CN107098317A - The system and method for process for prepairng hydrogen peroxide by anthraquinone - Google Patents
The system and method for process for prepairng hydrogen peroxide by anthraquinone Download PDFInfo
- Publication number
- CN107098317A CN107098317A CN201710451706.3A CN201710451706A CN107098317A CN 107098317 A CN107098317 A CN 107098317A CN 201710451706 A CN201710451706 A CN 201710451706A CN 107098317 A CN107098317 A CN 107098317A
- Authority
- CN
- China
- Prior art keywords
- hydrogenation
- outlet
- hydrogenation reaction
- working solution
- catalyst
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B15/00—Peroxides; Peroxyhydrates; Peroxyacids or salts thereof; Superoxides; Ozonides
- C01B15/01—Hydrogen peroxide
- C01B15/022—Preparation from organic compounds
- C01B15/023—Preparation from organic compounds by the alkyl-anthraquinone process
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Abstract
The present invention relates to a kind of system and method for process for prepairng hydrogen peroxide by anthraquinone, the bottom of working liquid tank is by working liquid pump and working solution supply pipe is connected with the entrance of hydrogenation apparatus, the outlet of hydrogenation apparatus is connected with hydrogenation flow container, the bottom for hydrogenating flow container is connected by hydrogenating liquid pump, hydrogenation flow container efferent duct, hydrogenation liquid filter and hydride cooler with the entrance of oxidizing tower, and the outlet of oxidizing tower is connected with oxidation solution efferent duct；The outlet of hydrogenation reaction cauldron is connected with catalyst filter, and the outlet of each catalyst filter is connected with hydride outlet pipe and hydriding reactor working solution recoil tube respectively；Each catalyst filter bottom is connected with working solution supply pipe, and working solution supply pipe inserts the inner chamber of hydrogenation reaction cauldron from middle part；Catalyst adding tube is plugged with the top of hydrogenation reaction cauldron, hydrogen feed pipe extends downward into the bottom of hydrogenation reaction cauldron and turn extends upwardly to the lower central of hydrogenation reaction cauldron.The system can be produced continuously, and unit consumption of product is low, and production efficiency is high.
Description
Technical field
The present invention relates to a kind of system of process for prepairng hydrogen peroxide by anthraquinone, the invention further relates to a kind of anthraquinone production peroxide
Change hydrogen methods, belong to hydrogen peroxide manufacturing technology field.
Background technology
Hydrogen peroxide is a kind of important Inorganic Chemicals, be widely used in papermaking, weaving, medicine, chemical industry, electronics,
The fields such as environmental protection.Hydrogen peroxide produces water and oxygen after decomposing, and does not have secondary pollution to environment, meets the reason of green product production
Read.
In the prior art, hydrogen peroxide is generally produced by anthraquinone, anthraquinone is the palladium using 2- EAQs as carrier
For catalyst, hydrogen peroxide is directly combined to by hydrogen and oxygen, successively will be through processes such as over hydrogenation, oxidation, extraction and post processings.
Wherein hydrogenation is general is carried out in fixed bed, anthraquinone working solution in the presence of certain pressure, temperature and palladium catalyst, with
Hydrogenation occurs for hydrogen, produces hydrogen anthraquinone.The anthraquinone low production efficiency of fixed bed, unit scale are less than normal, product production
Raw material and power unit consumption are high, equipment is heavy, floor space is big, and manufacturing cost is high.
Hydrogen anthraquinone liquid is commonly called as hydride, after filtering and cooling, is admitted to oxidizing tower oxidation.Traditional oxidizing tower is sky
Chamber tower body, hydride and air enter in oxidizing tower from bottom simultaneously, stir while up, air bubble is than larger, hydrogen
The contact area for changing liquid and air is small, and oxidation efficiency will generally set and be saved in oxidation in section tower, oxidation under tower and oxidation than relatively low
Save tower to carry out after repeatedly aoxidizing, extraction process could be entered.Equipment investment is big, and oxidation efficiency is low.
The content of the invention
The primary and foremost purpose of the present invention is that overcoming problems of the prior art, there is provided a kind of anthraquinone production peroxide
Change the system of hydrogen, continuous production can be achieved in facility compact, and the production consumption of unit product is low, and production efficiency is high, manufacturing cost
It is low.
To solve above technical problem, a kind of system of process for prepairng hydrogen peroxide by anthraquinone of the invention, including working liquid tank,
Hydrogenation apparatus, hydrogenation flow container and oxidizing tower, the bottom of the working liquid tank are connected with the entrance for the liquid pump that works, the work
The outlet of liquid pump is connected by working solution supply pipe with the entrance of the hydrogenation apparatus, the outlet of the hydrogenation apparatus
It is connected by hydride outlet pipe with the hydrogenation flow container, the bottom of the hydrogenation flow container is connected with hydrogenating the entrance of liquid pump, institute
The outlet of hydrogenation liquid pump is stated by hydrogenating entering for flow container efferent duct, hydrogenation liquid filter and hydride cooler and the oxidizing tower
Mouth is connected, and the outlet of the oxidizing tower is connected with oxidation solution efferent duct, and the hydrogenation apparatus includes hydrogenation reaction cauldron, described
Hydride outlet is uniformly provided with the lower circumference of hydrogenation reaction cauldron, each hydride outlet is respectively with being looped around hydrogenation
The hydride loop pipe of kettle periphery is connected, and the hydride loop pipe is connected with catalyst filter general import pipe, the catalyst mistake
Filter inlet valve of the filter general import pipe respectively with each catalyst filter inlet is connected；Pacify respectively the outlet of each catalyst filter
Equipped with triple valve, the first outlet of the triple valve is connected with hydride outlet pipe, the second outlet of the triple valve and hydrogenation
Kettle working solution recoil tube is connected；Agitating shaft is provided with along the center line of the hydrogenation reaction cauldron, the agitating shaft is provided with agitating paddle
Leaf；The bottom of each catalyst filter is separately installed with catalyst filter flow reversal valve, the outlet of each catalyst filter flow reversal valve
It is connected respectively with catalyst filter flow reversal house steward, the lower end of the catalyst filter flow reversal house steward is connected with working solution supply pipe,
The working solution supply pipe is inserted the inner chamber of hydrogenation reaction cauldron from the middle part of the hydrogenation reaction cauldron short transverse and is bent downwardly
Extend to the axis of the hydrogenation reaction cauldron；The top of the hydrogenation reaction cauldron is provided with hydriding reactor gaseous phase outlet and is plugged with respectively
The catalyst adding tube and hydrogen feed pipe extended straight down, the upper end of the catalyst adding tube valve and catalyst are added by catalyst
The outlet connection of tank is added, inwall of the hydrogen feed pipe along hydrogenation reaction cauldron extends to bottom and the turn of hydrogenation reaction cauldron
Extend upwardly to the lower central of the hydrogenation reaction cauldron.
Relative to prior art, the present invention achieves following beneficial effect：Working solution in working liquid tank is by work liquid pump
Conveyed by working solution supply pipe to hydrogenation apparatus, the hydride of hydrogenation apparatus production is entered by hydride outlet pipe
Enter to hydrogenate flow container to keep in, hydrogenation flow container efferent duct be then pumped into by hydride, the removal of impurity is gone in first hydrogenated liquid filter filtering,
The temperature of hydride is reduced to less than 40 DEG C by hydride cooler, and feeding oxidizing tower is aoxidized, and the oxidized liquid of oxidation solution is defeated
Outlet pipe is exported.When hydrogenation apparatus produces hydride, open catalyst addition valve and appropriate catalyst is put into hydrogenation reaction cauldron, together
Shi Xinxian working solution enters the center of hydrogenation reaction cauldron liquid Space from working solution supply pipe and sprayed downwards, in stirrer paddle
Agitation under spread to surrounding downwards；Fresh hydrogen sprays upwards from the lower port of hydrogen feed pipe, in the agitation of stirrer paddle
Under be separated into multiple minute bubbles and spread upward all round, the opposite convection current of fresh working solution and hydrogen enables both rapid
Mix and react；Anthraquinone in working solution generates hydrogen anthraquinone, nitrogen and residue in the presence of powdered palladium catalyst with hydrogen reaction
Unreacted hydrogen is discharged from the hydriding reactor gaseous phase outlet at the top of hydrogenation reaction cauldron.Uniformly set in the lower circumference of hydrogenation reaction cauldron
Put hydride outlet and import hydride loop pipe, be conducive to hydride uniformly to be flowed out in whole circumference.Most of catalyst mistakes
Filter is normal all in working condition, and now triple valve is in first outlet conducting, second outlet closed mode, catalyst filter
After catalyst is retained, the hydride of cleaning flows out into hydride outlet pipe from the first outlet of triple valve；When catalyst filtering
When excessive catalyst is accumulated on the filter core of device, on the one hand cause the filter capacity of catalyst filter to decline, on the other hand can reduce
The concentration of catalyst in hydrogenation reaction cauldron, influences the progress of hydrogenation, and triple valve now is switched into first outlet closing, second
Conducting state is exported, while the hydride opened in catalyst filter flow reversal valve, hydriding reactor working solution recoil tube enters the catalyst
Filter, the catalyst for being deposited in cartridge surface is rushed, and is entered through catalyst filter flow reversal valve and catalyst filter flow reversal house steward
Working solution supply pipe, follows fresh working solution to return in hydrogenation reaction cauldron, and all catalyst are recycled.Set multiple
Catalyst filter, is easy to carry out the recoil of catalyst in turn, it is ensured that fluid bed being capable of continuous and stable production；Such as fluid bed is in work
When, keep a catalyst filter to be in recoil state, remaining catalyst filter is in working condition, can both improve production
Efficiency, improves the yield of hydrogen anthraquinone, can ensure the filter efficiency of each catalyst filter again, it is ensured that catalyst in hydrogenation reaction cauldron
Concentration, makes fluid bed all the time in stable working condition.By the commutation of triple valve, the switching of normal work and recoil is very
It is convenient and swift.The system hydrogenation of the present invention is rapid, and the catalyst concentration in hydrogenation reaction cauldron is stable, being capable of steady and continuous output
The hydride of high-quality, and hydrogen unit consumption is low, hydrogenation efficiency is high.
