CN102453500A - Catalytic cracking method and equipment for hydrocarbon oil - Google Patents
Catalytic cracking method and equipment for hydrocarbon oil Download PDFInfo
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- CN102453500A CN102453500A CN2010105195351A CN201010519535A CN102453500A CN 102453500 A CN102453500 A CN 102453500A CN 2010105195351 A CN2010105195351 A CN 2010105195351A CN 201010519535 A CN201010519535 A CN 201010519535A CN 102453500 A CN102453500 A CN 102453500A
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Abstract
The invention discloses a catalytic cracking method for hydrocarbon oil. The method is characterized by comprising the following steps of: (1) undergoing a first contact reaction on a hydrocarbon oil raw material and a first cracking catalyst in a first reactor, and performing first oil-agent separation on a mixture of oil gas and the catalyst after the first contact reaction; (2) undergoing a second contact reaction on oil gas obtained after first oil-agent separation and a second newly-added cracking catalyst in a second reactor, and performing second oil-agent separation; and (3) feeding a part of or all of a spent catalyst obtained in the step (2) into the first reactor. The invention further provides catalytic cracking equipment for hydrocarbon oil. Due to the adoption of the method and the equipment, the problem of poor activity in the second reactor caused by great reduction in the activity of the catalyst discharged from the first reactor is solved, and the yields of dry gas and coke can be lowered greatly.
Description
Technical field
The present invention relates to a kind of hydrocarbon oil catalytic cracking method and hydrocarbon oil catalytic cracking equipment.
Background technology
Catalytic cracking is one of most important secondary processing means in refining of petroleum field.
From development in recent years, catalytic cracking technology will continue development around following main aspect:
The processing heavy feed stock.Owing to, utilize catalytic cracking technology processing heavy, inferior feedstock oil such as normal pressure residual oil, vacuum residuum, wax tailings and diasphaltene wet goods can obtain bigger economic benefit to the raising of continuous growth of the demand of lightweight oil and crude oil price.How solving in processing problem such as serious, the coke yield height of heavy metal contamination catalyzer during heavy feed stock, is the developing important directions of catalytic cracking process.
The novel process that adapts to multiple production needs.For example, the oiling bonded novel technique of industrial chemicals such as the technology of light oil with high yield oil and voluminous ethene, propylene, butylene.
Reduce environmental pollution.Along with the increasingly stringent of environmental regulation, the essential more fuel and the product of cleaning produced of catalytic cracking is as reducing the quantity discharged of content of olefin in gasoline, sulphur content and CCU itself.
Riser reactor has that the unit volume treatment capacity is big, gas-solid contact efficiency advantages of higher and widespread use.In the riser catalytic cracking reaction process, the raw oil after the preheating contacts, vaporizes and react with high temperature catalyst from revivifier after nozzle gets into reactor drum, and the reaction times is greatly about 3 seconds.But because the contrary gravity field of gas-solid and stream flows; Exist the bigger diameter of axle to the mobile ununiformity in the riser tube, the gas-solid back-mixing is big, residence time skewness etc.; And because the sedimentation of coke that generates in the reaction process on catalyst surface and active site, sharply descends activity of such catalysts.Research shows that the catalyst activity in riser tube exit has only about 1/3 of initial activity at present, and reaction was carried out about 1 second, and activity of such catalysts descends about 50%.Like this, sharply descend in the second half section of riser reactor activity of such catalysts, katalysis greatly weakens, and heat cracking reaction increases, and produces more dry gas and increases content of olefin in gasoline.
Catalytic cracking reaction is the reaction system of a complicacy, is a parallel consecutive reaction process on the whole.Main reaction has reactions such as cracking, cyclisation, isomerizing, aromizing, hydrogen transference, alkylation, condensation.Above-mentioned reaction needed different reaction conditions is beneficial to the cracking reaction of heat absorption like high temperature, and is unfavorable for hydrogen transference, isomerizing and alkylated reaction.These several kinds reactions all are the important reactions in the catalytic cracking process, but their reaction conditions is a contradiction.For addressing this problem, software engineering researchers invent many relevant art solve, such as ending agent technology, two-stage riser technological (CN1118539C), series connection riser tube technology MIP (CN1237477A), technological (CN1069054A) technology of double lifting leg etc.CN1237477A has proposed catalyst cracker is divided into the notion of two reaction zones, and has developed corresponding riser reactor.Its main thought is the first reaction zone riser tube with the cracking reaction that generates alkene is main, generates second reaction zone that the intermediate product that is rich in alkene gets into hole enlargement again and carries out secondary reaction.The reaction of second reaction zone mainly comprises the cracking of isomerizing, hydrogen transference and appropriateness, reaches the purpose that reduces gasoline olefin and increased low carbon olefine output.
CN1065903C discloses a kind of method of producing low-carbon alkene and high aromatic-hydrocarbon gasoline simultaneously, comprises that making heavy petroleum hydrocarbon and water vapor is that the riser tube bottom contacts with zeolite containing catalyst in the bottom of a compound reactor of being made up of riser tube and dense phase fluidized bed; To be the dense phase fluidized bed bottom contact with zeolite containing catalyst from riser tube on the top that makes light petroleum hydrocarbon get into compound reactor; Reaction product isolated obtains dry gas, liquefied gas, gasoline, diesel oil and slurry oil; Reclaimable catalyst recycles after stripping and regeneration.The characteristics of this method are that the heavy crude hydrocarbon feed with catalyzer catalytic cracking reaction takes place in riser reactor earlier; Post reaction mixture gets into fluidized-bed reactor together with catalyzer and carries out aromatization with light petroleum hydrocarbon afterwards; Thereby in same device, carrying out catalytic cracking and aromatization under the katalysis of same catalyzer successively; Improve the particularly productive rate of propylene of low-carbon alkene, the aromaticity content in the gasoline is increased to about 80 weight %.
Summary of the invention
The objective of the invention is for a kind of hydrocarbon oil catalytic cracking method different with prior art and hydrocarbon oil catalytic cracking equipment are provided.
The invention provides a kind of hydrocarbon oil catalytic cracking method, it is characterized in that, this method may further comprise the steps:
(1) make the hydrocarbon oil crude material and first cracking catalyst in first reactor drum, carry out first contact reacts; Oil gas after first contact reacts and mixture of catalysts are carried out first finish separate, the catalyzer after first finish separates obtains reclaimable catalyst behind stripping;
(2) oil gas that obtains after the separation of first finish is carried out second contact reacts with initiate second cracking catalyst in second reactor drum and/or fluidized-bed reactor; Oil gas after second contact reacts and mixture of catalysts are carried out second finish separates; Catalyzer after second finish separates obtains reclaimable catalyst behind stripping, subsequent separation system is derived and be delivered to the oil gas after second finish is separated;
(3) step (2) gained reclaimable catalyst is partly or entirely sent in said first reactor drum in the step (1);
Wherein, Said first reactor drum is a riser reactor; Said second reactor drum is riser reactor or fluidized-bed reactor, and said first cracking catalyst and second cracking catalyst are identical or different, is selected from least a in live catalyst, regenerated catalyst and half regenerated catalyst.
