CN105586077A - Heavy oil coking equipment - Google Patents
Heavy oil coking equipment Download PDFInfo
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- CN105586077A CN105586077A CN201410562515.0A CN201410562515A CN105586077A CN 105586077 A CN105586077 A CN 105586077A CN 201410562515 A CN201410562515 A CN 201410562515A CN 105586077 A CN105586077 A CN 105586077A
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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, and the whole world is clean to lightweightThe demand rapid growth of fuel oil, adds environmental requirement increasingly strict, makes heavy oil deep processing technologyBecome the emphasis of petroleum refining industry of world today development. Particularly inferior heavy oil density is large, viscosity is high, weightTenor is high, sulfur content is high, nitrogen content is high, resin and asphalt content high, gives crude oilProcessing (the especially secondary operations of heavy oil) has brought larger difficulty. The current raising heavy oil transformation degree of depth,The earned value techniques that increases light-end products output still mainly relies on coking, RFCC and residual hydrogenation placeThe techniques such as reason. Wherein, coking is that to take off charcoal technique be that main inferior heavy oil (particularly residual oil) transformsPrimary means. And delay coking process has that de-charcoal is thorough, flow process simple, technology maturation, plant investmentThe feature such as lower, has become one of important process of processing of heavy oil.
Delayed coking is a kind of heat processing technique of degree of depth thermal cracking, can be that coking is dry by heavy oil transformationThe products such as gas, liquefied gas, coker gasoline, coker gas oil, wax tailings, coke. Conventionally coking vapourThe yield sum of oil, coker gas oil and wax tailings is as the liquid yield of delayed coking, and liquid yield isThe most important technical-economic index of coking process. The conventional main flow process of delay coking process is: heavy oil existsIn the radiating furnace tube of heating furnace, be warmed up to coking temperature (being generally 490-515 DEG C of left and right) by Fast HeatingAfter, enter coke drum from the bottom of coke drum, in coke drum, carry out pyrogenetic reaction, the coke of generation staysIn coke drum, the oil gas of generation is overflowed to enter fractionating column from top of coke tower and is carried out fractionation, obtains cokingRecycle oil at the bottom of gas (comprising coker gasoline), coker gas oil, wax tailings and tower. Wherein, coke drumBe generally two, two coke drums use in turn, and one of them carries out decoking after being full of coke, hot logisticsSwitch to another coke drum and carry out pyrogenetic reaction. The coke generating in coke drum is monoblock shape, mainly dividesFor the higher needle coke of economic worth, general sponge coke and poor shot coke, transition coke. Decoking mistakeJourney mainly comprises that reduce coke temperature in tower little steamed out, steamed out greatly, cold Jiao (note cooling water), draining,Remove coke in tower unload top cover and bottom, hole and cut Jiao's (with giant), upper top cover and bottom,Warm tower (logical steam) etc.
Processing heavy oil is tending towards in poor quality at present, and the increase of carbon residue, asphalitine and tenor etc. is prolongedThe operation of coking plant has late brought challenge, and not only product distribution variation, liquid yield reduce, Er QieyuanThe coking of material in heating furnace tube further aggravates, and directly has influence on the long-term operation of device. In addition,The decoking process of delayed coking coke drum belongs to intermittently operated, and its program is many, and length consuming time also can produce largeAmount sewage, has not only increased the energy consumption and the running cost that install, also environment has been caused to immense pressure.
In order to improve the liquid yield of delayed coking and to extend the on-stream time of delayed coking, petroleum refining is groundThe person of studying carefully has researched and developed relevant technology.
For example, CN1599784A discloses a kind of delay of producing anisotropy free-flowing shot cokeCoking method, the method comprises vacuum residuum feed and oxidant is connect at the temperature of about 150-325 DEG CTouch, then enter heating furnace and be heated to the required temperature of coking, then in coke drum, generate anisotropyFree-pouring shot coke. Although the method can obtain shot coke, and save coke cleaning step,But because needing elder generation to contact with oxidant before entering heating furnace, vacuum residuum feed there is oxidation insteadAnswer and condensation reaction, therefore can further aggravate the coking of heating furnace tube, thereby affect continuous lifeProduce, this technique is difficult to industrialization.
CN101619237A and CN101619238A disclose delayed coking and vacuum distillation process phaseIn conjunction with technique, improved the liquid yield of delayed coking unit, improved the character of heavy wax tailings.But the method still needs delayed coking raw material to be directly heated in heating furnace tube coking temperatureDegree, therefore, has aggravated the coking of boiler tube, thereby can shorten the on-stream time of device.
In addition, in order to slow down the coking of delayed coker unit furnace boiler tube, petroleum refining researcher researchWith developed relevant technology. Research shows, in delayed coking raw material, adds diluent, freedomBase inhibitor, arene coking inhibitor, anti-coking agent etc. can suppress heating-furnace to a certain extentThe coking of pipe, extend on-stream time, but mode of heating all belongs to indirect mode conventionally (by addingHot stove boiler tube tube wall heat exchange heating), the thermal efficiency is low, and therefore boiler tube green coke problem can efficient solution not determined,And liquid yield does not have essence to promote, coke drum decoking environmental issue is still outstanding.
