CN103849424A - Lift pipe reactor pre-lifting device and process flow thereof - Google Patents
Lift pipe reactor pre-lifting device and process flow thereof Download PDFInfo
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- CN103849424A CN103849424A CN201410036557.0A CN201410036557A CN103849424A CN 103849424 A CN103849424 A CN 103849424A CN 201410036557 A CN201410036557 A CN 201410036557A CN 103849424 A CN103849424 A CN 103849424A
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Abstract
The invention relates to a lift pipe reactor pre-lifting device and a process flow thereof. The lift pie reactor pre-lifting device comprises a fluidized vapor ring, a pre-lifting vapor nozzle, a pre-lifting vapor pipe, an expansion section, a single-action slide valve and a regeneration inclined pipe. An inner conveyor pipe is arranged in the expansion section, the lower part of the inner conveyor pipe is connected with the upper part of the pre-lifting vapor pipe, and the inner diameter of the pre-lifting device is twice as large as the inner diameter of the upper part of a lift pipe reactor. By adopting the method in which the inner conveyor pipe is increased, the inner diameter of the pre-lifting device is increased and therefore the structure of the expansion section is changed, the catalyst entering the expansion section has a sufficient buffering space, so that the blanking pressure fluctuation of the regeneration inclined pipe is reduced, the bias current generated by an S-shaped movement orbit can be eliminated, the pre-lifting vapor pipe can avoid the regeneration inclined pipe, the direct impact of the pre-lifting vapor on a blanking port of the regeneration inclined pipe can be avoided, the circulating capacity of the catalyst of a settlement regenerator can be increased, the catalyst in the lift pipe can be uniformly distributed, and the yield of a target product can be improved.
Description
Technical field
The present invention relates to a kind of riser reactor, particularly relate to a kind of riser reactor pre-riser and technical process thereof.
Background technology
Catalytic cracking technology is the technology generally adopting in petrochemical refining's industry, and a large amount of heavy oil residues that produce in the refining of petroleum course of processing (accounting for stock oil more than 60%) can be converted into gasoline, diesel oil and the petroleum gas of heavy demand in national economy by this technology.
Riser reactor is the nucleus equipment in catalytic cracking unit.This equipment is that length is about 40 meters, and diameter is about 0.5 meter～1.0 meters, vertically arranged tubular reactor.Heavy feed stock in production process---residual oil is continuously sent into tubular reactor inside, under the condition of 500 ℃ of high temperature and catalyzer, carries out cracking reaction, and resultant of reaction is gasoline, diesel oil and petroleum gas etc.Catalytic cracking riser reactor is by its inside function, and soaking section, top reaction terminating section and end gas-solid sharp separation section four parts of generally being mixed by bottom pre lift zone, middle part charging contact form.Wherein the flow distribution situation of oil gas and catalyzer in conversion zone, product that contact efficiency directly affects catalytic cracking reaction distribute and object product yield, and in riser reactor between oil, agent contact efficiency often have much relations with the prearranged assignment state of pre lift zone exit catalyzer.Particularly, along with the development of residual oil catalytic cracking, the prearranged assignment situation of catalyzer directly affects yield of light oil, coke and dry gas yied to a great extent.
In conventional catalytic cracking unit, regenerated catalyst has side direction initial velocity after entering from the side riser tube, under lift gas effect, produce again acceleration upwards, two kinds of results that speed is synthetic, make catalyzer motion collision wall obliquely, bounce-back collides another wall then, thereby forms S type movement locus, cause catalyzer bias current, make catalyzer extremely inhomogeneous at riser tube axial distribution of solids density.
Conventional riser tube catalyzer radial density distribution is little near central zone density of catalyst, large near Bian Bi region density of catalyst, and first stock oil inject riser tube central zone through nozzle, like this, on conventional riser tube cross section, central zone agent-oil ratio is less, and Bian Bi region agent-oil ratio is larger.That is to say, in the little shortage of heat that provides of central zone internal cause agent-oil ratio, fully cracking of stock oil.And make stock oil cross cracking in lifting tube edge wall region because agent-oil ratio provides greatly too much heat, thereby object product yield is reduced.
Therefore before stock oil enters riser tube, catalyzer on riser reactor cross section being uniformly distributed, for oil gas uniform contact provides good prearranged assignment environment, is very important.
Because the defect that above-mentioned existing riser reactor pre-riser exists, practical experience and the expertise of the inventor based on being engaged in this type of product design manufacture and enriching for many years, and the utilization of cooperation scientific principle, actively research and innovation in addition, to founding a kind of new riser reactor pre-riser, can improve general existing riser reactor pre-riser, make it have more practicality.Through constantly research, design, and after repeatedly studying sample and improving, finally create the present invention who has practical value.
