CN205133519U - Process flexicoking process units of heavy oil inferior - Google Patents
Process flexicoking process units of heavy oil inferior Download PDFInfo
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- CN205133519U CN205133519U CN201520873599.XU CN201520873599U CN205133519U CN 205133519 U CN205133519 U CN 205133519U CN 201520873599 U CN201520873599 U CN 201520873599U CN 205133519 U CN205133519 U CN 205133519U
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Abstract
The utility model discloses a process flexicoking process units of heavy oil inferior, include: one promotes tubular reactor, should promote tubular reactor and be provided with upper portion export, a lower extreme opening, first coke carrier entry and a feed inlet, a settler, the upper portion export that should promote tubular reactor is stretched into in this settler to this settler has upper portion export, and a regenerator, this settler sets up in the upper portion of this regenerator to this regenerator has lower part export and first coke carrier export, and this first coke carrier export sets up in the side lower part of this regenerator. The utility model discloses can improve the not good problem of the common fluidization situation of flexicoking.
Description
Technical field
The utility model relates to the Refinery Coking technique in refining of petroleum, particularly a kind of flexicoking process unit adopting gasoline stock to process inferior heavy oil.
Background technology
21 century, China's refining industry will face development and the situation that coexists of risk.Because ever-increasing oil product and the demand of supplying raw materials for petrochemical complex will determine that China's refining industry has certain tempo within the new millennium, but limiting it will face great risk simultaneously by factors such as petroleum resources.If say, last century 80, the nineties China's refining industry in sulfur crude processing, have the words of important breakthrough, so 21 century China's refining industry one of important development direction to greatly develop the processing of heavy crude (super heavy crude) exactly, develop more efficient coking process independently and propose under such background.
Heavy oil upgrading can be divided into catalysis processing and on-catalytic processing.Catalysis complete processing comprises heavy oil fluid catalytic cracking, the technique such as residue fixed-bed hydrogenation (VRDS) and the floating bed hydrocracking developed.On-catalytic processing comprises the techniques such as viscosity breaking, coking and solvent deasphalting.
Delayed coking is the crude conversion technology that refinery is widely applied, it is the Main Means of state's residual oil weight-lightenings such as the U.S., China, Venezuela, India, Canada, the whole world has more than 170 and overlaps residual oil delayed coking unit in operation, total working ability more than 400,000,000 tons, China's delayed coking working ability in 2012 has reached 1.13 hundred million tons.The integrated oil company of the U.S. and China all has autonomous residual oil delayed coking complete set technology.Fluid coking is a kind of coking process technology developed by EXXON company the fifties.After, succeed in developing again flexicoking technique on this basis.Compared with delay coking process; these two techniques have raw material and operation flexibility is high; have that temperature of reaction is high, liquid yield is high, coke (fluid coking) and the advantage such as gas recovery ratio is lower, especially device cleaner production and environment protection aspect have greatly improved than delayed coking.Early stage fluid coking generates the coke powder not having Suitable applications in a large number, and invests and the more high reason of process cost, and industrially promotion and application are less than delay coking process.Coke powder, owing to being configured with coke powder equipment for gasification, can being changed into low heat value gas, substantially not generate coke powder by flexicoking.But, also occur in flexicoking that fluidized status is not good, the obvious shaking phenomenon of fluidized-bed, the problem such as reactor coking rate has been fast.
Riser reactor has some application in heavy oil fluid catalytic cracking field, particularly in order to improve yield of light oil and direct production clear gusoline, there is the heavy oil catalytic cracking process technology of multi-form reactor assembly in recent years, as two-stage riser fluid catalytic cracking technology (TSRFCC), maximizing iso-paraffins catalytic cracking technology (MIP) and catalytically cracked gasoline auxiliary reactor modification technology etc.Such as, Chinese patent CN201020699182.3 discloses a kind of single riser reactor being conducive to processing inferior heavy oil.Be that boundary is divided into charging reaction zone, olefine reaction district with alkene by riser tube, total reaction severity control district, the wikipedia type undergauge throat tubular construction that exit design one section of diameter in charging reaction zone is less than feed zone, at trunnion, place is connected with low pressure steam pipe; In olefine reaction district, the diameter of the riser tube cooling section of hypomere is greater than the diameter of described feed zone, and riser tube cooling section is provided with heat removing tube, and the entrance of this heat removing tube group is connected with low-pressure saturated steam, and outlet is connected with supersaturated vapor line; The entrance in total reaction severity control district is the wikipedia type undergauge throat tubular construction that one section of diameter is less than feed zone throat pipe diameter, and at trunnion, place is connected with low pressure steam pipe.Reach larger proportion processing heavy raw oil, optimize product slates, petrol and diesel oil yield is high, and gasoline olefin is lower, isoparaffin increases obviously, reduces the object of coke yield.And for example, Chinese patent CN1258562 discloses a kind of riser reactor for fluidized catalytic conversion, and the cross section circular diameter of this reactor is different and consecutive variations with height for reactor, and minimum diameter is 0.003 ~ 0.1:1 with the ratio of total reactor height.This design, for needing the catalytic conversion process that the reaction times is longer, reaction velocity is lower, as voluminous gaseous olefin technique, ensure that enough reaction times and reaction velocity, greatly reduces the height of reactor, save investment.But for riser reactor in heavy oil upgrading, the application in particularly non-catalytic cracking coking process, still seldom sees prior art.
Therefore, how to design a kind of flexicoking process unit, make it can solve above-mentioned defect existing in prior art, namely become those skilled in the art's problem demanding prompt solution.
Utility model content
The purpose of this utility model is to provide a kind of flexicoking process unit processing inferior heavy oil, makes it can improve the not good problem of the common fluidized status of flexicoking.