As the improvement of the present invention, the top of the agitating shaft is set with center sleeve, the upper end of the center sleeve with
The inwall closing connection of the hydrogenation reaction cauldron, the lower end of the center sleeve is inserted into the liquid Space of hydrogenation reaction cauldron；
The hydriding reactor gaseous phase outlet is connected with the air inlet of reactor condenser, and the exhaust outlet of the reactor condenser passes through tail gas
Exhaust-control valve is connected with tail gas blow-down pipe, and the leakage fluid dram of the reactor condenser passes through condensate liquid return duct and the center
The top of sleeve pipe is connected.Center sleeve and permeability cell lead to condensate liquid to the gas-phase space formation fluid-tight at the top of hydrogenation reaction cauldron
Road keeps apart with the gas-phase space at the top of hydrogenation reaction cauldron, and the condensate liquid for entering center sleeve is delivered into reactor liquid phase
The central area in space.The reacted kettle condenser condensation of the non-incoagulable gas such as the solvent vapo(u)r discharged from hydriding reactor gaseous phase outlet
Turn into liquid again afterwards, center sleeve is flowed back to from condensate liquid return duct, continue to participate in the reaction of hydrogenation reaction cauldron, be conducive to reducing
Material loss；Exhaust Emission Control valve can control the discharge capacity of tail gas and adjust the pressure in hydrogenation reaction cauldron, center sleeve
Fluid-tight effect gas at the top of hydrogenation reaction cauldron can be avoided to enter condensate liquid return duct, condensate liquid is from the lower end of center sleeve
The central area of reactor liquid Space is directly reached after outflow, it is mixed with fresh working solution rapidly under the agitation of stirrer paddle
Amount to being spread to surrounding downwards, with the upward uniform hybrid reaction of hydrogen.
As a further improvement on the present invention, along the inwall of the hydrogenation reaction cauldron liquid Space at least provided with vertical together
Baffle plate, the diameter extension of the cross section of the vertical baffle plate along hydrogenation reaction cauldron.The rotation of stirrer paddle, can drive working solution to revolve
Turn, circulation is formed in hydrogenation reaction cauldron inner chamber, stable circulation causes the material of the material and circulation internal layer of circulation outer layer to be difficult to
Mixing；Vertical baffle plate is radially inserted in circulation layer, is conducive to thoroughly destroying circulation layer so that working solution can be rapid with hydrogen
Hydrogenation occurs for uniform mixing.
As a further improvement on the present invention, the lower end of the catalyst filter flow reversal house steward is connected to the big of taper
Hold circumference on, taper be sleeved on the periphery of the working solution supply pipe and with working solution supply pipe coaxial line, taper
Big end seal close, the small end of taper towards hydrogenation reaction cauldron and it is relative with working solution supply pipe connect, the working solution supply
The part that pipe is located in taper is provided with the aditus laryngis of reduced diameter, and the aditus laryngis stretches to the small end of taper.Catalyst
The catalyst that filter recoil is reclaimed enters in taper from catalyst filter flow reversal house steward, and fresh working solution is supplied in working solution
Pipe high speed flow forward, flow velocity is accelerated at aditus laryngis, pressure reduction, and suction work is played to entering the catalyst in taper
With catalyst is able to be uniformly dispersed rapidly in fresh working solution, it is to avoid catalyst conglomeration enters hydrogenation reaction cauldron.
As a further improvement on the present invention, the bottom of the hydrogenation reaction cauldron is provided with the ring with hydrogenation reaction cauldron coaxial line
Shape set, the inwall of the circumference of the annular sleeve and the hydrogenation reaction cauldron is spaced a distance, and each hydride outlet is located at
On the hydrogenation reaction cauldron circumference contour with annular sleeve axial direction middle part；The bottom of the agitating shaft is provided with lower stirring paddle
Leaf, the lower stirring paddle leaf is located in the annular sleeve, and the middle part of the agitating shaft is provided with upper stirrer paddle；The working solution is supplied
Outlet to pipe is positioned at the top of the upper stirrer paddle；The outlet of the hydrogen feed pipe is located in the annular sleeve lower port
The lower section of the heart.Annular sleeve is blocked to the formation of each hydride outlet, fresh hydrogen after the discharge of the port of hydrogen feed pipe, first to
The center of upper entrance annular sleeve, the lower stirring paddle leaf rotated smashes and is separated into multiple bubbles into the circulation in annular sleeve
In, annular sleeve prevents hydrogen gas bubbles from choking from hydride outlet；Fresh working solution flows out against upper stirrer paddle from top to bottom,
It is scattered to surrounding on one side downwards on one side under the rotational agitation of upper stirrer paddle, be conducive to the hydrogen gas bubbles with rising uniformly to mix
Close, hydrogenation occurs rapidly, annular sleeve can equally avoid the fresh working solution having just enter into from directly choking from hydride outlet；
The working solution sprayed downwards is flowed up again after being mixed with the hydrogen gas bubbles of lower section so that most fresh working solution first with hydrogen
Concentration highest region is contacted, and is conducive to improving hydrogenation efficiency.
As a further improvement on the present invention, the top center of the oxidizing tower is provided with oxidizing tower gaseous phase outlet, the oxygen
The upper portion side wall for changing tower is connected with oxidizing tower hydride entrance, and the oxidizing tower hydride entrance is located on the liquid level line of oxidizing tower
Side, the bottom of the oxidizing tower is provided with air distribution device, the air distribution device and the total air of oxidizing tower on oxidizing tower
Entrance is connected, and the bottom centre of the oxidizing tower exports provided with oxidizing tower；It is horizontal provided with multiple tracks along oxidizing tower short transverse
Tower tray is aoxidized, the oxidation tower tray of adjacent layer mutually staggers make the runner of working solution S-shaped in the horizontal direction.Compressed air is by bottom
Air distribution device be distributed into numerous bubbles, flow from bottom to top；Hydrogen anthraquinone liquid enters from the oxidizing tower hydride entrance on top
Enter in oxidizing tower, fall first on the oxidation tower tray of top layer, it is then S-shaped successively to flow downward, hydrogen anthraquinone liquid while to flow down
Dynamic, while occurring oxidation reaction generation hydrogen peroxide with the oxygen in bubble, counter-current flow, working solution is presented with air in working solution
Contact is most ozone when flowing to oxidation tower bottom, to ensure that oxidation reaction is properly completed, then from the oxygen of bottom
Change tower outlet outflow.The oxidation tower tray of adjacent layer mutually staggers in the horizontal direction makes working solution flow downward while in level
Direction, which is formed, repeatedly turns back, and extends the flow distance of working solution, also extends the time of contact of working solution and oxygen, be conducive to
Hydrogen anthraquinone liquid turns into hydrogen peroxide by exhaustive oxidation.Oxidizing tower hydride entrance can prevent oxidation solution above liquid level line and choke
Enter in hydrogen anthraquinone liquid pipe road, it is to avoid upper track formation is polluted.