The present invention also provides a kind of hydrocarbon oil catalytic cracking equipment; This equipment comprises first reactor drum, first settlement separator, second reactor drum and second settlement separator; Said first reactor drum is a riser reactor; Said second reactor drum is riser reactor or fluidized-bed reactor; The bottom of first reactor drum is communicated with the first catalyzer input tube, catalyst recirculation pipe, the first spent agent output tube, first the lifting medium input tube and first feed-pipe in advance, and first feed-pipe is positioned at the first catalyzer input tube, catalyst recirculation pipe and first promotes medium input tube top in advance; The outlet on the first reactor drum top is positioned at first settlement separator, and has first gas-solid separator in this exit of first settlement separator and be used for the material that comes out from first reactor drum is carried out gas solid separation; The top of first settlement separator has at least one opening, is used for being communicated with the opening for feed of second reactor drum; The bottom of second reactor drum is communicated with the second catalyzer input tube, and the opening for feed of second reactor drum is positioned at second catalyzer input tube top; The outlet on the second reactor drum top is positioned at second settlement separator; And have second gas-solid separator is used for the material that comes out from second reactor drum is carried out gas solid separation in the exit of said second reactor drum; The bottom of second settlement separator is communicated with the second spent agent output tube; Said catalyst recirculation pipe is communicated with this second spent agent output tube or directly is communicated with the bottom of second settlement separator; The top of second settlement separator is provided with gas pipeline, and subsequent separation system is derived and be delivered to the oil gas that is used for reaction is generated.
The present invention makes full use of the advantage of riser reactor, in conjunction with the notion in differential responses district, a kind of novel hydrocarbon oil catalytic cracking equipment and hydrocarbon oil catalytic cracking method is provided; Promptly; Raw oil after the preheating is introduced into first reactor drum, contacts the generation catalytic cracking reaction in short-term with high-temperature regenerated catalyst, then finish is separated; Catalyzer goes revivifier regeneration behind stripping, and oil gas then gets into second reactor drum and contacts with catalyzer from revivifier and react.At second reactor drum, can take different operating conditions according to the difference of target product, as being target, can take low temperature, high agent-oil ratio operation to reduce gasoline olefin; When with low carbene, when being rich in aromatic type gasoline and being target product, can take relatively harsh operational condition, i.e. high temperature, high agent-oil ratio operation.
The present invention sends into second reactor drum through making after the gained mixture separation goes out catalyzer behind first reactor reaction; On the one hand through the high activated catalyst after or the regeneration fresh in the use of second reactor drum; Thereby the catalyst activity that can avoid coming out owing to first reactor drum reduces the active insufficient problem in second reactor drum that causes greatly, thereby can effectively bring into play the effect as second reactor drum of second stage reactor; On the other hand through the product that obtains behind first reactor reaction is directly sent in second reactor drum without separation, thus can avoid the part charging to cool off repeatedly and to gasify shortcoming that energy expenditure increases.In addition, take place at one section riser reactor because green coke reaction is most of, therefore green coke is less on two sections riser reactor inner catalysts, and it is active that the spent agent activity that two sections riser reactors are discharged is higher than the spent agent that one section riser reactor discharges.Spent agent through two sections riser reactors of a part are discharged turns back to one section riser reactor; With get into fresh dose of one section riser reactor, regenerator, partly rise agent again or their mixture mixes; Can reduce by one section riser reactor finish contact temperature, the rising agent oil ratio.
Description of drawings
Fig. 1 is the structural representation of the hydrocarbon oil catalytic cracking equipment of first kind of embodiment of the present invention;
Fig. 2 is the structural representation of the hydrocarbon oil catalytic cracking equipment of second kind of embodiment of the present invention;
Fig. 3 is the structural representation of the hydrocarbon oil catalytic cracking equipment of the third embodiment of the present invention.
Embodiment
According to hydrocarbon oil catalytic cracking method provided by the invention; This method may further comprise the steps: (1) makes the hydrocarbon oil crude material and first cracking catalyst in first reactor drum, carry out first contact reacts; Oil gas after first contact reacts and mixture of catalysts are carried out first finish separate, the catalyzer after first finish separates obtains reclaimable catalyst behind stripping;
(2) oil gas that obtains after the separation of first finish is carried out second contact reacts with initiate second cracking catalyst in second reactor drum and/or fluidized-bed reactor; Oil gas after second contact reacts and mixture of catalysts are carried out second finish separates; Catalyzer after second finish separates obtains reclaimable catalyst behind stripping, subsequent separation system is derived and be delivered to the oil gas after second finish is separated;
(3) step (2) gained reclaimable catalyst is partly or entirely sent in said first reactor drum in the step (1);
Wherein, Said first reactor drum is a riser reactor; Said second reactor drum is riser reactor/or fluidized-bed reactor, and said first cracking catalyst and second cracking catalyst are identical or different, is selected from least a in live catalyst, regenerated catalyst and half regenerated catalyst.
The said first catalytic time can be 0.1-3 second, was preferably 0.5-2.5 second.Through controlling for the first catalytic time, the reaction raw materials overcracking can be prevented, thereby the yield of coke and dry gas can be reduced, improve the yield of target product thus.
Under the preferable case, hydrocarbon oil crude material is 0.01-0.8MPa, more preferably 0.1-0.5MPa with the pressure that first cracking catalyst contacts in first reactor drum; Temperature is 450-680 ℃, more preferably 450-580 ℃; The agent weight of oil is than for 1-20: 1, and 3-15 more preferably: 1.
Further under the preferable case, hydrocarbon oil crude material is 0.1-0.5MPa with the pressure that first cracking catalyst contacts in first reactor drum, and temperature is 480-580 ℃, and the agent weight of oil is than being 3-15: 1.
Among the present invention, the agent weight of oil in said first reactor drum is than the gross weight that is meant all interior catalyzer of first reactor drum (comprise initiate second cracking catalyst and from the spent agent of second reactor drum) and the weight ratio of hydrocarbon oil crude material.
The said initiate second cracking catalyst consumption is as the criterion to carry out the second catalytic requirement in satisfied second reactor drum; Under the preferable case; The weight ratio of first cracking catalyst and reclaimable catalyst described in first reactor drum is 1: 0.001-0.8, more preferably 1: 0.01-0.6.
When said second reactor drum was riser reactor, under the preferable case, the said second catalytic residence time was 0.1-10 second, and pressure is 0.01-0.6MPa, and temperature is 400-680 ℃, and the agent weight of oil is than being 1-40: 1.The further preferred said second catalytic residence time is 0.5-8 second, and pressure is 0.1-0.3MPa, and temperature is 485-650 ℃, and the agent weight of oil is than being 3-30: 1.
When said second reactor drum was fluidized-bed reactor, under the preferable case, the second catalytic condition comprised that weight space velocity is 1-50 hour
-1, temperature of reaction is 400-680 ℃, and pressure is 0.01-0.6MPa, and the agent weight of oil is than being 1-20: 1.Further under the preferable case, the second catalytic condition comprises that weight space velocity is 2-40 hour
-1, temperature of reaction is 460-650 ℃, and pressure is 0.1-0.6MPa, and the agent weight of oil is than being 1-20: 1.
The said second catalytic condition can be confirmed according to required target product, as being target to reduce gasoline olefin, can take low temperature, high agent-oil ratio operation; When with low carbene, when being rich in aromatic type gasoline and being target product, can take relatively harsh operational condition, i.e. high temperature, high agent-oil ratio operation.For example, when title product was low-carbon alkene, use temperature was 650-750 ℃ of preferred 680-700 ℃ a regenerated catalyst, and made temperature of reaction be 480-650 ℃ to be preferably 490-550 ℃; When title product was the especially low alkene of gasoline, high-octane rating, low-sulphur oil, use temperature was 650-700 ℃ of preferred 660-690 ℃ a regenerated catalyst, and made temperature of reaction be 450-530 ℃ to be preferably 485-520 ℃.