For achieving the above object, the utility model provides a kind of flexicoking process unit processing inferior heavy oil, comprising:
One gasoline stock, this gasoline stock is provided with a upper outlet, a lower ending opening, one first coke carrier inlet and an opening for feed, this upper outlet and this lower ending opening are arranged at the two ends up and down of this gasoline stock respectively, this the first coke carrier inlet is arranged at the side-lower of this gasoline stock, this opening for feed is arranged at the middle and lower part of this gasoline stock, further, this opening for feed connects an atomizing steam entrance and a stock oil entrance;
One settling vessel, the upper outlet of this gasoline stock stretches in this settling vessel, and this settling vessel has a upper outlet;
One revivifier, this settling vessel is arranged at the top of this revivifier, and this revivifier has a lower part outlet and one first coke carrier outlet, and this first coke carrier outlet is arranged at the side lower part of this revivifier.
By above-mentioned flexicoking process unit, the utility model can carry out a pyrogenic reaction as the reactor in flexicoking technique by a gasoline stock, described pyrogenic reaction is: take inferior heavy oil as stock oil, in described gasoline stock, carry out thermo-cracking, produce oil gas and the coke of full cut.Specifically, this flexicoking process unit using method is as follows: promote steam from a lower ending opening input of this gasoline stock, and input hot coke carrier from one first coke carrier inlet of gasoline stock side-lower, hot coke carrier is advanced with the top of flow-like to this gasoline stock under the effect promoting steam; From opening for feed input atomizing steam and a stock oil of this gasoline stock middle and lower part, make stock oil enter this gasoline stock with Sprayable, and be attached to hot coke carrier surface, move upward with hot coke carrier; Stock oil is made to carry out this pyrogenic reaction at this gasoline stock inner edge rising edge, heavy hydrocarbon component thermo-cracking in reacted rear stock oil is oil gas (comprising gas phase hydrocarbon component, petroleum naphtha, diesel oil and wax oil etc.) and the coke powder of full cut, hot coke carrier for pyrogenic reaction heat is provided after become cold coke carrier; By unreacted in the oil gas of full cut, coke powder, cold coke carrier and stock oil completely heavy hydrocarbon component input in this settling vessel along the upper outlet of this gasoline stock, then the oil gas of full cut is wherein discharged along settling vessel upper outlet, collect coke powder, and to make in stock oil unreacted completely heavy hydrocarbon component fall into this revivifier and discharge from the lower part outlet of this revivifier, and make cold coke carrier fall into this revivifier and discharge from one first coke carrier outlet of this revivifier side lower part.
Wherein, the pipeline of this opening for feed and this gasoline stock are the angle of 30 ~ 45 °.
Wherein, the middle part of this gasoline stock is provided with a turning oil reflux inlet, is connected with the lower part outlet of this revivifier.In stock oil, heavy hydrocarbon component is cooled in settling vessel and revivifier completely for unreacted, after the lower part outlet of this revivifier is discharged, reenters this gasoline stock, again carry out pyrogenic reaction along turning oil reflux inlet.
Wherein, Level control is established on this gasoline stock top.
Wherein, the height of this gasoline stock is 10 ~ 20 meters, is preferably 18 meters.
Wherein, the diameter of this gasoline stock is 150mm ~ 200mm.
Wherein, also comprise a well heater, be connected with the first coke carrier inlet of this gasoline stock and the first coke carrier outlet of this revivifier.The cold coke carrier that this well heater is used for this first coke carrier outlet is discharged is heated to be hot coke carrier, then inputs this gasoline stock from this first coke carrier inlet.The circulation of coke carrier between this well heater, this gasoline stock, this settling vessel and this revivifier is for maintaining by promoting steam, and the impellent of coke carrier loop is determined by the pressure equilibrium parameter of revivifier and well heater.
Wherein, on the first coke carrier inlet of this gasoline stock and the connecting pipeline of this well heater, a guiding valve is provided with.The internal circulating load of coke carrier is controlled by this guiding valve, and the sliding contact of guiding valve surface uses hard surface process to make minimise wear, coke line (comprising stack gas) use unique heat-resisting/wear resistance lining.
Wherein, also comprise a gasifier, be connected with this well heater, and this gasifier has a gas inlet and a steam-in.This gasifier is used for coke powder pyrogenic reaction generated, and the steam that the air inputted with this gas inlet and this steam-in input reacts, and generates containing CO
2, CO, H
2with synthetic gas and the heat of rare gas element.Described synthetic gas carries the heat that reaction generates, and coke powder, air and steam are fed in well heater, in the lump for well heater bed fluidisation and heat transmission completely with unreacted.Thus, the cold coke carrier in well heater is heated to be hot coke carrier, and coke powder major part is discharged from the coke powder relief outlet of well heater bottom, and small portion coke powder is mixed in gas.
Wherein, also comprise a recovery system, be connected to the top of this well heater, this recovery system comprises the vapour generator, a cyclonic separator, a coke powder collection device, a gas desulphurisation plant and the sulfur recovery facility that are linked in sequence.In input well heater, air, steam and synthetic gas (and the coke powder carried secretly in gas) are discharged in recovery system by well heater top, sequentially pass through the vapour generator of this recovery system, cyclonic separator, coke powder collection device, gas desulphurisation plant and sulfur recovery facility.After coke powder is separated in cyclonic separator, be recovered in coke powder collection device, discharged by the coke powder relief outlet of coke powder tripping device.Remaining gas fraction (synthetic gas, air, steam) is then by this gas desulphurisation plant, sour water is discharged from a sour water outlet of gas desulphurisation plant, again by sulfur recovery facility, final generating clean fuel gas, for other equipment of refinery or third party user.
The utility model also provides a kind of flexicoking processing method of processing inferior heavy oil, comprising:
Carry out a pyrogenic reaction using a gasoline stock as the reactor in flexicoking technique, described pyrogenic reaction is: take inferior heavy oil as stock oil, in described gasoline stock, carry out thermo-cracking, produces oil gas and the coke of full cut.