As a further improvement on the present invention, each oxidation tower tray is circular in unfilled corner, the middle part of each oxidation tower tray
For oxide regions, the oxide regions are uniformly densely covered with multiple oxidation tower tray air-vents, the both sides edge phase of the oxide regions
Mutually parallel, the side of the oxide regions is the descending liquid region of hollow out, and the opposite side of the oxide regions is to be made up of closed plate
Liquid receiving area domain, the oxide regions are connected with the periphery in liquid receiving area domain with the inwall of oxidizing tower；Adjacent layer descending liquid region
Phase differ 180 °；The oxidation tower tray edge adjacent with descending liquid region is connected with vertical baffle plate, the vertical baffle plate
Upper limb is parallel and higher than oxidation tower tray, and the lower edge of the vertical baffle plate is crossed oxidation tower tray and extended downwardly.The working solution on upper strata is first
First fall in the liquid receiving area domain being made up of closed plate, then level flows to oxide regions；During air flows upwards, minute bubbles are easy
Mutually collide, assemble, being bonded into larger bubble, when air pocket is reached below the oxide regions of oxidation tower tray, being oxidized tower
Disk air-vent is divided into numerous minute bubbles again, considerably increases the specific surface area of bubble, during the oxidized region for the treatment of fluid flow,
It is in contact with countless minute bubbles, contact area is big, good mixing.Air pocket is oxidized tower tray again for several times in uphill process
Tiny bubble is divided into, oxidation efficiency is substantially increased, as long as an oxidizing tower can be properly completed the oxidation of hydrogen anthraquinone liquid,
Reduce equipment investment and production cost.Working solution can just flow downward in the oxidation excessively vertical baffle plate of tower tray overflow, extend
Working solution is conducive to being substantially oxidized in the residence time of oxide regions；Simultaneously the lower edge of vertical baffle plate extend downwardly one section away from
From the air chamber of lower ending opening being collectively forming with oxidation tower tray and oxidizing tower barrel, by air seal below oxidation tower tray, it is to avoid
Air flows directly up from descending liquid region, forces air across each oxidation tower tray air-vent and flows up, completes by force to big
The cutting of bubble.
As a further improvement on the present invention, the inner chamber of the oxidizing tower is provided with inlet bend and the oxidizing tower hydride
Entrance is connected, and the lower end outlet of the inlet bend is below the liquid level line of oxidizing tower and close to the inwall of oxidizing tower, top layer
The liquid receiving area domain for aoxidizing tower tray is located at the underface of the inlet bend.The lower end outlet of inlet bend is located at below liquid level line,
Fluid-tight is formed, hydrogen anthraquinone liquid flows downward, and fall in top layer after the lower end outlet outflow of inlet bend along the inwall of oxidizing tower
The liquid receiving area domain of tower tray is aoxidized, then advection to oxide regions are aoxidized, it is ensured that all hydrogen anthraquinone liquid completely flow through
Oxidized region, makes oxidation more thorough.
As a further improvement on the present invention, oxidizing tower capturing device, each layer are installed at the oxidizing tower gaseous phase outlet
Aoxidize tower tray is respectively arranged below with spiral condenser, and the outer wall of the oxidizing tower is wound with multigroup semicanal condenser, each institute
Semicanal condenser is stated respectively to be located between adjacent two layers oxidation tower tray, and using the flow direction of low in and high out.Oxidizing tower capturing device
Foam can be caught, it is to avoid drop flies out from oxidizing tower gaseous phase outlet；Because the oxidation reaction of hydrogen anthraquinone liquid is exothermic reaction,
Each layer oxidation tower tray is respectively arranged below spiral condenser, and working solution can be cooled down in time；Half and half pipework condensation device
Oxidizing tower can paragraph by paragraph be cooled down, make the uniform temperature fields of whole oxidizing tower.
It is another object of the present invention to overcome problems of the prior art anthraquinone to be produced there is provided one kind
The method of hydrogen oxide, can be achieved continuous production, and the production consumption of unit product is low, and production efficiency is high, and manufacturing cost is low.
To solve above technical problem, the method for present invention production hydrogen peroxide, it is characterised in that successively including following step
Suddenly, hydrogenation solvent is (1) configured；(2) hydrogenation is constituted after 2- EAQs and 2- amyl anthraquinones are added into above solvent
Working solution, wherein adding 2- EAQs in every liter of solvent（80~110）2- amyl anthraquinones are added in g/L, every liter of solvent（60
~140）G/L, working solution is placed in working liquid tank；(3) prepare powdered palladium catalyst to be placed in catalyst addition tank；(4) will be appropriate
Catalyst puts into hydrogenation reaction cauldron, while fresh working solution enters the center of hydrogenation reaction cauldron liquid Space and sprayed downwards,
Spread under the agitation of stirrer paddle to surrounding downwards；Fresh hydrogen sprays upwards from the lower port of hydrogen feed pipe, in agitating paddle
Multiple minute bubbles are separated under the agitation of leaf to spread upward all round, are sufficiently mixed and are stirred with fresh working solution；(5) work
Anthraquinone in liquid generates hydrogen anthraquinone in the presence of powdered palladium catalyst with hydrogen reaction；(6) the gaseous substance on hydrogenation reaction cauldron top
Discharge and condensed from hydriding reactor gaseous phase outlet, incoagulable gas includes unreacted hydrogen and discharged from tail gas blow-down pipe, cold
Lime set is returned in center sleeve；(7) hydride flows out into each catalyst together with powder catalyst from hydrogenation reaction cauldron lower circumference
Filter is filtered；The hydride of cleaning enters hydrogenation flow container；(8) the hydride in hydrogenation flow container is pumped out by hydride, through removing
After impurity and cooling, feeding oxidizing tower is aoxidized, the oxidized liquid efferent duct output of obtained oxidation solution；(9) in turn to each catalyst
Filter is recoiled, and the catalyst for being deposited in cartridge surface is rushed, supplied through catalyst filter flow reversal house steward into working solution
Pipe, follows fresh working solution to return in hydrogenation reaction cauldron；The percent by volume of step (1) middle hydrogenation solvent formula one is：Two
Isobutyl carbinol（45~50）V%, C10 aromatic hydrocarbons（50~55）V%, both volume summations are 100%；(1) middle hydrogenation is molten for step
The percent by volume of agent prescription two is：Tetrabutyl urea（12~30）V%, trioctyl phosphate（8~12）V%, C10 aromatic hydrocarbons：（60~
76）V%, the volume summation of three is 100%.
Relative to prior art, the present invention achieves following beneficial effect：Fresh working solution is evenly distributed on hydrogenation
On the lower circumference of reactor, and spray downwards；Hydrogen is divided into numerous tiny bubble hydrogens by densely covered hydrogen dispensing orifice, increases
The big contact area of hydrogen and working solution, and most fresh working solution contacts with density of hydrogen highest region first, favorably
In hydrogenation occurs rapidly, hydrogenation efficiency is improved.After catalyst flows out with hydride, retained by catalyst filter, by turn
Recoil returns to hydrogenation reaction cauldron, by the lasting Rational flow of catalyst, both ensure that the filter efficiency of catalyst filter, and had kept again
Catalyst concentration in hydrogenation reaction cauldron.The catalyst and hydrogen that the present invention is used are able to whole recyclings, advantageously reduce list
The production consumption of position product, improves hydrogenation efficiency, reduces production cost.
C10 aromatic hydrocarbons in hydrogenation solvent formula one is used to dissolve 2- EAQs and 2- amyl anthraquinones, diisobutyl
Methanol increases the solubility of 2- EAQs and 2- amyl anthraquinones.
C10 aromatic hydrocarbons in hydrogenation solvent formula two mainly dissolves 2- EAQs, 2- amyl anthraquinones and reaction and produced
Tetrahydrochysene 2- EAQs, and the 2- ethyl hydrogen anthraquinones and tetrahydrochysene 2- ethyl hydrogen anthraquinones that generate after hydrogenation can not be dissolved；Therefore also
The trioctyl phosphate and tetrabutyl urea that can dissolve 2- ethyl hydrogen anthraquinones and tetrahydrochysene 2- EAQs are needed as polar solvent.This hair
It is bright that there is higher C10 arene contents, working solution proportion can be avoided to increase, extraction tower operating difficulties is caused；Trioctyl phosphate
Have the advantages that high boiling point, non-stimulated taste, dissolved hydrogen anthraquinone ability are strong, but if too high levels, working solution can be caused to glue
Degree increase, causes mass transfer difficult；Tetrabutyl urea is transparent or slightly yellowish liquid, and viscosity is slightly bigger than water, has and water
The advantages of density contrast is big, surface tension is big, relative to trioctyl phosphate to the molten of 2- ethyl hydrogen anthraquinones and tetrahydrochysene 2- EAQs
Solution degree is big, and distribution coefficient of the hydrogen peroxide in two-phase is big.Solvent composition combination and ratio using the present invention so that working solution
With volatilization loss it is small, using safety, favourable operating environment, reduction raffinate hydrogen peroxide content, improve the excellent of extract concentration
Point, due to being reduced with the stock solubility of water so that the TOC of dioxygen aquatic products（Total organic carbon）Content is greatly reduced, and is conducive to
The lifting of product quality.
Brief description of the drawings
The present invention is further detailed explanation with reference to the accompanying drawings and detailed description, accompanying drawing only provide with reference to
Illustrate to use, be not used to the limitation present invention.
Fig. 1 is the flow chart of the system of process for prepairng hydrogen peroxide by anthraquinone of the present invention.
Fig. 2 is the structural representation of hydrogenation reaction cauldron in Fig. 1.
Fig. 3 is the top view of hydride outlet and hydride loop pipe in Fig. 2.
Fig. 4 is catalyst filter flow reversal house steward and the schematic diagram of second of connection scheme of working solution supply pipe.
