CN205182691U - Thick liquid attitude bed circulation flow reactor - Google Patents
Thick liquid attitude bed circulation flow reactor Download PDFInfo
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- CN205182691U CN205182691U CN201520967220.1U CN201520967220U CN205182691U CN 205182691 U CN205182691 U CN 205182691U CN 201520967220 U CN201520967220 U CN 201520967220U CN 205182691 U CN205182691 U CN 205182691U
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Abstract
The utility model provides a thick liquid attitude bed circulation flow reactor, includes tedge, downtake, filtering component, filtration recoil device and regularly carries out on -off operation's auto -change over device, tedge upper portion intercommunication downtake upper portion, tedge bottom intercommunication downtake bottom, tedge bottom be equipped with feed inlet, the tedge top is equipped with the gas outlet, the downtake in set up filtering component to set up the purified liquor outlet through filtering component, the purified liquor outlet still communicate and filter the recoil device, on the downtake, the filtering component lower part sets up the auto -change over device that can regularly carry out on -off operation. The utility model provides a thick liquid attitude bed circulation flow reactor still is equipped with the auto -change over device that can regularly carry out on -off operation in downtake department, and filter the dead end and the crossflow filtration mode combines together with the help of this auto -change over device, can guarantee the steady running of filter long period.
Description
Technical field
The utility model relates to a kind of reactor of petrochemical industry, more particularly, relates to a kind of slurry bed circulatory flow reactor.
Background technology
Paste state bed reactor is a kind of conventional gas-liquid contact reaction equipment, has high liquid storage amount.For the catalytic reaction process that reaction heat is very large, use paste state bed reactor effectively can remove reaction heat, the isothermal operation of realization response device, ensure the normal operation of reactor, be therefore widely applied in current chemical process.And slurry bed circulatory flow reactor is the efficient heterophase reactor of one grown up on the basis of slurry bed system bubbling reactor.Slurry bed circulatory flow reactor, except all advantages having slurry bed system bubbling reactor and have, can also make the fluid of its inside do well-regulated circulating, thus enhance the mixing between reactant, diffusion, heat transfer and mass transfer.
In order to eliminate the impact of diffusion in paste state bed reactor, the even more fine grain catalyst of general employing tens microns, eliminate the impact of diffusion in catalyst, there is very high reaction specific surface and activity, the consumption of catalyst can be greatly reduced, simultaneous reactions device inside have evenly flow regime, therefore there is good technical development prospect.But also bring product thereupon and be separated this difficult problem with catalyst granules.How effectively to realize solid-liquor separation, become and using the key technology in slurry reactor process.
The solid-liquor separation of paste state bed reactor catalyst slurry generally carries out outside reactor, and usually adopt the mode of filtration or sedimentation, the catalyst separated still needs to send back to as a slurry in reactor.
Hydrogen peroxide is a kind of important Inorganic Chemicals, and producing water and oxygen after decomposing, to environment non-secondary pollution, is a kind of green chemical.Generally adopt the anthraquinone production carrying out hydrogen peroxide both at home and abroad at present.Process for prepairng hydrogen peroxide by anthraquinone is using anthraquinone derivative as working material, and under the effect of catalyst, the anthraquinone derivative hydrogenation of will dissolve in organic solvent with hydrogen, generates corresponding hydrogen anthraquinone.Then, hydrogen anthraquinone oxidation Hydrogen Peroxide and anthraquinone derivative.Finally, obtain certain density aqueous hydrogen peroxide solution as product with the hydrogen peroxide in water extraction organic solvent, the working solution containing anthraquinone derivative and organic solvent is then recycled.Wherein, the efficiency of anthraquinone hydrogenation process directly determines output and the concentration of hydrogen peroxide, marginal to the production tool of whole hydrogen peroxide.At present domestic the most frequently used in anthraquinone hydrogenation process be down-type fixed-bed reactor, i.e. trickle bed reactor, but fixed bed reactors exist that catalyst use efficiency is low, reaction selectivity is low, temperature distributing disproportionation is even in bed, catalyst local liquid holdup is large and working solution is degraded serious problem.And the reactor adopting gas and liquid flowing to move upward is the optimal selection carrying out anthraquinone derivative hydrogenation process.This type of reactor comprises tubular type suspended-bed reactor, bubbling bed reactor and paste state bed reactor.Also flow in the process of flowing at gas-liquid two-phase, working solution and hydrogen anthraquinone mixed solution are as continuous phase, and hydrogen-containing gas is as decentralized photo, both the treating capacity of working solution and the utilization rate of catalyst can have been improved, increase anthraquinone conversion ratio, overcome again fixed bde catalyst bed local liquid holdup large, the problem of the working solution degraded that temperature distributing disproportionation causes.