Wherein, described pyrogenic reaction comprises the steps:
1) this gasoline stock and a settling vessel and a revivifier are formed a flexicoking reactive system jointly, make this settling vessel be arranged at the top of this revivifier, and the upper outlet of this gasoline stock stretches in this settling vessel;
2) steam is promoted from a lower ending opening input of this gasoline stock, and input hot coke carrier from one first coke carrier inlet of gasoline stock side-lower, hot coke carrier is advanced with the top of flow-like to this gasoline stock under the effect promoting steam;
3) from opening for feed input atomizing steam and a stock oil of this gasoline stock middle and lower part, make stock oil enter this gasoline stock with Sprayable, and be attached to hot coke carrier surface, move upward with hot coke carrier;
4) stock oil is made to carry out this pyrogenic reaction at this gasoline stock inner edge rising edge, heavy hydrocarbon component thermo-cracking in reacted rear stock oil is oil gas (comprising gas phase hydrocarbon component, petroleum naphtha, diesel oil and wax oil etc.) and the coke powder of full cut, hot coke carrier for pyrogenic reaction heat is provided after become cold coke carrier;
5) by unreacted in the oil gas of full cut, coke powder, cold coke carrier and stock oil completely heavy hydrocarbon component input in this settling vessel along the upper outlet of this gasoline stock, then the oil gas of full cut is wherein discharged along settling vessel upper outlet, collect coke powder, and to make in stock oil unreacted completely heavy hydrocarbon component fall into this revivifier and discharge from the lower part outlet of this revivifier, and make cold coke carrier fall into this revivifier and discharge from one first coke carrier outlet of this revivifier side lower part.
Wherein, in step 3) in, during from this opening for feed of this gasoline stock middle and lower part input atomizing steam and stock oil, be to be inclined upwardly charging with this gasoline stock angle that is 30 ~ 45 °.
Wherein, in step 4) in, specifically, stock oil is attached to hot coke carrier surface as a mist, move upward with fluidised hot coke carrier, in the process, the heat entrained by hot coke carrier is relied on to carry out pyrogenic reaction (the gas phase hydrocarbon component that pyrogenic reaction generates, further promote the fluidization of hot coke carrier, namely, attached to the fluidization of the hot coke carrier of mist stock oil, is produce under the gas phase hydrocarbon component acting in conjunction promoting steam and reaction generation).Make charging close to plug flow thus, decrease back-mixing, thus can improve the phenomenon that the common fluidized status of flexicoking is not good, fluidized-bed obviously rocks, and improve the problems such as reactor coking rate is fast.
Wherein, in step 5) in, unreacted heavy hydrocarbon component cooled in settling vessel and revivifier (cooling can be undertaken by waiting for another strand the cold stock oil heat exchange that enters gasoline stock) completely in stock oil, after the lower part outlet of this revivifier is discharged, reenter this gasoline stock along the turning oil reflux inlet be arranged in the middle part of this gasoline stock, again carry out pyrogenic reaction.
Wherein, in step 5) in, the oil gas of full cut inputs after in this settling vessel along the upper outlet of this gasoline stock, first the coke powder removed in wherein gas phase hydrocarbon component is separated through cyclonic separator, then again the oil gas of this full cut is cooled (cooling can be undertaken by waiting for another strand the cold stock oil heat exchange that enters gasoline stock), finally again the upper outlet of the oil gas of this full cut from this settling vessel is discharged, be separated into the hydrocarbon component of downstream needs through coke separation column.
Wherein, in step 5) in, coke powder lays respectively at two places, and a part is mixed in gas phase hydrocarbon component, and another part is deposited on cold coke carrier.After coke powder is collected, for heat needed for pyrogenic reaction after a part of incendivity, remainder coke can carry out water-gas reaction with water vapour and generate water-gas, isolate further hydrogen for refinery other with hydrogen production device.
Wherein, in step 5) in, cold coke carrier is after the first coke carrier outlet of this revivifier is discharged (now the temperature of cold coke carrier is 510 ~ 520 DEG C), enter a well heater and carry out heat exchange, be heated to be after hot coke carrier until cold coke carrier, again input this gasoline stock from this first coke carrier inlet.
Wherein, this cold coke carrier and this hot coke carrier are granularity at the refinery coke of 40 ~ 1000 μm.
Wherein, the circulation of coke carrier between this well heater, this gasoline stock, this settling vessel and this revivifier is for maintaining by promoting steam, and the impellent of coke carrier loop is determined by the pressure equilibrium parameter of revivifier and well heater.And, a guiding valve is provided with on the first coke carrier inlet of this gasoline stock and the connecting pipeline of this well heater, the internal circulating load of coke carrier is controlled by this guiding valve, the sliding contact surface of guiding valve uses hard surface process to make minimise wear, coke line (comprising stack gas) use unique heat-resisting/wear resistance lining.
Wherein, the heat of this well heater is provided by a gasifier, this gasifier has a gas inlet and a steam-in, by the coke powder that this pyrogenic reaction generates, the steam that the air inputted with this gas inlet and this steam-in input carries out reacting that (temperature of reaction is 927 ~ 982 DEG C, this temperature controls by regulating the ratio of air and steam, and the air velocity that the amount of coke in gasifier enters gasifier by adjustment controls), generate containing CO
2, CO, H
2with synthetic gas and the heat of rare gas element.Described synthetic gas carries the heat that reaction generates, and coke powder, air and steam are fed in well heater, in the lump for well heater bed fluidisation and heat transmission completely with unreacted.Thus, cold coke carrier in well heater is heated to be hot coke carrier, coke powder major part is discharged from the coke powder relief outlet of well heater bottom, small portion coke powder is mixed in gas, next, in air, steam and synthetic gas in input well heater and gas, the coke powder that is mingled with then is discharged in a recovery system by well heater top, sequentially by a vapour generator of this recovery system, a cyclonic separator, a coke powder collection device, a gas desulphurisation plant and a sulfur recovery facility.After coke powder is separated in cyclonic separator, be recovered in coke powder collection device, discharged by the coke powder relief outlet of coke powder tripping device.Remaining gas fraction (synthetic gas, air, steam) is then by this gas desulphurisation plant, sour water is discharged from a sour water outlet of gas desulphurisation plant, again by sulfur recovery facility, final generating clean fuel gas, for other equipment of refinery or third party user.