Fig. 5 is the front view of oxidizing tower in Fig. 1.
Fig. 6 is the top view of odd-level oxidation tower tray in Fig. 5.
Fig. 7 is the top view of even level oxidation tower tray in Fig. 5.
Fig. 8 is the structural representation of spiral condenser in Fig. 5.
Fig. 9 is the structural representation of air distribution device in Fig. 5.
Figure 10 is the schematic cross-section of the hollow gas branch pipes of Fig. 9.
In figure：1. hydrogenation reaction cauldron；1a. hydriding reactor gaseous phase outlets；1b. hydride outlets；1c. center sleeves；1d. is vertical
Baffle plate；1e. annular sleeves；1f. agitating shafts；1g. stirrer paddles；1h. hydride loop pipes；2. catalyst adds tank；3. reactor is cold
Condenser；4. catalyst filter；5. oxidizing tower；5a. oxidizing tower gaseous phase outlets；5b. oxidizing tower hydride entrances；5c. oxidizing towers are total
Air intake；5d. oxidizing towers are exported；5e. oxidizing tower capturing devices；5f. inlet bends；5g. aoxidizes tower tray；5g1. zoneofoxidation
Domain；5g2. liquid receiving areas domain；5g3. descending liquids region；5. aoxidize tower tray air-vent；The vertical baffle plates of 5h.；5j. spiral condensers；5k.
Semicanal condenser；5m. air distribution devices；5m1. air mains；5m2. air branch pipes；5m3. air dispensing orifices；V1. catalyst adds
Plus valve；V2. triple valve；V3. filter inlet valve；V4. catalyst filter flow reversal valve；V5. Exhaust Emission Control valve；T1. work
Flow container；T2. flow container is hydrogenated；L1. liquid filter is hydrogenated；C1. hydride cooler；B1. work liquid pump；B2. liquid pump is hydrogenated；G1.
Working solution supply pipe；G1a. taper；G2. hydrogen feed pipe；G3. catalyst adding tube；G4. tail gas blow-down pipe；G5. condensate liquid
Return duct；G6. catalyst filter general import pipe；G7. hydride outlet pipe；G8. hydriding reactor working solution recoil tube；G9. catalyst mistake
Filter return header；G10. flow container efferent duct is hydrogenated；G11. compressed air hose；G12. oxidation solution efferent duct.
Embodiment
As shown in Figure 1 and Figure 2, the system of process for prepairng hydrogen peroxide by anthraquinone of the present invention includes working liquid tank T1, hydrogenation dress
Put, hydrogenate flow container T2 and oxidizing tower 5, working liquid tank T1 bottom is connected with the entrance for the liquid pump B1 that works, and work liquid pump B1's goes out
Mouth is connected by working solution supply pipe G1 with the entrance of hydrogenation apparatus, and the outlet of hydrogenation apparatus passes through hydride outlet
Pipe G7 is connected with hydrogenation flow container T2, and hydrogenation flow container T2 bottom is connected with hydrogenating liquid pump B2 entrance, hydrogenation liquid pump B2 outlet
It is connected by hydrogenating flow container efferent duct G10, hydrogenation liquid filter L1 and hydride cooler C1 with the entrance of oxidizing tower 5, is aoxidized
The outlet of tower 5 is connected with oxidation solution efferent duct G12.
Working solution in working liquid tank T1 is conveyed from work liquid pump B1 by working solution supply pipe G1 to hydrogenation apparatus,
The hydride of hydrogenation apparatus production enters hydrogenation flow container T2 by hydride outlet pipe G7 and kept in, then by hydrogenation liquid pump B2
The removal of impurity is gone in feeding hydrogenation flow container efferent duct G10, first hydrogenated liquid filter L1 filterings, and filtering accuracy is 1 μ, hydride cooling
The temperature of hydride is reduced to less than 40 DEG C by device C1, and feeding oxidizing tower 5 row oxidation, the oxidized liquid efferent duct G12 of oxidation solution is defeated
Go out.
As shown in Fig. 2 hydrogenation apparatus includes being uniformly provided with hydrogenation reaction cauldron 1, the lower circumference of hydrogenation reaction cauldron 1
Hydride outlet 1b, each hydride outlet 1b are connected with being looped around the hydride loop pipe 1h of hydrogenation reaction cauldron periphery respectively, hydrogen
Change liquid loop pipe 1h be connected with catalyst filter general import pipe G6, catalyst filter general import pipe G6 respectively with each catalyst filter
The filter inlet valve V3 of 4 entrances is connected；The outlet of each catalyst filter 4 is separately installed with triple valve V2, the of triple valve V2
One outlet is connected with hydride outlet pipe G7, and triple valve V2 second outlet is connected with hydriding reactor working solution recoil tube G8；Along hydrogen
The center line for changing reactor 1 is provided with agitating shaft 1f, and agitating shaft 1f is provided with stirrer paddle 1g；The bottom of each catalyst filter 4 point
Be not provided with catalyst filter flow reversal valve V4, each catalyst filter flow reversal valve V4 outlet respectively with catalyst filter flow reversal house steward
G9 is connected, and catalyst filter flow reversal house steward G9 lower end is connected with working solution supply pipe G1, and working solution supply pipe G1 is anti-from hydrogenation
The middle part of kettle short transverse is answered to insert the inner chamber of hydrogenation reaction cauldron 1 and be bent downwardly the axis for extending to hydrogenation reaction cauldron 1；Hydrogenation
The top of reactor 1 is provided with hydriding reactor gaseous phase outlet 1a and is plugged with the catalyst adding tube G3 and hydrogen extended straight down respectively
Supply pipe G2, catalyst adding tube G3 upper end are connected by the outlet that catalyst adds valve V1 with catalyst adds tank 2, hydrogen feed pipe
Inwalls of the G2 along hydrogenation reaction cauldron 1 extends to the bottom of hydrogenation reaction cauldron 1 and turn extends upwardly to the bottom of hydrogenation reaction cauldron 1
Center.
Open catalyst addition valve V1 and appropriate catalyst is put into hydrogenation reaction cauldron 1, while fresh working solution is from working solution
Supply pipe G1 enters the center of hydrogenation reaction cauldron liquid Space and sprayed downwards, downwards to surrounding under stirrer paddle 1g agitation
Diffusion；Fresh hydrogen sprays upwards from hydrogen feed pipe G2 lower port, is separated under stirrer paddle 1g agitation multiple small
Bubble spreads upward all round, and the opposite convection current of fresh working solution with hydrogen enables both to mix and react rapidly；Work
Make the anthraquinone in liquid in the presence of powdered palladium catalyst with hydrogen reaction generation hydrogen anthraquinone, nitrogen and remaining unreacted hydrogen from
Hydriding reactor gaseous phase outlet 1a discharges at the top of hydrogenation reaction cauldron.Hydride is uniformly arranged in the lower circumference of hydrogenation reaction cauldron 1 to go out
Mouth 1b simultaneously imports hydride loop pipe 1h, is conducive to hydride uniformly to be flowed out in whole circumference.
Most of catalyst filters 4 are normal all in working condition, and now triple valve V2 is in first outlet conducting, second
Port closing state, after catalyst filter 4 retains catalyst, the hydride of cleaning is gone forward side by side from triple valve V2 first outlet outflow
Enter hydride outlet pipe G7；When accumulating excessive catalyst on the filter core of catalyst filter 4, on the one hand cause catalyst filter 4
Filter capacity decline, on the other hand can reduce the concentration of catalyst in hydrogenation reaction cauldron 1, influence the progress of hydrogenation, now
Triple valve V2 is switched into first outlet closing, second outlet conducting state, while catalyst filter flow reversal valve V4 is opened, hydrogenation
Hydride in kettle working solution recoil tube G8 enters the catalyst filter, the catalyst for being deposited in cartridge surface is rushed, through catalyst
Filter flow reversal valve V4 and catalyst filter flow reversal house steward G9 enters working solution supply pipe G1, follows fresh working solution to return to hydrogenation
In reactor 1, all catalyst are recycled.
Multiple catalyst filters are set, are easy to carry out the recoil of catalyst in turn, it is ensured that fluid bed being capable of continuous and stable production；
For example fluid bed operationally, keeps a catalyst filter to be in recoil state, and remaining catalyst filter is in work shape
State, can both improve production efficiency, improve the yield of hydrogen anthraquinone, can ensure the filter efficiency of each catalyst filter again, it is ensured that
The concentration of catalyst in hydrogenation reaction cauldron 1, makes fluid bed all the time in stable working condition.
Agitating shaft 1f top is set with center sleeve 1c, and center sleeve 1c upper end is sealed with the inwall of hydrogenation reaction cauldron 1
Connection is closed, center sleeve 1c lower end is inserted into the liquid Space of hydrogenation reaction cauldron 1.
