CN101678299A

CN101678299A - Hydrogen-oxygen blender-distributor

Info

Publication number: CN101678299A
Application number: CN200780052095A
Authority: CN
Inventors: G·P·托勒; K·M·范登布谢
Original assignee: UOP LLC
Current assignee: Honeywell UOP LLC
Priority date: 2007-01-11
Filing date: 2007-01-11
Publication date: 2010-03-24
Also published as: EP2114558A1; KR20100014773A; WO2008085522A1; EP2114558A4; NO20092803L; JP2010515653A

Abstract

The present invention discloses a kind of equipment that is used to produce hydrogen peroxide.Described equipment is realized the large-scale production of hydrogen peroxide by the liquid that produces the carrying bubble cloud.For the bubble that is produced, it has small volume before producing hydrogen peroxide flowing through reaction bed.

Description

Hydrogen-oxygen blender-distributor

Technical field

The present invention relates to the production of hydrogen peroxide, and more particularly, the present invention relates to the large-scale production of hydrogen peroxide.

Background technology

At present, the method for the extensive plant-scale production hydrogen peroxide implemented of great majority is to make hydrogen and oxygen produce indirect reaction under the situation of use alkyl-anthraquinone (alkylanthraquinone) as work materials.In first catalytic hydrogenation step, the alkyl-anthraquinone that is dissolved in the working solution that comprises organic solvent (for example Di-Isobutyl methyl alcohol (di-isobutylcarbinol) and methyl naphthalene) is converted to the alkyl anthrahydroquinone.In independently autoxidation step, produce alkyl-anthraquinone once more and produced hydrogen peroxide thereby this compound that is reduced is oxidized.Subsequently, implement to separate, thereby produce the bussiness class product by water collection, refining and concentration operation.

Generally, this indirect formation H ₂O ₂Production decision increased complexity and needed higher installation cost and operating cost, in this scheme, support that body medium is reduced and oxidized subsequently.A noticeable shortcoming is: alkyl-anthraquinone has higher dissolubility at the water collection medium that is used for the separation of hydrogen peroxide product.This has aggravated the loss of working solution and has caused hydrogen peroxide product to be subjected to the pollution of organic substance, and when hydrogen peroxide was concentrated into the level that is suitable for transporting, this organic substance can produce reaction with this peroxide.Second problem relates to the dissolubility of water collection solution in the alkyl-anthraquinone working solution.Thereby, wet working solution is recycled to indirect oxidation during the stage when being separated from aqueous phase, the water " hole (aqueous phase " pockets ") " that is in the remnants in the organic solution provides such zone, and hydrogen peroxide product can be concentrated to the degree that becomes harmful in this zone.The 3rd problem relates to when a small amount of hydrogen peroxide of needs, how occurs under the situation of organic contamination in can not causing water soluble materials stream, and organic compound is used and reclaims.

Compare with the scheme of this alkyl-anthraquinone, flow the scheme of direct synthesize hydrogen peroxide by Gaseous Hydrogen supply material stream and gaseous state oxygen supply material and want much simple, much also economical.Although at US4, disclosed such technology in 832,938 B1 and other list of references, this commercialization attempts causing having occurred industrial accident, and this is because the intrinsic explosion hazard of this technology causes.That is, at normal temperatures and pressures, the explosive concentrations of the hydrogen in oxygen-hydrogen attitude mixture is 4.7-93.9%, and this percentage is percent by volume.As seen, this scope is an extremely wide scope.

By inert gas such as nitrogen etc. this gaseous mixture is diluted and can change the concentration limit of these two kinds of gases based on inert free gas hardly, this point also is known.In normal pressure range (0.1-20MPa) and range of temperature (0-100 ℃), explosive scope can change knownly hardly.In addition, even these reactants are placed in together to be in inflammability scope ratio in addition under homogeneous state, but set up this homogeneous process from pure component, still to temporarily pass through this inflammability scope at least inevitably.These reasons cause being not easy to reduce with hydrogen-oxygen directly contacting relevant risk of explosion.

In the field that hydrogen-oxygen directly contacts, some effort have been made so that in liquid phase, comprise their reaction.For example, US 5,925, and 588 B1 have disclosed following content: use to have adorned hydrophobicity/hydrophily and support the catalyst of body so that optimal performance under the aqueous solution liquid phase is provided.In addition, US 6,042, and 804 B1 have disclosed following content: the microbubble of hydrogen and oxygen is dispersed in the acidic aqueous solution liquid medium that flows fast that comprises catalyst.Yet regrettably: hydrogen reactant and oxygen reactant only slightly are dissolved in the disclosed reactant aqueous solution solvent of these lists of references.

