CN102463078A - Boiling bed catalyst on-line priming system - Google Patents
Boiling bed catalyst on-line priming system Download PDFInfo
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- CN102463078A CN102463078A CN201010539161XA CN201010539161A CN102463078A CN 102463078 A CN102463078 A CN 102463078A CN 201010539161X A CN201010539161X A CN 201010539161XA CN 201010539161 A CN201010539161 A CN 201010539161A CN 102463078 A CN102463078 A CN 102463078A
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Abstract
The invention discloses a boiling bed catalyst on-line priming system, the system comprises a liquid jet pump, a protection pot and a circulating pump; the liquid jet pump comprises a sprayed liquid inlet tube, a suction cavity, a pipework segment and an expansion segment, a catalyst inlet and a rotational flow liquid inlet are provided in the suction cavity, the circulating pump inlet is connected with a hot high-pressure separator, the circulating pump outlet is connected with the rotational flow liquid inlet. According to the invention, the circulating pump is used for sucking hot high-pressure separator liquid phase and enters in the liquid jet pump, negative pressure is generated in the suction cavity, the powder catalyst is sucked and introduced in the suction cavities, and is mixed with liquid phase at the rotational flow liquid inlet, pipework segment and the expansion segment enter into a reactor for completing the on-line priming process. According to the invention, the hot high-pressure separator liquid phase is taken as a conveying medium, so that a transferring oil system can be simplified, the introduced rotational flow liquid simplifies the flushing system; the protection pot is a high temperature high pressure container with small volume, the catalyst priming pot is an intermediate pressure container, so that a series problems of high temperature high pressure devices can be avoided, the security is high, and the equipment investment can be greatly reduced.
Description
Technical field
The present invention relates to online loading system of a kind of fluidized bed reactor catalyst and the online charging method of catalyst.
Background technology
Get into 21 century, the oil demand amount increases with development of world economy year by year, and crude oil poor qualityization, heaviness are global trend, increases the light Fuel oil yield, improves the oil utilization rate and becomes the present target of PETROLEUM PROCESSING in the future that reaches.It is wide that the boiling bed hydrogenation technology has adaptability to raw material, and characteristics such as flexible operation be one of important means of weight, residual oil deep processing, so the boiling bed hydrogenation technology become petroleum refining industry's developing focus.Fluidized bed reactor is the up flow type three-phase fluid bed reactor, and its maximum characteristics are that the catalyst granules that flows can be implemented in adding and discharge under the normal running operating mode, and do not influence the carrying out of reaction and the operation of device.Therefore, the catalyst in the fluidized bed reactor is carried out timing add row, can guarantee the activity of catalyst in reactor, thereby realize the continuous long-term operation of residual hydrocracking process.
The fluidized bed reactor working condition pressure is between 14～18MPa; Temperature range is between 360～440 ℃; Under HTHP, catalyst annotated in the reactor of HTHP and do not influence reaction and normally carry out, and can not to have the equipment risk be suitable difficulty for a short time.
US3398085, US3547809 have introduced a kind of process that adopts transferring oil to carry catalyst respectively; In this process, earlier catalyst is placed in the transfer jar (adding the agent jar) of a low-pressure state; At first utilize pump to set up conveying oil circuit from the transferring oil storage tank to reactor; The pressure of transfer jar is raised to consistent with reactor pressure or is higher than reactor pressure, utilize differential pressure to drive catalyst and get into and carry oil circuit, with transferring oil catalyst is dashed and deliver to reactor.The shortcoming of this scheme is: need a complete transferring oil system, comprise the transferring oil storage tank, high-pressure delivery pump; The catalyst transfer jar of a HTHP of needs adds catalyst when transfer jar low pressure, the transfer pressure tank is risen to be higher than reactor pressure then, catalyst is filled in the reactor again.In this process, high-temperature service experience pressure is from the cyclic process of low pressure to high pressure, and the device security risk is too big, and operation is very complicated in actual industrial.It is the charging method of motive force that US4398852 has introduced a kind of Hydrogen Vapor Pressure that adopts; This method is provided with a high-pressure bottle; High-pressure bottle links to each other with reactor through a straight tube, earlier catalyst is put in the high-pressure bottle, utilizes Hydrogen Vapor Pressure that catalyst is pressed in the reactor.This method is simple, but hydrogen after the pressurization easily with catalyst granules compacting in pipeline, gas is passed by slit between the catalyst granules, causes line clogging; Have catalyst residue in the high-pressure bottle of each filling back; Need a HTHP transfer jar, the device security risk is too big.