Summary of the invention
Main purpose of the present invention is, overcome the defect that existing riser reactor pre-riser exists, and provide a kind of new riser reactor pre-riser, technical problem to be solved is, riser tube inner catalyst can be uniformly distributed, for oil gas uniform contact provides good prearranged assignment environment, thereby improve object product yield, be very suitable for practicality.
The object of the invention to solve the technical problems realizes by the following technical solutions.A kind of riser reactor pre-riser proposing according to the present invention, comprise fluidization steam vapor ring 1, pre-lift vapor-nozzle 2, pre-lift vapour pipe 3, expanding reach 5, single-linkage sliding valve 6 and regenerator sloped tube 7, wherein, expanding reach 5 is arranged on riser reactor 10 bottoms, the interior pre-lift vapour pipe 3 that arranges of expanding reach 5, on pre-lift vapour pipe 3 tops, pre-lift vapor-nozzle 2 is set, in pre-lift vapor-nozzle 2 bottoms, fluidization steam vapor ring 1 is set, regenerator sloped tube 7 is connected with expanding reach 5 by single-linkage sliding valve 6, characterized by further comprising interior transfer lime 4, this interior transfer lime 4 is arranged in expanding reach 5, interior transfer lime 4 bottoms are connected with pre-lift vapour pipe 3 tops.
The object of the invention to solve the technical problems also can be applied to the following technical measures to achieve further.
Aforesaid riser reactor pre-riser, the internal diameter of wherein said riser reactor pre-riser is twice than the internal diameter on riser reactor top.
The object of the invention to solve the technical problems also realizes by the following technical solutions.The technical process of a kind of riser reactor pre-riser proposing according to the present invention, comprises following technical process: from sedimentation regenerator 8, flow out 700 ℃ of high temperature silicon phosphate catalysts, flow into expanding reach 5 through regenerator sloped tube 7; The dust-like silicate catalyst that flows into expanding reach 5 is formed fluidized state by fluidization steam vapor in fluidization steam vapor ring 1, the high velocity vapor stream spraying from pre-lift vapor-nozzle 2,50～80kg/m is carried and be mixed to form to its jet adsorption by silicate catalyst around
3the high speed catalyst stream of concentration, this high speed catalyzer is under the castering action of pre-lift steam, and the interior transfer lime 4 of flowing through, injects riser reactor 10 middle parts; The annular space that fluidization steam vapor in fluidization steam vapor ring 1 forms from interior transfer lime 4 and riser reactor 10 upwards flows, give the limit wall filling at riser reactor 10 middle parts, make the high speed catalyzer that flows into riser reactor middle part 10 to riser reactor 10 central distribution; At riser reactor 10 middle parts, before high speed catalyst stream is radial scattering, spray into stock oil from stock oil feed nozzle 9, after stock oil fully mixes with catalyzer, carry out catalytic cracking reaction 500 ℃ of hot environments.
By technique scheme, the present invention at least has following advantages and beneficial effect:
1. the catalyzer that enters expanding reach has enough cushioning pockets, both can reduce the pressure surge of regenerator sloped tube blanking, can eliminate again the effect of its horizontal force, thereby eliminates the bias current producing because of S type movement locus.
2. because pre-lift vapour pipe can be avoided regenerator sloped tube, avoid the direct impact of pre-lift steam to regenerator sloped tube feed opening, thereby the blanking resistance of regenerator sloped tube is reduced greatly, guarantee the unobstructed and steady of blanking, catalyst recirculation ability between sedimentation regenerator two devices (top settling vessel and bottom revivifier) is increased, and the turndown ratio of device is improved.
3. catalyzer enters riser reactor middle part in the beam of interior transfer lime formation high speed catalyst stream, before being radial scattering, sprays into stock oil, can guarantee that nozzle region catalyzer radial density is uniformly distributed.
4. fluidization steam vapor upwards flows from the annular space of pre-lift vapour pipe and the formation of interior transfer lime, further to the wall filling of riser reactor limit, be conducive to catalyzer to riser reactor central distribution, the even hybrid reaction of stock oil and catalyzer, improves object product yield.
The present invention is by increasing interior transfer lime 4, increase pre-riser internal diameter, thereby change the method for expanding reach 5 structures, eliminate the bias current problem under horizontal force action, change lifting tube edge wall district agent-oil ratio high, the bad Distribution Phenomena that central section agent-oil ratio is low, thus make stock oil in the rapid flash distillation of the interior energy of riser reactor 10, gasification, cracking, realize the object that reduces gasoline olefin and sulphur content.New texture makes catalyzer single circulation to riser tube by regenerator sloped tube, become catalyzer by regenerator sloped tube to expanding reach, then by expanding reach the binary cycle system to interior transfer lime.Make catalytic cracking unit have higher handiness, turndown ratio and good adaptability, guarantee the good fluidized state of catalytic cracking unit, met the needs of long-term operation.