Other list of references, promptly US 4,336, and 240 B1 and US 4,347,231 B1 have disclosed two-phase reaction system, and this system has the homogeneous catalyst in the organic facies of being dissolved in.As the ground of mentioning in the previous document of these two lists of references, there is the shortcoming that hinders its commercialization usually in the homogeneous catalyst system.Disadvantageous character comprises: the catalyst stability under the reaction condition is relatively poor, the dissolubility of catalyst in reaction medium is limited and the reactivity of production hydrogen peroxide is lower.What in addition, be positioned at two-phase liquid reaction system top comprises gaseous state H ₂/ O ₂Environment kept being dissolved in the equilibrium concentration of these reactants in the liquid phase.Therefore, this gaseous atmosphere that is positioned at the reaction liquid top must be in outside the flammability range, has therefore limited the scope of the potential reaction agent mol ratio in the liquid phase greatly.

There is two types the reactor of in water, making hydrogen peroxide at present.First kind is slurry reactor, and in this reactor, bubble and catalyst are dispersed in the mobile liquid phase.Although this is favourable for mixing and provides good heat transfer and the quality transmission that except catalyst recovery and method for recycling, this method also needs a large amount of expensive catalysts.Second reactor is a trickle bed reactor, and in this reactor, gas and liquid flow through on the packed bed of catalyst.The major defect of trickle bed reactor is: gas is continuous phase and channel size therefore need be less, and therefore needs the smaller particles size, can prevent that just hydrogen and oxygen from entering precarious position.

Provide a kind of device and technology of making a large amount of hydrogen peroxide based on needs, the while does not need too much chemical substance and guarantees the method that environment is safer, and can not produce waste product material stream, will be useful.

Summary of the invention

Method provided by the present invention has overcome the shortcoming of present hydrogen peroxide manufacture method, and this method is to produce a large amount of hydrogen and the carrier of oxygen mixture that exists with the decentralized photo that is scattered in the minute bubbles in the liquid.The invention provides a kind of equipment that produces the mixture of hydrogen and oxygen as micro-bubble.The present invention includes a pair of plate, many the littler passages that are used for carrying second gas that wherein first plate many littler passages that are used for carrying first gas that have the main channel and limit in described first plate, and second plate have the main channel and limit in described second plate.Described plate is when being stacked together, making described first gaseous matter stream and described second gaseous matter stream produce in the described littler passage of described second plate mixes, and at described littler passage place, described admixture of gas is discharged from as minute bubbles and enters in the liquid substance stream.

In another embodiment, described equipment comprises coldplate, and described coldplate also provides the liquid substance that is used to carry the described bubble that is discharged from described littler passage stream.The described coldplate and first gas distribution plate and second gas distribution plate stack together with the repetitive mode of first plate, second plate, coldplate.

In another embodiment, described equipment comprises the reactor that is used for being produced by liquid and the bubble that comprises hydrogen and oxygen hydrogen peroxide.This design makes the liquid of carrying bubble cloud flow through this reactor, and wherein said bubble cloud can't be agglomerated into bigger bubble at this reactor place, thereby has guaranteed the safe operation of this reactor.

One of ordinary skill in the art will should be readily appreciated that other purpose of the present invention, advantage and application by following specific embodiments and the drawings.Can obtain attached purpose of the present invention, embodiment and details by following specific embodiment of the present invention.

Description of drawings

Fig. 1 is the design of first plate of this blender;

Fig. 2 is the design of second plate of this blender;

Fig. 3 is the schematic diagram of first plate and second plate, and schematically shows the situation of this plate that flows through this blender;

Fig. 4 is the design of the coldplate of this blender;

Fig. 5 is the diagrammatic sketch of the distributor (sparger) that assembles, and gas and liquid flow in this distributor;

Fig. 6 A and Fig. 6 B are the designs of first plate with blender of loop configurations, and wherein Fig. 6 A is that top view and Fig. 6 B are cutaway views;

Fig. 7 A and Fig. 7 B are the designs of second plate with blender of loop configurations, and wherein Fig. 7 A is that top view and Fig. 7 B are cutaway views;

Fig. 8 is the schematic diagram of first plate and second plate, and schematically shows the situation of this plate that flows through this blender;

Fig. 9 A and Fig. 9 B are the designs of coldplate with blender of loop configurations, and wherein Fig. 9 A is that top view and Fig. 9 B are cutaway views;

Figure 10 is to use the design of radial reactor of the distributor designs of Fig. 5;

Figure 11 is used to produce the distributor of hydrogen peroxide and the schematic diagram at different levels of reactor;

Figure 12 is the schematic diagram at different levels that utilizes the hydrogen peroxide reactor of convection current; With

Figure 13 is the schematic diagram of the Mixed Design of hydrogen peroxide reactor.