In sum, need at present a kind of coking behavior that can either improve heating furnace tube of exploitation badly, again canEnough improve the coking heavy oil equipment of liquid yield.
Summary of the invention
The object of the invention is can not realize improvement heating in order to overcome existing delayed coking equipment simultaneouslyThe coking behavior of stove boiler tube also improves the defect of liquid yield, and a kind of new coking heavy oil equipment is provided.
Particularly, coking heavy oil equipment provided by the invention comprises heating furnace, coke gasification reaction device, spraying JiaoChange tower, cyclone separator and fractionating column, described spraying coking tower comprises the top straight tube reaction being interconnectedDistrict and bottom cone collecting region, be arranged on straight tube reaction zone top, described top and with described spraying cokingAtomizer and side outlet that the feed(raw material)inlet of tower is communicated with; Coking heavy oil raw material is at described heating furnaceRadiation heating district in carry out preheating, introduce institute through the coking heavy oil raw material of preheating via described feed(raw material)inletState in spraying coking tower and carry out atomization by described atomizer, from the combustion chamber of described heating furnaceCarry out deoxidation containing oxygen high-temperature gas by described coke gasification reaction device, the deoxidation high-temperature gas after deoxidation passes throughThe hot-wind inlet that is arranged in described spraying coking tower top is introduced described spraying coking tower and with atomization stateThe contact of coking heavy oil raw material, so that the coking heavy oil raw material of described atomization state reaches coking temperature and carries out JiaoChange reaction, the coke meal in pyrogenetic reaction product is collected from described bottom cone collecting region bottom, cokeOil gas in product and coke fine powder are introduced described cyclone separator and are carried out from described side outletOil gas separates with coke fine powder, introduces in fractionating column and carries out cut from the oil gas of described cyclone separatorSeparate.
The discovery of the present inventor after further investigation, existing delayed coking equipment only wraps conventionallyDraw together heating furnace, coking tower and fractionating column, in actual production process, coking heavy oil raw material is at heating furnaceIn radiation heating district through the heat exchange of boiler tube tube wall and indirect to coking temperature, afterwards again by heating after liquidThe coking heavy oil raw material of state is introduced coking tower to carry out pyrogenetic reaction, finally by coking at the bottom of coking tower towerProduct is carried out cut separation in fractionating column. But, adopt this indirect (by boiler tube pipeWall heat exchange) mode and directly by coking heavy oil raw material one-time heating to coking temperature and heavy oil JiaoThe mode that change raw material carries out coking with liquid form not only easily causes the coking in heating furnace tube, andAnd liquid yield is also lower.
And coking heavy oil equipment provided by the invention by newly-increased described coke gasification reaction device, spraying coking tower andCyclone separator, not only can reduce the coking in heating furnace tube, but also can improve liquid yield.Concrete principle is as follows: on the one hand, and when coking heavy oil equipment provided by the invention is reacted for coking heavy oil,Heating furnace only plays the effect of preheating coking heavy oil raw material, and do not need the existing coking heavy oil equipment of pictureHeating furnace equally by coking heavy oil heating raw materials to coking temperature (being generally 490-515 DEG C), pyrogenetic reactionThermal source carry and enter by high-temperature gas, described high-temperature gas is in spraying coking tower directly and after preheatingCoking heavy oil raw material contact and reach coking temperature, therefore, can significantly reduce the knot of heating furnace tubeBurnt; On the other hand, the atomizer arranging in described spraying coking tower can disperse coking heavy oil raw materialBecome tiny oil droplet, enlarge markedly the contact-making surface between coking heavy oil raw material and the high-temperature gas of unit volumeLong-pending, and spraying coking tower can negative-pressure operation, thus not only can make the biography of whole pyrogenetic reaction processHeat energy power greatly strengthens, green coke amount reduces, liquid yield increases, and the coke generating is to have necessarilySize distribution can fluidized particles, easily fluidisation is carried, and has saved coke cleaning step, has saved expense and timeCost, production process does not have decoking waste water, has reduced treatment step and the intractability of follow-up waste water. ThisOutward, described coke gasification reaction device can reduce the oxygen content in high-temperature gas as early as possible, prevents the coking tower of sprayingThe possibility of burning, exploding, has ensured the security using.
Other features and advantages of the present invention are described in detail the detailed description of the invention part subsequently.
Brief description of the drawings
Accompanying drawing is to be used to provide a further understanding of the present invention, and forms a part for description, withDetailed description of the invention one is below used from explanation the present invention, but is not construed as limiting the invention. ?In accompanying drawing:
The structural representation of the coking heavy oil equipment that Fig. 1 provides for a kind of detailed description of the invention of the present invention;
The structural representation of the spraying coking tower that Fig. 2 provides for a kind of detailed description of the invention of the present invention;
The structural representation of the coke gasification reaction device that Fig. 3 provides for a kind of detailed description of the invention of the present invention;
The part-structure signal of the coking heavy oil equipment that Fig. 4 provides for a kind of detailed description of the invention of the present inventionFigure.