The said method of first cracking catalyst of inactivation of isolating in the reaction product can comprise reaction product is carried out sharp separation and/or settlement separate.
According to the present invention; Oil gas after first contact reacts and mixture of catalysts are carried out first finish separates; Catalyzer after first finish separates obtains the method for reclaimable catalyst for as well known to those skilled in the art behind stripping; For example, can adopt the oil gas after first contact reacts is contacted with the stripping medium with mixture of catalysts, carry out steam stripped method.The method that oil gas after first contact reacts and mixture of catalysts are contacted with the stripping medium can be carried out stripping and contacts for feeding the stripping medium in the oil gas after first contact reacts in stripper and the mixture of catalysts.Said stripping medium can for various not with the material of oil gas and mixture of catalysts reaction, for example can be water vapour.Said steam stripped concrete operations condition and method have been conventionally known to one of skill in the art.
According to one embodiment of the present invention; This method also comprises in second reactor drum adds hydrocarbon ils; Oil gas and initiate second cracking catalyst after making the hydrocarbon ils added and first finish separating are carried out said second contact reacts, and said hydrocarbon ils is one or more in said hydrocarbon oil crude material, dry gas, liquefied gas, lighter hydrocarbons, gasoline, diesel oil, recycle stock, the slurry oil.
Oil gas after second contact reacts and mixture of catalysts are carried out second finish separate, the catalyzer after second finish separates obtains reclaimable catalyst behind stripping method also can adopt the isolating method of above-mentioned first finish.
Among the present invention,, adopt one section first reactor drum of catalyst replaced after regenerating to lose most of active catalyzer, help oil gas and further react at second reactor drum.Can adopt different operating conditions according to different target products at two sections second reactor drums.For example, when being title product, can under the high temperature high severity, react with the low-carbon alkene.When hanging down the alkene high-octane rating to produce, when low-sulphur oil is product, can adopting low temperature demulcent reaction conditions.Second reaction zone is owing to adopt second reactor drum, and the gas-solid contact efficiency is high, and the residence time is long, helps the generation of target product.At i.e. first reactor drum of first stage reactor, be main with the cracking reaction of heavy oil, and at i.e. second reactor drum of second stage reactor; It then is the secondary reaction of the intermediate product after the preliminary cracking; Secondary reaction needs a bit, and like secondary cracking of hydrogen transference, isomerizing, intermediate product alkene etc., some is unnecessary; Reaction generates dry gas, condensation reaction green coke etc. like overcracking.Adopt two reactor drums, the different operating mode, suitable condition that just can the various reactions of flexible not only can improve feed stock conversion, improves product and distributes, and can also improve the quality of products.
Reclaimable catalyst behind the second-stage reaction is returned in one section reaction with agent-oil ratio that improves one section reaction or the temperature that reduces by one section reaction, thereby can further improve feed stock conversion, improve product and distribute and improve the quality of products.
The present invention can be suitable for the plurality of raw materials type, like various distillates, deasphalted oil, wax tailings, the hydrogenation heavy oil of time processing, mix refining long residuum, vacuum residuum and all kinds crude oil.
First cracking catalyst according to the invention and second cracking catalyst can be the various cracking catalyst that is used for the cracking hydrocarbon oil reaction well known in the art; And first cracking catalyst is identical with the composition of second cracking catalyst, but said first cracking catalyst and second cracking catalyst can be independently selected from least a in live catalyst, regenerated catalyst and half regenerated catalyst separately.For example can be Y zeolite catalyzer and/or the sieve catalyst that contains ZSM-5.Under the preferable case; Said cracking catalyst is the cracking catalyst that contains molecular sieve, said molecular sieve be contain or not phosphorus element-containing y-type zeolite, contain or do not contain REE ultrastable Y, contain or one or more in the supersiliceous zeolite with five-membered ring structure, β zeolite, mordenite, omega zeolite of phosphorus element-containing not.Above-mentioned catalyzer for example can be the catalytic cracking agent MLC-500 poiser produced of the Sinopec catalyst Co. that is purchased and the MMC-2 catalyzer poiser of voluminous low-carbon (LC).
According to hydrocarbon oil catalytic cracking method provided by the invention, under the preferable case, this method can also may further comprise the steps:
(4) the said reclaimable catalyst of step (1) gained and the said reclaimable catalyst of step (2) remainder are carried out coke burning regeneration, obtain regenerated catalyst, perhaps obtain regenerated catalyst and half regenerated catalyst;
(5) regenerated catalyst and/or half regenerated catalyst that obtain after will regenerating return first reactor drum and/or second reactor drum.
Reclaimable catalyst is carried out regenerated condition and method for conventionally known to one of skill in the art, and the present invention repeats no more at this.
The present invention can be used to produce the different target product like low alkene, high isoparaffin gasoline; Low-carbon alkenes such as fecund ethene, propylene, butylene are also produced the cracking process that is rich in aromatic type gasoline, and the sulphur content of gasoline products is also than adopting conventional catalytic cracking process that remarkable reduction is arranged.
Hydrocarbon oil crude material is introduced into one section first reactor drum and in the presence of two sections spent agents that obtain, contacts with first cracking catalyst and carry out initial reaction; Gas-solid separates then; The catalyzer of carbon deposit removes the revivifier coke burning regeneration behind stripping; Second reactor drum that the oil gas entering is two sections contacts with second cracking catalyst, further reaction.Adopt the present invention, can improve the raw material per pass conversion, reduce the productive rate of dry gas and coke, improve product and distribute.According to the difference of target product, two reactor drums can be taked different operating conditions, realize flexible operating.
Although the catalytic cracking technology of segmentation reaction also can be raw material one section reaction zone contact with catalyzer react after; Oil gas and catalyst separating get into the later separation device, separate the gasoline, diesel oil or the unconverted heavy oil that obtain and advance two sections reactor reaction again.But have the part charging to cool off repeatedly and to gasify like this, energy expenditure increases.Therefore the present invention preferably carries out first finish in the outlet of first reactor drum and separates, and catalyzer goes regeneration behind stripping, oil gas without separate or extra cooling step after directly follow-up second reactor drum of entering and the second cracking catalyst contact reacts.The operational condition of two reactor drums is different, can give full play to riser tube and the advantage of two kinds of reactor drums of bed and the effect of catalyzer, improves raw material per pass conversion and target product selectivity, and can improve quality product, makes it more to meet the requirement of environmental regulation.In addition, prior art adopts one section reaction zone catalyst system therefor to continue to get into the reaction of second-stage reaction district and since this part catalyzer through one section reaction after activity reduce greatly, so limited two sections roles.The present invention is on the basis of existing catalytic cracking technology, and a kind of built-up type catalytic cracking reaction technology and device are provided.Concrete grammar is: raw oil contacts, reacts with regenerated catalyst at one section first reactor drum earlier; Reacted oil gas gets into two sections reactor drum continuation reaction after isolating catalyzer soon, two sections part spent agent returns one section first reactor drum and the regenerator mixed cycle is used.Adopt the present invention, can adopt different operating modes to reach optimum feed stock conversion and product selectivity at two reactor drums to differential responses raw material and products scheme.