Above-mentioned explanation is only the general introduction of technical solution of the present invention, in order to better understand technique means of the present invention, and can be implemented according to the content of specification sheets, and for above and other object of the present invention, feature and advantage can be become apparent, below especially exemplified by preferred embodiment, and coordinate accompanying drawing, be described in detail as follows.
Accompanying drawing explanation
Fig. 1 is riser reactor pre-riser schematic cross-section of the present invention.
[main element nomenclature]
1: fluidization steam vapor ring 2: pre-lift vapor-nozzle
3: pre-lift vapour pipe 4: interior transfer lime
5: expanding reach 6: single-linkage sliding valve
7: regenerator sloped tube 8: sedimentation regenerator
9: stock oil feed nozzle 10: riser reactor
Embodiment
Technique means and effect of taking for reaching predetermined goal of the invention for further setting forth the present invention, below in conjunction with accompanying drawing and preferred embodiment, to its embodiment of riser reactor pre-riser, method, step, feature and effect thereof of proposing according to the present invention, be described in detail as follows.
Riser reactor pre-riser schematic cross-section of the present invention as shown in Figure 1.
This riser reactor pre-riser comprises: fluidization steam vapor ring 1, pre-lift vapor-nozzle 2, pre-lift vapour pipe 3, interior transfer lime 4, expanding reach 5, single-linkage sliding valve 6 and regenerator sloped tube 7.Wherein, expanding reach 5 is arranged on the bottom of riser reactor 10, interior interior transfer lime 4 and the pre-lift vapour pipe 3 of arranging of expanding reach 5, pre-lift vapour pipe 3 tops are connected with interior transfer lime 4 bottoms, on pre-lift vapour pipe 3 tops, pre-lift vapor-nozzle 2 is set, in pre-lift vapor-nozzle 2 bottoms, fluidization steam vapor ring 1 is set, sedimentation regenerator 8 is connected with expanding reach 5 by regenerator sloped tube 7, there is single-linkage sliding valve 6 junction, and stock oil feed nozzle 9 is arranged on riser reactor 10 middle parts.
High temperature silicon phosphate catalyst from sedimentation regenerator 8 in regenerator sloped tube 7 flows into expanding reach 5, under the effect of bottom fluidization steam ring 1, form fluidized state, the fluidization steam vapor that fluidization steam vapor ring 1 flows out keeps the catalyzer of expanding reach 5 bottoms in dense fluidized state, the high velocity vapor stream spraying from pre-lift vapor-nozzle 2,50～80kg/m is carried and be mixed to form to its jet adsorption by silicate catalyst around
3the high speed catalyst stream of concentration, this high speed catalyzer forms high speed catalyzer a fluid stream under the castering action of pre-lift steam, the interior transfer lime 4 of flowing through, inject riser reactor 10 middle parts, after the stock oil spraying into stock oil feed nozzle 9 fully mixes, carry out catalytic cracking reaction 500 ℃ of hot environments, thereby obtain desired product.
The above, it is only preferred embodiment of the present invention, not the present invention is done to any pro forma restriction, although the present invention discloses as above with preferred embodiment, but not in order to limit the present invention, any those skilled in the art, do not departing within the scope of technical solution of the present invention, when can utilizing the technology contents of above-mentioned announcement to make a little change or being modified to the equivalent embodiment of equivalent variations, in every case be not depart from technical solution of the present invention content, any simple modification of above embodiment being done according to technical spirit of the present invention, equivalent variations and modification, all still belong in the scope of technical solution of the present invention.
Claims (3)
1. a riser reactor pre-riser, comprise fluidization steam vapor ring (1), pre-lift vapor-nozzle (2), pre-lift vapour pipe (3), expanding reach (5), single-linkage sliding valve (6) and regenerator sloped tube (7), wherein, expanding reach (5) is arranged on riser reactor (10) bottom, pre-lift vapour pipe (3) is set in expanding reach (5), on pre-lift vapour pipe (3) top, pre-lift vapor-nozzle (2) is set, in pre-lift vapor-nozzle (2) bottom, fluidization steam vapor ring (1) is set, regenerator sloped tube (7) is connected with expanding reach (5) by single-linkage sliding valve (6), characterized by further comprising interior transfer lime (4), this interior transfer lime (4) is arranged in expanding reach (5), interior transfer lime (4) bottom is connected with pre-lift vapour pipe (3) top.