The specific embodiment

Thereby the present invention includes and a kind ofly be used for making hydrogen and oxygen to mix on a large scale so that react producing hydrogen peroxide (H at water ₂O ₂) equipment.The problem that enlarges the hydrogen peroxide manufacture scale is: a large amount of hydrogen peroxide that produced will form the hydrogen of a large amount of volumes and the mixture of oxygen.This is a kind of situation that has potential danger.Therefore, desirable is to produce a large amount of hydrogen and oxygen that mix, but the decentralized photo that this hydrogen and oxygen is in be scattered in the minute bubbles in the water exists, thereby so that they are soluble in water rapidly and produce reaction and produce hydrogen peroxide.The present invention proposes a kind of new design that is suitable for the extensive blender that uses.

In one embodiment, described equipment comprises the array of plate, and wherein every block of plate has the passage that forms in described plate, and described plate is connected in together.The means that are used to form passage include, but not limited to etching, compacting, punching press and milling and are well-known in affiliated field.The means that are used for described plate is linked together are well-known in affiliated field, and include, but not limited to utilize the method for diffusion combination, soldering and welding.Described array preferably has paired plate, and wherein said plate carries out stacked with the order that replaces.As shown in Figure 1, first plate 10 in a pair of plate has first side, opposite side and the first, second, third and the 4th edge.Plate 10 has main channel 12, and described main channel has inlet 14 and is positioned at a plurality of outlets 16 on the side of plate 10.The main channel forms in plate by etching, compacting, punching press or milling mode, and this main channel is run-through board 10 not.First plate 10 further has many littler passages 18, and described many littler passages and this main channel 12 are positioned on the same side of plate 10, and wherein every littler passage 18 has the inlet that is communicated with corresponding outlet 16 fluids that come autonomous channel 12.This littler passage 18 has outlet 20 respectively, and described outlet extends through plate 10 to opposite side, thereby forms the otch array on the opposite side of this plate.In this particular example, this littler passage 18 does not extend to the edge of plate 10, and in other embodiments, this passage may extend to the edge of plate 10.

This embodiment further comprises second plate 30 in a pair of plate, and as shown in Figure 2, and this second plate has first side, opposite side and the first, second, third and the 4th edge.Plate 30 has main channel 32, and described main channel has inlet 34 and is positioned at a plurality of outlets 36 on the side of plate 30.The main channel forms in plate by etching, compacting, punching press or milling mode, and this main channel is run-through board 30 not.Second plate 30 further has many littler passages 38, and described many littler passages and this main channel 32 are positioned on the same side of plate 30, and wherein every littler passage 38 has the inlet that is communicated with corresponding outlet 36 fluids that come autonomous channel 32.This littler passage 38 has outlet 40 respectively, and described outlet is at edge's opening of second plate 30.As this main channel 32, this littler passage 38 does not extend through this plate 30 and arrives opposite side.

Two boards 10,30 has the

littler passage

18,38 of equal number respectively, and every passage 18 all has corresponding passage 38.When plate 10,30 when stacked, corresponding

littler passage

18,38 is aligned, thereby makes the outlet 20 of this littler passage 18 of this first plate be communicated with corresponding passage 38 fluids of second plate.The littler passage 18 of this first plate has outlet 20, and described outlet ends in the littler passage 38 of second plate.The part in outlet 20 downstreams of the littler passage 18 that is positioned at first plate of the littler passage 38 of second plate provides the zone that makes from the gas mixing of two passes 18,38.Second more the length of this part in the passage aisle 38 is selected so that realized that good gas mixed be discharged from the outlet 40 of more passage aisle of second plate at admixture of gas before for this.

When many to plate 10,30 by stacked and attached solid together the time, the embodiment that is produced will have rectangular prism shape, this shape has six limits, thereby has formed distributor.The inlet of the main channel 12 of first plate will be positioned on the limit, and the inlet of the main channel 32 of second plate will be positioned on second side relative with this first side, and the array of little outlet will be positioned on the 3rd side, and the array of this little outlet is the outlet 40 of the littler passage 38 of second plate.This make the gas that enters

main channel

12,32 can realize good mixing and as mixture from this more the outlet 40 of passage aisle be discharged from.Flow through this more under the situation of the outlet 40 of passage aisle at liquid, bubble cloud is carried in the liquid, thereby has improved the quality transmission so that admixture of gas is dissolved in the liquid.

