnace tube
Coking, but also liquid yield can be improved, great prospects for commercial application.
The preferred embodiment of the present invention described in detail above, but, the present invention is not limited in above-mentioned implementation method
Detail, in range of the technology design of the invention, various simple variants can be carried out to technical scheme, this
A little simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned specific 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 is no longer separately illustrated.
Additionally, can also be combined between a variety of implementation methods of the invention, 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 (11)
1. a kind of coking heavy oil equipment, it is characterised in that the coking heavy oil equipment includes heating furnace (a), coke gasification reaction device
B (), spraying coking tower (c), cyclone separator (d) and fractionating column (e), spraying coking tower (c) are upper including what is be interconnected
Portion's straight tube reaction zone (c21) and bottom cone collecting region (c22), be arranged at the top of the top straight tube reaction zone (c21) and
The atomizer (c18) and side outlet (c19) connected with the feed(raw material)inlet (c25) of spraying coking tower (c)；Heavy oil
Coking raw material is preheated in the radiant heating area of the heating furnace (a), and preheated coking heavy oil raw material is via the original
Material entrance (c25) is introduced into spraying coking tower (c) and is atomized by the atomizer (c18), is added from described
The oxygen-containing high-temperature gas of the combustion chamber of hot stove (a) carries out deoxidation by coke gasification reaction device (b), through the deoxidation high temperature after deoxidation
Gas is introduced into spraying coking tower (c) and and mist by the hot-wind inlet (c24) at the top of spraying coking tower (c)
Change the coking heavy oil raw material contact of state, so that the coking heavy oil raw material of the atomization state reaches coking temperature and to carry out coking anti-
Should, the coke meal in pyrogenetic reaction product from bottom cone collecting region (c22) bottom collection, in coke gasification reaction product
Oil gas and coke fines are introduced into the cyclone separator (d) from the side outlet (c19) carries out oil gas and coke fines
Separate, the oil gas from the cyclone separator (d) carries out fraction seperation in being introduced into the fractionating column (e).
2. coking heavy oil equipment according to claim 1, wherein, the interior bore of the atomizer (c18) is 0.5-
50mm。
3. coking heavy oil equipment according to claim 2, wherein, the atomizer (c18) sets or inclines vertically downward
Set obliquely, and acute angle between the axial line and horizontal plane of the atomizer (c18) is 10-90 DEG C.
4. coking heavy oil equipment according to claim 1, wherein, spraying coking tower (c) also includes being arranged on described
Gas distribution grid (c30) at the top of straight tube reaction zone (c21) and being connected with the hot-wind inlet (c24), the gas distribution
Plate (c30) is used to for the deoxidation high-temperature gas to carry out gas distribution.
5. the coking heavy oil equipment according to any one in claim 1-4, wherein, spraying coking tower (c) is also wrapped
Include the chev(e)ron baffle (c20) being arranged on directly over the side outlet (c19), and the chev(e)ron baffle (c20) opening
Down, the induced duct of the side outlet (c19) is deposited in for the coke granule for preventing generation.
6. coking heavy oil equipment according to claim 5, wherein, the angle β of the chev(e)ron baffle (c20) is 10-
150°。
7. the coking heavy oil equipment according to any one in claim 1-4, wherein, spraying coking tower (c) it is upper
The ratio of height to diameter in portion's straight tube reaction zone (c21) is 2-10:1, the cone angle of the bottom cone collecting region (c22) is 10-150 °.
8. the coking heavy oil equipment according to any one in claim 1-4, wherein, coke gasification reaction device (b) is gas
Solid fluidized bed reactor；Fluidisation state solid (b28) of filling is the coke meal and/or Jiao in coke gasification reaction device (b)
Charcoal fine powder, the oxygen-containing high-temperature gas be introduced into coke gasification reaction device (b) from the bottom of coke gasification reaction device (b) in it is described
Fluidisation state solid (b28) contact to carry out redox reaction, it is reacted after deoxidation high-temperature gas from the coke gasification reaction device
The Base top contact of (b).
9. the coking heavy oil equipment according to any one in claim 1-4, wherein, the fractionating column (e) also includes setting
The reactor outer circulation pipeline in fractionating column (e) bottom is put, for recycle column bottom withdrawing oil.
10. coking heavy oil equipment according to claim 9, wherein, the side-lower of the fractionating column (e) is provided with feedstock oil
Entrance (e1), and the bottom of the fractionating column (e) connects with the radiant heating area of the heating furnace (a).
The 11. coking heavy oil equipment according to any one in claim 1-4, wherein, set at the top of the fractionating column (e)
Coking dry gas outlet (e11), and coking dry gas outlet (e11) and the combustion chamber of the heating furnace (a) are equipped with, will be divided
The coking dry gas for separating out are used as the fuel of the heating furnace (a) and generate the oxygen-containing high-temperature gas.
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| CN107974273B (en) * | 2016-10-25 | 2021-02-09 | 中国石油化工股份有限公司 | Heavy oil viscosity reducing method |
| CN107974272B (en) * | 2016-10-25 | 2020-06-16 | 中国石油化工股份有限公司 | Heavy oil viscosity reducing equipment and heavy oil viscosity reducing method |
| CN106833717A (en) * | 2017-03-05 | 2017-06-13 | 刘金凤 | A kind of fractionation apparatus for heavy oil sophisticated category |
| CN109777468B (en) * | 2017-11-14 | 2021-07-09 | 中国石油化工股份有限公司 | Processing method of high-viscosity heavy oil |
| CN109777467B (en) * | 2017-11-14 | 2021-05-04 | 中国石油化工股份有限公司 | Processing method for reducing viscosity of high-viscosity oil |
| CN111603884A (en) * | 2020-06-22 | 2020-09-01 | 中国石油化工股份有限公司 | System and method for effectively removing impurities carried in catalytic dry gas in ethylbenzene preparation process |
| CN113381263B (en) * | 2021-08-11 | 2021-10-15 | 南通斯高蕊机械设备有限公司 | Intelligent production device of high-uniformity carbon brush |
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| EP0520977A2 (en) * | 1991-06-25 | 1992-12-30 | Oberösterreichische Ferngas Aktiengesellschaft | Process and apparatus for the low temperature carbonization of at least partially organic waste |
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