Wherein, this inferior heavy oil is at least one in vacuum residuum, long residuum, heavy crude, decompressed wax oil, oil sands bitumen, de-oiled asphalt, deasphalted oil, residual hydrogenation heavy oil, thermal cracking residue, the extraction oil of lube oil finishing, the turning oil of catalytic cracking and clarified oil, cracking of ethylene residual oil and tar-bitumen.
Wherein, Level control is established on this gasoline stock top, to control the pyrogenic reaction time, meets the needs of riser tube pyrogenic reaction time.
Wherein, this pyrogenic reaction temperature is 515 ~ 565 DEG C, is preferably 520 ~ 550 DEG C.Namely, according to design of the present utility model, pyrogenic reaction is carried out as the reactor in flexicoking technique using gasoline stock, desired reaction temperature higher 30 ~ 50 DEG C than conventional delayed coking reaction temperature (conventional delayed coking reaction temperature is about 490 ~ 510 DEG C), control pyrogenic reaction temperature of the present utility model within the scope of this, the technique effect of the utility model expection could be realized, the problems such as solution reactor coking speed is fast, and pyrogenic reaction liquid yield of the present utility model is higher, and in product, olefin(e) centent is high.
Wherein, in this pyrogenic reaction, the oil circulation ratio of charcoal of this gasoline stock is 1:11 ~ 12 (weight ratios).That is, the coke recycle of the application is larger than Conventional catalytic cracking agent-oil ratio.
Wherein, this pyrogenic reaction process does not need configuration large air separation plant supply pure oxygen.
Wherein, the time of this pyrogenic reaction is 15 ~ 30s.That is, the process that stock oil carries out this pyrogenic reaction at this gasoline stock inner edge rising edge is about 15 ~ 30s.
Wherein, the height of this gasoline stock is 10 ~ 20 meters, is preferably 18 meters.The height of this gasoline stock is determined by reaction required time.
Wherein, the diameter of this gasoline stock is 150mm ~ 200mm.The diameter of this gasoline stock is determined by inlet amount.The linear speed that gasoline stock of the present utility model adopts is opening for feed place is 4 ~ 7m/s, and the upper outlet place of gasoline stock is 12 ~ 18m/s.
Compared with prior art, the utility model adopts and promotes tubular type coking reactor, replace the original major diameter reactor of flexicoking, thus improve the problems such as the common fluidized status of flexicoking is not good, the obvious shaking phenomenon of fluidized-bed, reactor coking rate are fast.Effectively can control coke powder reserve in reactor, improve liquid product yield.
Below in conjunction with the drawings and specific embodiments, the utility model is described in detail, but not as to restriction of the present utility model.
Accompanying drawing explanation
Fig. 1 is the flexicoking process unit schematic diagram that the utility model one preferred embodiment provides;
Fig. 2 is the combination schematic diagram of the flexicoking process unit that provides of the utility model one preferred embodiment and auxiliary equipment thereof;
Wherein, Reference numeral:
1 gasoline stock
11 upper outlet
12 stock oil entrances
13 turning oil reflux inlets
14 atomizing steam entrances
16 first coke carrier inlets
161 guiding valves
17 lower ending openings
2 settling vessels
21 upper outlet
3 revivifiers
31 first coke carrier outlet
32 lower part outlets
4 well heaters
41 coke powder relief outlets
5 gasifiers
51 steam-ins
52 gas inlets
6 vapour generators
7 cyclonic separators
8 coke powder collection devices
81 coke powder relief outlets
9 gas desulphurisation plant
91 sour water outlets
10 sulfur recovery facilities
Embodiment
Below in conjunction with the drawings and specific embodiments, the utility model is described in detail, but not as to restriction of the present utility model.
Please refer to Fig. 1, Fig. 2, for improving the not good problem of the common fluidized status of flexicoking, the utility model provides a kind of flexicoking process unit processing inferior heavy oil, comprising:
One gasoline stock 1, this gasoline stock 1 is provided with upper outlet 11, lower ending opening 17,1 first coke carrier inlet 16 and an opening for feed, this upper outlet 11 and this lower ending opening 17 are arranged at the two ends up and down of this gasoline stock 1 respectively, this the first coke carrier inlet 16 is arranged at the side-lower of this gasoline stock 1, this opening for feed is arranged at the middle and lower part of this gasoline stock 1, further, this opening for feed connects atomizing steam entrance 14 and a stock oil entrance 12;
One settling vessel 2, the upper outlet 11 of this gasoline stock 1 stretches in this settling vessel 2, and this settling vessel 2 has a upper outlet 21;
One revivifier 3, this settling vessel 3 is arranged at the top of this revivifier 3, and this revivifier 3 has lower part outlet 32 and an one first coke carrier outlet 31, and this first coke carrier outlet 31 is arranged at the side lower part of this revivifier 3.
By above-mentioned flexicoking process unit, the utility model can carry out a pyrogenic reaction as the reactor in flexicoking technique by a gasoline stock 1, described pyrogenic reaction is: take inferior heavy oil as stock oil, in described gasoline stock 1, carry out thermo-cracking, produce oil gas and the coke of full cut.Specifically, this flexicoking process unit using method is as follows: promote steam from a lower ending opening 17 input of this gasoline stock 1, and input hot coke carrier from one first coke carrier inlet 16 of gasoline stock 1 side-lower, hot coke carrier is advanced with the top of flow-like to this gasoline stock 1 under the effect promoting steam; From opening for feed input atomizing steam and a stock oil of this gasoline stock 1 middle and lower part, make stock oil enter this gasoline stock 1 with Sprayable, and be attached to hot coke carrier surface, move upward with hot coke carrier; Stock oil is made to carry out this pyrogenic reaction at this gasoline stock 1 inner edge rising edge, heavy hydrocarbon component thermo-cracking in reacted rear stock oil is oil gas (comprising gas phase hydrocarbon component, petroleum naphtha, diesel oil and wax oil etc.) and the coke powder of full cut, hot coke carrier for pyrogenic reaction heat is provided after become cold coke carrier; By unreacted in the oil gas of full cut, coke powder, cold coke carrier and stock oil completely heavy hydrocarbon component input in this settling vessel 2 along the upper outlet 11 of this gasoline stock 1, then the oil gas of full cut is wherein discharged along settling vessel 2 upper outlet, collect coke powder, and to make in stock oil unreacted completely heavy hydrocarbon component fall into this revivifier 3 and discharge from the lower part outlet 32 of this revivifier 3, and make cold coke carrier fall into this revivifier 3 and discharge from one first coke carrier outlet 31 of this revivifier 3 side lower part.