Fig. 3 schematically shows the mixing of two kinds of gases realizing by the present invention.First gas flows in the main channel 12 of first plate, and is as shown in arrow 15.First gas is assigned with subsequently and flows in the secondary channel 18, and is as shown in arrow 17.First gas is discharged from the secondary channel 18 of first plate and flows in the secondary channel of second plate, and is as shown in arrow 19.Second gas flows in the main channel 32 of second plate, and is as shown in arrow 25.Second gas is assigned with subsequently and flows in the secondary channel 38, and is as shown in arrow 27.First gas in the secondary channel 38 of second gas and inflow second plate as shown in arrow 19 mixes.The mixture of first gas and second gas is discharged from the secondary channel 38 of second plate, and is as shown in arrow 29.

In the present embodiment,

main channel

12,32 is made into certain size and has the degree of depth of width and the about 0.5mm of about 50mm, thereby makes that area of section is 25mm ²Littler

passage

18,38 is made into certain size and has the degree of depth of width and the about 0.2mm of about 0.2mm, thereby makes that area of section is 0.04mm ²The area of section of the present invention by making the main channel with this more the ratio of the area of section sum of passage aisle reach at least three to one mode realize this gas from the main channel to this better distribution of passage aisle.In the present embodiment, present channel size makes that each main channel can be corresponding to the littler passage more than 200.Make this littler passage use less channel size can realize that the stratiform of gas mixes, and this mode also is proved to be a kind of mode that hydrogen is mixed with oxygen, and can not cause burning.

Although the particular design of the more passage aisle of

present embodiment

18,38 has the effective diameter of 200 microns (0.2mm), more the channel shape of

passage aisle

18,38 and design only are subject to the composition of the gas that will mix by this distributor for these.In hydrogen and example that oxygen mixes at once, this

littler passage

18,38 has 50 microns (0.05mm) to 300 microns (0.3mm) and preferably is no more than the effective diameter of 200 microns (0.2mm).

Thereby produce hydrogen peroxide although the purposes of this design of the present invention is to make hydrogen to mix with oxygen, the present invention is not limited to these gas, but on the contrary, can mix by any stratiform gas of the invention process.

In another embodiment, the present invention includes coldplate 50, as shown in Figure 4.This coldplate 50 is also with acting on the conduit that liquid component is provided, and the bubble that is discharged from outlet 40 can be carried in the described liquid component.Coldplate 50 is designed so that be stacked in first plate 10 and second plate 30 with alternating sequence, i.e. first plate 10, second plate 30, coldplate 50, first plate 10, second plate 30, coldplate 50 etc.

Coldplate 50 is designed to have the passage 52 of series of parallel.Passage 52 forms in this plate with etching, punching press, compacting, milling or alternate manner.Passage 52 has inlet 54 and outlet 56.When plate was stacked together, the outlet 40 of the outlet 56 of coldplate 50 and the more passage aisle of second plate was positioned on the same side of stacked structure.Fig. 5 shows the diagrammatic sketch of the distributor 62 that assembles, and there is shown

gas access

58,60 and gas vent 40, and liquid upwards flows through coldplate passage 52, wherein disperses alveolate fluid thereby produce.

Gas access

58,60 is with the corresponding

main channel inlet

14,34 of independent gas guiding plate 10,30.Coldplate 50 uses for the 3rd component, and in this particular instance, the 3rd component is a liquid.The liquid that can be used among the present invention comprises water, methyl alcohol, ethanol and composition thereof.Preferred liquid is water.Coldplate 50 can be designed (not shown) so that have littler passage, and described littler passage is used for by coming carrying the 3rd gaseous component with the cooling duct suitable manifold that 54 fluids are communicated with that enters the mouth.Can use a plurality of distributors 62 so that promote the generation of bubble with configuration in parallel or serial configured.

In the 3rd embodiment, sheetpile (stack) but is not provided with coldplate 50 still as mentioned above.This embodiment comprises and is used for the manifold (not shown) of liquid that the outlet 40 of distributor is passed in carrying.This manifold preferably guides fluid so that it flows through on the outlet side of distributor along the shorter direction of size.This manifold can be separated so that form independently passage, thereby fluid is prevented further also that separately the bubble of institute's carrying in the liquid phase from producing merging.