Description of reference numerals
A-heating furnace; B-coke gasification reaction device; B27-gas distributor; B28-fluidisation state solid; B29-solidAdd entrance; B31-solid discharging opening; The c-coking tower of spraying; C18-atomizer; C19-side outlet; C20-Chev(e)ron baffle; C21-top straight tube reaction zone; C22-bottom cone collecting region; C24-hot-wind inlet; C25-Feed(raw material)inlet; C30-gas distribution grid; D-cyclone separator; E-fractionating column; E1-feedstock oil entrance; E11-The outlet of coking dry gas; The outlet of e12-liquefied gas; The outlet of e13-coker gasoline; The outlet of e14-coker gas oil; E15-Wax tailings outlet; N-pipe network; K-coke meal collecting tank; M-coke fines collection tank; G-pump; F-Air blast; H-air-introduced machine; 2-is through the coking heavy oil raw material of preheating; 3-is containing oxygen high-temperature gas; 4-deoxidation is highWet body; The mixture of 6-oil gas and coke fine powder; 7-the first stripped vapor; 9-the second stripped vapor;10-oil gas; Withdrawing oil at the bottom of 16-tower; 17-coking raw material.
Detailed description of the invention
Below the specific embodiment of the present invention is elaborated. Should be understood that, retouch in this placeThe detailed description of the invention of stating only, for description and interpretation the present invention, is not limited to the present invention.
In the present invention, in the situation that not doing contrary explanation, the noun of locality of use as " upper and lower, left,Right " typically refer to the direction of coking heavy oil equipment of the present invention under working condition, namely institute in accompanying drawingThe direction of showing.
As depicted in figs. 1 and 2, coking heavy oil equipment provided by the invention comprises that heating furnace a, coke are anti-Answer device b, spraying coking tower c, cyclone separator d and fractionating column e, described spraying coking tower c comprises phaseIntercommunicated top straight tube reaction zone c21 and bottom cone collecting region c22, be arranged on described top straight tubeAtomizer reaction zone c21 top and that be communicated with the feed(raw material)inlet c25 of described spraying coking tower cC18 and side outlet c19; Coking heavy oil raw material carries out in the radiation heating district of described heating furnace aPreheating, introduces described spraying coking tower through the coking heavy oil raw material 2 of preheating via described feed(raw material)inlet c25In c and by described atomizer c18, carry out atomization, from the combustion chamber of described heating furnace a containing oxygenHigh-temperature gas 3 carries out deoxidation by described coke gasification reaction device b, and the deoxidation high-temperature gas 4 after deoxidation is logicalCross the hot-wind inlet c24 that is arranged in described spraying coking tower c top introduce described spraying coking tower c and withThe coking heavy oil raw material contact of atomization state, so that the coking heavy oil raw material of described atomization state reaches coking temperatureAnd carrying out pyrogenetic reaction, the coke meal in pyrogenetic reaction product is from the bottom of described bottom cone collecting region c22Portion collects, and the mixture 6 of the oil gas in coke gasification reaction product and coke fine powder is from described side outlet c19Introduce in described cyclone separator d and carry out separating of oil gas and coke fine powder, from described cyclone separatorThe oil gas 10 of d is introduced in described fractionating column e and is carried out cut separation.
Described heating furnace a mainly plays two effects, and the one, former at its radiation heating district preheating coking heavy oilMaterial, the 2nd, provide containing oxygen high-temperature gas in its combustion chamber. Because the boiler tube of heating furnace a only plays pre-thermogravimetricThe effect of oil coking raw material, and do not need described coking heavy oil heating raw materials to cracking reaction temperature, because ofThis, the coking speed of coking heavy oil raw material in boiler tube can be able to obvious reduction, and the operation cycle can obtainObviously to extend. As a rule, the temperature of described coking heavy oil raw material after heating furnace a preheating can be50-400 DEG C, is preferably 300-400 DEG C. The concrete structure of described heating furnace a can with prior art phaseSame or similar, therefore not to repeat here. In addition in order to promote the burning of fuel in heating furnace a, and make,What in heating furnace a, produce can be supplied to coke gasification reaction device b and spraying coking smoothly containing oxygen high-temperature gasTower c, can arrange the air blast f being communicated with the combustion chamber of described heating furnace a. In addition, work as coking heavy oilFor example, when the temperature of raw material (come from fractionating column e tower at the bottom of coking raw material) has reached preheat temperature,Described coking heavy oil raw material also can heat without described heating furnace a, and directly to spraying coking tower c charging.
According to coking heavy oil equipment provided by the invention, by described containing oxygen high-temperature gas at coke gasification reaction device bIn carry out deoxidation object in coking, burn, explode in order to prevent coking heavy oil raw materialPossibility, thus the security using ensured. Described can be existing various by adding containing oxygen high-temperature gasThe gas that hot stove a burning produces for example, can be the flue gas being produced by coke powder and/or coking dry combustion gas.In addition, the oxygen content in described deoxidation high-temperature gas can be for example, below 2 volume %, to be preferably0.03-2 volume %.