Hydriding reactor gaseous phase outlet 1a is connected with the air inlet of reactor condenser 3, and the exhaust outlet of reactor condenser 3 passes through
Exhaust Emission Control valve V5 is connected with tail gas blow-down pipe G4, the leakage fluid dram of reactor condenser 3 by condensate liquid return duct G5 with
Center sleeve 1c top is connected.It is cold from reacted kettles of non-incoagulable gas such as the hydriding reactor gaseous phase outlet 1a solvent vapo(u)rs discharged
Condenser 3 turns into liquid again after condensing, and center sleeve 1c is flowed back to from condensate liquid return duct G5, continues to participate in hydrogenation reaction cauldron 1
Reaction, is conducive to reducing material loss；Exhaust Emission Control valve V5 can control the discharge capacity of tail gas and adjust hydrogenation reaction cauldron 1
Interior pressure；Center sleeve 1c and permeability cell to the gas-phase space formation fluid-tight at the top of hydrogenation reaction cauldron, by condensate liquid passage with
Gas-phase space at the top of hydrogenation reaction cauldron is kept apart, and the gas at the top of hydrogenation reaction cauldron can be avoided to enter condensate liquid return duct
G5, condensate liquid directly reaches the central area of reactor liquid Space after center sleeve 1c lower end outflow, in stirrer paddle
Mix rapidly and spread jointly to surrounding downwards with fresh working solution under 1g agitation, with the upward uniform hybrid reaction of hydrogen.
Along the inwall of hydrogenation reaction cauldron liquid Space at least provided with vertical baffle plate 1d, vertical baffle plate 1d cross section edge together
The diameter extension of hydrogenation reaction cauldron 1.Stirrer paddle 1g rotation, can drive working solution to rotate, and be formed in hydrogenation reaction cauldron inner chamber
Circulation, stable circulation causes the material of circulation outer layer to be difficult to mix with the material of circulation internal layer；Vertical baffle plate 1d is radially inserted
Enter in circulation layer, be conducive to thoroughly destroying circulation layer so that working solution can uniformly mix rapidly generation hydrogenation with hydrogen.
Catalyst filter flow reversal house steward G9 lower end is connected with backflow pipe bend, the lower end insertion working solution of backflow pipe bend
In supply pipe G1, the outlet of backflow pipe bend is positioned at working solution supply pipe G1 center and in the same direction with the flow direction of working solution.
Catalyst from catalyst filter flow reversal house steward G9 that each catalyst filter recoil is reclaimed backflow pipe bend are directly injected into working solution
Supply pipe G1 center, the catalyst for making backflow rapidly using the jet action of fresh working solution spreads rapidly in fresh working solution
Open, play mixed uniformly effect, it is to avoid catalyst conglomeration enters hydrogenation reaction cauldron 1.
As shown in figure 3, another scheme is：Catalyst filter flow reversal house steward G9 lower end is connected to taper G1a's
On big end circumference, taper G1a be sleeved on working solution supply pipe G1 periphery and with working solution supply pipe G1 coaxial lines, taper
Sleeve pipe G1a big end seal is closed, taper G1a small end towards hydrogenation reaction cauldron 1 and it is relative with working solution supply pipe G1 connect, work
Make the aditus laryngis that parts of the liquid supply pipe G1 in taper G1a is provided with reduced diameter, aditus laryngis stretches to taper G1a
Small end.The catalyst that the recoil of catalyst filter is reclaimed enters in taper G1a from catalyst filter flow reversal house steward G9, fresh work
Make liquid in working solution supply pipe G1 high speed flow forwards, flow velocity is accelerated at aditus laryngis, pressure reduction, to entering taper
Catalyst in G1a plays swabbing action, and catalyst is able to be uniformly dispersed rapidly in fresh working solution, it is to avoid catalyst conglomeration enters hydrogen
Change reactor 1.
The bottom of hydrogenation reaction cauldron 1 is provided with the annular sleeve 1e with hydrogenation reaction cauldron coaxial line, annular sleeve 1e circumference and hydrogen
The inwall for changing reactor 1 is spaced a distance, and each hydride outlet 1b is located at hydrogenation reaction cauldron 1, and axially middle part is contour with annular sleeve
Circumference on；Agitating shaft 1f bottom is provided with lower stirring paddle leaf, and lower stirring paddle leaf is located in annular sleeve 1e, agitating shaft 1f middle part
Provided with upper stirrer paddle；Working solution supply pipe G1 outlet is positioned at the top of upper stirrer paddle；Hydrogen feed pipe G2 outlet position
Lower section in annular sleeve lower port center.
Annular sleeve 1e is blocked to each hydride outlet 1b formation, after fresh hydrogen is discharged from hydrogen feed pipe G2 port,
Annular sleeve 1e center is upwardly into first, and the lower stirring paddle leaf rotated smashes and is separated into multiple bubbles into annular sleeve 1e
In interior circulation, annular sleeve 1e prevents hydrogen gas bubbles from choking from hydride outlet 1b；Fresh working solution is from top to bottom against upper
Stirrer paddle flows out, under the rotational agitation of upper stirrer paddle, on one side downwards while, the hydrogen that is conducive to and rises scattered to surrounding
Gas bubble is uniformly mixed, and occurs hydrogenation rapidly, annular sleeve 1e can equally avoid the fresh working solution that has just enter into directly from
Hydride outlet 1b chokes；The working solution sprayed downwards is flowed up again after being mixed with the hydrogen gas bubbles of lower section so that most fresh
Working solution contacted first with density of hydrogen highest region, be conducive to improve hydrogenation efficiency.
As Fig. 5 shows, the top center of oxidizing tower 5 is provided with oxidizing tower gaseous phase outlet 5a, and the upper portion side wall of oxidizing tower 5 is connected with
Oxidizing tower hydride entrance 5b, oxidizing tower hydride entrance 5b are located above the liquid level line of oxidizing tower 5, and the bottom of oxidizing tower 5 is set
There are air distribution device 5m, air distribution device 5m to be connected with the total air intake 5c of the oxidizing tower on oxidizing tower 5, oxidizing tower is always empty
Gas entrance 5c is connected with compressed air hose G11.The bottom centre of oxidizing tower 5 exports 5d provided with oxidizing tower；Oxidizing tower export 5d with
The G12 connections of oxidation solution efferent duct.
Along the short transverse of oxidizing tower 5 provided with the horizontal oxidation tower tray 5g of multiple tracks, the oxidation tower tray 5g of adjacent layer is in level
Direction, which is mutually staggered, makes the runner of working solution S-shaped.
Compressed air is distributed into numerous bubbles by the air distribution device 5m of bottom, flows from bottom to top；Hydrogen anthraquinone liquid from
The oxidizing tower hydride entrance 5b on top enter oxidizing tower 5 in, fall first on the oxidation tower tray 5g of top layer, then it is S-shaped by
Sulfate layer flows downhill is moved, and hydrogen anthraquinone liquid is while flow downward, while occurring oxidation reaction generation hydrogen peroxide, work with the oxygen in bubble
Make liquid and air and be presented counter-current flow, it is most ozone that working solution, which flows to contacted during oxidation tower bottom, to ensure oxygen
Change reaction to be properly completed, then from the oxidizing tower outlet 5d outflows of bottom.The oxidation tower tray 5g of adjacent layer is mutual in the horizontal direction
Stagger working solution is flowed downward while in the horizontal direction formed repeatedly turn back, extend the flow distance of working solution,
The time of contact of working solution and oxygen is extended, is conducive to hydrogen anthraquinone liquid to turn into hydrogen peroxide by exhaustive oxidation.Oxidizing tower is hydrogenated
Liquid entrance 5b, which is located above liquid level line, can prevent oxidation solution and choke in hydrogen anthraquinone liquid pipe road, it is to avoid upper track formation is polluted.
As shown in Figure 6, Figure 7, each oxidation tower tray 5g is circular in unfilled corner, and each oxidation tower tray 5g middle part is oxide regions 5g1,
Oxide regions 5g1 is uniformly densely covered with multiple oxidation tower tray air-vents 5, and oxide regions 5g1 both sides edge is parallel to each other, zoneofoxidation
Domain 5g1 side is the descending liquid region 5g3 of hollow out, and oxide regions 5g1 opposite side is the liquid receiving area domain being made up of closed plate
Inwall of 5g2, oxide regions 5g1 and liquid receiving area domain the 5g2 periphery with oxidizing tower 5 is connected；The phase in adjacent layer descending liquid region
180 ° of position difference.The working solution on upper strata falls in the liquid receiving area domain 5g2 being made up of closed plate first, and then level is to oxide regions
5g1 flows；During air flows upwards, minute bubbles are easily mutually collided, assembled, being bonded into larger bubble, when air pocket is reached
When aoxidizing below tower tray 5g oxide regions 5g1, it is oxidized tower tray air-vent 5 and is divided into numerous minute bubbles again, increase
The specific surface area of bubble is added, during the oxidized region 5g1 for the treatment of fluid flow, has been in contact, contact area is big, mixes with countless minute bubbles
Close good.Air pocket is oxidized tower tray 5g and is divided into tiny bubble again for several times in uphill process, substantially increases oxidation
Efficiency, as long as an oxidizing tower can be properly completed the oxidation of hydrogen anthraquinone liquid, reduces equipment investment and production cost.