Summary of the invention
To the deficiency of prior art, the present invention provides a kind of improved boiling-bed catalyst online loading system.
Technical scheme of the present invention is:
The online loading system of a kind of boiling-bed catalyst comprises fluidized bed reactor, thermal high knockout drum, liquid jet pump, catalyst storage tank, protective pot and circulating pump, and wherein said pump entry links to each other with the liquid outlet of thermal high knockout drum; Described liquid jet pump comprises jetting fluid inlet tube, suction chamber, trunnion section and expansion segment; Be provided with catalyst inlet in suction chamber near a side of trunnion; Suction chamber is provided with the rotary fluid inlet tube near a side of jetting fluid inlet tube; Described rotary fluid inlet tube and suction chamber are tangent, and the end of jetting fluid inlet tube is a contraction section; Liquid jet pump links to each other with circulating-pump outlet with the rotary fluid inlet tube through the jetting fluid inlet tube respectively, and catalyst inlet is connected with the catalyst storage tank with protective pot successively, and the expansion segment outlet of liquid jet pump is connected with fluidized bed reactor.
The online loading system of ebullated bed according to the present invention is respectively arranged with valve at described protective pot upstream and downstream, on protective pot, also is provided with Pressure gauge simultaneously.
The jetting fluid inlet tube end of wherein said liquid jet pump is a contraction section, and the angle of throat of this contraction section is 15 °～60 °, and preferred 25 °～30 °, the length of trunnion section is 2～3 times of throat pipe diameter; Described suction chamber is concentric collapsible tube, and shrinking angle is 15 °～60 °, and preferred 30 °～40 °, length is 5～8 times of trunnion section diameter; The angle of flare of said expansion segment is 15 °～30 °, preferred 15 °～20 °.
The online loading system of catalyst of the present invention is provided with circulating pump under the thermal high knockout drum, the liquid-phase product that adopts the thermal high knockout drum utilizes the catalyst of liquid jet pump suction particulate form directly to get into fluidized bed reactor as pumped (conveying) medium.The very little HTHP protective pot of one volumes is set above liquid jet pump, and it is in order before suction chamber pressure is reduced to setting value after the jet pump operate as normal high-pressure system and low-pressure system to be isolated that protective pot is set.The protective pot top is provided with a medium pressure vessel catalyst storage tank.Described liquid jet pump has two liquid phase inlet tubes: a jetting fluid inlet tube forms jet suction chamber is produced suction; A rotary fluid inlet tube produces eddy flow and carries beaded catalyst entering throat of injector pipeline section in suction chamber, can effectively remove the catalyst that remains on the suction chamber wall, prevents the suction chamber obstruction.Protective pot is provided with Pressure gauge, during work, and first start up liquid jets pump; Form suction, protective pot is connected with injector earlier, regulates injector eddy flow liquid phase feed rate; Guarantee that protective pot upward pressure meter reading reaches requirement, simultaneously catalyst is placed in the catalyst storage tank, and feed nitrogen replacement and boost to protective pot pressure; Then protective pot is communicated with catalyst hooper, under draft and the effect of catalyst self gravitation, catalyst granules gets into liquid jet pump through protective pot; Earlier be involved in jet pump trunnion section by the liquid phase of eddy flow, the liquid-phase mixing with jet gets in the reactor again.
Fluidized bed reactor described in the system of the present invention has structure well known to those skilled in the art.The fluidized bed reactor of preferred set inside three phase separator, three phase separator can carry out gas-liquid-solid three-phase to reactant to be separated.For example, described fluidized bed reactor can adopt fluidized bed reactor of putting down in writing among the CN1448212A etc.