In annular embodiment, this equipment comprises the array of plate, and wherein every block of plate has loop configurations.For first embodiment, this array is with the stacked paired plate of alternating sequence.Fig. 6 A and Fig. 6 B show the top view and the cutaway view of first annular slab 70.Shown in Fig. 6 A and Fig. 6 B, first plate 70 of this pair of panel has top side, bottom side, inward flange and outward flange.Plate 70 has main channel 72, and described main channel has at least one inlet 74 on the outward flange that is positioned at this plate 70 and is positioned at a plurality of outlets 76 on the top side of plate 70.This first plate 70 further has many littler passages 78, and described many littler passages and main channel 72 are positioned on the same side of this plate 70, and wherein every littler passage 78 has the inlet that is communicated with corresponding outlet 76 fluids that come autonomous channel 72.This littler passage 78 has outlet 80 respectively, and described outlet extends through plate 70 and the bottom of arrival plate, thereby has formed the otch array on the bottom of plate 70.In the present embodiment, this littler passage 78 does not extend to the inward flange of plate 70.

This annular embodiment further comprises second plate 90 in the pair of panel, and shown in Fig. 7 A and Fig. 7 B, and described second plate has top side, bottom side, inward flange and outward flange.Fig. 7 A and Fig. 7 B show the top view and the cutaway view of second annular slab 90.Plate 90 has main channel 92, and this main channel has inlet 94 and is positioned at a plurality of outlets 96 on the side of plate 90.Second plate 90 further has many littler passages 98, and described many littler passages and main channel 92 are positioned on the same side of plate 90, and wherein every littler passage 98 has the inlet that is communicated with corresponding outlet 96 fluids that come autonomous channel 92.This littler passage 98 has outlet 100 respectively, and described outlet is at the inside edge opening of second plate 90.As the situation of main channel 92, this littler passage 98 does not extend through this plate 90 and arrives opposite side.The part of the littler passage 98 of second plate 90 provides such zone: the gas from

passage

78 and 98 mixed in this location before being discharged from outlet 100.

As the situation of first embodiment, this plate is handled by the mode of etching, punching press, milling, compacting, perhaps otherwise produces this plate by the known method in affiliated field.

In the present embodiment, sheetpile has formed tubular structure, and wherein liquid phase flows along the central area of this structure.Be discharged from that outlet 100 mist is dispersed in the liquid phase and along the length of this structure by carrying.When paired

plate

70,90 by stacked and attached solid together the time, the embodiment that is produced will have the helically coiled structure, thereby has formed the distributor with outer surface and inner surface.The inlet of the

main channel

72,92 of plate will be set on the outside, and little outlet array will be set on the inboard, the array of this little outlet is the outlet 100 of the more passage aisle 98 of second plate.The channel flow that liquid forms along the inner surface by sheetpile.When liquid flow through the outlet 100 of passage aisle more, bubble cloud was carried in this liquid, thereby has improved the transmission of quality so that admixture of gas is dissolved in the liquid.

Fig. 8 shows the situation that two kinds of gases mix by the present invention.First gas flows in the main channel 72 of first plate, shown in arrow 73.First gas flows in the secondary channel 78 of first plate, shown in arrow 75 subsequently.First gas is discharged from the bottom of first plate by the outlet shown in Fig. 6 B 80, and flows in the secondary channel 98 of second plate, shown in arrow 77.Second gas flows in the main channel 92 of second plate, shown in arrow 93.Second gas flows in the secondary channel 98 subsequently, shown in arrow 95.Second gas mixes the secondary channel 98 of second plate with first gas that flows out from first plate 70 shown in arrow 77.The mixture of first gas and second gas is discharged from the secondary channel 98 of second plate, shown in arrow 97.

In another embodiment, the present invention further comprises annular coldplate 110, and shown in Fig. 9 A and Fig. 9 B, this annular coldplate also provides the conduit that is used for liquid phase so that carrying is discharged from the admixture of gas of outlet 100 as bubble.Fig. 9 A and Fig. 9 B show the top view and the cutaway view of coldplate 110.Coldplate 110 comprises the main channel 112 that is used for liquid.Coldplate 110 further comprises at least one inlet 114 and a plurality of outlet 116.Coldplate 110 further comprises many littler distribution passages 118, and wherein every littler passage 118 has corresponding to the inlet of main channel outlet 116 and has outlet 119.Coldplate 110 has inward flange and outward flange, and exports 119 and be positioned in around the inward flange so that the liquid of passage aisle 118 distributes to being discharged from more.