Wherein, the pipeline of this opening for feed and this gasoline stock 1 are in the angle of 30 ~ 45 °.
Wherein, the middle part of this gasoline stock 1 is provided with a turning oil reflux inlet 13, is connected with the lower part outlet 32 of this revivifier 3.In stock oil, heavy hydrocarbon component is cooled in settling vessel 2 and revivifier 3 completely for unreacted, after the lower part outlet 32 of this revivifier 3 is discharged, reenters this gasoline stock 1, again carry out pyrogenic reaction along turning oil reflux inlet 13.
Wherein, Level control is established on this gasoline stock 1 top.
Wherein, the height of this gasoline stock 1 is 10 ~ 20 meters, is preferably 18 meters.
Wherein, the diameter of this gasoline stock 1 is 150mm ~ 200mm.
Wherein, also comprise a well heater 4, be connected with the first coke carrier inlet 16 of this gasoline stock 1 and the first coke carrier outlet 31 of this revivifier 3.This well heater 4 is heated to be hot coke carrier for the cold coke carrier of being discharged by this first coke carrier outlet 31, then inputs this gasoline stock 1 from this first coke carrier inlet 16.The circulation of coke carrier between this well heater 4, this gasoline stock 1, this settling vessel 2 and this revivifier 3 is for maintaining by promoting steam, and the impellent of coke carrier loop is determined by the pressure equilibrium parameter of revivifier 3 and well heater 4.
Wherein, on the first coke carrier inlet 16 of this gasoline stock 1 and the connecting pipeline of this well heater 4, a guiding valve 161 is provided with.The internal circulating load of coke carrier is controlled by this guiding valve 161, and the sliding contact of guiding valve 161 surface uses hard surface process to make minimise wear, coke line (comprising stack gas) use unique heat-resisting/wear resistance lining.
Wherein, also comprise a gasifier 5, be connected with this well heater 4, and this gasifier 5 has gas inlet 52 and a steam-in 51.The coke powder of this gasifier 5 for pyrogenic reaction being generated, the steam that the air inputted with this gas inlet 52 and this steam-in 51 input reacts, and generates containing CO
2, CO, H
2with synthetic gas and the heat of rare gas element.Described synthetic gas carries the heat that reaction generates, and coke powder, air and steam are fed in well heater 4, for well heater bed fluidisation and heat transmission in the lump completely with unreacted.Thus, the cold coke carrier in well heater 4 is heated to be hot coke carrier, and coke powder major part is discharged from the coke powder relief outlet 41 of well heater 4 bottom, and small portion coke powder is mixed in gas.
Wherein, also comprise a recovery system, be connected to the top of this well heater 4, this recovery system comprises vapour generator 6, cyclonic separator 7, coke powder collection device 8, gas desulphurisation plant 9 and the sulfur recovery facility 10 be linked in sequence.In input well heater 4, air, steam and synthetic gas (and the coke powder carried secretly in gas) are discharged in recovery system by well heater 4 top, sequentially pass through the vapour generator 6 of this recovery system, cyclonic separator 7, coke powder collection device 8, gas desulphurisation plant 9 and sulfur recovery facility 10.After coke powder is separated in cyclonic separator 7, be recovered in coke powder collection device 8, discharged by the coke powder relief outlet 81 of coke powder tripping device 8.Remaining gas fraction (synthetic gas, air, steam) is then by this gas desulphurisation plant 9, sour water is discharged from a sour water outlet 91 of gas desulphurisation plant 9, again by sulfur recovery facility 10, final generating clean fuel gas, for other equipment of refinery or third party user.
Please continue reference drawing 1 and Fig. 2, the utility model also provides a kind of flexicoking processing method of processing inferior heavy oil, comprising:
Carry out a pyrogenic reaction using a gasoline stock 1 as the reactor in flexicoking technique, described pyrogenic reaction is: take inferior heavy oil as stock oil, in described gasoline stock 1, carry out thermo-cracking, produces oil gas and the coke of full cut.
Wherein, described pyrogenic reaction comprises the steps:
1) this gasoline stock 1 and a settling vessel 2 and a revivifier 3 are formed a flexicoking reactive system jointly, make this settling vessel 2 be arranged at the top of this revivifier 3, and the upper outlet 11 of this gasoline stock 1 stretches in this settling vessel 2;
2) steam is promoted from a lower ending opening 17 input of this gasoline stock 1, and input hot coke carrier from one first coke carrier inlet 16 of gasoline stock 1 side-lower, hot coke carrier is advanced with the top of flow-like to this gasoline stock 1 under the effect promoting steam;
3) from opening for feed input atomizing steam and a stock oil of this gasoline stock 1 middle and lower part, make stock oil enter this gasoline stock 1 with Sprayable, and be attached to hot coke carrier surface, move upward with hot coke carrier;
4) stock oil is made to carry out this pyrogenic reaction at this gasoline stock 1 inner edge rising edge, heavy hydrocarbon component thermo-cracking in reacted rear stock oil is oil gas (comprising gas phase hydrocarbon component, petroleum naphtha, diesel oil and wax oil etc.) and the coke powder of full cut, hot coke carrier for pyrogenic reaction heat is provided after become cold coke carrier;
5) by unreacted in the oil gas of full cut, coke powder, cold coke carrier and stock oil completely heavy hydrocarbon component input in this settling vessel 2 along the upper outlet 11 of this gasoline stock 1, then the oil gas of full cut is wherein discharged along settling vessel 2 upper outlet 21, collect coke powder, and to make in stock oil unreacted completely heavy hydrocarbon component fall into this revivifier 3 and discharge from the lower part outlet 32 of this revivifier 3, and make cold coke carrier fall into this revivifier 3 and discharge from one first coke carrier outlet 31 of this revivifier 3 side lower part.