The general powdery microspherical catalyst that uses in this fluidized bed reactor.The reactive metal of said microspherical catalyst can be in nickel, cobalt, molybdenum or the tungsten one or more.Can comprise by weight percentage like the catalyst composition: nickel or cobalt are 0.5%～8% (calculating by its oxide); Molybdenum or tungsten are 1%～10% (calculating by its oxide), and carrier can be in aluminium oxide, silica, aluminium oxide-silicon oxide or the titanium oxide one or more.The shape of catalyst is extrudate or sphere, and bulk density is 0.3～0.8g/cm
3, particle diameter (spherical diameter or bar shaped diameter) is 0.1～0.8mm, specific area is 80～120m
2/ g.
Compared with prior art, the online loading system of fluidized bed reactor of the present invention has the following advantages:
1, adopts thermal high knockout drum liquid-phase product as pumped (conveying) medium, and need not from other devices to introduce transferring oil or the transferring oil system is set separately, simplified the design of transferring oil system; Under the effect of liquid jet pump, can either realize the online filling of boiling-bed catalyst, adhesion and the obstruction of catalyst granules in the liquid jet pump body can be effectively prevented again, thereby extra rinse-system can be saved.
2, loading system of the present invention has been cancelled the HTHP filling transfer jar in the conventional loading system, and it is high temperature and high pressure containers that conveying equipment has only protective pot, and volume is very little; Catalyst filling jar is a medium pressure vessel, has avoided a series of problems of high-temperature high-pressure apparatus, and is safe, can reduce equipment investment.
Description of drawings
Fig. 1 is the sketch map of the online loading system of boiling-bed catalyst of the present invention.
Fig. 2 is the structural representation of liquid ejector.
Fig. 3 is that the A of liquid ejector is to view.
The specific embodiment
Further specify technical scheme of the present invention and effect below in conjunction with accompanying drawing.
As shown in Figure 1, the online loading system of boiling-bed catalyst of the present invention comprises fluidized bed reactor 1, thermal high knockout drum 2, circulating pump 3, liquid jet pump 4, protective pot 5 and catalyst storage tank 6.Pipeline 7 is residual oil and hydrogen mixed feeding pipeline, and fluidized bed reactor 1 links to each other with high pressure hot separator 2 through pipeline 8, and thermal high knockout drum 2 links to each other with the cold anticyclone knockout drum through pipeline 10, links to each other with the heat low knockout drum through pipeline 9; The inlet of described circulating pump 3 links to each other with the liquid phase outlet of high pressure hot separator 2 through pipeline 11; Described liquid jet pump 4 links to each other with outlet of circulating pump with pipeline 13 through pipeline 12, and the outlet of liquid jet pump 4 links to each other with fluidized bed reactor 1 through pipeline 14; Place protective pot 5 directly over the described liquid jet pump 4, and link to each other with protective pot 5 through pipeline 15; Place catalyst storage tank 6 directly over the described protective pot 5, and link to each other with catalyst storage tank 6 through pipeline 16; Described catalyst storage tank 6 is provided with catalyst inlet pipeline 17, gas discharge line 18, nitrogen inlet pipeline 19, hydrogen inlet pipeline 20.
The structural representation of said liquid jet pump 4 is seen Fig. 2, Fig. 3.
As shown in Figure 2, liquid ejector 4 comprises suction chamber 21, trunnion section 22, expansion segment 23, jetting fluid inlet tube 24, rotary fluid inlet tube 25 and catalyst inlet pipe 26.Described suction chamber 21 is the concentric circles cone, and the contraction angle of cone is 15 °～60 °, and preferred 30 °～40 °, length is 3～8 times of trunnion section 22 diameters; The superficial liquid velocity of described trunnion section 22 is 2m/s～3m/s, and length of throat is 2～3 times of throat pipe diameter; The angle of flare of described expansion segment 23 is 15 °～30 °, preferred 15 °～20 °; Described jetting fluid inlet tube 24 is provided with contraction mouth, and the angle of throat of contraction mouth is 15 °～60 °, preferred 25 °～30 °; Described rotary fluid inlet tube tangential on the circumferential edge of suction chamber gets into, and sees Fig. 3.