2. riser reactor pre-riser according to claim 1, is characterized in that the internal diameter of wherein said riser reactor pre-riser is twice than the internal diameter on riser reactor top.
3. a technical process for riser reactor pre-riser, is characterized in that it comprises following technical process:
From sedimentation regenerator (8), flow out 700 ℃ of high temperature silicon phosphate catalysts, flow into expanding reach (5) through regenerator sloped tube (7);
The dust-like silicate catalyst that fluidization steam vapor in fluidization steam vapor ring (1) will flow into expanding reach (5) forms fluidized state, from the high velocity vapor stream of pre-lift vapor-nozzle (2) ejection, 50～80kg/m is carried and be mixed to form to its jet adsorption by silicate catalyst around
3the high speed catalyst stream of concentration, this high speed catalyzer is under the castering action of pre-lift steam, and the interior transfer lime (4) of flowing through, injects riser reactor (10) middle part;
The annular space that fluidization steam vapor in fluidization steam vapor ring (1) forms from interior transfer lime (4) and riser reactor (10) upwards flows, give the limit wall filling at riser reactor (10) middle part, make the high speed catalyzer that flows into riser reactor middle part (10) to riser reactor (10) central distribution;
At riser reactor (10) middle part, before high speed catalyst stream is radial scattering, spray into stock oil from stock oil feed nozzle (9), after stock oil fully mixes with catalyzer, carry out catalytic cracking reaction 500 ℃ of hot environments.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410036557.0A CN103849424A (en) | 2014-01-24 | 2014-01-24 | Lift pipe reactor pre-lifting device and process flow thereof |
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| CN201410036557.0A CN103849424A (en) | 2014-01-24 | 2014-01-24 | Lift pipe reactor pre-lifting device and process flow thereof |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108854869A (en) * | 2017-05-10 | 2018-11-23 | 中国石油天然气集团公司 | A kind of fine powder lifting device |
| CN113041963A (en) * | 2021-03-25 | 2021-06-29 | 洛阳智邦石化设备有限公司 | Promote catalyst distribution plate structure in advance |
| CN114426489A (en) * | 2020-10-15 | 2022-05-03 | 中国石油化工股份有限公司 | Device and method for preparing aniline by nitrobenzene hydrogenation |
Citations (5)
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|---|---|---|---|---|
| CN1174094A (en) * | 1996-08-20 | 1998-02-25 | 中国石油化工总公司 | Catalytic cracking riser reactor |
| CN1258560A (en) * | 1999-08-23 | 2000-07-05 | 中国石化集团洛阳石油化工工程公司 | Catalytic cracking riser reactor |
| CN2415832Y (en) * | 2000-01-30 | 2001-01-24 | 中国石油化工集团公司 | Catalytic cracking riser reactor |
| CN201988373U (en) * | 2010-12-31 | 2011-09-28 | 洛阳惠生石化工程股份有限公司 | Pre-lifter capable of improving catalyst distribution |
| CN203715573U (en) * | 2014-01-24 | 2014-07-16 | 洛阳智邦石化设备有限公司 | Pre-lifter of riser reactor |
-
2014
- 2014-01-24 CN CN201410036557.0A patent/CN103849424A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1174094A (en) * | 1996-08-20 | 1998-02-25 | 中国石油化工总公司 | Catalytic cracking riser reactor |
| CN1258560A (en) * | 1999-08-23 | 2000-07-05 | 中国石化集团洛阳石油化工工程公司 | Catalytic cracking riser reactor |
| CN2415832Y (en) * | 2000-01-30 | 2001-01-24 | 中国石油化工集团公司 | Catalytic cracking riser reactor |
| CN201988373U (en) * | 2010-12-31 | 2011-09-28 | 洛阳惠生石化工程股份有限公司 | Pre-lifter capable of improving catalyst distribution |
| CN203715573U (en) * | 2014-01-24 | 2014-07-16 | 洛阳智邦石化设备有限公司 | Pre-lifter of riser reactor |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108854869A (en) * | 2017-05-10 | 2018-11-23 | 中国石油天然气集团公司 | A kind of fine powder lifting device |
| CN108854869B (en) * | 2017-05-10 | 2023-10-31 | 中国石油天然气集团公司 | Fine powder lifting device |
| CN114426489A (en) * | 2020-10-15 | 2022-05-03 | 中国石油化工股份有限公司 | Device and method for preparing aniline by nitrobenzene hydrogenation |
| CN113041963A (en) * | 2021-03-25 | 2021-06-29 | 洛阳智邦石化设备有限公司 | Promote catalyst distribution plate structure in advance |
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Application publication date: 20140611 |