Wherein, in step 3) in, during from this opening for feed of this gasoline stock 1 middle and lower part input atomizing steam and stock oil, be to be inclined upwardly in the angle of 30 ~ 45 ° charging with this gasoline stock 1.
Wherein, in step 4) in, specifically, stock oil is attached to hot coke carrier surface as a mist, move upward with fluidised hot coke carrier, in the process, the heat entrained by hot coke carrier is relied on to carry out pyrogenic reaction (the gas phase hydrocarbon component that pyrogenic reaction generates, further promote the fluidization of hot coke carrier, namely, attached to the fluidization of the hot coke carrier of mist stock oil, is produce under the gas phase hydrocarbon component acting in conjunction promoting steam and reaction generation).Make charging close to plug flow thus, decrease back-mixing, thus can improve the phenomenon that the common fluidized status of flexicoking is not good, fluidized-bed obviously rocks, and improve the problems such as reactor coking rate is fast.
Wherein, in step 5) in, unreacted heavy hydrocarbon component cooled in settling vessel 2 and revivifier 3 (cooling can be undertaken by waiting for another strand the cold stock oil heat exchange that enters gasoline stock 1) completely in stock oil, after the lower part outlet 32 of this revivifier 3 is discharged, reenter this gasoline stock 1 along the turning oil reflux inlet 13 be arranged in the middle part of this gasoline stock 1, again carry out pyrogenic reaction.
Wherein, in step 5) in, the oil gas of full cut inputs after in this settling vessel 2 along the upper outlet 11 of this gasoline stock 1, first the coke powder removed in wherein gas phase hydrocarbon component is separated through cyclonic separator, then again the oil gas of this full cut is cooled (cooling can be undertaken by waiting for another strand the cold stock oil heat exchange that enters gasoline stock 1), finally again the upper outlet 21 of the oil gas of this full cut from this settling vessel 2 is discharged, be separated into the hydrocarbon component of downstream needs through coke separation column.
Wherein, in step 5) in, coke powder lays respectively at two places, and a part is mixed in gas phase hydrocarbon component, and another part is deposited on cold coke carrier.After coke powder is collected, for heat needed for pyrogenic reaction after a part of incendivity, remainder coke can carry out water-gas reaction with water vapour and generate water-gas, isolate further hydrogen for refinery other with hydrogen production device.
Wherein, in step 5) in, cold coke carrier is after the first coke carrier outlet 31 of this revivifier 3 is discharged (now the temperature of cold coke carrier is 510 ~ 520 DEG C), enter a well heater 4 and carry out heat exchange, be heated to be after hot coke carrier until cold coke carrier, again input this gasoline stock 1 from this first coke carrier inlet 16.
Wherein, this cold coke carrier and this hot coke carrier are granularity at the refinery coke of 40 ~ 1000 μm.
Wherein, the circulation of coke carrier between this well heater 4, this gasoline stock 1, this settling vessel 2 and this revivifier 3 is for maintaining by promoting steam, and the impellent of coke carrier loop is determined by the pressure equilibrium parameter of revivifier 3 and well heater 4.And, a guiding valve 161 is provided with on the first coke carrier inlet 16 of this gasoline stock 1 and the connecting pipeline of this well heater 4, the internal circulating load of coke carrier is controlled by this guiding valve 161, the sliding contact surface of guiding valve 161 uses hard surface process to make minimise wear, coke line (comprising stack gas) use unique heat-resisting/wear resistance lining.
Wherein, the heat of this well heater 4 is provided by a gasifier 5, this gasifier 5 has gas inlet 52 and a steam-in 51, by the coke powder that this pyrogenic reaction generates, the steam that the air inputted with this gas inlet 52 and this steam-in 51 input carries out reacting that (temperature of reaction is 927 ~ 982 DEG C, this temperature controls by regulating the ratio of air and steam, and the air velocity that the amount of coke in gasifier 5 enters gasifier 5 by adjustment controls), generate containing CO
2, CO, H
2with synthetic gas and the heat of rare gas element.Described synthetic gas carries the heat that reaction generates, and coke powder, air and steam are fed in well heater 4, for well heater 4 bed fluidisation and heat transmission in the lump completely with unreacted.Thus, cold coke carrier in well heater 4 is heated to be hot coke carrier, coke powder major part is discharged from the coke powder relief outlet 41 of well heater 4 bottom, small portion coke powder is mixed in gas, next, in air, steam and synthetic gas in input well heater 4 and gas, the coke powder that is mingled with then is discharged in a recovery system by well heater 4 top, sequentially by vapour generator 6, cyclonic separator 7, coke powder collection device 8, gas desulphurisation plant 9 and a sulfur recovery facility 10 of this recovery system.After coke powder is separated in cyclonic separator 7, be recovered in coke powder collection device 8, discharged by the coke powder relief outlet 81 of coke powder tripping device 8.Remaining gas fraction (synthetic gas, air, steam) is then by this gas desulphurisation plant 9, sour water is discharged from a sour water outlet 91 of gas desulphurisation plant 9, again by sulfur recovery facility 10, final generating clean fuel gas, for other equipment of refinery or third party user.
Wherein, this inferior heavy oil is at least one in vacuum residuum, long residuum, heavy crude, decompressed wax oil, oil sands bitumen, de-oiled asphalt, deasphalted oil, residual hydrogenation heavy oil, thermal cracking residue, the extraction oil of lube oil finishing, the turning oil of catalytic cracking and clarified oil, cracking of ethylene residual oil and tar-bitumen.