Operation principle below in conjunction with the online loading system of accompanying drawing brief account fluidized bed reactor catalyst of the present invention once.
Before catalyst began filling, all valves all were in closed condition.At first open valve 27, valve 28, valve 29 and valve 30, start circulating pump 3, set up through pipeline 11, pipeline 12, pipeline 14 conveying oil circuit from thermal high knockout drum 2 one liquid jet pumps 4 one fluidized bed reactors 1.Described circulating pump 3 is a high-temperature high pressure pump, its lift 15MPa～20MPa, and preferred 20MPa, the inlet pressure of circulating pump 3 is consistent with the pressure of thermal high knockout drum 2.
When starting circulating pump 3, open valve 31, the catalyst of dry state through the metering heating after pipeline 17 join in the catalyst storage tank 6.Microspherical catalyst is similar in catalyst and the CN1448212A, and diameter is 0.1mm～0.8mm.The adding mode can adopt artificial the adding, also can adopt wind-force to carry, and mode of heating can adopt chuck heating or heating using microwave.Shut off valve 31 is opened valve 33, and nitrogen gets in the catalyst storage tank 6 through pipeline 19, replaces repeatedly with nitrogen, and the gas of displacement is through valve 32, and pipeline 18 is discharged.Hydrogen gets in the catalyst storage tank 6 through pipeline 20, replaces repeatedly with hydrogen, and boosts to 1～4MPa, and the gas of displacement is through valve 32, and pipeline 18 is discharged.Protective pot 5 is a high temperature and high pressure containers, and diameter is equipped with Pressure gauge 37 only than pipeline 16 big grades on the protective pot 5.
Open valve 36, regulate pipeline 13 flows, pipeline 13 flows are 10%～30% of liquid jet pump aspiration, and rotary fluid inlet tube 25 entering from liquid jet pump 4 form eddy flow.Open valve 35; Treat that Pressure gauge 37 shows when pressure is lower than catalyst storage tank 6 pressure, open valve 34, catalyst gets into liquid jet pump 4 through protective pot 5; The trunnion section 22 that gets into liquid jet pump 4 with the liquid-phase mixing of eddy flow, being mixed with jetting fluid gets in the fluidized bed reactor 1.
Catalyst filling finishes the first shut off valve 35 in back, valve 34, shut off valve 30, valve 36, valve 29 and valve 28 successively again.Close circulating pump 3 again, valve 27.Shut off valve 33 then, open valve 32, and catalyst storage tank 6 is depressurized to normal pressure, and once filling finishes.
Claims (10)
1. the online loading system of boiling-bed catalyst comprises fluidized bed reactor, thermal high knockout drum, liquid jet pump, catalyst storage tank, protective pot and circulating pump, and wherein said pump entry links to each other with the liquid outlet of thermal high knockout drum; Described liquid jet pump comprises jetting fluid inlet tube, suction chamber, trunnion section and expansion segment, and the side near trunnion on suction chamber is provided with catalyst inlet, and the side near the jetting fluid inlet tube on the suction chamber is provided with the rotary fluid inlet tube; Liquid jet pump links to each other with circulating-pump outlet with the rotary fluid inlet tube through the jetting fluid inlet tube respectively, and catalyst inlet is connected with the catalyst storage tank with protective pot successively, and the expansion segment outlet of liquid jet pump is connected with fluidized bed reactor.
2. according to the described system of claim 1, it is characterized in that, valve is set respectively, on protective pot, also be provided with Pressure gauge simultaneously at described protective pot upstream and downstream.
3. according to the described system of claim 1, it is characterized in that described rotary fluid inlet tube and suction chamber are tangent.