When plate 70,90,110 stacked together with alternating sequence, present embodiment had formed the tubular structure (not shown) with inner catheter, was provided with the stratification of alternately the arranging outlet that is used for admixture of gas and liquid along this tubular structure.

In another embodiment, this equipment further comprises reaction bed.This equipment comprises the conduit of the liquid aliment that is used for this gas distributor of carrying process, and wherein this liquid is communicated with the outlet fluid of distributor.This liquid the liquid of bubble cloud through having become carrying after the outlet of distributor.The reaction bed (not shown) has the inlet that is communicated with the liquid fluid that is loaded with bubble cloud and has outlet.

In an embodiment of distributor of the present invention-combination of reactors device, a plurality of distributors 62 as shown in Figure 5 are disposed in around the helically coiled reactor core body 120 in the mode of array, as shown in figure 10, thereby have formed distributor-reactor unit 128.In the present embodiment, the array of the channel outlet 40 of distributor 62 is small enough to as the effective silk screen that catalyst is remained on the appropriate position.For distributor 62, then used optional silk screen (not shown) with bigger channel outlet 40.Distributor-reactor unit 128 comprises the inside silk screen 122 on the inner surface that is positioned at reactor core body 120.Silk screen 122 is separated reactor core body 120 and collection space 124, and wherein collection space 124 is the spaces that limited by the inwall 126 in inner silk screen 122 and the reactor.Silk screen 122 also provides the means that are used for the particle of reactor is remained on the appropriate position.Inwall 126 is that the pipeline by inside reactor provides, and this pipeline is made into certain size so that pressure falls minimizes, and collects the liquid that comprises hydrogen peroxide simultaneously.Can omit this pipeline alternatively, and the space that will be limited by inner silk screen 122 is as this inner space 124.This reactor is arranged provides a plurality of advantages.Radial reactor has overcome the pressure relevant with the trickle bed reactor with low particle size and has fallen restriction.The low particle size of trickle bed reactor is very necessary for preventing the atmospheric space that is used for the hydrogen-oxygen mixture.The radial reactor design makes and is easier to change reaction bed 120.The liquid that the design of distributor 62 minute bubbles with carrying enters in the reaction bed 120 rapid the distribution, and gas can not be agglomerated into bigger bubble.And distributor-reactor unit 128 is easy to manufactured and is assembled into module, thereby is convenient to the expansion scale, so that cover the flow velocity of relative broad range.

This reaction bed comprises the catalyst that is used for being formed by hydrogen and oxygen hydrogen peroxide.This catalyst comprises and is deposited at least a catalytic metal component that supports on the body that wherein this catalytic metal component is selected from the cohort that comprises platinum (Pt), palladium (Pd), ruthenium (Ru), rhodium (Rh), iridium (Ir), osmium (Os) and gold (Au).This catalyst preferably includes the mixture of two kinds of metals.In one embodiment, this catalyst comprises and is positioned at least a metal that is selected from above-mentioned substance that supports on the body.This supports the body material is to make catalyst can deposit superincumbent any inert material, and includes, but not limited to silica, aluminium oxide, titanium oxide, zirconia, carbon, carborundum, silica-alumina, diatomite, clay and molecular sieve.This support body preferably porous material so that provide bigger surface area for reaction.

Alternatively, distributor and reactor can be made into the unit, wherein utilize a plurality of this unit to produce hydrogen peroxide.

In an embodiment of hydrogen peroxide reactor, this equipment comprises at least two distributor-reactor grades, as shown in figure 11.Distributor-reactor unit 128 has liquid supplying apparatus 130, hydrogen feeding mechanism 58 and oxygen feeding mechanism 60.Hydrogen and oxygen arrive the distributor in the unit 128 and are dispersed in the liquid and flow through reaction bed in this unit 128.Distributor-reactor unit 128 has product outlet 132, and described product outlet comprises the liquid substance stream that remaining bubble in carrying.This product material flows to into gas-fluid separation applications unit 134, collects the gas of any remnants and this gas and liquid are separated in this unit.This liquid substance that comprises some hydrogen peroxide flows the distributor-reactor unit 128 that further is supplied to subsequently.The gas of any remnants is discharged from, or is directed to the other parts of this facility, and can be used for realizing burning or other purpose.Alternatively, gas-fluid separation applications unit 134 comprises the gas access that is communicated with plenum zone territory fluid.This makes can add gas so that the hydrogen-oxygen mixture that will be discharged from is diluted.Diluent gas can be inert gas such as nitrogen.Use advantage at different levels to be to make and in liquid, to produce the hydrogen peroxide of high concentration, and need not in any reactor, to provide higher gas liquid ratio.This helps producing the gas that is present in as bubble cloud in the liquid, has prevented to occur bigger gas volume by restriction bubble coalescent simultaneously.The volume ratio that flows to the oxygen of each reactor grade and hydrogen is preferably 1 or be stoichiometric proportion.