Extremely shown in Figure 3 like Fig. 1; Hydrocarbon oil catalytic cracking equipment provided by the invention comprises first reactor drum 2, first settlement separator 4, second reactor drum 5 and second settlement separator 6; Said first reactor drum is a riser reactor; Said second reactor drum is riser reactor or fluidized-bed reactor; The bottom of first reactor drum 2 is communicated with the first catalyzer input tube 1, catalyst recirculation pipe 9, the first spent agent output tube 10, first and promotes in advance that medium input tube 22 and first feed-pipe, 21, the first feed-pipes 21 are positioned at the first catalyzer input tube 1, catalyst recirculation pipe 9 and first promotes medium input tube 21 tops in advance; The outlet on first reactor drum, 2 tops is positioned at first settlement separator 4, and has first gas-solid separator 3 in this exit of first settlement separator 4 and be used for the material that comes out from first reactor drum 2 is carried out gas solid separation; The top of first settlement separator 4 has at least one opening, is used for being communicated with the opening for feed of second reactor drum 5; The opening for feed that the bottom of second reactor drum 5 is communicated with the second catalyzer input tube, 11, the second reactor drums 5 is positioned at the second catalyzer input tube, 11 tops; The outlet on second reactor drum, 5 tops is positioned at second settlement separator 6; And have second gas-solid separator 31 is used for the material that comes out from second reactor drum 5 is carried out gas solid separation in the exit of said second reactor drum 5; The bottom of second settlement separator 6 is communicated with the second spent agent output tube 8; Said catalyst recirculation pipe 9 is communicated with this second spent agent output tube 8 or directly is communicated with the bottom of second settlement separator 6; The top of second settlement separator 6 is provided with gas pipeline 25, and subsequent separation system is derived and be delivered to the oil gas that is used for reaction is generated.
According to the present invention, as long as first settlement separator 4 is communicated with second reactor drum 5, can realizes the oil gas that 4 separation of first settlement separator obtain sent in second reactor drum 5 and carry out second-stage reaction.Can realize above-mentioned connection through variety of way; For example; Can the top exit of first settlement separator 4 be communicated with (as shown in Figure 1) with the opening for feed of second reactor drum 5 through pipeline 15; Also can the opening for feed of second reactor drum 5 directly be connected (as shown in Figures 2 and 3) with first settlement separator, 4 tops, thus first settlement separator, 4 isolated oil gas directly the opening for feed of second reactor drum 5 through first settlement separator, 4 tops get in second reactor drum 5.
According to the present invention, said first gas-solid separator 31 and second gas-solid separator 32 can be preferably quick disconnector, more preferably inertial separator for the various separators that can realize catalyzer and oil gas gas solid separation separately.When said first gas-solid separator 31 and second gas-solid separator 32 were inertial separator, preferably each inertial separator was fixedly connected with the outlet of first reactor drum 2 and second reactor drum 5 separately.
Among the present invention, when said first reactor drum 2 and second reactor drum 5 were riser reactor, said first reactor drum 2 and second reactor drum 5 can be with various series system settings.A preferred embodiment of the invention, as shown in Figure 1, said first reactor drum 2 and second reactor drum 5 are arranged side by side, and are communicated with the opening for feed of second reactor drum 5 through the top exit of pipeline 15 with first settlement separator 4.Describe in the face of embodiment shown in Figure 1 down.
In this embodiment; Under the preferable case; This equipment also comprises the 4th gas-solid separator 71 and the 3rd gas-solid separator 72 that is positioned at second settlement separator, 6 tops that is positioned at first settlement separator 4; Be respectively applied for further the gas-oil mixture that first reactor drum 2 and second reactor drum 5 are produced and carry out gas solid separation, to isolate catalyst fines wherein.Said the 3rd gas-solid separator 72 and the 4th gas-solid separator 71 are preferably cyclonic separator separately.
Under the preferable case, as shown in Figure 1, also be provided with first collection chamber 13 in said first settlement separator 4, the oil gas of being used to collect from the 4th gas-solid separator 71, and this oil gas sent in second reactor drum 5; Also be provided with second collection chamber 14 in said second settlement separator 6, the oil gas of being used to collect from the 3rd gas-solid separator 72, and the oil gas of collecting derived and is delivered to subsequent separation system through gas pipeline 25.
According to another kind of preferred implementation of the present invention; When said second reactor drum is that fluidized-bed is when answering device; As shown in Figures 2 and 3; Said second settlement separator 6, second reactor drum 5, first settlement separator 4 and first reactor drum 2 set gradually from top to bottom, and the opening for feed of said second reactor drum 5 is communicated with the top of said first settlement separator 4.Under the situation of this embodiment, preferred second settlement separator 6, second reactor drum 5, first settlement separator 4 and the 2 coaxial settings of first reactor drum.Under the preferable case; Catalyst cracker provided by the invention also comprises the 3rd gas-solid separator 72 that is positioned at second settlement separator, 6 tops; Be used for the gas-oil mixture that second reactor drum produces is further carried out gas solid separation, to isolate the catalyst fines of wherein carrying secretly.Said the 3rd gas-solid separator 72 is preferably cyclonic separator.Because therefore the diameter of riser reactor will when second reactor drum 5 directly is communicated with first settlement separator 4, be compared with embodiment shown in Figure 1 much larger than the diameter of transportation pipe line usually, can reduce by the 4th gas-solid separator 71.
Under the preferable case, also be provided with second collection chamber 14 in said second settlement separator 6, the oil gas of being used to collect from the 3rd gas-solid separator 72, and the oil gas of collecting derived and is delivered to subsequent separation system through gas pipeline 25.Among the present invention, said collection chamber can be the various structures that can realize above-mentioned functions.
Under the preferable case, the bottom of the bottom of said first settlement separator 4 and/or second settlement separator (6) is provided with stripping stage separately, and the reclaimable catalyst that is used for that gas solid separation is obtained carries out gas and carries.When second reactor drum 5 and first reactor drum 2 adopt Fig. 2 and the mode that is provided with up and down shown in Figure 3; Can stripping stage (as shown in Figure 3) all be set in the bottom of first settlement separator 4 and the bottom of second settlement separator 6; Also can only be provided with stripping stage in the bottom of said first settlement separator 4; And the exit end of the said second spent agent output tube 8 is connected (as shown in Figure 2) with this stripping stage, thereby all can carrying out gas at the stripping stage of first settlement separator 4, the residue reclaimable catalyst of the reclaimable catalyst of first reactor drum 2 and second reactor drum 5 carries.When first reactor drum 2 and second reactor drum 5 adopt shown in Figure 1 when mode is provided with side by side; Can stripping stage (as shown in Figure 1) all be set in the bottom of first settlement separator 4 and the bottom of second settlement separator 6; Also can be only in the bottom of said first settlement separator 4 or only be provided with stripping stage in the bottom of said second settlement separator 6, and the exit end of the said second spent agent output tube 8 is connected with this stripping stage.The bottom of this stripping stage also is communicated with stripping medium input tube 24.
Preferably be provided with stripping baffles in the said stripping stage, to improve the gentle effect of putting forward of gas stripping efficiency.The set-up mode of stripping baffles has been conventionally known to one of skill in the art, repeats no more at this.
