CN103657538A - Method for loading and unloading catalysts for fixed fluidized bed reactor - Google Patents
Method for loading and unloading catalysts for fixed fluidized bed reactor Download PDFInfo
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Abstract
The invention relates to a method for loading and unloading catalysts for a fixed fluidized bed reactor, which aims to solve the problem in the prior art that the catalyst loading and unloading operations for the fixed fluidized bed reactor cannot be completed favorably. The method for loading and unloading catalysts for the fixed fluidized bed reactor comprises the following steps: (1) loading catalysts to the reactor: after loading the catalysts into a catalyst tank, introducing a fluidized gas, raising the pressure of the catalyst tank, and loading the catalysts to the reactor through a catalyst loading pipeline, wherein the fluidized gas enters the reactor via a distribution plate at the bottom of the reactor to keep the fluidization of the catalysts, and a filter is arranged in front of an outlet pipeline of the reactor; and (2) unloading the catalysts from the reactor: keeping the catalysts in the reactor at a fluidized state after reaction, starting a catalyst unloading pipeline valve after vacuumizing the catalyst tank, and closing an outlet pipeline valve of the reactor, wherein the catalysts enter the catalyst tank by the catalyst unloading pipeline, and a filter is arranged in front of an outlet pipeline of the catalyst tank. By the technical scheme, the problem is solved well; the method for loading and unloading catalysts for the fixed fluidized bed reactor can be applied to automatic loading and unloading processes of fixed fluidized bed catalysts.
Description
Technical field
The present invention relates to a kind of method of fixed fluidized-bed reactor handling catalyst.
Background technology
At present, fluidized-bed reaction technique has been widely used in the fields such as petrochemical industry, Coal Chemical Industry, fine chemistry industry, because it has temperature, control easily to, rapid deactivation catalyst is easily realized cyclic regeneration, easily realized the advantages such as large-scale production, fluid bed obtains increasing attention in the application of chemical field.
Fluidized-bed reaction-regeneration technology is applied in catalytic cracking (FCC) field in a large number, because FCC catalysqt deactivation speed is very fast, belong to a second level inactivation, so FCC is the basic riser reactor that all adopts at present, the FCC catalyst of inactivation loops back riser after regenerating in regenerator continues to use.The exploitation of FCC technique and catalyst, a large amount of experimental works is exactly to complete in vitro small-sized reaction unit.FCC catalyst performance evaluation device is the earliest ARCO device (the Wachted S of U.S. Atlanti Richfild company exploitation, J.Am.Chem.Soc, Div Petrol Chem Mtg, 1977), it can realize continuous reaction regeneration operation, riser reactor is connected in series by several close phase back-mixing fluid beds, non-plug-flow reaction device, so reaction effect falls far short compared with commercial plant.And aspect catalyst control, do not adopt guiding valve or plug valve and adopt probe, control effect very bad, cause the unstable of catalyst circulation amount.The experimental provision that FCC technological development afterwards adopts has adopted riser reactor, under nearly plug flow regime, check and rate catalyst performance and regenerating stability, the data that obtain have directiveness to the design of commercial plant, and flow to control at catalyst, also adopt the equipment such as guiding valve, guaranteed the stability that catalyst is mobile.CN 200820003767 has announced a kind of Multifunctional riser catalytic cracking test device, adopting small-sized plug valve to control catalyst flows, riser adopts multiple feed, and convenient disassembly, regenerator and settler adopt height to be arranged in juxtaposition, and this device may be used in FCC process exploitation and evaluating catalyst.And in initial FCC catalyst reaction performance evaluation, the more employing tradition of a lot of units is fixed fluidized bed, this is a kind of by the mode of reacting and regeneration examination is separately carried out, but often these fixed fluidized bed evaluation devices do not have good catalyst automatic loading and unloading method.
At present, due to the finiteness of petroleum resources, various countries unit or mechanism start to greatly develop Coal Chemical Industry or gas chemical industry, and the technique of wherein preparing low-carbon alkene (MTO) by synthesis gas through methanol causes increasing attention.In US 4499327 patents, silicoaluminophosphamolecular molecular sieve catalyst is applied to preparing olefin by conversion of methanol technique and studies in detail, think that SAPO-34 is the first-selected catalyst of MTO technique.It is selective that SAPO-34 catalyst has very high light olefin, and activity is also higher, and can make methanol conversion is reaction time of light olefin to be less than the degree of 10 seconds, more even reaches in the reaction time range of riser.But there is deactivation rate feature faster in this catalyst.In CN 200710111149, announced a kind of reactivity worth evaluation method of preparing low carbon olefin hydrocarbon by methanol fluid catalyst, adopt fixed fluidized bed, in charging, add carrier gas, to reduce the deactivation rate of catalyst, product analysis adopts the method for two root chromatogram column Conjoint Analysis, analyze oxygenatedchemicals and hydro carbons for one, analyze hydrogen and oxygenatedchemicals for one, adopt methane to carry out quantitatively as internal standard compound.But, in the method, the chromatography time of each sample was about 20 minutes, analysis time is long, the deactivation rate substantial deviation of catalyst is actual, and the settling section that exists diameter to amplify in traditional small fixed flowing bed, and close phase section diameter is generally shorter, and catalyst is easy to be brought into settling section by gas, the expansion of settling section diameter significantly increases the gas phase time of staying, has increased the generation of secondary response.Because this problem in industrial amplification process is can be by quick separated solution of gas-solid, so the data that adopt traditional fixed fluidized-bed reactor to obtain can not reflect the actual performance of catalyst.In addition, this fixed fluidized bed catalyst automatic loading and unloading device that is not equipped with equally.
Except FCC, MTO reaction field, a plurality of fields such as preparing gasoline by methanol, naphtha catalytic cracking, olefins by catalytic cracking, alkylation of toluene all adopt fluidized-bed process, the laboratory examination of these techniques fluid catalyst used substantially all adopts traditional fixed fluidized bed at present, and is not all equipped with catalyst automatic loading and unloading device.The present invention has solved the problems referred to above targetedly.
Summary of the invention
Technical problem to be solved by this invention is the problem that in prior art, fixed fluidized-bed reactor handling catalyst can not complete preferably automatically, and a kind of method of new fixed fluidized-bed reactor handling catalyst is provided.The method is for fixed fluidized bed catalyst automatic loading and unloading process, have advantages of simple to operate, safe, to change degree fast and automatically high.
For addressing the above problem, the technical solution used in the present invention is as follows: a kind of method of fixed fluidized-bed reactor handling catalyst, comprise the steps: that (1) fills catalyst to fixed fluidized-bed reactor: catalyst is packed into after catalyst tank, pass into fluidizing gas and keep fluidized state, catalyst tank is boosted, by dress agent pipeline, under the promotion of conveying gas, pack catalyst into reactor, fluidizing gas enters in reactor and keeps catalyst fluidization through reactor bottom distribution grid, before reactor outlet pipeline, filter is set; (2) from fixed fluidized-bed reactor, unload catalyst: having reacted, keep catalyst in reactor to be fluidized state, catalyst tank vacuumizes rear unlatching and unloads agent pipeline valve, off-response device outlet line valve, reactor outlet pipeline passes into purge gas and enters reactor, catalyst enters catalyst tank by unloading agent pipeline, before catalyst tank outlet line, filter is set.
In technique scheme, described dress agent pipeline is connected with reactor head, unloads agent pipeline and is connected with 1/8-1/4 reactor reaction zone, reactor bottom distribution grid top At The Height; Described catalyst tank outlet line is connected with vavuum pump, and on outlet line, is provided with emptying bypass; The described agent pipeline that unloads is provided with purge gas pipeline; Described catalyst tank bottom is provided with catalyst and draws off pipeline; Described catalyst tank top is provided with filter; Described distribution grid top is provided with flange, is connected with reactor body; Described fixed fluidized bed top is provided with settling section; Described purge gas is nitrogen; Described valve is manual switchover valve or magnetic valve.
Adopt method of the present invention, can realize the continued operation that fills agent, reacts, unloads agent, and do not need too much people's frock agent, unload agent manual operation, especially when unloading agent, the catalyst of higher temperature directly can be discharged into catalyst tank, for reactor carries out next reaction, reserve the time, improved conventional efficient, avoided unloading the problem that people is damaged that high temperature catalyst easily causes simultaneously.Therefore, method of the present invention, have advantages of simple to operate, safe in fixed fluidized bed catalyst automatic loading and unloading process, to change degree fast and automatically high.
Adopt technical scheme of the present invention: described dress agent pipeline is connected with reactor head, unload agent pipeline and be connected with 1/8-1/4 reactor reaction zone, reactor bottom distribution grid top At The Height; Described catalyst tank outlet line is connected with vavuum pump, and on outlet line, is provided with emptying bypass; The described agent pipeline that unloads is provided with purge gas pipeline; Described catalyst tank bottom is provided with catalyst and draws off pipeline, and described catalyst tank top is provided with filter; Described distribution grid top is provided with flange, is connected with reactor body; Described fixed fluidized bed top is provided with settling section; Described purge gas is nitrogen; Described valve is manual switchover valve or magnetic valve, for the cargo handling process of fixed fluidized bed catalyst, simple to operate, safe, to change degree fast and automatically high, and can under reactor higher temperature, unload agent, has obtained good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of scheme of the present invention.
In Fig. 1,1 is reactor stream oxidizing gases feeding line; 2 preheaters; 3 is distribution grid; 4 is flange; 5 reactor reaction zones; 6 is reactor decanting zone; 7 is dress agent pipeline; 9 for unloading agent pipeline; 10 is reactor outlet pipeline; 12 for unloading agent pipeline purge gas pipeline; 14 is catalyst tank; 15 is catalyst tank outlet line front filter; 16 is differential pressure measurement pipeline; 19 is catalyst tank outlet line emptying bypass; 20 is catalyst tank pressurized pipeline; 23 draw off pipeline for catalyst tank catalyst; 24 is vacuum pump outlet pipeline; 25 is catalyst tank outlet line; 26 is vavuum pump; 29 is reactor outlet pipeline purge gas pipeline; 30 is catalyst dress agent pipeline conveying gas; 31 is catalyst tank fluidizing gas feeding line; 32 is reactor outlet pipeline front filter; 8,11,13,16,17,18,21,22,27,28 be valve.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
The specific embodiment
[embodiment 1]
In fixed fluidized bed device as shown in Figure 1, 36 millimeters of reactor diameter φ, reactor reaction zone height is 600 millimeters, decanting zone diameter is 65 millimeters, be highly 400 millimeters, catalyst tank diameter is 100 millimeters, be highly 380 millimeters, reactor bottom is provided with distribution grid, dress agent pipeline is connected with reactor head, unloading agent pipeline is connected with reactor bottom distribution grid top 1/8 reactor reaction zone At The Height, catalyst tank outlet line is connected with vavuum pump, and on outlet line, be provided with emptying bypass, unload agent pipeline and be provided with purge gas pipeline, under valve 11 closed conditions, provide purge gas, , purge gas is nitrogen, to prevent that unloading agent pipeline stops up, catalyst tank bottom is provided with catalyst and draws off pipeline, dress agent pipeline is positioned at catalyst tank bottom equally, catalyst tank top is provided with outlet line and pressurized pipeline, filter is set before outlet line, outlet line one tunnel is connected with vavuum pump, one tunnel connects emptying bypass.Pressurized pipeline is for providing enough motive forces in dress agent process to catalyst tank.Dress agent pipeline is provided with conveying gas and enters pipeline, guarantees that catalyst enters reactor smoothly by enough power and do not stop up.The process that fixed fluidized-bed reactor fills agent, unloads agent is below described in detail in detail.