4. according to the described system of claim 1, it is characterized in that the jetting fluid inlet tube end of said liquid jet pump is a contraction section, the angle of throat of this contraction section is 15 °～60 °.
5. according to the described system of claim 4, it is characterized in that the angle of throat of said contraction section is 25 °～30 °.
6. according to the described system of claim 1, it is characterized in that the length of described trunnion section is 2～3 times of throat pipe diameter.
7. according to the described system of claim 1, it is characterized in that described suction chamber is concentric collapsible tube, angle of throat is 15 °～60 °, and the length of suction chamber is 5～8 times of trunnion section diameter.
8. according to the described system of claim 7, it is characterized in that the angle of throat of described concentric collapsible tube is 30 °～40 °.
9. according to the described system of claim 1, it is characterized in that the angle of flare of said expansion segment is 15 °～30 °.
10. according to the described system of claim 9, it is characterized in that the angle of flare of said expansion segment is 15 °～20 °.
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| CN 201010539161 CN102463078B (en) | 2010-11-05 | 2010-11-05 | Boiling bed catalyst on-line priming system |
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| CN 201010539161 CN102463078B (en) | 2010-11-05 | 2010-11-05 | Boiling bed catalyst on-line priming system |
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| CN102463078A true CN102463078A (en) | 2012-05-23 |
| CN102463078B CN102463078B (en) | 2013-08-28 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108940138A (en) * | 2018-07-23 | 2018-12-07 | 新奥科技发展有限公司 | A kind of fluidized-bed catalytic reactor |
| CN109999730A (en) * | 2019-04-26 | 2019-07-12 | 河南百优福生物能源有限公司 | A kind of online charging method of catalyst and device of biomass pyrolysis liquid fluidized bed reactor |
Citations (4)
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| JPS60147230A (en) * | 1984-01-10 | 1985-08-03 | Mitsubishi Heavy Ind Ltd | Liquid level detecting apparatus in three-phase fluidized reaction apparatus such as boiling bed reactor |
| WO1995022717A1 (en) * | 1994-02-18 | 1995-08-24 | The Babcock & Wilcox Company | Method and apparatus for controlling the bed temperature in a circulating fluidized bed reactor |
| CN1453334A (en) * | 2002-04-26 | 2003-11-05 | 中国石油化工股份有限公司 | Desending catalytic cracking reactor and its application |
| CN2761258Y (en) * | 2004-10-29 | 2006-03-01 | 中国石油化工股份有限公司 | Gas-liquid counterflow reactor |
-
2010
- 2010-11-05 CN CN 201010539161 patent/CN102463078B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60147230A (en) * | 1984-01-10 | 1985-08-03 | Mitsubishi Heavy Ind Ltd | Liquid level detecting apparatus in three-phase fluidized reaction apparatus such as boiling bed reactor |
| WO1995022717A1 (en) * | 1994-02-18 | 1995-08-24 | The Babcock & Wilcox Company | Method and apparatus for controlling the bed temperature in a circulating fluidized bed reactor |
| CN1453334A (en) * | 2002-04-26 | 2003-11-05 | 中国石油化工股份有限公司 | Desending catalytic cracking reactor and its application |
| CN2761258Y (en) * | 2004-10-29 | 2006-03-01 | 中国石油化工股份有限公司 | Gas-liquid counterflow reactor |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108940138A (en) * | 2018-07-23 | 2018-12-07 | 新奥科技发展有限公司 | A kind of fluidized-bed catalytic reactor |
| CN108940138B (en) * | 2018-07-23 | 2020-12-29 | 新奥科技发展有限公司 | Fluidized bed catalytic reactor |
| CN109999730A (en) * | 2019-04-26 | 2019-07-12 | 河南百优福生物能源有限公司 | A kind of online charging method of catalyst and device of biomass pyrolysis liquid fluidized bed reactor |
| CN109999730B (en) * | 2019-04-26 | 2022-02-25 | 河南百优福生物能源有限公司 | Online catalyst filling method and device for biomass pyrolysis liquid fluidized bed reactor |
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| CN102463078B (en) | 2013-08-28 |
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