Among the present invention; Said catalyst recirculation pipe 9 can be communicated with this second spent agent output tube (8); Thereby realize and the UNICOM of second settlement separator 6, also can directly be communicated with like Fig. 1 to shown in Figure 3 with the bottom of second settlement separator 6; An end that is catalyst recirculation pipe 9 is communicated with the bottom of first reactor drum 2, and the other end is communicated with the bottom of second settlement separator 6.Said catalyst recirculation pipe 9 can be communicated with first reactor drum 2 after the first catalyzer input tube 1 is communicated with in advance again, also can be communicated with first reactor drum 2 separately separately to shown in Figure 3 like Fig. 1.
Under the preferable case; Extremely shown in Figure 3 like Fig. 1; Said catalyst recirculation pipe 9 is provided with valve 12, is used to control the amount that gets into the catalyzer in first reactor drum 2 through catalyst recirculation pipe 9, controls first cracking catalyst in first reactor drum 2 thus and from the ratio of the spent agent of second reactor drum 5.
According to another embodiment of the invention, the bottom of said second reactor drum 5 also is communicated with second feeding line 23, thereby can replenish fresh raw oil to second reactor drum as required.
According to another embodiment of the invention; This hydrocarbon oil catalytic cracking equipment also comprises the catalyst regenerator (not shown); Thereby can or not regenerate behind the stripping the catalyst stripping of inactivation in first reactor drum 2 and second reactor drum 5, and the catalyzer after will regenerating returns and carries out the hydrocarbon oil catalytic cracking reaction in first reactor drum 2 and second reactor drum 5.When as shown in Figure 2, when the exit end of the said second spent agent output tube 8 was communicated with first settlement separator 4, said catalyst regenerator was communicated with the said first catalyzer input tube 1, catalyst recirculation pipe 9 and the first spent agent output tube 10.When the exit end of the said second spent agent output tube 8 is communicated with first settlement separator 4; Like Fig. 1 and Fig. 3, said catalyst regenerator and the said first catalyzer input tube 1, the second catalyzer input tube 11, the second spent agent output tube 8 and the first spent agent output tube 10 are communicated with.Said catalyst regenerator can be one, also can be a plurality of.
Among the present invention, said first reactor drum 2 is meant the tubular reactor among Fig. 1 to Fig. 3, and does not comprise catalyst regenerator and each separator.Can be interior tubular type first reactor drum, also can be outer tubular type first reactor drum.
The height of said first reactor drum 2 is preferably 1 with the ratio of the height of said second reactor drum 5: 0.1-20 further is preferably 1: 0.2-15.
The diameter ratio of the diameter of said first reactor drum 2 and said second reactor drum 5 is preferably 1: 1-20 further is preferably 1: 1-15.In above-mentioned preferable range, can guarantee the carrying out continuously of reaction times and reaction in two reactor drums better.
Among the present invention, the height of riser reactor refers to that position from an end feed(raw material)inlet of riser reactor is to the distance the other end reacting product outlet.When said riser reactor comprises that when promoting two sections of section and horizontal sections, the height of said riser reactor only refers to the length of the section of lifting.
Above-mentioned hydrocarbon oil catalytic cracking equipment below in conjunction with accompanying drawing is explained hydrocarbon oil catalytic cracking method of the present invention.As shown in Figure 1: the inlet that gets into first reactor drum 2 from the high temperature regeneration agent of revivifier by the first catalyzer input tube 1; And it is up under the preparatory castering action of the preparatory lifting medium of importing from preparatory lifting medium input tube 22; Contact with the raw oil that is got into by the nozzle of first feed-pipe 21, the raw oil generating gasification is also carried out first contact reacts.The first cracking mixture of catalysts of oil gas and inactivation gets into first settlement separator 4 through gas-solid quick disconnector 31 backs in first reactor drum, 2 exits afterwards, in the first cracking catalyst separating of this reaction oil gas and inactivation.First cracking catalyst of the inactivation that settles down through stripping stage or without stripping after the first spent agent output tube 10 is sent to the revivifier coke burning regeneration, accomplish a circulation.The stripping medium is preferably water vapor, is introduced by the first stripping medium input tube 22.Preferably be provided with stripping baffles in the stripping stage, to improve steam stripping efficiency.Oil gas after the gas solid separation is through as the cyclonic separator of the 4th gas-solid separator 71 once more after the gas solid separation; Oil gas gets into second reactor drum 5 through collection chamber 13, transportation pipe 15 successively; With contact from the reclaimable catalyst of catalyst recirculation pipe 9 and second cracking catalyst of the second catalyzer input tube 11; Proceed reaction; With after cyclonic separator as the 3rd gas-solid separator 72 separates, oil gas goes subsequent separation system through collection chamber 14, gas pipeline 25 to second cracking catalyst of reacted oil gas and inactivation through gas-solid quick disconnector 32.Separate the catalyzer that obtains and obtain reclaimable catalyst through stripping or after without stripping; A reclaimable catalyst part is carried out first reactor drum 2 through catalyst recirculation pipe 9; Another part removes the revivifier coke burning regeneration through the second spent agent output tube 10, accomplishes another catalyst recirculation.The stripping medium is recommended matter input tube 23 through second gas and is introduced second stripping stage 10.Two sections second reactor drum 5 can also be introduced second strand of raw oil via second feed-pipe 23 except introducing the oil gas from first stage reactor.The feed entrance point of second strand of raw oil can be more than transportation pipe any position, directly get into second reactor drum 5.Second strand of raw oil can be the raw oil identical with one section first reactor drum 2; Also can be in other catalytically cracked material or dry gas, liquefied gas, lighter hydrocarbons, gasoline, diesel oil, recycle stock, the slurry oil one or more etc. logistics, can also be as two section second reactor drum promote, the media such as water vapor of fluidizing medium.Second cracking catalyst that gets into two sections second reactor drum can be high temperature regeneration agent or the lower regenerator of temperature from the revivifier external warmer.When adopting the high temperature regeneration agent, be particularly conducive to low-carbon alkene and the low alkene stop bracket gasoline of production such as increasing output of ethylene, propylene, butylene.When adopting the regenerator of lesser temps, be particularly conducive to and produce the gasoline products that is rich in isoparaffin, low alkene, high aromatic hydrocarbons.
Fig. 2 is an another kind of way of realization of the present invention; First reactor drum 2 and two section second reactor drum 5 of being one section with Fig. 1 difference are provided with up and down; Thereby as stated; First reactor drum, 2 reacted oil gas are with after mixture of catalysts is separated through the first gas-solid quick disconnector 31; Need not directly to get into second reactor drum 5 that the charging port is positioned at first settlement separator, 4 tops with first collection chamber 13 and carry out second-stage reaction through the 4th gas-solid separator 71 shown in Figure 1, and from second reactor drum 5 through second settlement separator 6 isolated be used for the regenerated catalyzer through the first spent agent output tube 8 get into that first settlement separator 4 mixes with one section reclaimable catalyst, behind the stripping again the first spent agent output tube 10 of one section on warp be sent to catalyst regenerator and regenerate.
Fig. 3 is an another kind of way of realization of the present invention; With Fig. 2 difference be from second reactor drum 5 directly send into catalyst regenerator regeneration through the isolated regenerated reclaimable catalysts that are used for of second settlement separator 6 through the first spent agent output tube 8, and do not mix with first spent agent.