To fixed fluidized-bed reactor, fill agent: first catalyst is added in catalyst tank 14, and pass into fluidizing gas maintenance catalyst fluidization through pipeline 31, open valve 16, in catalyst tank, gas, through emptying bypass 19 emptying, controls by the aperture of control valve 16 scale of construction of dropping a hint.Open valve 17, to catalyst tank 14, pass into a large amount of gas, improve catalyst tank 14 pressure, the pressure of controlling catalyst 14 by the aperture of control valve 16,17 is to 0.2MPag.Under this state, valve 11, valve 21, valve 18, valve 22 are closed condition, and valve 13 is opened to unloading agent pipeline 9 and passed into purge gas.Following reaction device reaction zone 5 is warming up to 150 ℃, prepares the 5 dress agent to reactor reaction zone.Open valve 27, reaction zone 5 is interior passes into fluidizing gas through pipeline 1, controls fluidizing gas flow, guarantees that the interior gas phase linear speed of reaction zone 5 is at 0.08 meter per second.Open valve 8, through pipeline 30, to dress agent pipeline 7, pass into conveying wind simultaneously.Subsequently, open valve 21, to the agent of reaction zone 5 dress, until catalyst tank 14 Pressure Drops to reactor pressure quite after, show to fill agent and complete.After dress agent completes, shut off valve 21, valve 8, valve 17, valve 16, stop filling the fluidizing gas that agent pipeline is carried wind, stopped catalyst tank 14.The gas phase linear speed of reactor reaction zone 5 is increased to experiment desired level, starts experiment.
From fixed fluidized-bed reactor, unload agent: having reacted, reactor cuts out raw material, pass into fluidizing gas and keep catalyst fluidization.Now valve 11, valve 8, valve 16, valve 17, valve 21, valve 22, valve 18, valve 28 are closed condition, and valve 27, valve 13 are open mode.Temperature of reactor is 400 ℃, prepares to unload agent.Open valve 18, valve 16, start vavuum pump 26, catalyst tank 14 is vacuumized.After having vacuumized, shut off valve 27, opens valve 28, to reactor outlet pipeline 27, passes into purge gas, improves gradually reactor pressure to 0.15MPag.While starting to unload agent, open valve 11, shut off valve 13, catalyst enters catalyst tank 14 by unloading agent pipeline 9.Unload after agent completes, stop vavuum pump 26, open valve 27, shut off valve 11, valve 18, valve 28, pass into fluidizing gas in catalyst tank 14.Reactor does not need cooling can carry out next experiment.
Whole dress agent, unload in agent process, each valve switch, gas flow, pump etc. can be controlled automatically, and do not need human intervention, and can unload agent by high temperature, handling safety, simple not only, and improved conventional efficient.
Obviously, adopt method of the present invention, for the cargo handling process of fixed fluidized bed catalyst, simple to operate, safe, to change degree fast and automatically high, and can under reactor higher temperature, unload agent, there is larger technical advantage, can be used in the automatic loading and unloading process of fixed fluidized bed catalyst.
Claims (10)
1. a method for fixed fluidized-bed reactor handling catalyst, comprises the steps:
(1) to fixed fluidized-bed reactor dress catalyst: catalyst is packed into after catalyst tank, pass into fluidizing gas and keep fluidized state, catalyst tank is boosted, by dress agent pipeline, under the promotion of conveying gas, pack catalyst into reactor, fluidizing gas enters in reactor and keeps catalyst fluidization through reactor bottom distribution grid, before reactor outlet pipeline, filter is set;
(2) from fixed fluidized-bed reactor, unload catalyst: having reacted, keep catalyst in reactor to be fluidized state, catalyst tank vacuumizes rear unlatching and unloads agent pipeline valve, off-response device outlet line valve, reactor outlet pipeline passes into purge gas and enters reactor, catalyst enters catalyst tank by unloading agent pipeline, before catalyst tank outlet line, filter is set.