Wherein, Level control is established on this gasoline stock 1 top, to control the pyrogenic reaction time, meets the needs of riser tube pyrogenic reaction time.
Wherein, this pyrogenic reaction temperature is 515 ~ 565 DEG C, is preferably 520 ~ 550 DEG C.Namely, according to design of the present utility model, pyrogenic reaction is carried out as the reactor in flexicoking technique using gasoline stock 1, desired reaction temperature higher 30 ~ 50 DEG C than conventional delayed coking reaction temperature (conventional delayed coking reaction temperature is about 490 ~ 510 DEG C), control pyrogenic reaction temperature of the present utility model within the scope of this, the technique effect of the utility model expection could be realized, the problems such as solution reactor coking speed is fast, and pyrogenic reaction liquid yield of the present utility model is higher, and in product, olefin(e) centent is high.
Wherein, in this pyrogenic reaction, the oil circulation ratio of charcoal of this gasoline stock 1 is 1:11 ~ 12 (weight ratios).That is, the coke recycle of the application is larger than Conventional catalytic cracking agent-oil ratio.
Wherein, this pyrogenic reaction process does not need configuration large air separation plant supply pure oxygen.
Wherein, the time of this pyrogenic reaction is 15 ~ 30s.That is, the process that stock oil carries out this pyrogenic reaction at this gasoline stock 1 inner edge rising edge is about 15 ~ 30s.
Wherein, the height of this gasoline stock 1 is 10 ~ 20 meters, is preferably 18 meters.The height of this gasoline stock 1 is determined by reaction required time.
Wherein, the diameter of this gasoline stock 1 is 150mm ~ 200mm.The diameter of this gasoline stock 1 is determined by inlet amount.The linear speed that gasoline stock 1 of the present utility model adopts is opening for feed place is 4 ~ 7m/s, and upper outlet 11 place of gasoline stock is 12 ~ 18m/s.
Embodiment 1
In the present embodiment, a pyrogenic reaction is carried out using a gasoline stock 1 as the reactor in flexicoking technique, described pyrogenic reaction is: take inferior heavy oil as stock oil, in described gasoline stock 1, carry out thermo-cracking, produces oil gas and the coke of full cut.Wherein, described pyrogenic reaction comprises the steps:
1) this gasoline stock 1 and a settling vessel 2 and a revivifier 3 are formed a flexicoking reactive system jointly, make this settling vessel 2 be arranged at the top of this revivifier 3, and the upper outlet 11 of this gasoline stock 1 stretches in this settling vessel 2;
2) steam is promoted from a lower ending opening 17 input of this gasoline stock 1, and input hot coke carrier from one first coke carrier inlet 16 of gasoline stock 1 side-lower, hot coke carrier is advanced with the top of flow-like to this gasoline stock 1 under the effect promoting steam;
3) from an opening for feed input atomizing steam of this gasoline stock 1 middle and lower part and stock oil (to be inclined upwardly in the angle of 30 ~ 45 ° charging with this gasoline stock 1), stock oil is made to enter this gasoline stock 1 with Sprayable, and be attached to hot coke carrier surface, move upward with hot coke carrier;
4) stock oil is made to carry out this pyrogenic reaction at this gasoline stock 1 inner edge rising edge, heavy hydrocarbon component thermo-cracking in reacted rear stock oil is oil gas (comprising gas phase hydrocarbon component, petroleum naphtha, diesel oil and wax oil etc.) and the coke powder of full cut, hot coke carrier for pyrogenic reaction heat is provided after become cold coke carrier;
5) by unreacted in the oil gas of full cut, coke powder, cold coke carrier and stock oil completely heavy hydrocarbon component input in this settling vessel 2 along the upper outlet 11 of this gasoline stock 1, then the oil gas of full cut is wherein discharged along settling vessel 2 upper outlet 21, collect coke powder, and to make in stock oil unreacted completely heavy hydrocarbon component fall into this revivifier 3 and discharge from the lower part outlet 32 of this revivifier 3, and make cold coke carrier fall into this revivifier 3 and discharge from one first coke carrier outlet 31 of this revivifier 3 side lower part.
Wherein, this pyrogenic reaction temperature is 515 DEG C, and the pyrogenic reaction time is 15s; The height of riser reactor 1 is 10 meters, and diameter is 150mm, and the linear speed of employing is opening for feed place is 4m/s, upper outlet 11 place of gasoline stock is 12m/s; And the oil circulation ratio of charcoal of this riser reactor 1 is 1:11 (weight ratio).
Embodiment 2
In the present embodiment, a pyrogenic reaction is carried out using a gasoline stock 1 as the reactor in flexicoking technique, described pyrogenic reaction is: take inferior heavy oil as stock oil, in described gasoline stock 1, carry out thermo-cracking, produces oil gas and the coke of full cut.Wherein, described pyrogenic reaction step is identical with embodiment 1, and difference is:
Wherein, this pyrogenic reaction temperature is 565 DEG C, and the pyrogenic reaction time is 30s; The height of riser reactor 1 is 20 meters, and diameter is 200mm, and the linear speed of employing is opening for feed place is 7m/s, upper outlet 11 place of gasoline stock is 18m/s; And the oil circulation ratio of charcoal of this riser reactor 1 is 1:12 (weight ratio).
Embodiment 3
In the present embodiment, a pyrogenic reaction is carried out using a gasoline stock 1 as the reactor in flexicoking technique, described pyrogenic reaction is: take inferior heavy oil as stock oil, in described gasoline stock 1, carry out thermo-cracking, produces oil gas and the coke of full cut.Wherein, described pyrogenic reaction step is identical with embodiment 1, and difference is:
Wherein, this pyrogenic reaction temperature is 520 DEG C, and the pyrogenic reaction time is 20s; The height of riser reactor 1 is 18 meters, and diameter is 165mm, and the linear speed of employing is opening for feed place is 5m/s, upper outlet 11 place of gasoline stock is 14m/s; And the oil circulation ratio of charcoal of this riser reactor 1 is 1:11 (weight ratio).