Because the present invention adopts raw oil to be introduced into first reactor drum as first reaction zone; After the gas solid separation; Oil gas directly gets into second reactor drum and contacts the characteristics that continue reaction with second cracking catalyst, has made full use of the advantage of two-stage reaction, and is more flexible than production decision with prior art.Can improve feed stock conversion, improve product and distribute.This knockdown reactor drum pattern can be according to product demand flexible operational condition.Adopt riser reactor, the gas-solid axial backmixing reduces, and radial flow is more even, and the gas-solid short contact is suitable for harsh (high temperature, the short contact) catalytic cracking reaction of condition.Riser reactor can make full use of the initial activity of catalyzer; And the part spent agent through with second reactor drum is used for first reactor drum; Can under guaranteeing not increase the situation of fresh dose of consumption, effectively improve the agent-oil ratio and the temperature that reduces by first reactor drum in first reactor drum; Thereby the raising light oil yield reduces the generation of dry gas and coke.After the gas-solid mixture that comes out from one section first reactor drum separated in settling vessel, granules of catalyst removed the revivifier coke burning regeneration behind stripping, accomplish a circulation, and second reactor drum that oil gas then gets into as second reaction zone continues reaction.
Hydrocarbon oil catalytic cracking equipment provided by the invention can will existing two overlap the riser tube reaction units and couples together and realize through increasing a gas pipeline 15 and catalyst recirculation pipe 9; Also can be from the angle of compact construction; On the basis of existing riser tube reaction unit; Set up a settlement separator and a riser reactor in the bottom of riser reactor successively, and the spent agent outlet of the settlement separator on top is communicated with the catalyst inlet of the riser reactor of bottom realizes.Therefore hydrocarbon oil catalytic cracking equipment making of the present invention is simple, thereby method of the present invention also can be easy on existing technology basis, improve a little and realize having very strong flexibility.
More than, for the embodiment of riser reactor is illustrated, obviously, second reactor drum 5 of the present invention also can be various fluidized-bed reactors to said second reactor drum 5.Second reactor drum 5 is that the embodiment and the riser reactor of fluidized-bed reactor is similar, only needs to replace with fluidized-bed reactor as the riser reactor of said second reactor drum 5 and gets final product.Make the fluidized-bed reactor and second settlement separator 6 be integrated into a common chamber under the preferable case.
Below in conjunction with embodiment the present invention is further explained.
Raw oil A is the mixture that subtracts slag that decompressed wax oil is mixed 10 weight %; Raw oil B is a decompressed wax oil; Character is seen table 1, and catalyzer is the catalytic cracking agent MLC-500 poiser of Sinopec catalyst Co. production and the MMC-2 catalyzer poiser of voluminous low-carbon (LC), and its character is seen table 2.
Embodiment 1-3
This embodiment is used to explain hydrocarbon oil catalytic cracking equipment provided by the invention and hydrocarbon oil catalytic cracking method.
Adopt hydrocarbon oil catalytic cracking equipment shown in Figure 1, treatment capacity is 2kg/h, and first reactor drum and second reactor drum are riser reactor, and the aspect ratio of first reactor drum 2 and second reactor drum 5 is 1: 1.5, and the diameter ratio is 1: 1.The stripping medium is that temperature is 250 ℃ a water vapour.The catalyzer that first reactor drum 2 and second reactor drum 5 adopt is the MLC-500 poiser.Present embodiment is a purpose with voluminous light oil (gasoline+diesel oil), and the temperature of second reactor drum 5 is lower than the temperature of first reactor drum 2, and second reactor drum, 5 finishes are higher than the finish duration of contact of first reactor drum 2 duration of contact, and reaction conditions and result see table 3.
Comparative Examples 1
Raw materials used, catalyzer is identical with embodiment 1.Different is, hydrocarbon oil catalytic cracking equipment is disclosed tandem first reactor drum that has the extension diameter section reaction zone of CN1237477A, and the oil gas of one section reaction zone gets into the second-stage reaction district with catalyzer and continues reaction.This Comparative Examples is a purpose with voluminous light oil.Reaction conditions and result see table 3.
Comparative Examples 2
Raw materials used, catalyzer is identical with embodiment 1.Be not both, hydrocarbon oil catalytic cracking equipment is the disclosed compound reactor of being made up of riser tube and dense phase fluidized bed of CN1065903C, and the oil gas of one section reaction zone gets into the second-stage reaction district with catalyzer and continues reaction.This Comparative Examples is a purpose with voluminous light oil.Reaction conditions and result see table 3.
Embodiment 4-6
This embodiment is used to explain hydrocarbon oil catalytic cracking equipment provided by the invention and hydrocarbon oil catalytic cracking method.
Carry out the catalytic cracking of hydrocarbon ils according to the method for embodiment 1, different is, raw oil is raw oil B, and the catalyzer of first reactor drum and second reactor drum is the MMC-2 catalyzer.Present embodiment is purpose with the low-carbon olefines high-output, and the temperature of second reactor drum 5 is higher than the temperature of first reactor drum 2, and the reaction conditions of second reactor drum 5 is harsher than first reactor drum 2, and reaction conditions and result see table 4.
Comparative Examples 3
Used reaction raw materials, catalyzer are identical with embodiment 4, and hydrocarbon oil catalytic cracking equipment is identical with Comparative Examples 1.This Comparative Examples is purpose with the low-carbon olefines high-output.Reaction conditions and result see table 4.
Comparative Examples 4
Raw materials used, catalyzer is identical with embodiment 4.Be not both, hydrocarbon oil catalytic cracking equipment is the disclosed compound reactor of being made up of riser tube and dense phase fluidized bed of CN1065903C, and the oil gas of one section reaction zone gets into the second-stage reaction district with catalyzer and continues reaction.This Comparative Examples is purpose with the low-carbon olefines high-output.Reaction conditions and result see table 4.
Table 1
| Project | A | B |
| Density (20 ℃)/(g/cm 3) | 0.9092 | 0.8940 |
| Kinematic viscosity (80 ℃)/(mm 2/s) | 45.68 | 161.0 |
| Kinematic viscosity (100 ℃)/(mm 2/s) | 23.25 | 26.0 |
| Carbon residue/% | 4.6 | 0.8 |
| Element quality composition/% | ||
| C | 86.30 | 86.61 |
| H | 12.92 | 13.04 |
| S | 0.46 | 0.23 |
| N | 0.32 | 0.12 |
| Quality composition/the % of hydrocarbon system | ||
| Stable hydrocarbon | 55.6 | 59.8 |
| Aromatic hydrocarbons | 27.9 | 26.3 |
| Colloid | 15.7 | 13.3 |
| Bituminous matter | 0.8 | 0.6 |
| Metal content/μ g/g | ||
| Fe | 4.9 | 3.9 |
| Ni | 5.3 | 2.8 |
| V | 0.3 | 0.1 |
| Na | 3.2 | 1.8 |
| Boiling range/℃ | ||
| Over point | 285 | 284 |
| 10％ | 448 | 439 |
| 30％ | 499 | 484 |
| 50％ | - | 540 |
| 70％ | - | - |
Table 2
Table 3
Table 4
See from table 3 test-results; Under identical raw material and catalyst action; The embodiment 1-3 that with the light oil with high yield is purpose is obviously higher than Comparative Examples 1 and 2 light oil yields, and transformation efficiency also increases, and sub product dry gas+coke selectivity embodiment will be lower than Comparative Examples simultaneously.Gained gasoline product quality embodiment also is better than Comparative Examples.
See from table 4 test-results; The embodiment 4-6 that with voluminous light olefin is purpose is higher slightly than Comparative Examples 3 and 4 transformation efficiencys; Propene yield obviously improves; Yield of light oil embodiment also is higher than Comparative Examples, and dry gas+coke selectivity but is starkly lower than Comparative Examples simultaneously, and feed stock conversion and product selectivity all have bigger improvement.Gained gasoline products alkene embodiment reduces than Comparative Examples, and aromaticity content raises, and gasoline octane rating embodiment also is higher than Comparative Examples, and sulphur content is lower than Comparative Examples, and quality product is improved.
Embodiment 1-3 and embodiment 4-6 explain that also to adopt the present invention to invent the mode of production flexible, and two reactor drums can be taked different reaction conditions and different catalyst to the different target product.Feed stock conversion and high value added product selectivity improve, and quality product also improves, and has tangible economic benefit and social benefit.
Embodiment 7-9
This embodiment is used to explain hydrocarbon oil catalytic cracking equipment provided by the invention and hydrocarbon oil catalytic cracking method.
Adopt hydrocarbon oil catalytic cracking equipment shown in Figure 2, treatment capacity is 6kg/h, and first reactor drum and second reactor drum are respectively riser reactor and fluidized-bed reactor, and the aspect ratio of first reactor drum 2 and second reactor drum 5 is 2: 1, and the diameter ratio is 1: 5.The stripping medium is that temperature is 250 ℃ a water vapour.The catalyzer that first reactor drum 2 and second reactor drum 5 adopt is the MLC-500 poiser.Present embodiment is a purpose with voluminous light oil (gasoline+diesel oil), and reaction conditions and result see table 5.
Embodiment 10-11
This embodiment is used to explain hydrocarbon oil catalytic cracking equipment provided by the invention and hydrocarbon oil catalytic cracking method.
Adopt hydrocarbon oil catalytic cracking equipment shown in Figure 2, treatment capacity is 6kg/h, and first reactor drum and second reactor drum are respectively riser reactor and fluidized-bed reactor, and the aspect ratio of first reactor drum 2 and second reactor drum 5 is 2: 1, and the diameter ratio is 1: 5.The stripping medium is that temperature is 250 ℃ a water vapour.The catalyzer that first reactor drum 2 and second reactor drum 5 adopt is the MMC-2 poiser.Present embodiment is purpose with the low-carbon olefines high-output, and reaction conditions and result see table 5.
Table 5
| RON | 91 | 90.5 | 91.5 | 92 | 92.5 |
| MON | 81.5 | 81.0 | 81.5 | 81.5 | 81.5 |
| Sulphur content/μ g/g | 335 | 348 | 298 | 435 | 479 |
It can also be seen that from the result of table 4 and table 5, when said second reactor drum is fluidized-bed reactor or riser reactor, all can obtain effect preferably.
Claims (30)
1. a hydrocarbon oil catalytic cracking method is characterized in that, this method may further comprise the steps:
(1) make the hydrocarbon oil crude material and first cracking catalyst in first reactor drum, carry out first contact reacts; Oil gas after first contact reacts and mixture of catalysts are carried out first finish separate, the catalyzer after first finish separates obtains reclaimable catalyst behind stripping;
(2) oil gas that obtains after the separation of first finish is carried out second contact reacts with initiate second cracking catalyst in second reactor drum; Oil gas after second contact reacts and mixture of catalysts are carried out second finish separates; Catalyzer after second finish separates obtains reclaimable catalyst through stripping or after without stripping, and subsequent separation system is derived and be delivered to the oil gas after second finish is separated;
(3) step (2) gained reclaimable catalyst is partly or entirely sent in said first reactor drum in the step (1);
Wherein, Said first reactor drum is a riser reactor; Said second reactor drum is riser reactor or fluidized-bed reactor, and said first cracking catalyst and second cracking catalyst are identical or different, is selected from least a in live catalyst, regenerated catalyst and half regenerated catalyst.
2. hydrocarbon oil catalytic cracking method according to claim 1, wherein, the first catalytic time was 0.1-3 second.
3. hydrocarbon oil catalytic cracking method according to claim 2, wherein, the first catalytic time was 0.5-2.5 second.
4. according to any described hydrocarbon oil catalytic cracking method among the claim 1-3, wherein, the first catalytic pressure is 0.01-0.8MPa, and temperature is 450-680 ℃, and the agent weight of oil is than being 1-20: 1.
5. hydrocarbon oil catalytic cracking method according to claim 4, wherein, the first catalytic pressure is 0.1-0.5MPa, and temperature is 480-580 ℃, and the agent weight of oil is than being 3-15: 1.
6. hydrocarbon oil catalytic cracking method according to claim 1, wherein, the weight ratio of first cracking catalyst and reclaimable catalyst described in first reactor drum is 1: 0.001-0.8.
7. hydrocarbon oil catalytic cracking method according to claim 6, wherein, the weight ratio of first cracking catalyst and reclaimable catalyst described in first reactor drum is 1: 0.01-0.6.
8. hydrocarbon oil catalytic cracking method according to claim 1, wherein, said second reactor drum is a riser reactor; The said second catalytic residence time was 0.1-10 second; Pressure is 0.01-0.6MPa, and temperature is 400-680 ℃, and the agent weight of oil is than being 1-40: 1.
9. hydrocarbon oil catalytic cracking method according to claim 8, wherein, the said second catalytic residence time was 0.5-8 second, and pressure is 0.1-0.3MPa, and temperature is 485-650 ℃, and the agent weight of oil is than being 3-30: 1.
10. hydrocarbon oil catalytic cracking method according to claim 1, wherein, said second reactor drum is a fluidized-bed reactor, the second catalytic condition comprises that weight space velocity is 1-50 hour
-1, temperature of reaction is 400-680 ℃, and pressure is 0.01-0.6MPa, and the agent weight of oil is than being 1-20: 1.
11. hydrocarbon oil catalytic cracking method according to claim 10, wherein, the second catalytic condition comprises that weight space velocity is 2-40 hour
-1, temperature of reaction is 460-650 ℃, and pressure is 0.1-0.6MPa, and the agent weight of oil is than being 1-20: 1.
12. hydrocarbon oil catalytic cracking method according to claim 1; Wherein, This method also comprises in second reactor drum adds hydrocarbon ils; Oil gas and initiate second cracking catalyst after making the hydrocarbon ils added and first finish separating are carried out said second contact reacts, and said hydrocarbon ils is one or more in said hydrocarbon oil crude material, dry gas, liquefied gas, lighter hydrocarbons, gasoline, diesel oil, recycle stock, the slurry oil.
13. according to claim 1 or 12 described hydrocarbon oil catalytic cracking methods, wherein, said hydrocarbon oil crude material is time processing distillate, deasphalted oil, wax tailings, hydrogenation heavy oil, mix in refining long residuum, the vacuum residuum one or more.
14. hydrocarbon oil catalytic cracking method according to claim 1; Wherein, Said first cracking catalyst and/or second cracking catalyst are the cracking catalyst that contains molecular sieve, said molecular sieve be contain or not phosphorus element-containing y-type zeolite, contain or do not contain REE ultrastable Y, contain or one or more in the supersiliceous zeolite with five-membered ring structure, β zeolite, mordenite, omega zeolite of phosphorus element-containing not.
15. hydrocarbon oil catalytic cracking method according to claim 1, wherein, this method is further comprising the steps of:
(4) the said reclaimable catalyst of step (1) gained and the said reclaimable catalyst of step (2) remainder are carried out coke burning regeneration, obtain regenerated catalyst, perhaps obtain regenerated catalyst and half regenerated catalyst;
(5) regenerated catalyst that obtains after will regenerating and/or half regenerated catalyst are as said first cracking catalyst and/or second cracking catalyst.