2. the method that fixed fluidized-bed reactor loads and unloads catalyst according to claim 1, is characterized in that described dress agent pipeline is connected with reactor head, unloads agent pipeline and is connected with 1/8-1/4 reactor reaction zone, reactor bottom distribution grid top At The Height.
3. the method that fixed fluidized-bed reactor loads and unloads catalyst according to claim 1, is characterized in that described catalyst tank outlet line is connected with vavuum pump, and on outlet line, is provided with emptying bypass.
4. the method that fixed fluidized-bed reactor loads and unloads catalyst according to claim 1, unloads agent pipeline and is provided with purge gas pipeline described in it is characterized in that.
5. the method that fixed fluidized-bed reactor loads and unloads catalyst according to claim 1, is characterized in that described catalyst tank bottom is provided with catalyst and draws off pipeline.
6. the method that fixed fluidized-bed reactor loads and unloads catalyst according to claim 1, is characterized in that described catalyst tank top is provided with filter.
7. the method that fixed fluidized-bed reactor loads and unloads catalyst according to claim 1, is characterized in that described distribution grid top is provided with flange, is connected with reactor body.
8. the method that fixed fluidized-bed reactor loads and unloads catalyst according to claim 1, is characterized in that described fixed fluidized bed top is provided with settling section.
9. the method that fixed fluidized-bed reactor loads and unloads catalyst according to claim 1, is characterized in that described purge gas is nitrogen.
10. the method that fixed fluidized-bed reactor loads and unloads catalyst according to claim 1, is characterized in that described valve is manual switchover valve or magnetic valve.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105617952A (en) * | 2014-11-06 | 2016-06-01 | 中国石油化工股份有限公司 | Discharging system of fluidized bed reactor and method thereof |
| CN106000236A (en) * | 2016-07-08 | 2016-10-12 | 安徽晋煤中能化工股份有限公司 | Solid particle catalyst dismounting device and using method |
| CN107021360A (en) * | 2017-03-16 | 2017-08-08 | 神华集团有限责任公司 | Catalyst device for discharging and the methanol-to-olefins device with it |
| CN108192654A (en) * | 2018-03-20 | 2018-06-22 | 北京拓川科研设备股份有限公司 | A kind of medium-sized experimental facilities of catalytic cracking and experimental method |
| CN109100444A (en) * | 2018-10-11 | 2018-12-28 | 中触媒新材料股份有限公司 | A kind of fixed fluidized bed evaluating apparatus of MTO and method |
| CN109126641A (en) * | 2017-06-15 | 2019-01-04 | 神华集团有限责任公司 | Fischer-tropsch synthetic catalyst fluid bed reduction device and on-line period method |
| CN109355090A (en) * | 2018-10-22 | 2019-02-19 | 山东京博石油化工有限公司 | Catalytic cracking pilot test system unloads agent device and unloads agent blowing method |
| CN109603694A (en) * | 2018-11-23 | 2019-04-12 | 鲁西化工集团股份有限公司 | A kind of operating system and control method promoting fluidized bed running quality |
| CN113559791A (en) * | 2021-07-23 | 2021-10-29 | 陕西延长石油（集团）有限责任公司 | Catalyst unloading system and method for catalytic cracking unit |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2643991Y (en) * | 2003-07-09 | 2004-09-29 | 陈忠丽 | Adding apparatus of catalyzer |
| EP1595596A1 (en) * | 2004-04-29 | 2005-11-16 | Oxeno Olefinchemie GmbH | Gas/liquid distributor with a static mixer |
| CN101596370A (en) * | 2008-06-04 | 2009-12-09 | 中国石油天然气股份有限公司 | Catalyst filling member and filling method thereof |
| CN201362690Y (en) * | 2009-02-06 | 2009-12-16 | 中国石油化工集团公司 | Catalytic cracking regenerated catalyst automatic discharger |
| EP2295136A1 (en) * | 2008-06-30 | 2011-03-16 | Nippon Shokubai Co., Ltd. | Method of packing solid particulate substance into fixed-bed multitubular reactor |
| CN102211044A (en) * | 2010-04-02 | 2011-10-12 | 中国石油化工股份有限公司 | Catalyst particles and method for filling fluidized bed reactor catalyst |
| CN102463082A (en) * | 2010-11-17 | 2012-05-23 | 中国石油化工股份有限公司 | Reactor for evaluating fluidized bed catalyst |
-
2012
- 2012-09-05 CN CN201210325120.XA patent/CN103657538B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2643991Y (en) * | 2003-07-09 | 2004-09-29 | 陈忠丽 | Adding apparatus of catalyzer |
| EP1595596A1 (en) * | 2004-04-29 | 2005-11-16 | Oxeno Olefinchemie GmbH | Gas/liquid distributor with a static mixer |
| CN101596370A (en) * | 2008-06-04 | 2009-12-09 | 中国石油天然气股份有限公司 | Catalyst filling member and filling method thereof |
| EP2295136A1 (en) * | 2008-06-30 | 2011-03-16 | Nippon Shokubai Co., Ltd. | Method of packing solid particulate substance into fixed-bed multitubular reactor |
| CN201362690Y (en) * | 2009-02-06 | 2009-12-16 | 中国石油化工集团公司 | Catalytic cracking regenerated catalyst automatic discharger |
| CN102211044A (en) * | 2010-04-02 | 2011-10-12 | 中国石油化工股份有限公司 | Catalyst particles and method for filling fluidized bed reactor catalyst |
| CN102463082A (en) * | 2010-11-17 | 2012-05-23 | 中国石油化工股份有限公司 | Reactor for evaluating fluidized bed catalyst |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105617952A (en) * | 2014-11-06 | 2016-06-01 | 中国石油化工股份有限公司 | Discharging system of fluidized bed reactor and method thereof |
| CN105617952B (en) * | 2014-11-06 | 2019-08-20 | 中国石油化工股份有限公司 | A discharge system and method for a fluidized bed reactor |
| CN106000236A (en) * | 2016-07-08 | 2016-10-12 | 安徽晋煤中能化工股份有限公司 | Solid particle catalyst dismounting device and using method |
| CN107021360A (en) * | 2017-03-16 | 2017-08-08 | 神华集团有限责任公司 | Catalyst device for discharging and the methanol-to-olefins device with it |
| CN107021360B (en) * | 2017-03-16 | 2019-11-29 | 神华集团有限责任公司 | Catalyst device for discharging and methanol-to-olefins device with it |
| CN109126641A (en) * | 2017-06-15 | 2019-01-04 | 神华集团有限责任公司 | Fischer-tropsch synthetic catalyst fluid bed reduction device and on-line period method |
| CN108192654A (en) * | 2018-03-20 | 2018-06-22 | 北京拓川科研设备股份有限公司 | A kind of medium-sized experimental facilities of catalytic cracking and experimental method |
| CN108192654B (en) * | 2018-03-20 | 2023-11-14 | 北京拓川科研设备股份有限公司 | Medium-sized catalytic cracking experimental equipment and experimental method |
| CN109100444A (en) * | 2018-10-11 | 2018-12-28 | 中触媒新材料股份有限公司 | A kind of fixed fluidized bed evaluating apparatus of MTO and method |
| CN109355090A (en) * | 2018-10-22 | 2019-02-19 | 山东京博石油化工有限公司 | Catalytic cracking pilot test system unloads agent device and unloads agent blowing method |
| CN109603694A (en) * | 2018-11-23 | 2019-04-12 | 鲁西化工集团股份有限公司 | A kind of operating system and control method promoting fluidized bed running quality |
| CN113559791A (en) * | 2021-07-23 | 2021-10-29 | 陕西延长石油（集团）有限责任公司 | Catalyst unloading system and method for catalytic cracking unit |
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