Edge adjacent with descending liquid region 5g3 oxidation tower tray 5g is connected with vertical baffle plate 5h, and vertical baffle plate 5h upper limb is put down
Go and the lower edge higher than oxidation tower tray 5g, vertical baffle plate 5h is crossed oxidation tower tray 5g and extended downwardly.Working solution is in oxidation tower tray 5g
Overflow, which flows through vertical baffle plate 5h, can just flow downward, and extend residence time of the working solution in oxide regions 5g1, be conducive to being filled
Divide oxidation；Vertical baffle plate 5h lower edge extends downwardly a segment distance simultaneously, is collectively forming with oxidation tower tray 5g and oxidizing tower barrel
The air chamber of lower ending opening, by air seal below oxidation tower tray 5g, it is to avoid air flows directly up from descending liquid region 5g3,
Force air across each oxidation tower tray air-vent 5 to flow up, the cutting to air pocket is completed by force.
The inner chamber of oxidizing tower is connected provided with inlet bend 5f with oxidizing tower hydride entrance 5b, is brought out under inlet bend 5f
Mouth is located at below the liquid level line of oxidizing tower 5 and close to the inwall of oxidizing tower 5, and top layer oxidation tower tray 5g liquid receiving area domain 5g2 is located at
Inlet bend 5f underface.Inlet bend 5f lower end outlet is located at below liquid level line, forms fluid-tight, hydrogen anthraquinone liquid is from entrance
After bend pipe 5f lower end outlet outflow, flowed downward along the inwall of oxidizing tower 5, and fall to aoxidize tower tray 5g liquid receiving area domain in top layer
5g2, then advection aoxidized to oxide regions 5g1, it is ensured that all hydrogen anthraquinone liquid completely flow through oxidized region
5g1, makes oxidation more thorough.
The aperture for aoxidizing tower tray air-vent 5 is the centre-to-centre spacing between 3~6mm, adjacent oxidation tower tray air-vent 5 for 35~
40mm.Make bubble that there is very big specific surface area, and each oxidation tower tray air-vent 5, the mixing with working solution can be passed through
Fully.
Oxidizing tower capturing device 5e is installed at oxidizing tower gaseous phase outlet 5a.Oxidizing tower capturing device 5e can catch bubble
Foam, it is to avoid drop flies out from oxidizing tower gaseous phase outlet 5a.
As shown in Figure 9, Figure 10, air distribution device 5m includes the air main being connected with the total air intake 5c of oxidizing tower
5m1, air main 5m1 along oxidizing tower diameter extension, along air main 5m1 length direction be connected to many perpendicular to
Air main 5m1 air branch pipe 5m2, each air branch pipe 5m2 is parallel to each other, uniform intervals and in the approximately the same plane, empty
Gas main 5m1 and each air branch pipe 5m2 top are uniformly densely covered with least two air-discharging dispensing orifice 5m3 respectively.Air enters first
Enter air main 5m1, be then divided into multiple tributaries and respectively enter each air branch pipe 5m2, then by the air dispensing orifice of multiple rows of multiple row
5m3 is divided into tiny air bubble, and air dispensing orifice 5m3 aperture is 3~6mm so that the diameter very little of each air bubble, is increased
The big specific surface area of air, expands the contact surface of air and working solution, is conducive to improving oxidation efficiency.
As shown in Figure 5, Figure 8, each layer oxidation tower tray 5g is respectively arranged below with spiral condenser 5j.Due to hydrogen anthraquinone liquid
Oxidation reaction be exothermic reaction, be respectively arranged below spiral condenser 5j what each layer aoxidized tower tray 5g, can be right in time
Working solution is cooled down.
The outer wall of oxidizing tower 5 is wound with multigroup semicanal condenser 5k, and half and half pipework condensation device 5k is located at adjacent two layers oxygen respectively
Between change tower tray 5g, and using the flow direction of low in and high out.Half and half pipework condensation device 5k can paragraph by paragraph be cooled down to oxidizing tower 5, be made
The uniform temperature fields of whole oxidizing tower.
The method of present invention production hydrogen peroxide, in turn includes the following steps, (1) configures hydrogenation solvent；(2) to the above
The working solution that hydrogenation is constituted after 2- EAQs and 2- amyl anthraquinones is added in solvent, wherein adding 2- second in every liter of solvent
Base anthraquinone（80~110）2- amyl anthraquinones are added in g/L, every liter of solvent（60~140）G/L, working liquid tank is placed in by working solution
In T1；(3) prepare powdered palladium catalyst to be placed in catalyst addition tank 2, the particle diameter volume distributed median of palladium catalyst is：Particle diameter is more than 120 microns
Percent by volume be no more than 4%；The percent by volume that particle diameter is less than 80 microns is no more than 4%, and remaining particle diameter is 80~120 micro-
Rice；(4) open catalyst addition valve V1 and appropriate catalyst is put into hydrogenation reaction cauldron 1, while fresh working solution is supplied from working solution
Pipe G1 enters the center of hydrogenation reaction cauldron liquid Space and sprayed downwards, expands under stirrer paddle 1g agitation to surrounding downwards
Dissipate；Fresh hydrogen sprays upwards from hydrogen feed pipe G2 lower port, is separated under stirrer paddle 1g agitation multiple stingy
Bubble spreads upward all round, is sufficiently mixed and stirs with fresh working solution；(5) the anthraquinone in working solution is in powdered palladium catalyst
Effect is lower and hydrogen reaction generates hydrogen anthraquinone；(6) the gaseous substance on hydrogenation reaction cauldron top is discharged simultaneously from hydriding reactor gaseous phase outlet 1a
Condensed into reactor condenser 3, incoagulable gas includes unreacted hydrogen and discharged from tail gas blow-down pipe G4, and condensate liquid is returned to
In center sleeve；(7) hydride enters from each hydride outlet 1b in hydrogenation reaction cauldron lower circumference together with powder catalyst and hydrogenated
Liquid loop pipe 1h, then filtered through catalyst filter general import pipe G6 into each catalyst filter 4；Triple valve V2 is switched to first
Outlet conducting, second outlet closed mode, after catalyst filter 4 retains catalyst, the hydride of cleaning from triple valve V2 the
One outlet outflow simultaneously enters hydrogenation flow container T2 by hydride outlet pipe G7；(8) the hydride in hydrogenation flow container T2 is by hydrogenation liquid pump
B2 feeding hydrogenation flow container efferent duct G10, then hydrogenated liquid filter L1 filterings are gone after the removal of impurity and hydride cooler C1 coolings,
Feeding oxidizing tower 5 is aoxidized, the oxidized liquid efferent duct G12 outputs of obtained oxidation solution；(9) each catalyst filter 4 is entered in turn
Row recoil, first outlet closing, second outlet conducting state are switched to during recoil by triple valve V2, while opening catalyst filter
Hydride in return valve V4, hydriding reactor working solution recoil tube G8 enters the catalyst filter, will be deposited in touching for cartridge surface
Matchmaker's punching falls, and enters working solution supply pipe G1 through catalyst filter flow reversal valve V4 and catalyst filter flow reversal house steward G9, follows fresh
Working solution is returned in hydrogenation reaction cauldron 1.
Oxygen content and the continuous monitoring of carbon monoxide content, wherein oxygen must be carried out to the hydrogen that hydrogen feed pipe G2 is provided
Volumn concentration have to be lower than 1%, higher than the level, then must bypass hydrogenation reaction cauldron 1.Hydrogen feed pipe G2 supplies hydrogen
In carbon monoxide content have to be lower than 1.0ppm, it is to avoid palladium catalyst poisoning.
Reaction temperature in hydrogenation reaction cauldron 1 is 50~65 DEG C, and the working solution residence time is 0.25~0.55 hour, hydrogenation
Pressure in reactor 1 is that the pressure of fresh hydrogen in 100~150KPa, hydrogen feed pipe G2 is 0.25~0.35MPa.
Step (1) in hydrogenation solvent can be configured by following percent by volume, diisobutyl carbinol (DIBC)：（45~50）
V%, C10 aromatic hydrocarbons：（50~55）V%, both volume summations are 100%.C10 aromatic hydrocarbons is used to dissolve 2- EAQs and 2- amyl groups
Anthraquinone, diisobutyl carbinol (DIBC) increases the solubility of 2- EAQs and 2- amyl anthraquinones.