Utility model content
The technical problems to be solved in the utility model is to provide a kind of slurry bed circulatory flow reactor.
A kind of paste state bed reactor, comprise tedge, down-comer, filter assemblies, filter the switching device shifter of recoiling device and timing execution switching manipulation, described tedge top is communicated with down-comer top, be communicated with bottom described tedge bottom down-comer, feed(raw material)inlet is provided with bottom described tedge, tedge top is provided with gas vent, in described down-comer, filter assemblies is set, and assembly arranges purified liquor outlet after filtration, described purified liquor outlet is also communicated with filtration recoiling device, on down-comer, filter assemblies bottom arranges the switching device shifter that regularly can perform switching manipulation.
The beneficial effect of the slurry bed circulatory flow reactor that the utility model provides is:
The down-comer place of slurry bed circulatory flow reactor is provided with filter, in order to the solid-liquor separation of realization response logistics.Also be provided with the switching device shifter that regularly can perform switching manipulation at down-comer place, by this switching device shifter, dead-end filtration and cross-flow filtration pattern combined, the macrocyclic steady running of filter can be ensured.When plugged filtration media is serious, high pressure back-flushing technique is adopted to regenerate filter medium.Slurry bed circulatory flow reactor is combined with combination filtering technique, there is all even utilization ratio of catalyst distribution in reactor high, the advantage of uniformity of temperature profile.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the first embodiment of slurry bed circulatory flow reactor;
Fig. 2 is the schematic flow sheet of slurry bed circulatory flow reactor the second embodiment;
Fig. 3 is the third embodiment schematic flow sheet of slurry bed circulatory flow reactor.
Wherein: 1-phase feed entrance; 2-liquid phase feed entrance; 3-tedge; 4-gas vent; 5-down-comer; 6-filtrate district; 7-filter assemblies; 8-slurries district; 9-purified liquor outlet; 11-catalyst adds entrance; 12-catalyst unloads outlet; 14-filters recoiling device; 16-product Clear liquid tank; 17-expanding reach; 20-gas-liquid separator; 23-outer tube; 24 inner sleeves; Annular space between 26-inner sleeve and outer tube; Annular space between 27-outer tube and reactor wall; 13,15,18-pipeline.
Detailed description of the invention
Below describe detailed description of the invention of the present utility model in detail.Wherein, " top " of the container mentioned in description refers to the position of the 0-50% of container from top to bottom, " bottom " of container refers to the position of the 50%-100% of container from top to bottom, " bottom " of container refers to that the position of the 90%-100% of container from top to bottom, " top " of container refer to the position of the 0-10% of container from top to bottom.
A kind of slurry bed circulatory flow reactor, comprise tedge, down-comer, filter assemblies, filter recoiling device and the switching device shifter that regularly can perform switching manipulation, described tedge top is communicated with down-comer top, be communicated with bottom described tedge bottom down-comer, feed(raw material)inlet is provided with bottom described tedge, tedge top is provided with gas vent, in described down-comer, filter assemblies is set, and assembly arranges purified liquor outlet after filtration, described purified liquor outlet is also communicated with filtration recoiling device, on down-comer, filter assemblies bottom arranges the switching device shifter that regularly can perform switching manipulation.
In the slurry bed system that the utility model provides in circulation reaction unit, described slurry bed system hydrogenation reactor height can at 3-100m, preferably 5-30m, most preferably 8-20m, and diameter is at 0.5-10m, preferably 3-8m.
Preferably, described tedge top is the expanding reach that caliber expands.Preferably, described expanding reach is (1.2 ~ 6) with the diameter ratio of tedge: 1, more preferably (2 ~ 3): 1, described expanding reach and the aspect ratio of tedge are (0.1 ~ 0.5): 1.More preferably (0.2 ~ 0.3): 1.