In another optional embodiment of hydrogen peroxide reactor, this equipment comprises at least two distributor-reactor grades that have flow reactor design, as shown in figure 12.In this convection current design, last reactor unit 128a has from the liquid of previous reactor unit/gas-liquid separator and supplies with material stream 136, and hydrogen 58 and oxygen 60 are supplied to distributor under the situation with higher oxygen hydrogen volume ratio.Product material stream separates in gas-liquid separator 134, and in this gas-liquid separator, oxygen rich gas is drawn towards the distributor that is used for last reactor 128b.Last reactor 128b further receives from the liquid of the reactor 128c of front more and supplies with material stream, hydrogen 58 and the oxygen of the oxygen rich gas material stream 138 that comes to flow out since subsequent reaction device 128a.This process back repeats towards first reactor 128.This convection current design makes the higher oxygen hydrogen volume ratio that can realize the oxygen that exists with gas phase and hydrogen at last reactor grade place.Be in the feasible selectivity of having improved hydrogen peroxide of operation under the excessive situation of oxygen concentration in last level.By this process, the oxygen hydrogen volume of gaseous state is than along with this process increases to the propelling of subsequent reaction device from a reactor.For last reactor, desirable is to make the oxygen hydrogen volume than between 2 and 10, and for first reactor, and desirable is that to make oxygen hydrogen volume ratio be 1.This makes has realized higher total OTR, has kept such advantage simultaneously: promptly, make the gas-liquid volume ratio that can keep lower in each reactor grade and keep higher oxygen concentration in the level of back.

In another embodiment (not shown) of reactor, this reactor has the convection current design type of simplification.This design is known as false to flow reactor design.The flow process of this design is identical in conjunction with the described flow process of Figure 11 with top face, but the volume ratio of oxygen hydrogen fluid changes in 1 to 20 scope, and this ratio increases to the ratio between 1 and 20 at last level place from 1 of first reactor.Final ratio is preferably between 2 and 4.

In another optional embodiment, this reacting appliance has flow process as shown in figure 13.Except having increased the recycle substance stream that is used for liquid phase, this stream is with top to combine the described stream of Figure 11 similar.Arrive the inlet of last reactor grade 128a by pump 140 from the part recirculation of the product liquid material of last reactor 128a stream.The use of recycle substance stream only should be used under such situation: promptly the ratio of the oxygen hydrogen volume for last reactor 128a is greater than 2.As the modification of this embodiment, recycle substance stream can be directed to the inlet of the reactor that is positioned at last reactor 128a upstream, but this reactor should be one in a plurality of reactors of the most approaching last reactor 128a.

An embodiment (not shown) also makes the removable reactor grade that passes through of catalyst.The selection of catalysts that is used to produce hydrogen peroxide has been proved to be along with the inactivation of catalyst and has increased.Because desirable is to have higher selectivity in the reactor of back, therefore providing and making catalyst is favourable from the reactor design that reactor unit 128 moves to subsequent reaction device unit 128, and new catalyst is added in first reactor unit 128.A kind of method that designs this reactor is that reactor unit 128 is stacked in together, thereby makes the reactor unit 128 of winning be positioned at the top, and subsequently the level be stacked in below.Catalyst is added in the top unit subsequently, and the catalyst in the reactor will migrate downward into subsequently unit, and catalyst is withdrawn from from last reactor unit and is separated.

Embodiments of the invention make the volume flow rate ratio can utilize lower gas and liquid, and this makes it possible to form stable bubble cloud in liquid phase, and embodiments of the invention make the hydrogen peroxide that can produce high concentration.In addition, use the reactor unit of series connection to make and to control service condition to a greater extent and to make the selectivity that can improve hydrogen peroxide manufacture.

Although invention has been described in conjunction with being considered to preferred embodiment at present above, but be appreciated that the present invention is not limited to disclosed embodiment, and be intended to cover multiple modification and equivalent arrangements in the scope that is included in appended claims.

Claims

1, a kind of equipment that is used for mixing two gas, described equipment comprises:

At least one first plate (10), wherein said first plate limits the first gas main channel (14), the described first gas main channel has inlet (14) and a plurality of outlet (16), and described first plate limits many first gas secondary channels (18), and wherein every first gas secondary channel has inlet and the first gas secondary channel outlet (20) that is communicated with corresponding first gas main channel outlet fluid; With

At least one second plate (30), wherein said second plate limits the second gas main channel (32), the described second gas main channel has inlet (34) and a plurality of outlet (36), and described second plate limits many second gas secondary channels (38), and wherein every second gas secondary channel has inlet and the second gas secondary channel outlet (40) that is communicated with corresponding second gas main channel outlet fluid;

Wherein every first gas secondary channel outlet (20) exports (40) fluid with the second gas secondary channel and is communicated with, and wherein said first plate (10) and second plate (20) with the order that replaces by stacked and be held togather so that form gas distributor (62) with first gas access, second gas access and mixed gas outlet.

2, equipment according to claim 1, further comprise manifold, described manifold has a plurality of inlets that are communicated with described secondary channel outlet (40) fluid, be used to permit at least one inlet that the 3rd component enters and be used to discharge described first gas, at least one outlet of the mixture of described second gas and described the 3rd component, wherein said manifold comprises the plate that limits many passages, wherein at least one outlet in every passage and the described first gas secondary channel outlet (40) and in the secondary outlet of described second gas (40) at least one export fluid and are communicated with, and described every passage has at least one inlet that is used for described the 3rd component and is used to discharge described first gas, at least one outlet of the mixture of described second gas and described the 3rd component.

3, equipment according to claim 1 and 2, further comprise coldplate (50), wherein said coldplate (50) comprises many passages (52), and every passage (52) has inlet (54) and outlet (56), and described cooling duct outlet (56) is communicated with described second gas secondary channel outlet (40) fluid.

4, according to each described equipment in the claim 1,2 or 3, be further characterized in that, the outlet of the described first gas secondary channel (18) ends in the described second gas secondary channel (38), and the part in the outlet downstream that is positioned at the described first gas secondary channel (18) of the wherein said second gas secondary channel (38) comprises that effective diameter is less than 300 microns mixing portion.

5, according to each described equipment in the claim 1 to 4, further comprise:

The liquid supplying duct, described liquid supplying duct has the inlet that is used for the liquid aliment, and described inlet is communicated with described gas distributor (62) fluid, and described liquid supplying duct has the outlet that is used for liquid, and bubble cloud in described liquid carrying; With

Reaction bed, described reaction bed have inlet that is communicated with described liquid supplying duct outlet fluid and the outlet that forms reactor-distributor unit.

6, equipment according to claim 5, wherein said reaction bed comprises catalyst, described catalyst comprises and is deposited at least a catalytic metal component that supports on the body, wherein this catalytic metal component is selected from and comprises platinum (Pt), palladium (Pd), ruthenium (Ru), rhodium (Rh), iridium (Ir), osmium (Os), the cohort of gold (Au) and composition thereof, and the wherein said body that supports comprises such material, and described material is selected from and comprises silica, aluminium oxide, titanium oxide, zirconia, carbon, carborundum, silica-alumina, diatomite, clay, the cohort of molecular sieve and composition thereof.

7, according to each described equipment in the claim 1 to 6, further comprise reaction bed, wherein said reaction bed comprises:

Have the annular reaction bed (120) of cylinder form substantially, described annular reaction bed accessory has inner surface and outer surface;

Catalyst keeps silk screen (122); With

Product conduit (124);

Wherein said distributor (62) is set on the surface in inner surface or the outer surface, described catalyst keeps silk screen (122) to be set on another surface in described inner surface or the outer surface, and described product conduit is communicated with surfactant fluid by described maintenance silk screen limited boundary.

8, equipment according to claim 7, wherein said reaction bed comprises and is positioned at the load supported catalyst, wherein said catalyst comprises at least a metal, described metal is selected from the cohort that comprises platinum (Pt), palladium (Pd), ruthenium (Ru), rhodium (Rh), iridium (Ir), osmium (Os), gold (Au) and composition thereof, and the wherein said body that supports comprises such material, and described material is selected from the cohort that comprises silica, aluminium oxide, titanium oxide, zirconia, carbon, carborundum, silica-alumina, diatomite, clay, molecular sieve and composition thereof.

9, according to each described equipment in the claim 1 to 4, wherein said first plate (10) and described second plate (30) limit the passage with rectangle plane configuration.

10, according to each described equipment in the claim 1 to 4, wherein said first plate (70) and described second plate (90) limit has the radially passage of configuration.