Embodiment 4
In the present embodiment, a pyrogenic reaction is carried out using a gasoline stock 1 as the reactor in flexicoking technique, described pyrogenic reaction is: take inferior heavy oil as stock oil, in described gasoline stock 1, carry out thermo-cracking, produces oil gas and the coke of full cut.Wherein, described pyrogenic reaction step is identical with embodiment 1, and difference is:
Wherein, this pyrogenic reaction temperature is 550 DEG C, and the pyrogenic reaction time is 25s; The height of riser reactor 1 is 15 meters, and diameter is 180mm, and the linear speed of employing is opening for feed place is 6m/s, upper outlet 11 place of gasoline stock is 16m/s; And the oil circulation ratio of charcoal of this riser reactor 1 is 1:12 (weight ratio).
Below in conjunction with specific experiment data, technique effect of the present utility model is described in detail.
The utility model has carried out contrast test in laboratory to the flexicoking technique of prior art and employing gasoline stock processing inferior heavy oil.This testing apparatus by gasoline stock 1, well heater 4 and vaporizer 5 and oil gas be separated and the part such as desulfurization of low heating value gas forms.Gasoline stock 1 height 14m, internal diameter is 186mm.Opening for feed is nozzle and prolongs circumference to be evenly arranged, and nozzle installation angle is 30 °, promotes steam and adopts steam and nitrogen.
By controlling gasoline stock 1 top material level, make pyrogenic reaction speed at about 20 seconds.Temperature of reaction selects 530 DEG C.The oil circulation ratio of charcoal is 11 ~ 12 (weights).Thermophore-Jiao grain is granularity 40 ~ 1000 μm, the refinery coke that median particle size is 400 μm.Material balance contrast is as follows:
Table 1 existing flexicoking technology material balance
Table 2 adopts riser reactor flexicoking technology material balance
Contrast as can be seen from material balance: the utility model can effectively slow down reactor coking rate; Meanwhile, liquid product yield is improved.
As can be seen here, compared with prior art, the utility model adopts and promotes tubular type coking reactor, replaces the original major diameter reactor of flexicoking, really can improve the problems such as the common fluidized status of flexicoking is not good, the obvious shaking phenomenon of fluidized-bed, reactor coking rate are fast.Also effectively can control coke powder reserve in reactor, improve liquid product yield.
Certainly; the utility model also can have other various embodiments; when not deviating from the utility model spirit and essence thereof; those of ordinary skill in the art can make various corresponding change and distortion according to the utility model, but these change accordingly and are out of shape the protection domain that all should belong to the utility model claim.
Claims (10)
1. process a flexicoking process unit for inferior heavy oil, it is characterized in that, comprising:
One gasoline stock, this gasoline stock is provided with a upper outlet, a lower ending opening, one first coke carrier inlet and an opening for feed, this upper outlet and this lower ending opening are arranged at the two ends up and down of this gasoline stock respectively, this the first coke carrier inlet is arranged at the side-lower of this gasoline stock, this opening for feed is arranged at the middle and lower part of this gasoline stock, further, this opening for feed connects an atomizing steam entrance and a stock oil entrance;
One settling vessel, the upper outlet of this gasoline stock stretches in this settling vessel, and this settling vessel has a upper outlet; And
One revivifier, this settling vessel is arranged at the top of this revivifier, and this revivifier has a lower part outlet and one first coke carrier outlet, and this first coke carrier outlet is arranged at the side lower part of this revivifier.
2. the flexicoking process unit of processing inferior heavy oil according to claim 1, is characterized in that, the pipeline of this opening for feed and this gasoline stock are the angle of 30 ~ 45 °.
3. the flexicoking process unit of processing inferior heavy oil according to claim 1, is characterized in that, the middle part of this gasoline stock is provided with a turning oil reflux inlet, is connected with the lower part outlet of this revivifier.
4. the flexicoking process unit of processing inferior heavy oil according to claim 1, is characterized in that, Level control is established on this gasoline stock top.
5. the flexicoking process unit of processing inferior heavy oil according to claim 1, is characterized in that, the height of this gasoline stock is 10 ~ 20 meters.
6. the flexicoking process unit of processing inferior heavy oil according to claim 1, is characterized in that, the diameter of this gasoline stock is 150mm ~ 200mm.
7. the flexicoking process unit of processing inferior heavy oil according to claim 1, is characterized in that, also comprises a well heater, is connected with the first coke carrier inlet of this gasoline stock and the first coke carrier outlet of this revivifier.
8. the flexicoking process unit of processing inferior heavy oil according to claim 7, is characterized in that, on the first coke carrier inlet of this gasoline stock and the connecting pipeline of this well heater, be provided with a guiding valve.
9. the flexicoking process unit of processing inferior heavy oil according to claim 7, is characterized in that, also comprises a gasifier, is connected with this well heater, and this gasifier has a gas inlet and a steam-in.
10. the flexicoking process unit of processing inferior heavy oil according to claim 7, it is characterized in that, also comprise a recovery system, be connected to the top of this well heater, this recovery system comprises the vapour generator, a cyclonic separator, a coke powder collection device, a gas desulphurisation plant and the sulfur recovery facility that are linked in sequence.
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| CN201520873599.XU CN205133519U (en) | 2015-11-04 | 2015-11-04 | Process flexicoking process units of heavy oil inferior |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106635124A (en) * | 2015-11-04 | 2017-05-10 | 中国石油天然气股份有限公司 | Flexible coking process method and device for processing inferior heavy oil |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106635124A (en) * | 2015-11-04 | 2017-05-10 | 中国石油天然气股份有限公司 | Flexible coking process method and device for processing inferior heavy oil |
| CN106635124B (en) * | 2015-11-04 | 2018-10-16 | 中国石油天然气股份有限公司 | Process the flexicoking process and device of inferior heavy oil |
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