Preferably, in the slurry bed circulatory flow reactor that the utility model provides, arrange guide shell in described expanding reach, described guide shell maximum gauge is (0.5 ~ 0.9) with the diameter ratio of expanding reach: 1.Guide shell is the homogeneous cylinder of diameter, or a cylindrical section of from top to bottom reduced, or is made up of the multistage cylinder that diameter is different.Along leaving space with expanding reach top wall on described guide shell, under described guide shell along with expanding reach bottom wall leave space, space in expanding reach is divided in guide shell by guide shell, annular space two parts between guide shell and expanding reach wall, and two parts space communicates respectively in guide shell upper and lower.
Preferably, described guide shell is two-layer sleeve pipe.
In the slurry bed circulatory flow reactor that the utility model provides, the bottom of described tedge is provided with feed(raw material)inlet, and described feed(raw material)inlet can be one, also can arrange gas-phase feed mouth and liquid phase feeding mouth respectively.
Preferably, bottom described tedge, feed(raw material)inlet place arranges fluid distributor.Described fluid distributor can be one, and gas-phase feed and liquid phase feeding can share a fluid distributor after mixing.Also gaseous fluid distributor and liquid phase fluid distributor can be set respectively.When described feed(raw material)inlet is respectively gas-phase feed mouth and liquid phase feeding mouth, gaseous fluid distributor and liquid fluid distributor are set respectively at gas-phase feed mouth and liquid phase feeding mouth place.Gas-phase feed and liquid phase feeding are by independently gaseous distributer and liquid phase distributor enter reactor respectively.
Preferably, described fluid distributor position is lower than tedge bottom and junction, solid-liquid separator bottom.The perforate direction of more preferably described fluid distributor bottom tedge, to prevent solids particles precipitate at reactor bottom by the souring of fluid.
Connecting line bottom described down-comer bottom or down-comer and tedge arranges catalyst and unloads outlet, on the connecting line bottom described down-comer and tedge or catalyst is set bottom tedge adds entrance.Described catalyst adds entrance and is arranged on catalyst and unloads outlet downstream.Because course of reaction inevitably causes wearing and tearing and the inactivation of a part of catalyst, in order to ensure the activity of catalyst in reactor, need wearing and tearing and the inactivation of periodic detection catalyst, according to circumstances unload outlet extraction portion at catalyst and divide fine powder and decaying catalyst; And add entrance by catalyst, regular replenishment fresh catalyst.Catalyst replacement process does not need to stop work, and extends the operation cycle of whole device.
In the paste state bed reactor that the utility model provides, described down-comer and the diameter ratio of tedge are (1-10): 1, most preferably (1-5): 1.Described down-comer is one or more.Down-comer arranges filter assemblies, for the further Separation of Solid and Liquid of slurries be separated through preliminary gas-liquid-solid three-phase from paste state bed reactor top, the solid catalyst particle in isolated by filtration slurries.Described filter assemblies can be one or more groups.Filter assemblies can be ceramic membrane, metal film, forming metal screen cloth, one or more the combination of sintering orifice plate, non-woven bag etc.Down-comer inner space is divided into slurries district and clear liquid area by filter assemblies, and slurries district is communicated with by bottom pipeline and paste state bed reactor; Arrange purified liquor outlet in clear liquid area, product clear liquid is by purified liquor outlet discharging.
The paste state bed reactor that the utility model provides is preferably as anthraquinone legal system hydrogen peroxide slurry bed system hydrogenation reactor.Slurry bed system hydrogenation reactor structure as hydrogen peroxide processed is simple, reaction mass is at paste state bed reactor interior orientation circulation, improve the flow uniformity of each phase of gas-liquid-solid in reactor, concentration and Temperature Distribution evenly, avoid the probability of excessive hydrogenation, improve hydrogen effect, and then improve the concentration of the rear hydrogen peroxide product of extraction.
In order to meet the requirement of ultralow catalyst granules content in product clear liquid, especially described slurry wound reaction unit is as anthraquinone hydrogenation reactor, for ensureing the security of anthraquinone hydrogenation liquid subsequent oxidation operation, preferably, described slurry bed circulatory flow reactor also comprises secondary filter, for the micro-solid catalyst granules in further products of separated clear liquid.Described down-comer supernatant outlet secondary filter.Three-stage filtration equipment can also be set after cascade filtration equipment again, guarantee that catalyst was blocked fully before oxidation operation.