Described deoxidation high-temperature gas mainly plays the effect of thermal medium, by former the coking heavy oil of described atomization stateAfter material contacts with deoxidation high-temperature gas, can be by the temperature of described coking heavy oil raw material by heat exchange actionDegree is increased to coking temperature. Therefore, as long as the temperature of described deoxidation high-temperature gas and consumption can make instituteThe temperature of stating the coking heavy oil raw material of atomization state rises to coking temperature (being generally 490-515 DEG C).For example, the temperature of described deoxidation high-temperature gas can be 490-950 DEG C conventionally, is preferably 550-850 DEG C.
The present invention is not particularly limited the concrete structure of described coke gasification reaction device b, as long as can will containOxygen in oxygen high-temperature gas is removed substantially. For example, described coke gasification reaction device b can be gas-solid flowFluidized bed reactor. As shown in Figure 3, in described coke gasification reaction device b, be filled with fluidisation state solid b28, itsCan be described coke meal and/or coke fine powder, the described oxygen high-temperature gas 3 that contains be from described coke gasification reaction deviceThe bottom of b is introduced in described coke gasification reaction device b and is also contacted to be oxidized with described fluidisation state solid b28(oxygen and coke gasification reaction generate CO or CO in former reaction2And a small amount of water), high through reacted deoxidationWet body 4 is from the Base top contact of described coke gasification reaction device b. Wherein, the condition of described redox reactionComprise that reaction temperature can be 450-750 DEG C, reaction pressure can be 0-0.15MPa, and the reaction time canThink 0.1-5min. In the present invention, described pressure all refers to gauge pressure. Be seated in described coke gasification reaction device bMiddle coke meal and/or coke fine powder can come from respectively described spraying coking tower c bottom and/or described inCyclone separator d bottom. Particularly, described coke meal and/or coke fine powder can be passed through to described JiaoThe solid of charcoal reactor b adds entrance b29 to be introduced in described coke gasification reaction device b, described containing oxygen high-temperature gasWith this part coke blacking effect deoxidation, the fugitive constituent in coke blacking enters gas phase simultaneously, through reacted JiaoCharcoal meal and/or coke fine powder can be drawn by the solid discharging opening b31 of described coke gasification reaction device b, alsoCan continue to stay in coke gasification reaction device b and react. More preferably, described coke gasification reaction device b also comprises and establishingPut below described coke gasification reaction device b and with the gas distributor being communicated with containing oxygen high-temperature gas entranceB27, so not only can make to realize more equably and distributing containing oxygen high-temperature gas, thereby by oxygen whereinGas content is down to lower level, but also can play and support described coke gasification reaction device b at the initial stage of going into operationIn the effect of fluidisation state solid b28. Described gas distributor b27 can be existing various can be realThe feed distributor that existing gas uniform distributes, concrete structure is known to the skilled person, and does not do at thisRepeat.
The interior bore of described atomizer c18 is preferably 0.5-50mm, can make like this coking heavy oilRaw material after atomization, obtain size to fit (droplet size is about 20-500 μ droplet m), therebySignificantly improve the contact area between coking heavy oil raw material and the thermal medium high-temperature gas of unit volume, increaseHeat and mass ability, and further improve liquid yield. The quantity of described atomizer c18 can basisThe volume of described spraying coking tower c and the disposal ability of unit interval are reasonably selected, for example,In the time that the volume disposal ability larger, the unit interval of described spraying coking tower c is stronger, described atomization sprayThe quantity of mouth c18 can correspondingly increase; When the volume of described spraying coking tower c less, the unit intervalWhen disposal ability is more weak, the quantity of described atomizer c18 can correspondingly reduce. As a rule, described inThe quantity of atomizer c18 can be 4-12. Described in multiple atomizer c18 are preferably evenly distributed onThe top of top straight tube reaction zone c21. In addition, described atomizer c18 can arrange vertically downward,Also can be tilted to lower setting, and acute angle between axial line and the horizontal plane of described atomizer c18 folderAngle can be 10-90 DEG C. The concrete structure of described atomizer c18 is known to the skilled person,Therefore not to repeat here.
According to coking heavy oil equipment provided by the invention, preferably, described spraying coking tower c also comprises positionIn being arranged on distribution of gas described straight tube reaction zone c21 top and that be communicated with described hot-wind inlet c24Plate c30, described gas distribution grid c30 is for introducing described spraying coking by described deoxidation high-temperature gas 4Before tower c, carry out distribution of gas, can make so described deoxidation high-temperature gas 4 in described spraying cokingIn tower c, be uniformly distributed, thus the contact area between further increase and the coking heavy oil raw material of atomization,And improve liquid yield. The concrete structure of described gas distribution grid c30 can with described coking reactor bIn gas distributor b27 identical, and can be all this area routine select, therefore not to repeat here.
According to coking heavy oil equipment provided by the invention, preferably, described spraying coking tower c also comprises and establishingPut the chev(e)ron baffle c20 directly over described side outlet c19, and described chev(e)ron baffle c20Opening down, can prevent that like this coke granule generating is deposited on the induced duct of side outlet c19.Angle and the length of the present invention to described chev(e)ron baffle c20 is not particularly limited, as long as can preventThe coke granule generating is deposited on the induced duct of side outlet c19. For example, described herringbone gearThe angle β of plate c20 can be 10-150 °, is preferably 30-100 °. The angle of described chev(e)ron baffle c20Degree setting will make the angle between baffle surface and horizontal plane be less than the angle of repose of coke meal. In addition,Described side outlet c19 and chev(e)ron baffle c20 all can be arranged on described top straight tube reaction zone c21Junction with bottom cone collecting region c22.
The present invention is not particularly limited the size of described coking heavy oil equipment. For example, described spraying is burntThe ratio of height to diameter of changing the top straight tube reaction zone c21 of tower c can be 2-10:1, is preferably 2-8:1. Under describedThe cone angle of the cone collecting region c22 of portion can be 10-150 °, is preferably 70-120 °. In addition described heat,Wind entrance c24 and side outlet c19 diameter can be all that the routine of this area is selected, and therefore not to repeat here.
In addition, the below of described spraying coking tower c and cyclone separator d is respectively arranged with coke meal receiptsCollection tank k and coke fines collection tank m, pass through the coke of self gravitation sedimentation from described spraying coking tower cMeal falls into coke meal collecting tank k, and falls into by the isolated coke fine powder of cyclone separator dIn coke fines collection tank m. In addition, in order to improve liquid yield, preferably, can be at coke mealIn collecting tank k and coke fines collection tank m, pass into respectively the first stripped vapor 7 and the second stripped vapor 9,Can purge the coke granule generating like this, by the oil gas stripping of its absorption out, after strippingCoke meal and a coke fine powder part are transported in coke gasification reaction device b as fluidisation state solid b28,Remainder equipment leading out or as the fuel of heating furnace a.
The present invention is not particularly limited the condition of described pyrogenetic reaction, for example, and described pyrogenetic reactionIt can be 490-515 DEG C that condition generally includes coking temperature, is preferably 495-505 DEG C; Coking pressure canFor-0.01MPa to 0.1MPa, be preferably-0.01MPa to 0MPa; Scorch time can be0.01-20min, is preferably 0.1-5min. In addition, the negative-pressure operation of described spraying coking tower c is conducive toThe raising of product liquid yield. Wherein, the internal pressure of described spraying coking tower c can be by being arranged onThe rotating speed of air-introduced machine h on the pipeline of connection cyclone separator d and fractionating column e regulates.
According to coking heavy oil equipment provided by the invention, for by smooth the coking heavy oil raw material 2 through preheatingBe delivered to the feed(raw material)inlet c25 that is positioned at described spraying coking tower c top, can be communicated with described heating furnaceOn pipeline between a and spraying coking tower c, pump g is set.
The present invention is not particularly limited the kind of described cyclone separator d, as long as can coke is thinPowder separates with oil gas, thereby obtains coke fine powder in the bottom of described cyclone separator d, and top is obtainedOil gas, be specially as well known to those skilled in the artly, therefore not to repeat here.
According to a kind of detailed description of the invention of the present invention, as shown in Figure 4, described coke gasification reaction device b, sprayMist coking tower c and cyclone separator d are of coupled connections, and now, described coke gasification reaction device b is gas-solid fluidizedBed bioreactor. Come self-spray coking tower c and cyclone separator d bottom respectively through the first stripped vapor7 and second coke granules after stripped vapor 9 strippings are directly introduced in described coke gasification reaction device b as streamChange state solid b28, contain oxygen high-temperature gas 3 from coke gasification reaction device b bottom introducing solid with described fluidisation stateBody b28 contacts to carry out deoxidation, and the deoxidation high-temperature gas after deoxidation is from the top of described coke gasification reaction device bPortion draws, and enters in spraying coking tower c and carry out heat exchange with the coking heavy oil raw material 2 through preheating.
Main improvements of the present invention are to have increased newly described coke gasification reaction device b and cyclone separator d alsoInternal structure to coking tower c is improved, and the structure of described fractionating column e and operation can be with existingThere is technology identical. For example, as shown in Figure 1, from the oil gas 10 of described cyclone separator d in fractionationIn tower e, be fractionated into coking dry gas, liquefied gas, coker gasoline, coker gas oil and wax tailings, that is, and instituteState and on fractionating column e, be correspondingly provided with respectively coking dry gas outlet e11, liquefied gas outlet e12, coker gasolineOutlet e13, coker gas oil outlet e14 and wax tailings outlet e15. Described coking dry gas can be used asThe fuel of heating furnace a and being back in the combustion chamber of heating furnace a, also can arrange outward and be incorporated in pipe network n.
According to coking heavy oil equipment provided by the invention, preferably, described fractionating column e also comprises and being arranged onThe outer circulation pipeline of described fractionating column e bottom, for withdrawing oil at the bottom of recycle column 16, can play and wash like thisIn the de-oil gas of introducing fractionating column e, carry secretly not by the effect of the isolated coke fine powder of cyclone separator dReally. More preferably, on described outer circulation pipeline, be also provided with heat exchanger.
According to coking heavy oil equipment provided by the invention, preferably, the side-lower setting of described fractionating column eHave feedstock oil entrance e1, and the bottom of described fractionating column e is communicated with the radiation heating district of described heating furnace a,Coking heavy oil raw material is introduced and connects with withdrawing oil at the bottom of tower 16 and coking oil gas from described feedstock oil entrance e1Touch to catch after coke fine powder residual in oil gas the end as coking raw material 17 from described fractionating column ePortion draws and enters and in the radiation heating district of described heating furnace a, carries out preheating (if coking raw material 17Temperature has reached preheat temperature, described coking raw material 17 directly can be entered to spraying coking tower cMaterial), not only can prevent like this accumulation of coke fine powder in fractionating column e, but also can make full use ofThermal source in fractionating column heats coking raw material, has prospects for commercial application.
According to coking heavy oil equipment provided by the invention, preferably, the top of described fractionating column e is provided withCoking dry gas outlet e11, and described coking dry gas outlet e11 is communicated with the combustion chamber of described heating furnace a,Isolated coking dry gas is contained to oxygen High Temperature Gas as the fuel of described heating furnace a combustion chamber and described in generatingBody, can realize effective utilization of raw material like this.
Described coking heavy oil raw material can be the conventional various coking heavy oil raw materials that use in this area, for example canThink decompression residuum, reduced crude, heavy crude, de-oiled asphalt, residual hydrogenation heavy oil, thermal cracking weightThe tar of the recycle oil of extraction oil, the catalytic cracking of oil, lube oil finishing and clarified oil, cracking of ethylene,At least one in coal tar, shale oil, oil-sand heavy oil, bitumen etc.
The fine particle coke of described spraying coking tower c output is mainly the coke of spheroidal, coke granuleDiameter be generally 0.001-1mm. The mobility of these spheroidal coke is better, can be than being easier to andDischarge from spraying coking tower c rapidly. Wherein, can be deposited on described spraying coking by self gravitationThe particle diameter of the coke meal of tower c bottom can be 0.01-1mm, is preferably 0.02-1mm; And need logicalThe particle diameter of crossing the coke fine powder of cyclone separator d and Oil-gas Separation can be 0.001-0.1mm, is preferably0.001-0.05mm. On the inwall of described spraying coking tower c, be likely stained with a small amount of coke granule stickyConnect thing, can in the time of shut-down (breakdown) mainteance, adopt conventional hydraulic decoking method to remove.
Below will describe the present invention by embodiment.
In following examples, coking heavy oil equipment used as Figure 1-3, comprising: heating furnace a, JiaoCharcoal reactor b, spraying coking tower c, cyclone separator d and fractionating column e; Described coke gasification reaction device b isGas-solid fluidized bed reactor, wherein the fluidisation state solid b28 of filling is the mixed of coke meal and coke fine powderCompound; Described spraying coking tower c comprises the top straight tube reaction zone c21 and the bottom cone receipts that are interconnectedCollection district c22, be arranged on straight tube reaction zone c21 top, described top and with the raw material of spraying coking tower c(in nozzle, bore is 1mm to the atomizer c18 arranging vertically downward that entrance c25 is communicated with, and quantity is6, evenly arrange at the top of described top straight tube reaction zone c21), be arranged on described straight tube reaction zoneGas distribution grid c30 c21 top and that be communicated with the hot-wind inlet c24 of spraying coking tower c, be arranged onSide outlet c19, the Yi Jishe of top straight tube reaction zone c21 and cone collecting region c22 junction, bottomPut directly over side outlet c19 and downward opening chev(e)ron baffle c20 (angle β is 90 °), instituteThe ratio of height to diameter of stating the top straight tube reaction zone c21 of spraying coking tower c is that 5:1 (is highly 10m, internal diameterFor 2m), the cone angle of bottom cone collecting region c22 is 60 °, the diameter of hot-wind inlet c24 is 400mm,The diameter of side outlet c19 is 300mm; The top of described fractionating column e is provided with the outlet of coking dry gasE11, bottom is provided with outer circulation pipeline, and side-lower is provided with feedstock oil entrance e1, and described fractionating columnThe bottom of e is communicated with the radiation heating district of described heating furnace a, coking dry gas outlet e11 and heating furnace aCombustion chamber be communicated with.