16. hydrocarbon oil catalytic cracking equipment; This equipment comprises first reactor drum (2), first settlement separator (4), second reactor drum (5) and second settlement separator (6); Said first reactor drum is a riser reactor; Said second reactor drum is riser reactor or fluidized-bed reactor; The bottom of said first reactor drum (2) is communicated with the first catalyzer input tube (1), catalyst recirculation pipe (9), the first spent agent output tube (10), first lifting medium input tube (22) and first feed-pipe (21) in advance, and first feed-pipe (21) is positioned at the first catalyzer input tube (1), catalyst recirculation pipe (9) and first promotes medium input tube (21) top in advance; The outlet on first reactor drum (2) top is positioned at first settlement separator (4), and has first gas-solid separator (31) in this exit of first settlement separator (4) and be used for the material that comes out from first reactor drum (2) is carried out gas solid separation; The top of first settlement separator (4) has at least one opening, is used for being communicated with the opening for feed of second reactor drum (5); The bottom of second reactor drum (5) is communicated with the second catalyzer input tube (11), and the opening for feed of second reactor drum (5) is positioned at the second catalyzer input tube (11) top; The outlet on second reactor drum (5) top is positioned at second settlement separator (6); And have second gas-solid separator (32) is used for the material that comes out from second reactor drum (5) is carried out gas solid separation in the exit of said second reactor drum (5); The bottom of second settlement separator (6) is communicated with the second spent agent output tube (8); Said catalyst recirculation pipe (9) is communicated with this second spent agent output tube (8) or directly is communicated with the bottom of second settlement separator (6); The top of second settlement separator (6) is provided with gas pipeline (25), and subsequent separation system is derived and be delivered to the oil gas that is used for reaction is generated.
17. hydrocarbon oil catalytic cracking equipment according to claim 16; Wherein, Said first gas-solid separator (31) and second gas-solid separator (32) inertial separator of respectively doing for oneself, and each inertial separator is fixedly connected with the outlet of first reactor drum (2) with second reactor drum (5) separately.
18. according to claim 16 or 17 described hydrocarbon oil catalytic cracking equipment; Wherein, Said first reactor drum (2) and second reactor drum (5) are arranged side by side, and the opening at the top of said first settlement separator (4) is communicated with through pipeline (15) with the opening for feed of said second reactor drum (5).
19. hydrocarbon oil catalytic cracking equipment according to claim 18; Wherein, This equipment also comprises the 4th gas-solid separator (71) that is positioned at first settlement separator (4) and is positioned at the 3rd gas-solid separator (72) at second settlement separator (6) top, said the 3rd gas-solid separator (72) and the 4th gas-solid separator (71) cyclonic separator of respectively doing for oneself.
20. hydrocarbon oil catalytic cracking equipment according to claim 19 wherein, also is provided with first collection chamber (13) in said first settlement separator (4), the oil gas of being used to collect from the 4th gas-solid separator (71), and this oil gas sent in second reactor drum (5); Also be provided with second collection chamber (14) in said second settlement separator (6), the oil gas of being used to collect from the 4th gas-solid separator (72), and the oil gas of collecting derived and is delivered to subsequent separation system through gas pipeline (25).
21. according to claim 16 or 17 described hydrocarbon oil catalytic cracking equipment; Wherein, Said second reactor drum (5) is a riser reactor; Said second settlement separator (6), second reactor drum (5), first settlement separator (4) and first reactor drum (2) set gradually from top to bottom, and the opening for feed of said second reactor drum (5) is communicated with the top of said first settlement separator (4).
22. hydrocarbon oil catalytic cracking equipment according to claim 21, wherein, this equipment also comprises the 3rd gas-solid separator (72) that is positioned at second settlement separator (6) top, and said the 3rd gas-solid separator (72) is a cyclonic separator.
23. hydrocarbon oil catalytic cracking equipment according to claim 21; Wherein, Also be provided with second collection chamber (14) in said second settlement separator (6); Be used to collect oil gas from the 3rd gas-solid separator (72), and the oil gas of collecting derived and is delivered to subsequent separation system through gas pipeline (25).
24. hydrocarbon oil catalytic cracking equipment according to claim 21, wherein, the bottom of said first settlement separator (4) is provided with stripping stage, and the exit end of the said second spent agent output tube (8) is connected with this stripping stage.
25. according to claim 18 or 21 described hydrocarbon oil catalytic cracking equipment, wherein, the bottom of the bottom of said first settlement separator (4) and second settlement separator (6) is provided with stripping stage separately.
26., wherein, be provided with stripping baffles in the said stripping stage according to claim 24 or 25 described hydrocarbon oil catalytic cracking equipment.
27. hydrocarbon oil catalytic cracking equipment according to claim 16, wherein, said catalyst recirculation pipe (9) is provided with valve (12), is used for control gets into the catalyzer in first reactor drum (2) through catalyst recirculation pipe (9) amount.
28. hydrocarbon oil catalytic cracking equipment according to claim 16, wherein, the bottom of said second reactor drum (5) also is communicated with second feeding line (23).
29. hydrocarbon oil catalytic cracking equipment according to claim 16; Wherein, The ratio of the height of the height of said first reactor drum (2) and said second reactor drum (5) is 1: 0.1-20, the diameter ratio of the diameter of said first reactor drum (2) and said second reactor drum (9) is 1: 1-20.
30. hydrocarbon oil catalytic cracking equipment according to claim 18; Wherein, This equipment also comprises catalyst regenerator, and said catalyst regenerator is communicated with the said first catalyzer input tube (1), the second catalyzer input tube (11) and the first spent agent output tube (10).
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| WO2018141243A1 (en) * | 2017-02-03 | 2018-08-09 | 石宝珍 | Catalytic conversion reaction method and reactor |
| CN107286972A (en) * | 2017-07-21 | 2017-10-24 | 石宝珍 | A kind of catalysis conversion method of producing more propylene |
| CN107286972B (en) * | 2017-07-21 | 2019-11-22 | 石宝珍 | A kind of catalysis conversion method of producing more propylene |
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| CN109678634B (en) * | 2017-10-18 | 2022-03-11 | 中国石油化工股份有限公司 | Catalytic cracking method for increasing yield of ethylene and propylene |
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| CN111054281A (en) * | 2018-10-17 | 2020-04-24 | 中国石油化工股份有限公司 | Catalyst fluidized bed reactor, reaction system and method using system |
| CN111054281B (en) * | 2018-10-17 | 2022-03-11 | 中国石油化工股份有限公司 | Catalyst fluidized bed reactor, reaction system and method using system |
| CN111704927A (en) * | 2020-07-09 | 2020-09-25 | 青岛京润石化设计研究院有限公司 | Method and device for preparing olefin and aromatic hydrocarbon by catalytic conversion of petroleum hydrocarbon raw material |
| CN114195612A (en) * | 2020-09-02 | 2022-03-18 | 青岛京润石化设计研究院有限公司 | Method and device for preparing propylene and ethylene by catalytic conversion of petroleum hydrocarbon |
| CN114133955A (en) * | 2021-12-01 | 2022-03-04 | 胜帮科技股份有限公司 | Device and method for preparing olefin by petroleum hydrocarbon cascade fluidization cracking |
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