The using method of the slurry bed circulatory flow reactor that the utility model provides, be preferred for preparing hydrogen peroxide, anthraquinone working solution and hydrogen-containing gas enter bottom tedge, mix with the slurries in tedge and move upward, in the presence of a hydrogenation catalyst, anthraquinone derivative hydrogenation reaction in working solution obtains hydrogen anthraquinone, in the gas-liquid separation of tedge top, when arranging guide shell, gas-liquid-solid three-phase can be strengthened through guide shell to be separated, gas from gas outlet is discharged, slurries enter further isolated by filtration Hydrogenation catalyst granule wherein in down-comer, isolated liquid phase is discharged as hydride through purified liquor outlet, hydride obtains the oxidation solution containing hydrogen peroxide in oxidation reactor with oxygen reaction, oxidation solution obtains hydrogenperoxide steam generator and working solution through extract and separate.
Preferred clear liquid enters in secondary filter and filters, and in described secondary filter, catalyst granules is filtered member obstruction, forms filter cake, regularly discharges secondary filter; Filtering through cascade filtration equipment the clear liquid obtained is hydride.Secondary filter can realize the meticulous separation of solid liquid phase, guarantees the security that subsequent oxidation operates.
When not stopping work, unloading outlet by the catalyst on slurry bed circulatory flow reaction unit and regularly taking out catalyst fines and decaying catalyst, and adding entrance regularly to fresh makeup catalyst in reactor by catalyst.
In the method preparing hydrogen peroxide, the reaction temperature in described tedge is 35 ~ 80 DEG C, preferably 55 ~ 75 DEG C; Reaction pressure is 0.1 ~ 0.5MPa, preferably 0.2 ~ 0.3MPa.It is formulated that described working solution is that alkyl-anthraquinone is dissolved in organic solvent.Working solution disclosed in prior art can be adopted, generally mixed by a certain percentage by components such as anthraquinone derivative, heavy aromatics, trioctyl phosphates and form.The catalyst adopted is the supported catalyst of load regulation group VIII metal on heat-resistant inorganic oxide.The catalyst with hydrogenation/dehydrogenation performance can be adopted in prior art, such as the catalyst of load group VIII noble metals.
When the utility model arranges guide shell, guide shell makes fluid be formed in expanding reach to stream, the three phase separation of strengthening reaction liquid, catalyst and gas.In slurries, gas can fully remove, and the most of catalyst granules in expanding reach is stayed in expanding reach and tedge, alleviates the operation burden of subsequent technique, reduces the probability of catalyst abrasion.In the fluid product that solid-liquid separator filters, solid content is lower.Partially catalyzed agent circulates between tedge and solid-liquid separator, improves the concentration of catalyst bottom tedge, make the concentration of slurries and Temperature Distribution evenly, improve utilization rate and the reaction efficiency of catalyst.Slurry bed system hydrogenation reactor provided by the invention can avoid there is flow dead and focus in reactor, reduces catalyst abrasion probability, effective prolong operation cycle.As the anthraquinone hydrogenation reactor preparing hydrogen peroxide, the probability of working solution over-hydrogenation effectively can be reduced.Further illustrate anthraquinone legal system hydrogen peroxide slurry bed system hydrogenation reactor provided by the invention and application below in conjunction with accompanying drawing, but the present invention is not therefore subject to any restriction.
The first embodiment of the slurry bed circulatory flow reactor that accompanying drawing 1 provides for the utility model, as shown in Figure 1, slurry bed circulatory flow reactor, comprise tedge 3, down-comer 5, filter assemblies 7 and filter recoiling device 14, be provided with feed(raw material)inlet bottom tedge 3, tedge 3 top is provided with gas vent 4, and described down-comer 5 arranges filter assemblies 7, the inner space of filter assemblies 7 is divided into slurries district 8 and filtrate district 6, and the clear liquid area of down-comer 5 arranges purified liquor outlet 9.Preferred purified liquor outlet 9 is positioned at the top in filtrate district.Described purified liquor outlet 9 is communicated with product Clear liquid tank 16 through pipeline 15, is also communicated with through pipeline 13 and filters recoiling device 14, and on down-comer 3, filter assemblies 7 bottom arranges and regularly can perform the switching device shifter 10 of switching manipulation.
Phase feed and liquid phase feed enter paste state bed reactor from gas feed 2 and liquid-inlet 1 respectively, mix with the slurries in tedge 3, fully contact and react in the process risen with catalyst.Depart from the complete gas of the top unreacted of tedge 3 and slurries, discharge reactor from gas vent 4 and do further process.
Slurries from tedge top enter in the filter assemblies 7 of down-comer, under the differential pressure action of screen pipe both sides, carry out solid-liquor separation.Filtrate enters Clear liquid tank 16 by purified liquor outlet 9, pipeline 15, and the partially catalyzed agent particle be trapped in screen pipe 8 continues to flow downward with slurries, and circulation flows in tedge 3 and continues to participate in reaction.
When slurry bed system external loop reactor starts running, first keep switching device shifter 10 to be in closed condition, now filtered model is dead-end filtration.Reaction clear liquids a large amount of in the process flows into hydrogenation flow container 16 by pipeline 15, and the inwall that a catalyst granules part is deposited in screen pipe forms filter cake, and a part is deposited in the upper port place of switching device shifter 10.After a period of time, control switching device shifter 10 and be in opening, now filtered model is cross-flow filtration.In the process, the slurries of down-comer internal circulation flow, effectively can wash away the particle of screen pipe inwall accumulation and the particle of switching device shifter 10 upper port accumulation, recover the permeability of screen pipe, and catalyst return in tedge 3 simultaneously with slurries.The mode that this alternate combinations is filtered can realize filter long period and high-throughout steady running.
When the pressure reduction of screen pipe both sides is higher than 0.25MPa, backwashing system 14 is started working.First close the valve on pipeline 15, keep the control valve on switching device shifter 10 and pipeline 13 to be in opening, by the high pressure of recoil tank 14, backwash medium enters 6 pairs, filtrate district screen pipe and carries out back flush.Be blocked in and filter in pore and the catalyst granules be deposited on inwall departs from screen pipe under the effect of backwash medium, to be scattered in slurries and in Returning reactor tedge 3.When the pressure reduction of screen pipe both sides is lower than 0.05MPa, close control valve on pipeline 13, open the valve on pipeline 15, and make switching device shifter 10 regularly execution switch motion carry out filter operation.Wherein backwash medium can adopt inert gas as nitrogen, also can adopt reaction clear liquid.
The bottom of down-comer 5 is provided with catalyst outlet 12, for the catalyst of the catalyst fines and inactivation of discharging wearing and tearing; Described down-comer is also provided with catalyst and adds entrance 11, in order to ensure the activity of catalyst in reactor, regularly carries out supplementing of fresh catalyst.Catalyst adds entrance 11 and is arranged on catalyst and unloads outlet 12 downstream.
The second embodiment of the slurry bed circulatory flow reactor that accompanying drawing 2 provides for the utility model, as shown in Figure 2, the top of tedge 3 is expanding reach 17, down-comer top arranges gas-liquid separation section 20, at the expanding reach on tedge top, the flow velocity of slurries reduces, larger particle generation sedimentation returns in tedge 3 and continues to participate in reaction, slurries enter in gas-liquid separation section 20 bubble removed further wherein, gas-liquid separation section top is communicated with through the top of pipeline 18 with tedge 3, the gas on gas-liquid separation section top enters expanding reach 17 top, paste state bed reactor is discharged from gas vent 4.
The third embodiment schematic diagram of the slurry bed circulatory flow reactor that accompanying drawing 3 provides for the utility model.As shown in Figure 3, in the expanding reach 17 on tedge top, guide shell is set.Described guide shell maximum gauge is 0.5 ~ 0.9:1 with the diameter ratio of expanding reach.Guide shell can be two-layer sleeve pipe, comprises inner sleeve 24 and outer tube 23, and when slurries are when flowing through inner sleeve 24 and being inner, the flow velocity of slurries reduces, and flow to and change, part bubble is separated with slurries, discharges from pipeline 4.The solid particles sediment that particle diameter is larger returns in tedge 3 and continues to participate in reaction, all the other solid particles enter the annular gap 26 between inner sleeve 24 and outer tube 23 with slurries and flow downward, in the bottom of annular gap 26, slurries carry most solid particle and flow in tedge 3, after converging with the slurries main body upwards flowed, together flow in inner sleeve 24, slurries complete internal circulation flow by inner sleeve 24.In annular gap 26 between inner sleeve and outer tube, only there is a fraction of solid particle upwards to flow into the annular gap 27 between reactor wall and outer tube with slurries, and enter gas-liquid separation section 20 by pipeline 19.Slurries, after gas-liquid separation section 20 removes bubble further, enter in the filter assemblies of down-comer and carry out solid-liquor separation.