In following examples and comparative example:
Feedstock oil is same residual oil (its character is in table 1), and inlet amount is 25kg/h; Fractionating column eMiddle 460 DEG C of above cuts of atmospheric boiling point at the bottom of tower are extracted out as withdrawing oil at the bottom of tower; Recycle ratio refers in fractionationThe weight ratio of non-fresh feed oil part and fresh feed oil part in oil at the bottom of tower; Spraying coking tower c and revolvingDischarging again after the collecting tank of wind separator d below all passes into stripped vapor STRENGTH ON COKE particle and purges.
Embodiment 1-3
Embodiment 1-3 adopts coking heavy oil equipment provided by the invention to carry out the side of coking heavy oil for illustratingMethod.
Feedstock oil is introduced fractionating column e from the feedstock oil entrance e1 of fractionating column e, and and then from describedAt the bottom of the tower of fractionating column e, in the radiation heating district of introducing heating furnace a, carry out preheating, through the feedstock oil warp of preheatingIntroduce in described spraying coking tower c and carry out atomization by atomizer c18 by feed(raw material)inlet c25,To the atomization state droplet of 20-500 μ m, from obtaining through burning coking dry gas of the combustion chamber of heating furnace aTo carry out deoxidation by coke gasification reaction device b, the deoxidation high-temperature gas after deoxidation containing oxygen high-temperature gas 34 (wherein oxygen content is 0.1 volume %) are by being positioned at the hot-wind inlet c24 at spraying coking tower c topIntroduce in spraying coking tower c and contact with above-mentioned atomization state droplet, so that described atomization state droplet reachesTo coking temperature and carry out pyrogenetic reaction, the coke meal (particle diameter is 0.02-1mm) in pyrogenetic reaction productCollect the oil gas in coke gasification reaction product and Jiao from bottom cone collecting region c22 bottom by settlementThe mixture 6 of charcoal fine powder (particle diameter is 0.001-0.05mm) is introduced cyclone separator from side outlet c19In d, carry out separating of oil gas and coke fine powder, introduce fractionating column e from the oil gas 10 of cyclone separator dIn carry out cut separation, by isolated tower top coking dry gas as the fuel of heating furnace a combustion chamber rawBecome containing oxygen high-temperature gas 3, in fractionating column e bottom, the oil gas 10 that carrys out self-spray coking tower c returns with at the bottom of towerAfter stream oil 16 and the feedstock oil heat exchange from feedstock oil entrance e1, form coking raw material 17, this coking raw material17 circulations as coking heavy oil raw material from introducing the radiation heating district of heating furnace a at the bottom of the tower of described fractionating column eIn carry out preheating. Wherein, reaction condition is as shown in table 2, and result is as shown in table 3.
Comparative example 1
This comparative example is for illustrating the method that adopts existing delayed coking equipment to carry out delayed coking.
This comparative example delayed coking equipment used comprises: heating furnace, coking tower and fractionating column; Described JiaoThe inside of changing tower is hollow structure; The bottom of fractionating column is provided with outer circulation pipeline, and side-lower is provided with formerMaterial oil-in, and the bottom of described fractionating column is communicated with described heating furnace. Former by feedstock oil from fractionating columnIntroduce in fractionating column material oil-in, and and then from introducing the radiation heating of heating furnace at the bottom of the tower of described fractionating columnIn district, be heated to coking temperature, introduce afterwards in coking tower and carry out pyrogenetic reaction, then pyrogenetic reaction is producedThing carries out cut separation in fractionating column. In fractionating column bottom, from the oil gas of coking tower and backflow at the bottom of towerAfter oil and the feedstock oil heat exchange from feedstock oil entrance, form coking raw material, this coking raw material circulation is as heavyOil coking raw material is for pyrogenetic reaction. Wherein, reaction condition is as shown in table 2, and result is as shown in table 3.
Table 1
| Project name | Index |
| Density (20 DEG C), kg/m3 | 1009 |
| Sulfur content, % by weight | 3 |
| Carbon residue content, % by weight | 20.0 |
| Pour point, DEG C | >50℃ |
| Composition, w% | |
| Saturated hydrocarbon content, % by weight | 17.0 |
| Arene content, % by weight | 55.1 |
| Resin and asphalt total content, % by 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 feedstock 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 |
| The spraying coking tower air inlet scale of construction, 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 |
| The time of staying of 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, coking heavy oil equipment provided by the invention not only can reduce heating furnaceCoking in boiler tube, but also can improve liquid yield, have prospects for commercial application.
More than describe the preferred embodiment of the present invention in detail, still, the present invention is not limited to above-mentioned realityExecute the detail in mode, within the scope of technical conceive of the present invention, can be to technical side of the present inventionCase is carried out multiple simple variant, and these simple variant all belong to protection scope of the present invention.
It should be noted that in addition each the concrete technology spy described in above-mentioned detailed description of the inventionLevy, in reconcilable situation, can combine by any suitable mode. For fear of needn'tThe repetition of wanting, the present invention is to the explanation no longer separately of various possible combinations.