Under the solvent formula, the hydrogenation efficiency that embodiment one~tetra- reaches is as shown in table 1：
Table 1
。
Step (1) in hydrogenation solvent can also be configured by following percent by volume, tetrabutyl urea：（12~30）V%,
Trioctyl phosphate：（8~12）V%, C10 aromatic hydrocarbons：（60~76）V%, the volume summation of three is 100%.C10 aromatic hydrocarbons mainly dissolves
The tetrahydrochysene 2- EAQs that 2- EAQs, 2- amyl anthraquinones and reaction are produced, and the 2- ethyls generated after hydrogenation can not be dissolved
Hydrogen anthraquinone and tetrahydrochysene 2- ethyl hydrogen anthraquinones；Therefore also need to that the tricresyl phosphate of 2- ethyl hydrogen anthraquinones and tetrahydrochysene 2- EAQs can be dissolved
Monooctyl ester and tetrabutyl urea are used as polar solvent.The present invention has higher C10 arene contents, and working solution proportion can be avoided to increase
Greatly, extraction tower operating difficulties is caused；Trioctyl phosphate has the advantages that high boiling point, non-stimulated taste, dissolved hydrogen anthraquinone ability are strong,
But if too high levels, work fluid viscosity can be caused to increase, cause mass transfer difficult；Tetrabutyl urea is transparent or slightly slightly yellow
Liquid, viscosity is slightly bigger than water, has the advantages that and water density difference is big, surface tension is big, relative to trioctyl phosphate to 2-
The solubility of ethyl hydrogen anthraquinone and tetrahydrochysene 2- EAQs is big, and distribution coefficient of the hydrogen peroxide in two-phase is big.Using the present invention
Solvent composition combination and ratio so that working solution have volatilization loss it is small, using safety, favourable operating environment, reduction raffinate
Liquid hydrogen peroxide content, the advantage for improving extract concentration, due to being reduced with the stock solubility of water so that dioxygen aquatic products
TOC（Total organic carbon）Content is greatly reduced, and is conducive to the lifting of product quality.
Under the solvent formula, the hydrogenation efficiency that embodiment five~eight reaches is as shown in table 2：
Table 2
。
It the foregoing is only the preferable possible embodiments of the present invention, non-therefore the limitation present invention patent protection model
Enclose.In addition to the implementation, the present invention can also have other embodiment, and the direction of such as left and right can be exchanged, all uses etc.
With the technical scheme replaced or equivalent transformation is formed, all fall within the protection domain of application claims.The present invention is without description
Technical characteristic can be realized by or using prior art, will not be repeated here.
Claims (10)
1. a kind of system of process for prepairng hydrogen peroxide by anthraquinone, including working liquid tank, hydrogenation apparatus, hydrogenation flow container and oxidation
Tower, the bottom of the working liquid tank is connected with the entrance for the liquid pump that works, and the outlet of the work liquid pump passes through working solution supply pipe
It is connected with the entrance of the hydrogenation apparatus, the outlet of the hydrogenation apparatus passes through hydride outlet pipe and the hydrogenation
Flow container is connected, and the bottom of the hydrogenation flow container is connected with hydrogenating the entrance of liquid pump, and the outlet of the hydrogenation liquid pump passes through hydride
Tank efferent duct, hydrogenation liquid filter and hydride cooler are connected with the entrance of the oxidizing tower, and the outlet of the oxidizing tower connects
It is connected to oxidation solution efferent duct, it is characterised in that：The hydrogenation apparatus is included under hydrogenation reaction cauldron, the hydrogenation reaction cauldron
It is uniformly provided with hydride outlet on portion's circumference, each hydride outlet is respectively with being looped around the hydride of hydrogenation reaction cauldron periphery
Loop pipe is connected, and the hydride loop pipe is connected with catalyst filter general import pipe, the catalyst filter general import pipe point
Filter inlet valve not with each catalyst filter inlet is connected；The outlet of each catalyst filter is separately installed with triple valve, institute
The first outlet for stating triple valve is connected with hydride outlet pipe, second outlet and the hydriding reactor working solution recoil tube of the triple valve
It is connected；Agitating shaft is provided with along the center line of the hydrogenation reaction cauldron, the agitating shaft is provided with stirrer paddle；Each catalyst filter
Bottom be separately installed with catalyst filter flow reversal valve, the outlet of each catalyst filter flow reversal valve respectively with catalyst filter
Return header is connected, and the lower end of the catalyst filter flow reversal house steward is connected with working solution supply pipe, the working solution supply pipe
Insert the inner chamber of hydrogenation reaction cauldron from the middle part of the hydrogenation reaction cauldron short transverse and be bent downwardly and extend to the hydrogenation instead
Answer the axis of kettle；The top of the hydrogenation reaction cauldron is provided with touching that hydriding reactor gaseous phase outlet and being plugged with respectively extends straight down
Matchmaker's adding tube and hydrogen feed pipe, the upper end of the catalyst adding tube outlet company that valve adds tank with catalyst is added by catalyst
Connect, inwall of the hydrogen feed pipe along hydrogenation reaction cauldron extends to the bottom of hydrogenation reaction cauldron and turn extend upwardly to it is described
The lower central of hydrogenation reaction cauldron.
2. the system of process for prepairng hydrogen peroxide by anthraquinone according to claim 1, it is characterised in that：The top of the agitating shaft
Center sleeve is set with, the upper end of the center sleeve is connected with the inwall closing of the hydrogenation reaction cauldron, the center sleeve
Lower end be inserted into the liquid Space of hydrogenation reaction cauldron；The air inlet phase of the hydriding reactor gaseous phase outlet and reactor condenser
Even, the exhaust outlet of the reactor condenser is connected by Exhaust Emission Control valve with tail gas blow-down pipe, the reactor condensation
The leakage fluid dram of device is connected by condensate liquid return duct with the top of the center sleeve.
3. the system of process for prepairng hydrogen peroxide by anthraquinone according to claim 1, it is characterised in that：Along the hydrogenation reaction cauldron
The inwall of liquid Space is at least provided with vertical baffle plate together, and the cross section of the vertical baffle plate is prolonged along the diameter of hydrogenation reaction cauldron
Stretch.
4. the system of process for prepairng hydrogen peroxide by anthraquinone according to claim 1, it is characterised in that：The catalyst filter is returned
Stream house steward lower end be connected on the big end circumference of taper, taper be sleeved on the periphery of the working solution supply pipe and
With working solution supply pipe coaxial line, the big end seal of taper is closed, the small end of taper towards hydrogenation reaction cauldron and with work
Liquid supply pipe is relative to be connect, and the part that the working solution supply pipe is located in taper is provided with the aditus laryngis of reduced diameter, institute
State the small end that aditus laryngis stretches to taper.
5. the system of process for prepairng hydrogen peroxide by anthraquinone according to claim 1, it is characterised in that：The hydrogenation reaction cauldron
Bottom is provided with the annular sleeve with hydrogenation reaction cauldron coaxial line, the inwall interval of the circumference of the annular sleeve and the hydrogenation reaction cauldron
One segment distance, each hydride outlet is located on the hydrogenation reaction cauldron circumference contour with annular sleeve axial direction middle part；
The bottom of the agitating shaft is provided with lower stirring paddle leaf, and the lower stirring paddle leaf is located in the annular sleeve, in the agitating shaft
Portion is provided with upper stirrer paddle；The outlet of the working solution supply pipe is positioned at the top of the upper stirrer paddle；The hydrogen supply
Lower section of the outlet of pipe positioned at the annular sleeve lower port center.
6. the system of process for prepairng hydrogen peroxide by anthraquinone according to claim 1, it is characterised in that：The top of the oxidizing tower
Center is provided with oxidizing tower gaseous phase outlet, and the upper portion side wall of the oxidizing tower is connected with oxidizing tower hydride entrance, the oxidizing tower
Hydride entrance is located above the liquid level line of oxidizing tower, and the bottom of the oxidizing tower is provided with air distribution device, the air point
It is connected with device with the total air intake of the oxidizing tower on oxidizing tower, the bottom centre of the oxidizing tower exports provided with oxidizing tower；Edge
Oxidizing tower short transverse mutually staggers make work in the horizontal direction provided with the horizontal oxidation tower tray of multiple tracks, the oxidation tower tray of adjacent layer
The runner for making liquid is S-shaped.
7. the system of process for prepairng hydrogen peroxide by anthraquinone according to claim 6, it is characterised in that：It is each it is described oxidation tower tray be in
Unfilled corner is circular, and the middle part of each oxidation tower tray is oxide regions, and it is saturating that the oxide regions are uniformly densely covered with multiple oxidation tower trays
Stomata, the both sides edge of the oxide regions is parallel to each other, and the side of the oxide regions is the descending liquid region of hollow out, the oxygen
The opposite side for changing region is the liquid receiving area domain that is made up of closed plate, and the periphery in the oxide regions and liquid receiving area domain is and oxidizing tower
Inwall be connected；The phase in adjacent layer descending liquid region differs 180 °；The oxidation tower tray edge adjacent with descending liquid region connects
Vertical baffle plate is connected to, the upper limb of the vertical baffle plate is parallel and higher than oxidation tower tray, and the lower edge of the vertical baffle plate gets over peroxidating
Tower tray is extended downwardly.
8. the system of process for prepairng hydrogen peroxide by anthraquinone according to claim 6, it is characterised in that：The inner chamber of the oxidizing tower
It is connected provided with inlet bend with the oxidizing tower hydride entrance, the lower end outlet of the inlet bend is located at the liquid level of oxidizing tower
Below line and close to the inwall of oxidizing tower, the liquid receiving area domain of top layer oxidation tower tray is located at the underface of the inlet bend.
