CN112499592A - System and process for preparing hydrogen peroxide based on anthraquinone method - Google Patents
System and process for preparing hydrogen peroxide based on anthraquinone method Download PDFInfo
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- CN112499592A CN112499592A CN201910867789.3A CN201910867789A CN112499592A CN 112499592 A CN112499592 A CN 112499592A CN 201910867789 A CN201910867789 A CN 201910867789A CN 112499592 A CN112499592 A CN 112499592A
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- C01B15/00—Peroxides; Peroxyhydrates; Peroxyacids or salts thereof; Superoxides; Ozonides
- C01B15/01—Hydrogen peroxide
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- C01B15/023—Preparation from organic compounds by the alkyl-anthraquinone process
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Abstract
The invention relates to a system and a process for preparing hydrogen peroxide based on an anthraquinone process, which comprises the following steps: hydrogenation tower, micro-interface generator, filtering and cooling unit, oxidation tower and extraction tower. The invention forms micron-sized bubbles by crushing hydrogen, mixes the micron-sized bubbles with the working solution containing anthraquinone derivatives or the hydrogenated solution containing 2-ethyl hydrogen anthraquinone to form gas-liquid emulsion, increases the phase interface area of gas-liquid two phases, achieves the effect of strengthening mass transfer within a lower preset operating condition range, improves the hydrogenation and oxidation efficiency of the working solution containing anthraquinone derivatives, improves the hydrogen reaction rate, saves the cost and reduces the danger, extracts the mixture of 2-ethyl anthraquinone and hydrogen peroxide by the extraction tower, and performs countercurrent extraction on the mixture of a water phase from top to bottom and from bottom to top, thereby realizing rapid extraction.
Description
Technical Field
The invention relates to the technical field of a method for preparing hydrogen peroxide by using an anthraquinone process, in particular to a system and a process for preparing hydrogen peroxide by using the anthraquinone process.
Background
Hydrogen peroxide (H)2O2) The aqueous solution is an important inorganic peroxide, has the characteristics of oxidability, bleachability, green and environment-friendly use process and the like, can be applied to the fields of fabric and paper pulp decoloration, chemical synthesis, wastewater treatment, medical treatment, metallurgy, military industry, food processing and the like, and can be used as an oxidant, a bleaching agent, a disinfectant, a polymer initiator, a cross-linking agent, a propellant and the like. With the stricter environmental protection regulations, the production capacity of products such as propylene oxide, green caprolactam and the like produced by a hydrogen peroxide direct oxidation process (HPPO process) is increased, so that H is generated2O2The market demand of (2) is strong.
The production method of hydrogen peroxide includes anthraquinone method, electrolytic method, isopropanol oxidation method, inorganic reaction method, and direct hydrogen-oxygen synthesis method. Among them, the anthraquinone process is the mainstream method for producing hydrogen peroxide at home and abroad at present.
The anthraquinone process of producing hydrogen peroxide is to use 2-Ethyl Anthraquinone (EAQ) as carrier and heavy Arene (AR) and trioctyl phosphate (TOP) as mixed solvent to compound solution with certain composition, and under the catalysis of Pd or Ni catalyst, alkyl anthraquinone is catalytically hydrogenated and air oxidized alternately to produce hydrogen peroxide extracted with water to form coarse hydrogen peroxide for reuse. Is equivalent to H2And O2Synthesis of H2O2. The anthraquinone process is mainly divided into four steps of hydrogenation, oxidation, extraction and post-treatmentAnd (4) carrying out the following steps. Among them, hydrogenation is a key step in the production of hydrogen peroxide by the anthraquinone process. The activity and selectivity of the anthraquinone hydrogenation catalyst determine the efficiency and unit consumption of the hydrogenation process to a great extent, and the hydrogenation catalyst with high activity and high selectivity can improve the yield of hydrogen peroxide, reduce the degradation of anthraquinone, reduce the production cost and create better economic benefit.
Chinese patent publication No.: CN106395755A discloses a method for preparing hydrogen peroxide by an anthraquinone method, which comprises the steps of contacting a working solution containing anthraquinone derivatives with hydrogen in a fiber catalyst in a fiber catalytic reactor, and reacting under the action of a catalytic active component of the fiber catalyst to generate a hydrogenated liquid; oxidizing the alkyl anthraquinone with air to generate an oxidizing solution containing hydrogen peroxide and the alkyl anthraquinone, extracting the hydrogen peroxide in the oxidizing solution with water, purifying and concentrating to obtain a hydrogen peroxide product with a certain concentration, and recycling the extracted working solution containing the alkyl anthraquinone. It can be seen that the method has the following problems:
firstly, in the method, the fiber catalyst is contacted with the anthraquinone derivative-containing working solution and hydrogen only through the fiber catalytic reactor, the hydrogen enters the fiber catalytic reactor through the hydrogen distributor to form large bubbles, and the bubbles cannot be fully contacted with the fiber catalyst and the anthraquinone derivative working solution due to overlarge volume, so that the hydrogenation efficiency of the system is reduced.
Secondly, in the method, under the condition that the contact between hydrogen and the fiber catalyst and the anthraquinone derivative working solution is insufficient, the hydrogenation degree is reduced, the subsequent oxidation and extraction efficiency is directly influenced, the hydrogen content of the flammable and explosive raw materials in the system is increased, and the residual hydrogen flows out along a hydrogen second tail gas outlet, so that the production cost is increased, and the method has certain danger.
Thirdly, the method only introduces air through the air distributor, and oxidizes the alkyl anthraquinone through the air to generate the oxidizing liquid containing hydrogen peroxide and the alkyl anthraquinone, and the bubbles have too large volume and cannot be fully contacted with the alkyl anthraquinone, so that the reaction efficiency of the system is reduced.
Disclosure of Invention
Therefore, the invention provides a system and a process for preparing hydrogen peroxide based on an anthraquinone method, which are used for solving the problem of low system reaction efficiency caused by-products generated by uneven mixing of materials in the prior art.