In addition, between various embodiment of the present invention, also can be combined, as long as itsWithout prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (11)
1. a coking heavy oil equipment, is characterized in that, described coking heavy oil equipment comprise heating furnace (a),Coke gasification reaction device (b), spraying coking tower (c), cyclone separator (d) and fractionating column (e), described inSpraying coking tower (c) comprises the top straight tube reaction zone (c21) and the bottom cone collecting region that are interconnected(c22), be arranged on described top straight tube reaction zone (c21) top and with described spraying coking tower (c)Feed(raw material)inlet (c25) be communicated with atomizer (c18) and side outlet (c19); Heavy oil JiaoChange raw material and carry out preheating in the radiation heating district of described heating furnace (a), former through the coking heavy oil of preheatingMaterial is introduced in described spraying coking tower (c) and by described atomization and is sprayed via described feed(raw material)inlet (c25)Mouth (c18) carries out atomization, passes through institute from the combustion chamber of described heating furnace (a) containing oxygen high-temperature gasState coke gasification reaction device (b) and carry out deoxidation, the deoxidation high-temperature gas after deoxidation is by being positioned at described sprayingThe hot-wind inlet (c24) at coking tower (c) top is introduced in described spraying coking tower (c) and and atomizationThe coking heavy oil raw material contact of state, goes forward side by side so that the coking heavy oil raw material of described atomization state reaches coking temperatureRow pyrogenetic reaction, the coke meal in pyrogenetic reaction product is from cone collecting region (c22) end, described bottomPortion collects, and the oil gas in coke gasification reaction product and coke fine powder are introduced institute from described side outlet (c19)State in cyclone separator (d) and carry out separating of oil gas and coke fine powder, from described cyclone separator (d)Oil gas introduce in described fractionating column (e) and carry out cut separation.
2. coking heavy oil equipment according to claim 1, wherein, described atomizer (c18)Interior bore be 0.5-50mm.
3. coking heavy oil equipment according to claim 2, wherein, described atomizer (c18)Arrange vertically downward or be tilted to lower setting, and axial line and the horizontal plane of described atomizer (c18)Between acute angle angle be 10-90 DEG C.
4. coking heavy oil equipment according to claim 1, wherein, described spraying coking tower (c)Also comprise be arranged on described straight tube reaction zone (c21) top and be communicated with described hot-wind inlet (c24)Gas distribution grid (c30), described gas distribution grid (c30) is for entering described deoxidation high-temperature gasRow distribution of gas.
5. according to the coking heavy oil equipment described in any one in claim 1-4, wherein, described sprayMist coking tower (c) also comprises the chev(e)ron baffle (c20) being arranged on directly over described side outlet (c19),And described chev(e)ron baffle (c20) is opening down, for preventing that the coke granule generating is deposited in instituteState on the induced duct of side outlet (c19).
6. coking heavy oil equipment according to claim 5, wherein, described chev(e)ron baffle (c20)Angle β be 10-150 °.
7. according to the coking heavy oil equipment described in any one in claim 1-4, wherein, described sprayThe ratio of height to diameter of the top straight tube reaction zone (c21) of mist coking tower (c) is 2-10:1, described bottom coneThe cone angle of collecting region (c22) is 10-150 °.
8. according to the coking heavy oil equipment described in any one in claim 1-4, wherein, described JiaoCharcoal reactor (b) is gas-solid fluidized bed reactor; The fluidisation state of filling in described coke gasification reaction device (b)Solid (b28) is described coke meal and/or coke fine powder, and the described oxygen high-temperature gas that contains is from described cokeIntroduce in described coke gasification reaction device (b) and described fluidisation state solid (b28) bottom of reactor (b)Contact to carry out redox reaction, through reacted deoxidation high-temperature gas from described coke gasification reaction device (b)Base top contact.
9. according to the coking heavy oil equipment described in any one in claim 1-4, wherein, described pointHeat up in a steamer tower (e) and also comprise the outer circulation pipeline that is arranged on described fractionating column (e) bottom, at the bottom of recycle columnWithdrawing oil.
10. coking heavy oil equipment according to claim 9, wherein, described fractionating column (e)Side-lower is provided with feedstock oil entrance (e1), and the bottom of described fractionating column (e) and described heating furnace (a)Radiation heating district be communicated with.
11. according to the coking heavy oil equipment described in any one in claim 1-4, wherein, and described pointThe top of heating up in a steamer tower (e) is provided with coking dry gas outlet (e11), and described coking dry gas outlet (e11)Be communicated with the combustion chamber of described heating furnace (a), isolated coking dry gas is used as to described heating furnace (a)Fuel and generate described containing oxygen high-temperature gas.
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| CN106833717A (en) * | 2017-03-05 | 2017-06-13 | 刘金凤 | A kind of fractionation apparatus for heavy oil sophisticated category |
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| CN107974273A (en) * | 2016-10-25 | 2018-05-01 | 中国石油化工股份有限公司 | A kind of method of heavy oil visbreaking |
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| CN109777467A (en) * | 2017-11-14 | 2019-05-21 | 中国石油化工股份有限公司 | A kind of processing method of high-viscosity oil visbreaking |
| 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 |
| 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 |
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