Along having certain gap with expanding reach 2 top on expanding reach 2 inner draft tube, clearance height is within the scope of 10 ~ 500mm.Leave gap bottom edge and expanding reach under guide shell, form circulation for fluid at guide shell interior or exterior space.Guide shell position can adjust according to actual conditions.
Below describe the preferred embodiment of the present invention in detail by reference to the accompanying drawings, but the present invention is not limited to the detail in above-mentioned embodiment.
Further illustrate slurry bed circulatory flow reactor and methods for using them provided by the invention by the following examples, but not thereby limiting the invention.
Hydrogen effect assay method in embodiment: get 5mL hydride in separatory funnel, then add the heavy aromatics of 10mL and the H of 20mL
2sO
4solution (H
2sO
4be 1:4 with the volume ratio of water); Logical O in above-mentioned mixed solution
2, till bubbling is oxidizing to glassy yellow or crocus (about 10 ~ 15min); With pure water extractive reaction liquid 4 ~ 5 times, about 20mL water at every turn; With the KMnO of concentration 0.1mol/L in extract
4standard liquid is titrated to blush, and 30s is colour-fast is terminal.Then hydrogen effect (gH
2o
2/ L)=concentration of standard solution (0.1mol/L) × standard liquid volume (mL) × 17.01/5.
The catalyst adopted is: the palladium-carbon catalyst Pd110 that Yu Rui Chemical Co., Ltd. produces, and design parameter is as follows: bullion content 10% ± 0.2%, specific area>=950m
2/ g, metal surface area 85 ~ 105m
2/ g, carrier average grain diameter 100 μm.
Working solution is: the 1:1 ratio mixing by volume of 2-EAQ and solvent, and solvent is made up of C10 aromatic hydrocarbons and trioctyl phosphate, the two 3:1 ratio mixing by volume.
Embodiment 1
Embodiment 1 illustrates that paste state bed reactor provided by the invention is applied to the anthraquinone effect preparing hydrogen peroxide.
Adopt the paste state bed reactor shown in accompanying drawing 3, wherein, reaction tedge is of a size of Φ 150 × 5000mm, expanding reach is of a size of Φ 450 × 1500mm, guide shell is made up of inner sleeve and outer tube, and outer tube is of a size of Φ 400 × 500mm, and inner sleeve is of a size of Φ 300 × 550mm.Down-comer is of a size of Φ 150 × 1500mm, and the ceramic membrane filter assembly that two groups of height are 500mm is equipped with in inside, sets when each filter differential pressure reaches 0.06MPa and carries out automatic backflushing, and backwash liquid reacts clear liquid after filtering.Clear liquid after filtration enters secondary filter, and the filter medium installed in secondary filter is non-woven bag.
Hydrogen-containing gas and working solution are after premix, enter in tedge by the fluid distributor bottom tedge, backward upper flowing is mixed with the working solution containing catalyst granules, anthraquinone derivative simultaneously in hydride and hydrogen reaction, gas-liquid-solid three-phase initial gross separation in expanding reach, hydrogen-containing gas is discharged by the gas vent of reactor head.Slurries enter in solid-liquid separator, discharged, then introduce secondary filter through the clear liquid obtained after filter medium by purified liquor outlet, and the hydride being rich in solid particle not through filter medium returns continuation participation reaction bottom tedge bottom solid-liquid separator.The air speed of the hydride in secondary filter is 0.3hr
-1, filtration pressure difference is about 0.8MPa, and after secondary filter filters, the solid content in clear liquid is for being less than 5ppm.The hydride that secondary filter obtains enters oxidation reactor, is obtained by reacting hydrogen peroxide and working solution with oxygen-containing gas, and obtains hydrogenperoxide steam generator after extraction tower extraction.The operating condition of oxidation reactor is: temperature is 50 DEG C, and pressure is 0.2MPa.The operating condition of extraction tower is: temperature is 55 DEG C, and pure water flow is 12m
3/ h.Reaction condition after stable operation and the results are shown in Table 1.
Table 1 synthesize hydrogen peroxide reaction condition and result
| Project | Embodiment 1 |
| Reaction temperature, DEG C | 50 |
| Reaction pressure, Mpa | 0.2 |
| Working solution inlet amount, m 3/h | 1 |
| H 2Inlet amount, Nm 3/h | 4 |
| Gas superficial gas speed, m/s | 0.64 |
| Liquid is speed in solid-liquid separator, m/s | 0.04 |
| Hydrogen is imitated, gH 2O 2/l | 14 |
Claims (11)
1. a slurry bed circulatory flow reactor, it is characterized in that, comprise tedge, down-comer, filter assemblies, filter the switching device shifter of recoiling device and timing execution switching manipulation, described tedge top is communicated with down-comer top, be communicated with bottom described tedge bottom down-comer, feed(raw material)inlet is provided with bottom described tedge, tedge top is provided with gas vent, in described down-comer, filter assemblies is set, and assembly arranges purified liquor outlet after filtration, described purified liquor outlet is also communicated with filtration recoiling device, on down-comer, filter assemblies bottom arranges the switching device shifter that regularly can perform switching manipulation.
2. according to slurry bed circulatory flow reactor according to claim 1, it is characterized in that, described tedge top is the expanding reach that caliber expands.
3. according to slurry bed circulatory flow reactor according to claim 2, it is characterized in that, described expanding reach is 1.2 ~ 6:1 with the diameter ratio of tedge, and aspect ratio is 0.1 ~ 0.5:1.
4. according to slurry bed circulatory flow reactor according to claim 3, it is characterized in that, described expanding reach is 2 ~ 3 with the diameter ratio of tedge, and aspect ratio is 0.2 ~ 0.3.
5. according to slurry bed circulatory flow reactor according to claim 4, it is characterized in that, described down-comer top arranges gas-liquid separator, and the top of described gas-liquid separator is communicated with tedge top.
6. according to the slurry bed circulatory flow reactor in claim 2-5 described in any one, it is characterized in that, in described expanding reach, guide shell is set.
7. according to slurry bed circulatory flow reactor according to claim 6, it is characterized in that, described guide shell maximum gauge is 0.5 ~ 0.9:1 with the diameter ratio of expanding reach.
8. according to slurry bed circulatory flow reactor according to claim 7, it is characterized in that, described guide shell is two-layer sleeve pipe.
9. according to the slurry bed circulatory flow reactor in claim 1-5 and 7,8 described in any one, it is characterized in that, bottom described tedge, feed(raw material)inlet place arranges fluid distributor, and the position of described fluid distributor is lower than tedge bottom and down-comer bottom junctions.
10. according to slurry bed circulatory flow reactor according to claim 9, it is characterized in that, the perforate direction of described fluid distributor is bottom tedge.
11. according to the slurry bed circulatory flow reactor in claim 1-5 and 7,8 described in any one, it is characterized in that, connecting line bottom described down-comer bottom or down-comer and tedge arranges catalyst and unloads outlet, on the connecting line bottom described down-comer and tedge or catalyst is set bottom tedge adds entrance.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108854859A (en) * | 2018-07-27 | 2018-11-23 | 中化蓝天霍尼韦尔新材料有限公司 | A kind of suspension liquid phase reaction unit and operation method |
| CN111013501A (en) * | 2019-10-25 | 2020-04-17 | 河北美邦工程科技股份有限公司 | Slurry bed continuous hydrogenation reaction device and method |
| CN113368698A (en) * | 2021-08-16 | 2021-09-10 | 山东浦创流体技术有限公司 | Silicon carbide ceramic membrane filter equipment |
-
2015
- 2015-11-27 CN CN201520967220.1U patent/CN205182691U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108854859A (en) * | 2018-07-27 | 2018-11-23 | 中化蓝天霍尼韦尔新材料有限公司 | A kind of suspension liquid phase reaction unit and operation method |
| CN108854859B (en) * | 2018-07-27 | 2023-08-18 | 中化蓝天霍尼韦尔新材料有限公司 | Suspension gas-liquid phase reaction device and operation method |
| CN111013501A (en) * | 2019-10-25 | 2020-04-17 | 河北美邦工程科技股份有限公司 | Slurry bed continuous hydrogenation reaction device and method |
| CN111013501B (en) * | 2019-10-25 | 2021-09-14 | 河北美邦工程科技股份有限公司 | Slurry bed continuous hydrogenation reaction device and method |
| CN113368698A (en) * | 2021-08-16 | 2021-09-10 | 山东浦创流体技术有限公司 | Silicon carbide ceramic membrane filter equipment |
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