In one aspect, the invention provides a system for preparing hydrogen peroxide based on an anthraquinone process, comprising:
the hydrogenation tower is used for providing a reaction site for the working solution containing the anthraquinone derivatives and hydrogen;
a micro-interface generator provided with a hydrogenation tower for providing a reaction site for the anthraquinone derivative-containing working solution and hydrogen;
the filtering and cooling unit is arranged on the side wall of the hydrogenation tower and is used for filtering and cooling the hydrogenated material output by the hydrogenation tower;
the oxidation tower is connected with the filtering and cooling unit and is used for providing a reaction site for the materials and the oxygen output by the filtering and cooling unit;
the extraction tower is used for extracting and separating the materials output by the oxidation tower;
and the micro-interface generator is arranged at the appointed positions in the hydrogenation tower and the oxidation tower, converts the pressure energy of gas and/or the kinetic energy of liquid into bubble surface energy and transmits the bubble surface energy to the hydrogen, so that the hydrogen is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, the mass transfer area between the anthraquinone derivative-containing working solution and the hydrogen is increased, the thickness of a liquid film is reduced, the mass transfer resistance is reduced, and the anthraquinone derivative-containing working solution and the micron-sized bubbles are mixed to form a gas-liquid emulsion after being crushed, so that the mass transfer efficiency and the reaction efficiency between the anthraquinone derivative-containing working solution and the hydrogen are enhanced within the range of preset operating conditions.
Further, the micro-interface generator includes:
the first micro-interface generator is arranged at the bottom of the reaction zone of the hydrogenation tower and used for crushing hydrogen to form micron-sized bubbles, outputting the micron-sized bubbles to the hydrogenation tower after the crushing is finished, and mixing the micron-sized bubbles with the anthraquinone derivative-containing working solution in the hydrogenation tower to form a gas-liquid emulsion;
and the second micro-interface generator is arranged at the bottom of the reaction zone of the oxidation tower and used for crushing oxygen to form micron-scale bubbles, outputting the micron-scale bubbles to the hydrogenation tower after the crushing is finished, and mixing the micron-scale bubbles with the 2-ethyl hydrogen anthraquinone solution in the oxidation tower to form a gas-liquid emulsion.
Further, the hydrogenation column comprises:
a hydrogen feeding pipeline which is arranged on the side wall of the hydrogenation tower and is connected with the first micro-interface generator, and is used for conveying hydrogen to the first micro-interface generator so that the first micro-interface generator can crush the hydrogen;
a working liquid feed pipe provided on the side wall of the hydrogen column above the hydrogen feed pipe for feeding the working liquid containing the anthraquinone derivative to the inside of the hydrogenation column;
the catalyst feeding hole is arranged on the side wall of the hydrogenation tower and positioned above the working solution feeding pipeline and used for placing the catalyst into the hydrogenation tower;
and the first tail gas outlet is arranged at the top of the hydrogenation tower and used for discharging tail gas.
Further, the oxidation tower comprises:
the air feeding pipeline is arranged on the side wall of the oxidation tower, is connected with the second micro-interface generator and is used for conveying air to the second micro-interface generator so that the second micro-interface generator can crush the air;
a hydrogenation liquid feed pipe disposed on the side wall of the oxidation tower above the air feed pipe for feeding the 2-ethylhydroanthraquinone solution to the inside of the oxidation tower;
the return pipe is arranged on the side wall of the oxidation tower and is used for returning the material output by the oxidation tower to the oxidation tower so as to enable the 2-ethyl hydrogen anthraquinone solution in the material to fully react;
the circulating pump is connected with the return pipe and is used for providing feedback power for the material output by the return pipe;
the second tail gas outlet is arranged at the top of the oxidation tower and used for discharging air;
and the discharge hole is arranged on the side wall of the oxidation tower and used for discharging the mixture of the 2-ethyl anthraquinone and the hydrogen peroxide.
Further, the filtering and cooling unit includes:
the filter is arranged at the upper part of the side wall of the hydrogenation tower, is connected with the liquid output end of the gas-liquid separator and is used for filtering the hydrogenated material output by the hydrogenation tower so as to filter solid impurities carried in the material;
the heat exchanger is connected with the filter and used for exchanging heat between the material output by the filter and the working solution containing the anthraquinone derivative so as to maintain the working solution containing the anthraquinone derivative within a preset temperature range;
and the hydrogenation cooler is arranged in the middle of the side wall of the hydrogenation tower, is connected with the heat exchanger and is used for cooling the heat-exchanged materials.
Further, the extraction column comprises:
a pure water feed pipe arranged at the top of the extraction tower for conveying pure water to the inside of the extraction tower;
the heater is connected with the pure water feeding pipeline and is used for preheating the pure water;
the pure water acidification metering pump is connected with the pure water feeding pipeline, is positioned below the heater and is used for adding phosphoric acid to adjust the acidity of the pure water;
the pure water pump is connected with the pure water feeding pipeline, is positioned below the pure water acidification metering pump and is used for conveying pure water;
and the hydrogen peroxide discharge pipeline is arranged at the bottom of the extraction tower and used for outputting hydrogen peroxide.
On the other hand, the technology for preparing hydrogen peroxide based on the anthraquinone method comprises the following steps:
step 1: feeding the anthraquinone derivative-containing working solution into the hydrogenation tower through the working solution feeding pipeline, and feeding the catalyst into the hydrogenation tower through the catalyst feeding hole;
step 2: hydrogen is conveyed into the hydrogenation tower through the hydrogen feeding pipeline, the hydrogen feeding pipeline conveys the hydrogen to the first micro-interface generator, the first micro-interface generator breaks the hydrogen to form micron-scale micron-sized bubbles, and after breaking is completed, the micron-scale bubbles are output to the hydrogenation tower by the first micro-interface generator and are mixed with the anthraquinone derivative-containing working solution to form a gas-liquid emulsion;
and step 3: carrying out hydrogenation reaction on the gas-liquid emulsion under the action of a catalyst to generate a mixture containing a 2-ethyl hydrogen anthraquinone solution, and after the reaction is finished, enabling the mixture to flow upwards and enter a gas-liquid separator;
and 4, step 4: after the mixture enters the gas-liquid separator, tail gas is discharged from the top of the gas-liquid separator, and hydrogenated liquid containing 2-ethyl hydrogen anthraquinone is discharged from the side surface of the gas-liquid separator and enters the filtering and cooling unit;
and 5: after the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone enters the filter, solid impurities carried in the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone remain in the filter, filtrate in the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone is discharged from the bottom of the filter and enters the heat exchanger, the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone in the heat exchanger exchanges heat with working liquid containing anthraquinone derivatives, the working liquid containing anthraquinone derivatives after heat exchange flows into the working liquid feeding pipeline, the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone after heat exchange enters the hydrogenation cooler, and the cooled hydrogenated liquid containing 2-ethyl hydrogen anthraquinone enters the oxidation tower;
step 6: conveying the hydrogenated liquid containing 2-ethyl hydroanthraquinone into the oxidation tower through the hydrogenated liquid feeding pipeline, wherein the air feeding pipeline can convey air to the second micro-interface generator, the second micro-interface generator is used for crushing the air to form micron-sized bubbles, and after the crushing is finished, the second micro-interface generator outputs the micron-sized bubbles to the oxidation tower and mixes the micron-sized bubbles with the hydrogenated liquid containing 2-ethyl hydroanthraquinone to form a gas-liquid emulsion;
and 7: the gas-liquid emulsion is subjected to oxidation reaction to generate a mixture containing 2-ethylanthraquinone and hydrogen peroxide, after the reaction is finished, the mixture flows upwards and flows back to the oxidation tower along the return pipe, a small amount of tail gas moves upwards and is discharged through the second tail gas outlet, and the mixture of the 2-ethylanthraquinone and the hydrogen peroxide after the tail gas is discharged is output to the oxidation tower through the discharge hole;
and 8: the mixture of the 2-ethyl anthraquinone and the hydrogen peroxide is transmitted to the bottom of the extraction tower through a discharge hole, pure water is transmitted into the heater through the pure water pump and is regulated by the pure water acidification metering pump, preheated pure water enters the inside of the extraction tower along the pure water feeding pipeline and is extracted with the mixture of the 2-ethyl anthraquinone and the hydrogen peroxide, and the extracted hydrogen peroxide is output to the extraction tower along the hydrogen peroxide discharging pipeline.
Furthermore, the reaction temperature in the hydrogenation tower in the process is 20-40 ℃, and the reaction pressure is 0.05-0.50 MPa.
Furthermore, the reaction temperature in the oxidation tower in the process is 20-45 ℃, and the reaction pressure is 0.10-0.20 MPa.
Further, the gas-liquid ratio in the first micro-interface generator is 300-: 1, the gas-liquid ratio in the second micro-interface generator is 400-: 1.
compared with the prior art, the method has the beneficial effects that the hydrogen is crushed to form micron-sized bubbles with micron scale, and the micron-sized bubbles and the anthraquinone derivative-containing working solution are mixed to form gas-liquid emulsion, so that the phase interface area of gas-liquid two phases is increased, the effect of strengthening mass transfer within a lower preset operating condition range is achieved, the hydrogenation efficiency of the anthraquinone derivative-containing working solution is improved, the hydrogen reaction rate is improved, the cost is saved, and the danger is reduced; the air is crushed to form micron-sized bubbles with micron scale, and the micron-sized bubbles are mixed with the hydrogenated liquid containing 2-ethyl hydroanthraquinone to form gas-liquid emulsion, so that the phase interface area of gas-liquid two phases is increased, the effect of strengthening mass transfer within a lower preset operating condition range is achieved, and the oxidation efficiency of the hydrogenated liquid containing 2-ethyl hydroanthraquinone is improved; extracting the mixture of 2-ethyl anthraquinone and hydrogen peroxide by an extraction tower, and performing countercurrent extraction on the mixture of a water phase from top to bottom and the mixture from bottom to top to realize rapid extraction; meanwhile, the system filters, exchanges heat and cools the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone output by the hydrogenation tower through the filtering and cooling unit to filter solid impurities carried in materials, exchanges heat with the working liquid containing anthraquinone derivatives, saves energy consumption, and cools the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone to reach a preset temperature range. In addition, the range of the preset operation condition can be flexibly adjusted according to different product requirements or different catalysts, so that the full and effective reaction is further ensured, the reaction rate is further ensured, and the purpose of strengthening the reaction is achieved.
Particularly, the invention also arranges a gas-liquid separator in the hydrogenation tower, and the produced 2-ethyl hydrogen anthraquinone hydrogenation liquid is separated and degassed by the gas-liquid separator, thereby improving the further oxidation efficiency of the 2-ethyl hydrogen anthraquinone hydrogenation liquid.
Furthermore, the material after the reaction is refluxed to fully use the unreacted raw material liquid in the material, so that the utilization rate of the material is improved, and the reaction efficiency of the system is further improved.
Furthermore, the hydrogenation tower and the oxidation tower are respectively provided with a first micro-interface generator and a second micro-interface generator, and the micro-bubble and the material are mixed more uniformly by using different types of micro-interface generators, so that the mixing efficiency of the material and the micro-bubble in the reactor is improved, and the reaction efficiency of the system is further improved.
In particular, the extraction tower provided by the invention is used for extracting the mixture of 2-ethyl anthraquinone and hydrogen peroxide, and the mixture of a water phase from top to bottom and from bottom to top are subjected to countercurrent extraction, so that the extraction efficiency is improved, and the rapid extraction is realized.
Furthermore, the pure water is subjected to acidity adjustment by the pure water acidification metering pump, the acidity of the extracting agent is ensured, the pure water is preheated by the heater, and the pure water enters the extraction tower within a preset temperature range, so that the extraction efficiency is improved.
Particularly, the filtering and cooling unit is used for filtering, heat exchanging and cooling the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone output by the hydrogenation tower so as to filter solid impurities carried in materials, and exchanging heat with the working liquid containing anthraquinone derivatives, so that the energy consumption is saved, and the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone is cooled to reach a preset temperature range so as to further improve the reaction efficiency of the system.
Drawings
FIG. 1 is a schematic structural diagram of a system for preparing hydrogen peroxide based on an anthraquinone process.
Detailed Description
Preferred embodiments of the present invention are described below with reference to the accompanying drawings. It should be understood by those skilled in the art that these embodiments are only for explaining the technical principle of the present invention, and do not limit the scope of the present invention.
It should be noted that in the description of the present invention, the terms of direction or positional relationship indicated by the terms "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, which are only for convenience of description, and do not indicate or imply that the device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Fig. 1 is a schematic structural diagram of a system for preparing hydrogen peroxide based on an anthraquinone process according to the present invention, including a hydrogenation tower 1, a micro-interface generator 2 (not shown), a filtering and cooling unit 3, an oxidation tower 4, and an extraction tower 5. The micro-interface generator 2 is arranged inside the hydrogenation tower 1 and the oxidation tower 4 and is used for crushing hydrogen and oxygen to form micron-sized bubbles and mixing the micron-sized bubbles with materials in the hydrogenation tower and the oxidation tower to form gas-liquid emulsion. The filtering and cooling unit 3 is connected with the hydrogenation tower 1 and the oxidation tower 4 and is used for filtering and cooling hydrogenated materials output by the hydrogenation tower, the oxidation tower 4 is used for providing a reaction site for the materials output by the filtering and cooling unit and oxygen, and the extraction tower 5 and the oxidation tower 4 are used for extracting and separating the materials output by the oxidation tower.
When the system operates, firstly, the anthraquinone derivative-containing working solution and the catalyst are conveyed into the hydrogenation tower 1, meanwhile, the hydrogen is conveyed into the hydrogenation tower 1, the hydrogen can enter the micro-interface generator 2, the micro-interface generator 2 breaks the hydrogen to form micron-scale bubbles and enables the micron-scale bubbles to be mixed with the anthraquinone derivative-containing working solution to form gas-liquid emulsion, the gas-liquid emulsion is subjected to hydrogenation reaction under the action of the catalyst to generate a mixture containing 2-ethyl hydrogen anthraquinone solution, the hydrogenation tower 1 can discharge tail gas in the reaction process out of the system and output the reacted mixture containing the 2-ethyl hydrogen anthraquinone solution to the filtering and cooling unit 3, the filtering and cooling unit 3 filters and cools the mixture, the air is conveyed to the oxidation tower 4 and enters the micro-interface generator 2, the micro-interface generator 2 breaks the air to form micron-scale bubbles and enables the micron-scale bubbles and the 2-containing micron-scale bubbles to be mixed with the mixture containing the 2-ethyl hydrogen And mixing the mixture of the ethyl hydroanthraquinone solution to form a gas-liquid emulsion, carrying out oxidation reaction on the gas-liquid emulsion to generate a mixture containing 2-ethyl anthraquinone and hydrogen peroxide, transmitting the mixture to the extraction tower 5, extracting the mixture containing 2-ethyl anthraquinone and hydrogen peroxide and pure water in the extraction tower 5, and outputting the extracted hydrogen peroxide to the extraction tower 5. It will be understood by those skilled in the art that the micro-interface generator 2 of the present invention can also be used in other multi-phase reactions, such as by micro-interfaces, micro-nano interfaces, ultra-micro interfaces, micro-bubble biochemical reactors or micro-bubble bioreactors, using micro-mixing, micro-fluidization, micro-bubble fermentation, micro-bubble bubbling, micro-bubble mass transfer, micro-bubble reaction, micro-bubble absorption, micro-bubble oxygenation, micro-bubble contact, etc. to form multi-phase micro-mixed flow, multi-phase micro-nano flow, multi-phase emulsified flow, multi-phase micro-flow, gas-liquid-solid micro-mixed flow, gas-liquid-solid micro-nano flow, gas-liquid-solid emulsified flow, gas-liquid-solid micro-structured flow, micro-bubbles, micro-micron-sized bubble flow, micro-foams, micro-bubble flow, micro-gas-liquid flow, gas-liquid-micro-nano emulsified flow, micro-, The multiphase fluid formed by micron-scale particles such as micro-bubbling flow, micro-nano bubbling and micro-nano bubbling flow or the multiphase fluid formed by micro-nano-scale particles (micro-interface fluid for short) effectively increases the phase boundary mass transfer area between the gas phase and/or the liquid phase and/or the solid phase in the reaction process.
With continued reference to fig. 1, the hydrogenation column 1 of the present invention includes a hydrogen gas feed line 11, a working fluid feed line 12, a catalyst feed port 13, and a first tail gas outlet 14. Wherein, the hydrogen feeding pipeline 11 is arranged on the side wall of the hydrogenation tower 1 and is connected with the micro-interface generator 2 for conveying hydrogen. The working liquid feed pipe 12 is provided on the side wall of the hydrogen column 1 above the hydrogen feed pipe 11 to feed the working liquid containing the anthraquinone derivative to the inside of the hydrogenation column. The catalyst feed port 13 is disposed on the sidewall of the hydrogenation tower 1 and above the working solution feed pipe 12 for feeding a catalyst into the hydrogenation tower, and the first tail gas outlet 114 is disposed at the top of the hydrogenation tower for discharging tail gas.
When the hydrogenation tower 1 is in operation, hydrogen is conveyed into the hydrogenation tower 1 through the hydrogen feeding pipeline 11, the hydrogen is conveyed to the micro-interface generator 2 through the hydrogen feeding pipeline 11, the hydrogen is crushed by the first micro-interface generator 21 to form micron-sized bubbles, after the crushing is completed, the micron-sized bubbles are output to the hydrogenation tower 1 through the micro-interface generator 2 and are mixed with the anthraquinone derivative-containing working solution in the hydrogenation tower to form a gas-liquid emulsion, and the gas-liquid emulsion is subjected to hydrogenation reaction under the action of a catalyst to generate a mixture containing 2-ethyl hydrogen anthraquinone solution.
Specifically, the hydrogen feeding pipeline 11 is disposed on the side wall of the hydrogenation tower 1 and connected to the micro-interface generator 2, and is configured to convey hydrogen to the first micro-interface generator, so that the first micro-interface generator can crush the hydrogen to form micron-sized bubbles, and mix the micron-sized bubbles with the working solution containing anthraquinone derivatives.
Referring still to fig. 1, the micro-interface generator 2 of the present invention includes a first micro-interface generator 21 and a second micro-interface generator 22. Wherein the first micro-interface generator 21 is arranged at the bottom of the reaction zone and is used for breaking the hydrogen into micron-sized bubbles. The second micro-interface generator 22 is arranged at the bottom of the reaction zone and is used for breaking oxygen into micron-sized bubbles. When the hydrogenation tower 1 is in operation, the first micro-interface generator 21 is used for crushing hydrogen to form micron-sized bubbles, and mixing the micron-sized bubbles with the anthraquinone derivative-containing working solution to form a gas-liquid emulsion, and the second micro-interface generator 22 is used for crushing oxygen to form micron-sized bubbles, and mixing the micron-sized bubbles with the 2-ethyl hydroanthraquinone solution in the oxidation tower to form the gas-liquid emulsion.
Specifically, the first micro-interface generator 21 of the present invention is a pneumatic micro-interface generator, which is connected to the hydrogen feeding pipe 11 and is used for breaking up the hydrogen fed from the hydrogen feeding pipe 11 and forming micron-sized bubbles. When the hydrogenation tower 1 is in operation, the hydrogen feeding pipeline 11 will convey hydrogen to the first micro-interface generator 21, the first micro-interface generator 21 will crush the hydrogen and form micron-sized bubbles, and after the crushing, the micron-sized bubbles are output to the hydrogenation tower and mixed with the anthraquinone derivative-containing working solution in the hydrogenation tower to form a gas-liquid emulsion for sufficient reaction.
Specifically, the second micro-interface generator 22 of the present invention is a pneumatic micro-interface generator, which is connected to the air feeding pipe and is used for breaking up the air conveyed by the air feeding pipe and forming micron-sized bubbles. When the oxidation tower 2 is in operation, the air feeding pipeline conveys air to the second micro-interface generator 22, the second micro-interface generator 22 crushes the air to form micron-sized bubbles, the micron-sized bubbles are output to the oxidation tower after the crushing is finished, and the micron-sized bubbles are mixed with the hydrogenated liquid containing 2-ethyl hydroanthraquinone in the oxidation tower to form a gas-liquid emulsion for sufficient reaction.
With continued reference to fig. 1, the filtration and cooling unit 3 of the present invention includes a filter 31, a heat exchanger 32, and a hydrogenation cooler 33. The filter 31 is arranged on the upper portion of the side wall of the hydrogenation tower 1 and connected with the liquid output end of the gas-liquid separator 12, and is used for filtering hydrogenated materials output by the hydrogenation tower to filter solid impurities carried in the materials, and the heat exchanger 32 is connected with the filter 31 and is used for exchanging heat between the materials output by the filter and the anthraquinone derivative-containing working solution, so that the anthraquinone derivative-containing working solution is maintained within a preset temperature range. The hydrogenation cooler 33 is arranged in the middle of the side wall of the hydrogenation tower 1 and connected with the heat exchanger 32, and is used for cooling the heat-exchanged materials, when the filtering and cooling unit 3 operates, the filter 31 receives the liquid-phase component discharged from the gas-liquid separator 12, and filters solid impurities in the liquid-phase component, the filtrate containing 2-ethylhydroanthraquinone enters the heat exchanger 32 to exchange heat with the working solution containing anthraquinone derivatives, and then the hydrogenation cooler 33 receives the 2-ethylhydroanthraquinone hydrogenated liquid discharged from the heat exchanger 32, and cools the solution.
With continued reference to fig. 1, the oxidation tower 4 of the present invention includes an air feeding pipe 41, a hydrogenated liquid feeding pipe 42, a return pipe 43, a circulation pump 44, a second tail gas outlet 45, and a discharge port 46. The air feeding pipe 41 is arranged on the side wall of the oxidation tower 4 and connected with the second micro-interface generator 22, and is used for conveying air to the second micro-interface generator so that the second micro-interface generator can break the air. The hydrogenated liquid feed line 42 is provided in the side wall of the oxidation tower 4 above the air feed line 41 to feed the 2-ethylhydroanthraquinone solution to the inside of the oxidation tower 4; the return pipe 43 is arranged on the side wall of the oxidation tower 4 and is used for returning the material output by the oxidation tower to the oxidation tower so as to enable the 2-ethyl hydrogen anthraquinone solution in the material to fully react. The circulating pump 44 is connected with the return pipe 43 and used for providing return power for the material output by the return pipe, the second tail gas outlet 45 is arranged at the top of the oxidation tower and used for discharging air, and the discharge hole 46 is arranged on the side wall of the oxidation tower and used for discharging the mixture of 2-ethyl anthraquinone and hydrogen peroxide. Through air feed pipe 41 is to carrying the air in the oxidation tower 4, air feed pipe 41 with second micro-interface generator 22 links to each other, second micro-interface generator 22 is broken to the air, forms micron order bubble of micron yardstick, and after the breakage was accomplished, second micro-interface generator 22 exports micron order bubble to oxidation tower 4 and with 2-ethyl hydrogen anthraquinone solution the oxidation tower mixes and forms the gas-liquid emulsion, and the gas-liquid emulsion fully reacts, produces the mixture that contains 2-ethyl anthraquinone and hydrogen peroxide.
As shown in fig. 1, the extraction tower 5 of the present invention includes a pure water feeding pipe 51, a heater 52, a pure water acid metering pump 53, a pure water pump 54, and a hydrogen peroxide discharging pipe 55. Wherein the pure water feed line 51 is provided at the top of the extraction column for delivering pure water to the inside of the extraction column. The heater 52 is connected to the pure water feed line for preheating the pure water. And the pure water acid adding metering pump 53 is connected with the pure water feeding pipeline and is positioned below the heater, and is used for adding phosphoric acid to adjust the acidity of the pure water. The pure water pump 54 is connected to the pure water feeding pipe and located below the pure water acidification metering pump for delivering pure water. The hydrogen peroxide discharge pipeline 55 is arranged at the bottom of the extraction tower and used for outputting hydrogen peroxide. When the extraction tower 5 operates, pure water is transmitted into the heater 52 through the pure water pump 54, the acidity of the pure water is adjusted through adjustment of the pure water acidification metering pump 53, the preheated pure water enters the extraction tower 5 along the pure water feeding pipeline 51 and is extracted with a mixture of 2-ethyl anthraquinone and hydrogen peroxide, and the extracted hydrogen peroxide is output to the extraction tower 5 along the hydrogen peroxide discharging pipeline 55. It is understood that the types and powers of the heater 52, the pure water acidification metering pump 53 and the pure water pump 54 are not particularly limited in this embodiment, as long as the heater 52, the pure water acidification metering pump 53 and the pure water pump 54 can reach their designated operating states.
In order that the objects and advantages of the invention will be more clearly understood, the invention is further described below with reference to examples; it should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
A technology for preparing hydrogen peroxide based on an anthraquinone method comprises the following steps:
step 1: feeding the anthraquinone derivative-containing working solution into the hydrogenation tower through the working solution feeding pipeline, and feeding the catalyst into the hydrogenation tower through the catalyst feeding hole;
step 2: hydrogen is conveyed into the hydrogenation tower through the hydrogen feeding pipeline, the hydrogen feeding pipeline conveys the hydrogen to the first micro-interface generator, the first micro-interface generator breaks the hydrogen to form micron-scale micron-sized bubbles, and after breaking is completed, the micron-scale bubbles are output to the hydrogenation tower by the first micro-interface generator and are mixed with the anthraquinone derivative-containing working solution to form a gas-liquid emulsion;
and step 3: carrying out hydrogenation reaction on the gas-liquid emulsion under the action of a catalyst to generate a mixture containing a 2-ethyl hydrogen anthraquinone solution, and after the reaction is finished, enabling the mixture to flow upwards and enter a gas-liquid separator;
and 4, step 4: after the mixture enters the gas-liquid separator, tail gas is discharged from the top of the gas-liquid separator, and hydrogenated liquid containing 2-ethyl hydrogen anthraquinone is discharged from the side surface of the gas-liquid separator and enters the filtering and cooling unit;
and 5: after the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone enters the filter, solid impurities carried in the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone remain in the filter, filtrate in the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone is discharged from the bottom of the filter and enters the heat exchanger, the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone in the heat exchanger exchanges heat with working liquid containing anthraquinone derivatives, the working liquid containing anthraquinone derivatives after heat exchange flows into the working liquid feeding pipeline, the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone after heat exchange enters the hydrogenation cooler, and the cooled hydrogenated liquid containing 2-ethyl hydrogen anthraquinone enters the oxidation tower;
step 6: conveying the hydrogenated liquid containing 2-ethyl hydroanthraquinone into the oxidation tower through the hydrogenated liquid feeding pipeline, wherein the air feeding pipeline can convey air to the second micro-interface generator, the second micro-interface generator is used for crushing the air to form micron-sized bubbles, and after the crushing is finished, the second micro-interface generator outputs the micron-sized bubbles to the oxidation tower and mixes the micron-sized bubbles with the hydrogenated liquid containing 2-ethyl hydroanthraquinone to form a gas-liquid emulsion;
and 7: the gas-liquid emulsion is subjected to oxidation reaction to generate a mixture containing 2-ethylanthraquinone and hydrogen peroxide, after the reaction is finished, the mixture flows upwards and flows back to the oxidation tower along the return pipe, a small amount of tail gas moves upwards and is discharged through the second tail gas outlet, and the mixture of the 2-ethylanthraquinone and the hydrogen peroxide after the tail gas is discharged is output to the oxidation tower through the discharge hole;
and 8: the mixture of the 2-ethyl anthraquinone and the hydrogen peroxide is transmitted to the bottom of the extraction tower through a discharge hole, pure water is transmitted into the heater through the pure water pump and is regulated by the pure water acidification metering pump, preheated pure water enters the inside of the extraction tower along the pure water feeding pipeline and is extracted with the mixture of the 2-ethyl anthraquinone and the hydrogen peroxide, and the extracted hydrogen peroxide is output to the extraction tower along the hydrogen peroxide discharging pipeline.
Wherein the anthraquinone derivative-containing working solution consists of 2-Ethyl Anthraquinone (EAQ), heavy aromatic hydrocarbon (AR) and trioctyl phosphate. It can be understood that the range of the preset operation conditions can be flexibly adjusted according to different product requirements or different catalysts, so as to ensure the full and effective reaction, further ensure the reaction rate and achieve the purpose of strengthening the reaction. Meanwhile, in the present embodiment, the kind of the catalyst is not particularly limited as long as the strengthening reaction can be smoothly performed.
Example 1
The system and the process are used for preparing hydrogen peroxide by an anthraquinone method, wherein:
in the process, the reaction temperature in the hydrogenation tower is 38 ℃, the reaction pressure is 0.05MPa, the anthraquinone content is 220g/L, and the flow rate of the working solution containing anthraquinone derivatives is 130h-1The gas-liquid ratio in the first micro-interface generator is 300: 1.
in the process, the reaction temperature in the oxidation tower is 35 ℃, the reaction pressure is 0.10MPa, and the flow rate of the hydrogenation liquid containing 2-ethyl hydrogen anthraquinone is 140h-1And the gas-liquid ratio in the second micro-interface generator is 400: 1.
after detection, the hydrogenation efficiency is 14.2g/L, the oxidation efficiency is 13.9g/L, and the conversion rate of the oxidation reaction is 97.9 percent after the system and the process are used.
Example 2
The system and the process are used for preparing hydrogen peroxide by an anthraquinone method, wherein:
in the process, the reaction temperature in the hydrogenation tower is 39 ℃, the reaction pressure is 0.15MPa, the anthraquinone content is 235g/L, and the flow rate of the working solution containing anthraquinone derivatives is 135h-1And the gas-liquid ratio in the first micro-interface generator is 350: 1.
in the process, the reaction temperature in the oxidation tower is 37 ℃, the reaction pressure is 0.13MPa, and the flow rate of the hydrogenation liquid containing 2-ethyl hydrogen anthraquinone is 145h-1And the gas-liquid ratio in the second micro-interface generator is 420: 1.
after detection, the hydrogenation efficiency is 14.6g/L, the oxidation efficiency is 14.3g/L, and the conversion rate of the oxidation reaction is 97.9 percent after the system and the process are used.
Example 3
The system and the process are used for preparing hydrogen peroxide by an anthraquinone method, wherein:
in the process, the reaction temperature in the hydrogenation tower is 42 ℃, the reaction pressure is 0.30MPa, the anthraquinone content is 245g/L, and the flow velocity of the working solution containing anthraquinone derivatives is 147h-1The gas-liquid ratio in the first micro-interface generator is 400: 1.
in the oxidation tower of the processThe reaction temperature is 40 ℃, the reaction pressure is 0.15MPa, and the flow rate of the hydrogenation liquid containing 2-ethyl hydrogen anthraquinone is 152h-1And the gas-liquid ratio in the second micro-interface generator is 450: 1.
after detection, the hydrogenation efficiency is 14.7g/L, the oxidation efficiency is 14.4g/L, and the conversion rate of the oxidation reaction is 98.0 percent after the system and the process are used.
Example 4
The system and the process are used for preparing hydrogen peroxide by an anthraquinone method, wherein:
in the process, the reaction temperature in the hydrogenation tower is 45 ℃, the reaction pressure is 0.40MPa, the anthraquinone content is 248g/L, and the flow rate of the working solution containing anthraquinone derivatives is 150h-1A gas-liquid ratio within the first micro-interfacial generator of 470: 1.
in the process, the reaction temperature in the oxidation tower is 43 ℃, the reaction pressure is 0.18MPa, and the flow rate of the hydrogenation liquid containing 2-ethyl hydrogen anthraquinone is 154h-1And the gas-liquid ratio in the second micro-interface generator is 460: 1.
after detection, the hydrogenation efficiency is 14.8g/L, the oxidation efficiency is 14.6g/L, and the conversion rate of the oxidation reaction is 98.6 percent after the system and the process are used.
Example 5
The system and the process are used for preparing hydrogen peroxide by an anthraquinone method, wherein:
in the process, the reaction temperature in the hydrogenation tower is 48 ℃, the reaction pressure is 0.50MPa, the anthraquinone content is 260g/L, and the flow rate of the working solution containing anthraquinone derivatives is 160h-1The gas-liquid ratio in the first micro-interface generator is 500: 1.
in the process, the reaction temperature in the oxidation tower is 45 ℃, the reaction pressure is 0.20MPa, and the flow rate of the hydrogenation liquid containing 2-ethyl hydrogen anthraquinone is 160h-1And the gas-liquid ratio in the second micro-interface generator is 500: 1.
after detection, the hydrogenation efficiency is 14.9g/L, the oxidation efficiency is 14.7g/L, and the conversion rate of the oxidation reaction is 98.6 percent after the system and the process are used.
Comparative example
The hydrogen peroxide is prepared by an anthraquinone process by using the prior art, wherein the process parameters selected in the embodiment are the same as those in the embodiment 4.
After the system and the process are used, the hydrogenation efficiency is 10.7g/L, the oxidation efficiency is 9.9g/L, and the conversion rate of the oxidation reaction is 73.8 percent.
So far, the technical solutions of the present invention have been described in connection with the preferred embodiments shown in the drawings, but it is easily understood by those skilled in the art that the scope of the present invention is obviously not limited to these specific embodiments. Equivalent changes or substitutions of related technical features can be made by those skilled in the art without departing from the principle of the invention, and the technical scheme after the changes or substitutions can fall into the protection scope of the invention.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention; various modifications and alterations to this invention will become apparent to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A system for preparing hydrogen peroxide based on an anthraquinone process is characterized by comprising the following steps:
the hydrogenation tower is used for providing a reaction site for the working solution containing the anthraquinone derivatives and hydrogen;
the filtering and cooling unit is arranged on the side wall of the hydrogenation tower and is used for filtering and cooling the hydrogenated material output by the hydrogenation tower;
the oxidation tower is connected with the filtering and cooling unit and is used for providing a reaction site for the materials and the oxygen output by the filtering and cooling unit;
the extraction tower is used for extracting and separating the materials output by the oxidation tower;
and the micro-interface generator is arranged at the appointed positions in the hydrogenation tower and the oxidation tower, converts the pressure energy of gas and/or the kinetic energy of liquid into bubble surface energy and transmits the bubble surface energy to the hydrogen, so that the hydrogen is crushed into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, the mass transfer area between the anthraquinone derivative-containing working solution and the hydrogen is increased, the thickness of a liquid film is reduced, the mass transfer resistance is reduced, and the anthraquinone derivative-containing working solution and the micron-sized bubbles are mixed to form a gas-liquid emulsion after being crushed, so that the mass transfer efficiency and the reaction efficiency between the anthraquinone derivative-containing working solution and the hydrogen are enhanced within the range of preset operating conditions.
2. The system for preparing hydrogen peroxide based on the anthraquinone process according to claim 1, wherein the micro-interface generator comprises:
the first micro-interface generator is arranged at the bottom of the reaction zone of the hydrogenation tower and used for crushing hydrogen to form micron-sized bubbles, outputting the micron-sized bubbles to the hydrogenation tower after the crushing is finished, and mixing the micron-sized bubbles with the anthraquinone derivative-containing working solution in the hydrogenation tower to form a gas-liquid emulsion;
and the second micro-interface generator is arranged at the bottom of the reaction zone of the oxidation tower and used for crushing oxygen to form micron-scale bubbles, outputting the micron-scale bubbles to the hydrogenation tower after the crushing is finished, and mixing the micron-scale bubbles with the 2-ethyl hydrogen anthraquinone solution in the oxidation tower to form a gas-liquid emulsion.
3. The system for preparing hydrogen peroxide based on the anthraquinone process according to claim 1, wherein the hydrogenation tower comprises:
a hydrogen feeding pipeline which is arranged on the side wall of the hydrogenation tower and is connected with the first micro-interface generator, and is used for conveying hydrogen to the first micro-interface generator so that the first micro-interface generator can crush the hydrogen;
a working liquid feed pipe provided on the side wall of the hydrogen column above the hydrogen feed pipe for feeding the working liquid containing the anthraquinone derivative to the inside of the hydrogenation column;
the catalyst feeding hole is arranged on the side wall of the hydrogenation tower and positioned above the working solution feeding pipeline and used for placing the catalyst into the hydrogenation tower;
and the first tail gas outlet is arranged at the top of the hydrogenation tower and used for discharging tail gas.
4. The system for preparing hydrogen peroxide based on the anthraquinone process according to claim 1, wherein the oxidation tower comprises:
the air feeding pipeline is arranged on the side wall of the oxidation tower, is connected with the second micro-interface generator and is used for conveying air to the second micro-interface generator so that the second micro-interface generator can crush the air;
a hydrogenation liquid feed pipe disposed on the side wall of the oxidation tower above the air feed pipe for feeding the 2-ethylhydroanthraquinone solution to the inside of the oxidation tower;
the return pipe is arranged on the side wall of the oxidation tower and is used for returning the material output by the oxidation tower to the oxidation tower so as to enable the 2-ethyl hydrogen anthraquinone solution in the material to fully react;
the circulating pump is connected with the return pipe and is used for providing feedback power for the material output by the return pipe;
the second tail gas outlet is arranged at the top of the oxidation tower and used for discharging air;
and the discharge hole is arranged on the side wall of the oxidation tower and used for discharging the mixture of the 2-ethyl anthraquinone and the hydrogen peroxide.
5. The system for preparing hydrogen peroxide based on the anthraquinone process according to claim 1, wherein the filtering and cooling unit comprises:
the filter is arranged at the upper part of the side wall of the hydrogenation tower, is connected with the liquid output end of the gas-liquid separator and is used for filtering the hydrogenated material output by the hydrogenation tower so as to filter solid impurities carried in the material;
the heat exchanger is connected with the filter and used for exchanging heat between the material output by the filter and the working solution containing the anthraquinone derivative so as to maintain the working solution containing the anthraquinone derivative within a preset temperature range;
and the hydrogenation cooler is arranged in the middle of the side wall of the hydrogenation tower, is connected with the heat exchanger and is used for cooling the heat-exchanged materials.
6. The system for preparing hydrogen peroxide based on the anthraquinone process according to claim 1, wherein the extraction tower comprises:
a pure water feed pipe arranged at the top of the extraction tower for conveying pure water to the inside of the extraction tower;
the heater is connected with the pure water feeding pipeline and is used for preheating the pure water;
the pure water acidification metering pump is connected with the pure water feeding pipeline, is positioned below the heater and is used for adding phosphoric acid to adjust the acidity of the pure water;
the pure water pump is connected with the pure water feeding pipeline, is positioned below the pure water acidification metering pump and is used for conveying pure water;
and the hydrogen peroxide discharge pipeline is arranged at the bottom of the extraction tower and used for outputting hydrogen peroxide.
7. A technology for preparing hydrogen peroxide based on an anthraquinone method is characterized by comprising the following steps:
step 1: feeding the anthraquinone derivative-containing working solution into the hydrogenation tower through the working solution feeding pipeline, and feeding the catalyst into the hydrogenation tower through the catalyst feeding hole;
step 2: hydrogen is conveyed into the hydrogenation tower through the hydrogen feeding pipeline, the hydrogen feeding pipeline conveys the hydrogen to the first micro-interface generator, the first micro-interface generator breaks the hydrogen to form micron-scale micron-sized bubbles, and after breaking is completed, the micron-scale bubbles are output to the hydrogenation tower by the first micro-interface generator and are mixed with the anthraquinone derivative-containing working solution to form a gas-liquid emulsion;
and step 3: carrying out hydrogenation reaction on the gas-liquid emulsion under the action of a catalyst to generate a mixture containing a 2-ethyl hydrogen anthraquinone solution, and after the reaction is finished, enabling the mixture to flow upwards and enter a gas-liquid separator;
and 4, step 4: after the mixture enters the gas-liquid separator, tail gas is discharged from the top of the gas-liquid separator, and hydrogenated liquid containing 2-ethyl hydrogen anthraquinone is discharged from the side surface of the gas-liquid separator and enters the filtering and cooling unit;
and 5: after the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone enters the filter, solid impurities carried in the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone remain in the filter, filtrate in the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone is discharged from the bottom of the filter and enters the heat exchanger, the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone in the heat exchanger exchanges heat with working liquid containing anthraquinone derivatives, the working liquid containing anthraquinone derivatives after heat exchange flows into the working liquid feeding pipeline, the hydrogenated liquid containing 2-ethyl hydrogen anthraquinone after heat exchange enters the hydrogenation cooler, and the cooled hydrogenated liquid containing 2-ethyl hydrogen anthraquinone enters the oxidation tower;
step 6: conveying the hydrogenated liquid containing 2-ethyl hydroanthraquinone into the oxidation tower through the hydrogenated liquid feeding pipeline, wherein the air feeding pipeline can convey air to the second micro-interface generator, the second micro-interface generator is used for crushing the air to form micron-sized bubbles, and after the crushing is finished, the second micro-interface generator outputs the micron-sized bubbles to the oxidation tower and mixes the micron-sized bubbles with the hydrogenated liquid containing 2-ethyl hydroanthraquinone to form a gas-liquid emulsion;
and 7: the gas-liquid emulsion is subjected to oxidation reaction to generate a mixture containing 2-ethylanthraquinone and hydrogen peroxide, after the reaction is finished, the mixture flows upwards and flows back to the oxidation tower along the return pipe, a small amount of tail gas moves upwards and is discharged through the second tail gas outlet, and the mixture of the 2-ethylanthraquinone and the hydrogen peroxide after the tail gas is discharged is output to the oxidation tower through the discharge hole;
and 8: the mixture of the 2-ethyl anthraquinone and the hydrogen peroxide is transmitted to the bottom of the extraction tower through a discharge hole, pure water is transmitted into the heater through the pure water pump and is regulated by the pure water acidification metering pump, preheated pure water enters the inside of the extraction tower along the pure water feeding pipeline and is extracted with the mixture of the 2-ethyl anthraquinone and the hydrogen peroxide, and the extracted hydrogen peroxide is output to the extraction tower along the hydrogen peroxide discharging pipeline.
8. A process for preparing hydrogen peroxide based on the anthraquinone process as claimed in claim 7, wherein the reaction temperature in the hydrogenation tower in the process is 38-48 ℃, and the reaction pressure is 0.05-0.50 MPa.
9. The process for preparing dioxygen-0 water based on anthraquinone method as claimed in claim 7, wherein the reaction temperature in the oxidation tower in said process is 35-45 ℃ and the reaction pressure is 0.10-0.20 MPa.
10. The process for preparing hydrogen peroxide based on the anthraquinone process as claimed in claim 7, wherein the gas-liquid ratio in the first micro-interface generator is 300-500: 1, the gas-liquid ratio in the second micro-interface generator is 400-: 1.
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| CN201910867789.3A CN112499592A (en) | 2019-09-14 | 2019-09-14 | System and process for preparing hydrogen peroxide based on anthraquinone method |
| PCT/CN2019/120126 WO2021047044A1 (en) | 2019-09-14 | 2019-11-22 | System and process for preparing hydrogen peroxide based on anthraquinone process |
| PCT/CN2019/120115 WO2021047038A1 (en) | 2019-09-14 | 2019-11-22 | Exhaust gas dust removal system and exhaust gas dust removal method using same |
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