9. the system of process for prepairng hydrogen peroxide by anthraquinone according to claim 6, it is characterised in that：The oxidizing tower gas phase goes out
Oxidizing tower capturing device is installed at mouthful, each layer oxidation tower tray is respectively arranged below with spiral condenser, the oxidizing tower
Outer wall is wound with multigroup semicanal condenser, and each semicanal condenser is located between adjacent two layers oxidation tower tray respectively, and uses
The flow direction of low in and high out.
10. the method that the production system any one of a kind of use claim 1 to 9 produces hydrogen peroxide, its feature exists
In, in turn include the following steps, (1) configure hydrogenation solvent；(2) 2- EAQs and 2- amyl group anthracenes are added into above solvent
The working solution of hydrogenation is constituted after quinone, wherein adding 2- EAQs in every liter of solvent（80~110）In g/L, every liter of solvent
Add 2- amyl anthraquinones（60~140）G/L, working solution is placed in working liquid tank；(3) preparation powdered palladium catalyst is placed in catalyst and added
Plus in tank；(4) appropriate catalyst is put into hydrogenation reaction cauldron, while fresh working solution enters hydrogenation reaction cauldron liquid Space
Center simultaneously sprays downwards, is spread under the agitation of stirrer paddle to surrounding downwards；Lower port of the fresh hydrogen from hydrogen feed pipe
Spray upwards, multiple minute bubbles are separated under the agitation of stirrer paddle and are spread upward all round, it is abundant with fresh working solution
It is mixed and stirred for；(5) the anthraquinone in working solution generates hydrogen anthraquinone in the presence of powdered palladium catalyst with hydrogen reaction；(6) hydrogenate anti-
Answer the gaseous substance on kettle top to discharge and condensed from hydriding reactor gaseous phase outlet, incoagulable gas include unreacted hydrogen from
Tail gas blow-down pipe is discharged, and condensate liquid is returned in center sleeve；Hydride together with powder catalyst from hydrogenation reaction cauldron lower circumference
On flow out into the filtering of each catalyst filter；The hydride of cleaning enters hydrogenation flow container；Hydrogenation flow container in hydride by
Hydride is pumped out, after going the removal of impurity and cooling, and feeding oxidizing tower is aoxidized, the oxidized liquid efferent duct of obtained oxidation solution
Output；(9) each catalyst filter is recoiled in turn, the catalyst for being deposited in cartridge surface is rushed, through catalyst filter flow reversal
House steward enters working solution supply pipe, follows fresh working solution to return in hydrogenation reaction cauldron；Step (1) middle hydrogenation solvent formula
One percent by volume is：Diisobutyl carbinol (DIBC)（45~50）V%, C10 aromatic hydrocarbons（50~55）V%, both volume summations are 100%；
The percent by volume of step (1) middle hydrogenation solvent formula two is：Tetrabutyl urea（12~30）V%, trioctyl phosphate（8~12）
V%, C10 aromatic hydrocarbons：（60~76）V%, the volume summation of three is 100%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710451706.3A CN107098317B (en) | 2017-06-15 | 2017-06-15 | System and method for producing hydrogen peroxide by anthraquinone process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710451706.3A CN107098317B (en) | 2017-06-15 | 2017-06-15 | System and method for producing hydrogen peroxide by anthraquinone process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107098317A true CN107098317A (en) | 2017-08-29 |
| CN107098317B CN107098317B (en) | 2023-06-27 |
Family
ID=59659599
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710451706.3A Active CN107098317B (en) | 2017-06-15 | 2017-06-15 | System and method for producing hydrogen peroxide by anthraquinone process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107098317B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108892108A (en) * | 2018-09-03 | 2018-11-27 | 江山市双氧水有限公司 | A kind of process system of hydride storage tank involved in the dilute product process units of hydrogen peroxide |
| CN109678121A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of efficient hydrogenation process and system of hydrogen dioxide solution production by anthraquinone process |
| WO2022078427A1 (en) * | 2020-10-14 | 2022-04-21 | 中国石油化工股份有限公司 | Method and system for preparing hydrogen peroxide |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1817838A (en) * | 2006-02-17 | 2006-08-16 | 黎明化工研究院 | Hydrogenation process of hydrogen peroxide fluidized bed by anthraquinone |
| WO2011134345A1 (en) * | 2010-04-29 | 2011-11-03 | 扬州惠通化工技术有限公司 | Hydrogenating system for producing hydrogen peroxide |
| CN103964394A (en) * | 2014-05-07 | 2014-08-06 | 无锡安竣化学工程科技有限公司 | Hydrogenation system for hydrogen peroxide production |
| CN206901770U (en) * | 2017-06-15 | 2018-01-19 | 扬州惠通化工科技股份有限公司 | The system of process for prepairng hydrogen peroxide by anthraquinone |
-
2017
- 2017-06-15 CN CN201710451706.3A patent/CN107098317B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1817838A (en) * | 2006-02-17 | 2006-08-16 | 黎明化工研究院 | Hydrogenation process of hydrogen peroxide fluidized bed by anthraquinone |
| WO2011134345A1 (en) * | 2010-04-29 | 2011-11-03 | 扬州惠通化工技术有限公司 | Hydrogenating system for producing hydrogen peroxide |
| CN103964394A (en) * | 2014-05-07 | 2014-08-06 | 无锡安竣化学工程科技有限公司 | Hydrogenation system for hydrogen peroxide production |
| CN206901770U (en) * | 2017-06-15 | 2018-01-19 | 扬州惠通化工科技股份有限公司 | The system of process for prepairng hydrogen peroxide by anthraquinone |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109678121A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of efficient hydrogenation process and system of hydrogen dioxide solution production by anthraquinone process |
| CN108892108A (en) * | 2018-09-03 | 2018-11-27 | 江山市双氧水有限公司 | A kind of process system of hydride storage tank involved in the dilute product process units of hydrogen peroxide |
| WO2022078427A1 (en) * | 2020-10-14 | 2022-04-21 | 中国石油化工股份有限公司 | Method and system for preparing hydrogen peroxide |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107098317B (en) | 2023-06-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107032303A (en) | The fluid bed production system and production method of hydrogen peroxide | |
| CN107098317A (en) | The system and method for process for prepairng hydrogen peroxide by anthraquinone | |
| CN104549066B (en) | Loop reaction device in slurry bed, application and method for producing hydrogen peroxide | |
| CN209507714U (en) | A kind of ozone oxidation reaction device | |
| CN206901770U (en) | The system of process for prepairng hydrogen peroxide by anthraquinone | |
| CN206616014U (en) | A kind of hydrogenation apparatus of hydrogeneous anthraquinone working solution | |
| CN107032306A (en) | Fluid bed produces the system and method for hydrogen peroxide | |
| CN106076211A (en) | A kind of bubble-liquid two-phase jet reactor and bubble-liquid two-phase jet response system | |
| CN109053412A (en) | Homogeneous premixing method before a kind of PTA energy saving device and CTA oxidation reaction | |
| CN108579639A (en) | A kind of device and method preparing ketoisophorone | |
| CN206901764U (en) | The system that fluid bed produces hydrogen peroxide | |
| CN104549065B (en) | A kind of slurry bed circulatory flow reactor and application and a kind of method for producing hydrogen peroxide | |
| CN207981116U (en) | A kind of slurry bed circulatory flow reactor | |
| CN104888668B (en) | A kind of F- T synthesis and the device and method separated | |
| CN206901763U (en) | Produce the fluid bed hydrogenation system of hydrogen peroxide | |
| CN107098318A (en) | Produce the fluid bed hydrogenation system and hydrogenation processes of hydrogen peroxide | |
| CN207091001U (en) | The fluid bed production system of hydrogen peroxide | |
| CN206901767U (en) | A kind of production system of hydrogen peroxide | |
| CN108404700B (en) | Airlift type rotary circulation mixing device without inner guide cylinder | |
| CN207091002U (en) | The process units of hydrogen peroxide | |
| CN102060399B (en) | Ammonia nitrogen removing device assisting organic compound denitrifier in treating high concentration ammonia nitrogen wastewater | |
| CN108128971A (en) | Wastewater treatment equipment containing dithio formate | |
| CN107032305A (en) | The production system and production method of a kind of hydrogen peroxide | |
| CN206901762U (en) | Fluid bed produces the hydrogenation apparatus of hydrogen peroxide | |
| CN204211485U (en) | Hydrogen peroxide production system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: No. 301, Wangjiang Road, economic and Technological Development Zone, Yangzhou City, Jiangsu Province Applicant after: Yangzhou Huitong Technology Co.,Ltd. Address before: No. 301, Wangjiang Road, economic and Technological Development Zone, Yangzhou City, Jiangsu Province Applicant before: YANGZHOU HUITONG CHEMICAL TECHNOLOGY CO.,LTD. |
|
| CB02 | Change of applicant information | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |