CN116477579A - Method for improving extraction yield and product quality of hydrogen peroxide produced by anthraquinone process - Google Patents
Method for improving extraction yield and product quality of hydrogen peroxide produced by anthraquinone process Download PDFInfo
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- CN116477579A CN116477579A CN202310180454.0A CN202310180454A CN116477579A CN 116477579 A CN116477579 A CN 116477579A CN 202310180454 A CN202310180454 A CN 202310180454A CN 116477579 A CN116477579 A CN 116477579A
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- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 title claims abstract description 511
- 238000000605 extraction Methods 0.000 title claims abstract description 81
- 238000000034 method Methods 0.000 title claims abstract description 79
- PYKYMHQGRFAEBM-UHFFFAOYSA-N anthraquinone Natural products CCC(=O)c1c(O)c2C(=O)C3C(C=CC=C3O)C(=O)c2cc1CC(=O)OC PYKYMHQGRFAEBM-UHFFFAOYSA-N 0.000 title claims abstract description 55
- 150000004056 anthraquinones Chemical class 0.000 title claims abstract description 55
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims abstract description 132
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 71
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims abstract description 66
- 230000003647 oxidation Effects 0.000 claims abstract description 63
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000000746 purification Methods 0.000 claims abstract description 39
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 34
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 34
- 208000005156 Dehydration Diseases 0.000 claims abstract description 28
- 230000018044 dehydration Effects 0.000 claims abstract description 28
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 28
- 238000000926 separation method Methods 0.000 claims abstract description 27
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 238000004519 manufacturing process Methods 0.000 claims abstract description 15
- 238000004581 coalescence Methods 0.000 claims abstract description 11
- 238000004064 recycling Methods 0.000 claims abstract description 10
- 238000002156 mixing Methods 0.000 claims abstract description 9
- 239000000945 filler Substances 0.000 claims description 63
- 238000012856 packing Methods 0.000 claims description 21
- 239000012141 concentrate Substances 0.000 claims description 17
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 16
- 229910001220 stainless steel Inorganic materials 0.000 claims description 16
- 239000010935 stainless steel Substances 0.000 claims description 16
- 239000000126 substance Substances 0.000 claims description 10
- 238000013329 compounding Methods 0.000 claims description 8
- YEVQZPWSVWZAOB-UHFFFAOYSA-N 2-(bromomethyl)-1-iodo-4-(trifluoromethyl)benzene Chemical compound FC(F)(F)C1=CC=C(I)C(CBr)=C1 YEVQZPWSVWZAOB-UHFFFAOYSA-N 0.000 claims description 7
- 239000002798 polar solvent Substances 0.000 claims description 6
- AKIIJALHGMKJEJ-UHFFFAOYSA-N (2-methylcyclohexyl) acetate Chemical compound CC1CCCCC1OC(C)=O AKIIJALHGMKJEJ-UHFFFAOYSA-N 0.000 claims description 5
- SNDGLCYYBKJSOT-UHFFFAOYSA-N 1,1,3,3-tetrabutylurea Chemical compound CCCCN(CCCC)C(=O)N(CCCC)CCCC SNDGLCYYBKJSOT-UHFFFAOYSA-N 0.000 claims description 4
- SJEBAWHUJDUKQK-UHFFFAOYSA-N 2-ethylanthraquinone Chemical compound C1=CC=C2C(=O)C3=CC(CC)=CC=C3C(=O)C2=C1 SJEBAWHUJDUKQK-UHFFFAOYSA-N 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 3
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 3
- MAKLMMYWGTWPQM-UHFFFAOYSA-N 2-butylanthracene-9,10-dione Chemical compound C1=CC=C2C(=O)C3=CC(CCCC)=CC=C3C(=O)C2=C1 MAKLMMYWGTWPQM-UHFFFAOYSA-N 0.000 claims description 2
- HXQPUEQDBSPXTE-UHFFFAOYSA-N Diisobutylcarbinol Chemical compound CC(C)CC(O)CC(C)C HXQPUEQDBSPXTE-UHFFFAOYSA-N 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims description 2
- 239000000047 product Substances 0.000 description 27
- 239000000243 solution Substances 0.000 description 22
- 238000010521 absorption reaction Methods 0.000 description 12
- 238000002360 preparation method Methods 0.000 description 12
- 230000000052 comparative effect Effects 0.000 description 10
- 239000012224 working solution Substances 0.000 description 10
- 230000000694 effects Effects 0.000 description 8
- 238000005984 hydrogenation reaction Methods 0.000 description 7
- 239000011347 resin Substances 0.000 description 7
- 229920005989 resin Polymers 0.000 description 7
- 239000000463 material Substances 0.000 description 4
- UMWZLYTVXQBTTE-UHFFFAOYSA-N 2-pentylanthracene-9,10-dione Chemical compound C1=CC=C2C(=O)C3=CC(CCCCC)=CC=C3C(=O)C2=C1 UMWZLYTVXQBTTE-UHFFFAOYSA-N 0.000 description 3
- 239000002131 composite material Substances 0.000 description 3
- 239000012024 dehydrating agents Substances 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- 239000003381 stabilizer Substances 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 239000007857 degradation product Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000012454 non-polar solvent Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- -1 anthraquinone compounds Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
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
- C01B15/013—Separation; Purification; Concentration
-
- 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
- Y02P20/10—Process efficiency
Abstract
The invention relates to the technical field of hydrogen peroxide production, and discloses a method for improving extraction yield and product quality of hydrogen peroxide produced by an anthraquinone process, which comprises the following steps: (1) Extracting the oxidation liquid by an extraction tower, obtaining raffinate from the tower top and obtaining crude hydrogen peroxide from the tower bottom; (2) Mixing the raffinate with the phosphoric acid concentrated solution, and then carrying out dehydration treatment to obtain a phosphoric acid solution containing hydrogen peroxide, wherein the hydrogen peroxide contained in the raffinate is brought into the crude hydrogen peroxide by preparing water for extraction in the step (1) and then entering the extraction tower again; (3) And (3) sequentially carrying out purification treatment and coalescence separation treatment on the crude hydrogen peroxide, entering the tower from the top of the stripping tower, carrying out countercurrent contact with air entering from the bottom of the stripping tower to carry out stripping, and finally producing hydrogen peroxide from the bottom of the stripping tower to obtain a hydrogen peroxide finished product. The invention improves the extraction yield of the hydrogen peroxide by recycling the hydrogen peroxide in the raffinate, can reduce the total organic carbon content and improves the quality of the hydrogen peroxide product.
Description
Technical Field
The invention relates to the technical field of hydrogen peroxide preparation, in particular to a method for improving extraction yield and product quality of hydrogen peroxide produced by an anthraquinone process.
Background
Hydrogen peroxide is widely used in many fields such as paper making, textile, chemical industry, environmental protection, electronic component manufacturing, and the like. The current industrial hydrogen peroxide production method is an anthraquinone method, which takes alkylanthraquinone dissolved in a mixed organic solvent as a carrier for cyclic hydrogenation and oxidation, and obtains hydrogen peroxide with a certain concentration through a series of procedures such as hydrogenation, oxidation, extraction, post-treatment and the like, wherein the anthraquinone plays a role of a working carrier, and hydrogen peroxide is produced through repeated hydrogenation and oxidation.
Since the density difference between the working fluid at the middle and upper parts of the extraction tower and the water is very small, the difference is generally only 60 to 80kg/m 3 The oil-water separation efficiency of the working solution at the middle and upper parts of the extraction tower and water is greatly reduced, a small amount of water is inevitably entrained in the working solution which is extracted from the extraction tower, namely raffinate, and a small amount of hydrogen peroxide is dissolved in the water, so that the raffinate contains hydrogen peroxide with lower concentration. The hydrogen peroxide content of the raffinate is referred to in industry as raffinate and is required to be not more than 0.3g/L. If the content of hydrogen peroxide in raffinate is too high, the extraction yield of hydrogen peroxide is reduced, the yield of hydrogen peroxide is directly affected, hydrogenation reaction is not facilitated, and more serious, the problem that the hydrogen peroxide is decomposed by a hydrogenation catalyst to bring potential safety hazard exists. In the prior safety accidents of the hydrogen peroxide production device, most of the safety accidents are caused by overhigh extraction residues. If the hydrogen peroxide content in the raffinate can be reduced, the method has positive significance for improving the extraction yield and the operation safety of the device.
Anthraquinone process uses anthraquinone as carrier for cyclic hydrogenation and oxidation, and dissolves the anthraquinone in polar solvent and nonpolar solvent to form working solution, wherein the nonpolar solvent is mainly used for dissolving anthraquinone, and heavy aromatic hydrocarbon is usually adopted; polar solvents are mainly used to dissolve the hydroanthraquinones produced by the hydrogenation of the anthraquinones, typically trioctyl phosphate and/or 2-methylcyclohexyl acetate. In addition, anthraquinone can gradually undergo side reactions in the long-term use process to generate anthraquinone degradation products, so that the composition of the working solution is more complex. Because of the solubility differences of different solvents, anthraquinone and anthraquinone degradation products in hydrogen peroxide, especially some polar organic compounds are more easily dissolved in polar hydrogen peroxide, so that a small amount of organic substances are inevitably dissolved or entrained in the hydrogen peroxide product in the extraction process. At present, most hydrogen peroxide devices adopt a purification tower added behind an extraction tower, aromatic hydrocarbon is used for treating hydrogen peroxide products so as to further reduce the total organic carbon content, but the total organic carbon content in the hydrogen peroxide products coming out of the purification tower is still higher, generally more than 150ppm, and when the production working condition is poor, the total organic carbon exceeds the index of 250ppm of the total organic carbon in hydrogen peroxide specified by GB/T1616-2014, and the products are light yellow, turbid and have larger peculiar smell, thus influencing the product quality. On the other hand, in order to avoid the adverse effect of macromolecular organic matters on the catalyst or product quality of the downstream device, the total organic carbon content in the hydrogen peroxide is required to be far lower than 250ppm in partial use cases.
The total organic carbon content in the hydrogen peroxide is greatly reduced by resin purification in industry, however, when the total organic carbon content in the hydrogen peroxide fed into the resin adsorption bed is higher, the load of a resin purification device is increased, the switching and regeneration frequency of the resin adsorption bed is also increased, and the production cost is obviously increased and the environmental protection pressure is also increased due to the fact that a large amount of waste water is generated in the switching and regeneration process of the resin bed. In addition, because hydrogen peroxide has stronger oxidizing property, the frequent switching and regeneration of the resin bed also increase the safety production risk. Therefore, on the premise of keeping economy, the total organic carbon content in the hydrogen peroxide product produced by the device is reduced by adopting proper measures, so that the product quality is improved, and the method has economic value and positive significance in both direct selling of the hydrogen peroxide product and prolonging of the switching period of the downstream resin adsorption bed.
Disclosure of Invention
In order to solve the technical problems, the invention aims to provide a method for improving the extraction yield and the product quality of hydrogen peroxide produced by an anthraquinone process, which can reduce the hydrogen peroxide content in raffinate, improve the extraction yield of hydrogen peroxide, reduce the total organic carbon content in hydrogen peroxide products and improve the quality of hydrogen peroxide products.
The aim of the invention is realized by the following technical scheme: the invention provides a method for improving extraction yield and product quality of hydrogen peroxide produced by an anthraquinone process, which comprises the following steps:
(1) Extracting the oxidation liquid by an extraction tower, obtaining raffinate from the tower top and obtaining crude hydrogen peroxide from the tower bottom;
(2) Mixing the raffinate with the phosphoric acid concentrated solution, and then carrying out dehydration treatment to obtain a phosphoric acid solution containing hydrogen peroxide, wherein the hydrogen peroxide contained in the raffinate is brought into the crude hydrogen peroxide by preparing water for extraction in the step (1) and then entering the extraction tower again; (3) And (3) sequentially carrying out purification treatment and coalescence separation treatment on the crude hydrogen peroxide, entering the tower from the top of the stripping tower, carrying out countercurrent contact with air entering from the bottom of the stripping tower to carry out stripping, and finally producing hydrogen peroxide from the bottom of the stripping tower to obtain a hydrogen peroxide finished product.
The invention mixes the raffinate and the phosphoric acid concentrated solution, and the density difference between the raffinate and the phosphoric acid concentrated solution can reach 300kg/m 3 The wastewater enters a dehydration tank for dehydration treatment, so that layering of an oil phase and a water phase can be accelerated, and the hydrogen peroxide content in the raffinate is reduced. Because phosphoric acid is required to be used as a stabilizer in the extraction process of producing hydrogen peroxide by the anthraquinone method, the phosphoric acid concentrate containing hydrogen peroxide can be used for preparing extraction water in an extraction tower, hydrogen peroxide and the phosphoric acid stabilizer can be simultaneously brought into water, and then hydrogen peroxide contained in raffinate enters the extraction tower again and is produced in a crude hydrogen peroxide form after being extracted by water, so that the hydrogen peroxide product can be entered, and the extraction efficiency is improved.
The crude hydrogen peroxide from the bottom of the extraction tower passes through the purification tower, and a hydrogen peroxide coalescer is arranged at the bottom of the purification tower, so that the aim of reducing the total organic carbon content in the hydrogen peroxide from the purification tower as much as possible is fulfilled.
Because anthraquinone compounds are difficult to remove by steam stripping, the hydrogen peroxide subjected to purification and coalescence filler separation treatment enters a steam stripping tower, air is utilized to strip the hydrogen peroxide, and the total organic carbon content in the hydrogen peroxide product after steam stripping is obviously reduced. The method can obviously reduce the total organic carbon content in the hydrogen peroxide under the premise of not increasing material consumption and negligible energy consumption loss.
Preferably, in the step (2), the mass fraction of phosphoric acid in the phosphoric acid concentrate is 40-80%; the mass ratio of the raffinate to the phosphoric acid concentrate is 200-500: 1.
the phosphoric acid concentrated solution is used as a raffinate dehydrating agent, the phosphoric acid diluted solution absorbed with hydrogen peroxide enters a concentrating tank for concentrating, and the phosphoric acid concentrated solution is returned to be used as the raffinate dehydrating agent for recycling. Since phosphoric acid is used as a stabilizer in the extraction process, no additional material is consumed for the system.
In the step (2), a dehydration tank is adopted for dehydration treatment, and a coalescing separation filler compounded by 316L stainless steel filler and PP filler is arranged in the dehydration tank; and the phosphoric acid solution containing hydrogen peroxide enters a concentration tank for concentration, and the phosphoric acid concentrate is obtained again for recycling.
Preferably, in the step (3), the purifying treatment is: purifying by countercurrent contact of heavy aromatic hydrocarbon and hydrogen peroxide, arranging a hydrogen peroxide coalescer at the bottom of the purifying tower, and discharging purified hydrogen peroxide from the bottom of the tower after coalescence and separation; the purifying tower is a plate tower or a filler tower, and the separation filler in the hydrogen peroxide coalescer is formed by compounding 316L stainless steel filler and PP filler or compounding 316L stainless steel filler and PTFE filler.
Preferably, the stripping tower is a packed tower, the top of the stripping tower is provided with a hydrogen peroxide feeding distributor, the lower part of the hydrogen peroxide feeding distributor is provided with a packing supported on a grid, and the lower part of the packing is provided with an air feeding distributor.
Preferably, in the step (3), the hydrogen peroxide feeding distributor is one of a tubular distributor, a trough distributor or a disk distributor; the air feeding distributor is a tubular distributor or a trough distributor; the filler is one of a pall ring, a ladder ring, a conjugate ring or a saddle ring.
Preferably, in step (3), the stripping is: the ratio of the hydrogen peroxide volumetric flow rate to the air volumetric flow rate entering the stripping tower is 1:6-45, the operation temperature of the stripping tower is 20-60 ℃, the air pressure is 0.05-0.60 MPaG, and the operation pressure does not need to be regulated after entering the stripping tower.
When the amount of hydrogen peroxide entering the stripping tower is fixed, the amount of the air entering the stripping tower is too small, the contact time of the hydrogen peroxide and the air is too short, the stripping effect can be greatly reduced, and even the stripping effect cannot be achieved; excessive air entering the stripping tower can cause the excessively high gas content in the tower, the residence time of hydrogen peroxide is too short and even atomized, and the stripping effect is reduced.
When the stripping temperature is too low, the stripping effect is obviously reduced; when the stripping temperature is too high, the decomposition of hydrogen peroxide is aggravated, so that hydrogen peroxide materials are lost and safety risks are brought. The operating pressure of the stripping tower depends on the air pressure before entering the oxidation tower, and a pressure reducing regulating valve is not required to be arranged on an air line entering the stripping tower, so that the energy loss of the compressed air is negligible.
Preferably, in the step (3), the air entering from the bottom of the stripping tower is compressed air before entering the oxidation tower in the process of producing hydrogen peroxide by the anthraquinone process, and the air containing a small amount of organic matters and hydrogen peroxide after being discharged from the stripping tower returns to the oxidation tower before finally entering the oxidation tower to participate in the oxidation reaction.
The air is compressed air before entering the oxidation tower in the process of producing hydrogen peroxide by the anthraquinone method, a decompression regulating valve is not arranged on an air pipeline entering the stripping tower, the operation pressure of the stripping tower is the same as that of the compressed air before entering the oxidation tower, and the energy loss is reduced to the greatest extent. The stripped air containing a small amount of organic matters and hydrogen peroxide, which is discharged from the stripping tower, returns to the oxidation tower before finally entering the oxidation tower to participate in the oxidation reaction of the hydrogenated liquid. Because the air before entering the oxidation tower is used for stripping the hydrogen peroxide, the air containing trace organic matters and the hydrogen peroxide after stripping is returned to the oxidation tower without additional consumption of air or configuration of an air compressor, and because the oxidation tower contains the working solution and the hydrogen peroxide at the same time, the method skillfully solves the problem of the going of the air containing trace organic matters and the hydrogen peroxide after stripping, and has no pollution to the environment.
Preferably, the total organic carbon substances in the hydrogen peroxide produced by the anthraquinone process comprise anthraquinone, heavy aromatic hydrocarbon and polar solvent.
Preferably, the anthraquinone is at least one of 2-ethyl anthraquinone, 2-butyl anthraquinone and 2-amyl anthraquinone; the polar solvent is at least one of trioctyl phosphate, 2-methylcyclohexyl acetate, tetrabutyl urea and diisobutyl methanol.
Compared with the prior art, the invention has the following beneficial effects:
by mixing concentrated phosphoric acid as dehydrating agent with raffinate, the density difference of water and oil phase reaches 300kg/m 3 The method increases the oil-water layering efficiency by 4 to 5 times, and greatly improves the oil-water layering efficiency, and then separates the oil-water layering efficiency through the coalescence-separation filler in the dehydration tank, so that the hydrogen peroxide content in the raffinate can be effectively reduced, the hydrogen peroxide yield during extraction is improved, and the system safety risk is reduced; the diluted phosphoric acid after water absorption is concentrated and then returned to the system for recycling, so that the consumption of phosphoric acid is not increased additionally;
the purification tower and the stripping tower are used in series, partial organic matters carried in the hydrogen peroxide, especially anthraquinone matters which are difficult to strip off, are separated and removed through the purification tower and the hydrogen peroxide coalescer, and then the air is used for stripping, so that the aim of remarkably reducing the total organic carbon content in the hydrogen peroxide is fulfilled;
the air used by the stripping tower is derived from the air before the hydrogen peroxide production device enters the oxidation tower, and the air containing trace organic matters and hydrogen peroxide after stripping does not need to consume air or be provided with an air compressor before returning to the oxidation tower, so that the problem of going to the air containing trace organic matters and hydrogen peroxide after stripping is solved, and the total organic carbon content in the hydrogen peroxide product can be obviously reduced on the premise of not increasing material consumption and having negligible energy consumption loss;
the method is suitable for various anthraquinone working solution systems, can obviously reduce the hydrogen peroxide content in the raffinate and the total organic carbon content in the hydrogen peroxide product on the premise of not increasing the production cost basically, and improves the extraction yield and the quality of the hydrogen peroxide product.
Drawings
FIG. 1 is a schematic diagram of the apparatus used in the method of the present invention.
The reference numerals are: the device comprises an extraction tower 1, a purification tower 2, a purification tower bypass 3, a heat exchanger 4, a hydrogen peroxide coalescer 5, a hydrogen peroxide coalescer bypass 6, a stripping tower 7, a stripping tower bypass 8, an oxidation tower air main pipe 9, a stripping tower air pipeline 10, a stripping tower air pipeline 11, an oxidation tower 12, a hydrogen peroxide 13, a mixer 14, a dehydration tank 15, a concentration tank 16, a raffinate 17, a dehydrated raffinate 18, a phosphoric acid thin solution 19 after water absorption, a phosphoric acid thick solution 20 after concentration and an extraction water preparation tank 21.
Detailed Description
The technical scheme of the present invention is described below by using specific examples, but the scope of the present invention is not limited thereto:
general examples
A method for improving extraction yield and product quality of hydrogen peroxide produced by an anthraquinone process comprises the following steps:
(1) After the oxidation liquid obtained by the anthraquinone method hydrogen peroxide production is extracted by the extraction tower 1, crude hydrogen peroxide is obtained from the bottom of the tower, and raffinate 17 is obtained from the top of the tower as shown in fig. 1.
(2) Mixing raffinate 17 from the top of an extraction tower 1 with phosphoric acid concentrated solution 20 in a mixer 14, then entering a dehydration tank 15 for dehydration treatment, wherein 316L stainless steel filler and PP filler composite coalescence-separation filler are arranged in the dehydration tank 15, and a dehydrated raffinate 18 and a phosphoric acid diluted solution 19 after water absorption are obtained; the phosphoric acid thin liquid 19 after water absorption enters a concentrating tank 16 for concentrating, and the obtained concentrated phosphoric acid thick liquid 20 returns to the mixer 14 for recycling; in addition, after the concentration, the phosphoric acid concentrate 20 contains hydrogen peroxide, and after the hydrogen peroxide reaches a certain concentration, the water for extraction in the preparation step (1) is prepared by entering the extraction water preparation tank 21, and then enters the extraction tower again, so that the hydrogen peroxide contained in the raffinate is brought into the crude hydrogen peroxide.
(3) The crude hydrogen peroxide from the bottom of the extraction tower 1 enters a purification tower 2 for purification treatment, the purification tower 2 is a plate tower or a filler tower, the purification treatment is purification by countercurrent contact of heavy aromatic hydrocarbon and hydrogen peroxide, a hydrogen peroxide coalescer 5 is arranged at the tower kettle of the purification tower 2, coalescing separation filler is arranged, and 316L filler and PP filler are compounded or 316L stainless steel filler and PTFE filler are compounded.
(4) The hydrogen peroxide which is subjected to purification and coalescence separation treatment to remove part of oil phase substances enters a stripping tower 7, the stripping tower 7 is a filler tower, the filler used is one of a pall ring, a stepped ring, a conjugated ring or a saddle ring, the top of the stripping tower 7 is provided with a hydrogen peroxide feeding distributor, the hydrogen peroxide feeding distributor is one of a tubular distributor, a groove type distributor or a disc type distributor, the filler supported on a grid is arranged below the hydrogen peroxide feeding distributor, an air feeding distributor is arranged below the filler, and the air feeding distributor is the tubular distributor or the groove type distributor; hydrogen peroxide enters the tower from the top of the stripping tower 7, and is in countercurrent contact with air entering from the bottom of the stripping tower 7 for stripping, the ratio of the volumetric flow rate of the hydrogen peroxide entering the stripping tower 7 to the volumetric flow rate of the air entering the stripping tower 7 in a standard state is 1:5-40, the operating temperature of the stripping tower 7 is 20-60 ℃, the operating pressure is 0.05-0.60 MPaG, and the hydrogen peroxide after stripping is produced from the bottom of the tower to obtain produced hydrogen peroxide 13.
In addition, the air adopted in the stripping tower is compressed air before entering the oxidation tower 12 in the process of producing hydrogen peroxide by an anthraquinone method, the air is connected with an air inlet stripping air pipeline 10 from an air main pipe 9 entering the oxidation tower 12, enters the tower from the bottom of the stripping tower 7, is in countercurrent contact with hydrogen peroxide in the stripping tower 7, returns to the air main pipe 9 entering the oxidation tower 12 from an air outlet stripping tower air pipeline 11, and finally enters the oxidation tower 12 to participate in oxidation reaction before the air which is led out from the stripping tower 7 returns to the oxidation tower 12.
The purifying tower bypass 3, the hydrogen peroxide coalescer bypass 6 and the stripping tower bypass 8 are used for checking the effect of the related towers, and are convenient for overhauling and maintaining each tower.
Examples 1 to 4
A method for improving extraction yield and product quality of hydrogen peroxide produced by an anthraquinone process comprises the following steps:
(1) The anthraquinone working solution system for producing hydrogen peroxide is a mixed solution composed of 2-ethyl anthraquinone, heavy aromatic hydrocarbon, trioctyl phosphate and 2-methylcyclohexyl acetate. And extracting the obtained oxidation liquid by the extraction tower 1 to obtain crude hydrogen peroxide from the bottom of the extraction tower, wherein the total organic carbon content in the crude hydrogen peroxide is 315ppm.
(2) Mixing raffinate 17 (400 parts by mass) with phosphoric acid concentrated solution 20 (1 part by mass, phosphoric acid content 75 wt%) in a mixer 14, then entering a dehydration tank 15 for dehydration treatment, wherein 316L of coalescence-separation filler compounded by stainless steel filler and PP filler is arranged in the dehydration tank 15, and obtaining dehydrated raffinate 18 and phosphoric acid diluted solution 19 after water absorption; the phosphoric acid thin liquid 19 after water absorption enters the concentration tank 16 for concentration, and the obtained concentrated phosphoric acid thick liquid 20 returns to the mixer 14 for recycling.
In addition, after the concentration, the phosphoric acid concentrate 20 contains hydrogen peroxide, and after the hydrogen peroxide reaches a certain concentration, the water for extraction in the preparation step (1) is prepared by entering the extraction water preparation tank 21, and then enters the extraction tower again, so that the hydrogen peroxide contained in the raffinate is brought into the crude hydrogen peroxide.
(3) The crude hydrogen peroxide enters a purifying tower 2 (a filler tower) for purification treatment, heavy aromatic hydrocarbon and hydrogen peroxide are in countercurrent contact for purification, a hydrogen peroxide coalescer 5 is arranged at the tower bottom of the purifying tower 2, coalescing separation filler (316L stainless steel filler and PP filler are adopted for compounding) is arranged, and the total organic carbon content in the purified hydrogen peroxide is 233ppm.
(4) Hydrogen peroxide which is subjected to purification and coalescence separation treatment to remove part of oil phase substances enters a stripping tower 7 (a packing tower, wherein the packing is pall rings), a hydrogen peroxide feeding distributor (a tubular distributor) is arranged at the top of the stripping tower 7, the packing supported on a grid is arranged below the hydrogen peroxide feeding distributor, and an air feeding distributor (a groove type distributor) is arranged below the packing; hydrogen peroxide enters the tower from the top of the stripping tower 7, and is in countercurrent contact with air entering from the bottom of the stripping tower 7 for stripping, the operating temperature of the stripping tower 7 is 45 ℃, the operating pressure is the same as the oxidation pressure and is 0.21MPaG, and the hydrogen peroxide after stripping is produced from the bottom of the tower.
In examples 1-4, the ratio of the volumetric flow rate of hydrogen peroxide into the stripping column 7 to the volumetric flow rate of air into the stripping column 7 at standard conditions was 1:5, 1:10, 1:20, 1:35, respectively.
In addition, the air adopted in the stripping tower is compressed air before entering the oxidation tower 12 in the process of producing hydrogen peroxide by an anthraquinone method, the air is connected with a stripping air pipeline 10 from an air main pipe 9 entering the oxidation tower 12, enters the tower from the bottom of the stripping tower 7 and is in countercurrent contact with hydrogen peroxide in the stripping tower 7, the air returned from an air path 11 at the top of the stripping tower to the air main pipe 9 entering the oxidation tower 12, and the air after being led out by the stripping tower 7 is returned to the oxidation tower 12 and finally enters the oxidation tower 12 to participate in oxidation reaction, and the operation pressure of the stripping tower 7 is the same as the oxidation pressure, so that the process does not need to adjust the air pressure again.
Example 5
A method for improving extraction yield and product quality of hydrogen peroxide produced by an anthraquinone process comprises the following steps:
(1) The anthraquinone working solution for producing hydrogen peroxide is a mixed system consisting of 2-amyl anthraquinone, heavy aromatic hydrocarbon, trioctyl phosphate and 2-methylcyclohexyl acetate. And extracting the obtained oxidation liquid by the extraction tower 1 to obtain crude hydrogen peroxide from the bottom of the extraction tower, wherein the total organic carbon content in the crude hydrogen peroxide is 338ppm.
(2) Mixing raffinate 17 (400 parts by mass) with phosphoric acid concentrated solution 20 (1 part by mass, phosphoric acid content 75 wt%) in a mixer 14, then entering a dehydration tank 15 for dehydration treatment, wherein 316L of coalescence-separation filler compounded by stainless steel filler and PP filler is arranged in the dehydration tank 15, and obtaining dehydrated raffinate 18 and phosphoric acid diluted solution 19 after water absorption; the phosphoric acid thin liquid 19 after water absorption enters the concentration tank 16 for concentration, and the obtained concentrated phosphoric acid thick liquid 20 returns to the mixer 14 for recycling.
In addition, after the concentration, the phosphoric acid concentrate 20 contains hydrogen peroxide, and after the hydrogen peroxide reaches a certain concentration, the water for extraction in the preparation step (1) is prepared by entering the extraction water preparation tank 21, and then enters the extraction tower again, so that the hydrogen peroxide contained in the raffinate is brought into the crude hydrogen peroxide.
(3) The crude hydrogen peroxide enters a purifying tower 2 (a filler tower) for purification treatment, heavy aromatic hydrocarbon and hydrogen peroxide are in countercurrent contact for purification, a hydrogen peroxide coalescer 5 is arranged at the tower bottom of the purifying tower 2, coalescing separation filler (316L stainless steel filler and PP filler are adopted for compounding) is arranged, and the total organic carbon content in the purified hydrogen peroxide is 256ppm.
(4) Hydrogen peroxide which is subjected to purification and coalescence separation treatment to remove part of oil phase substances enters a stripping tower 7 (a packing tower, wherein the packing is pall rings), a hydrogen peroxide feeding distributor (a tubular distributor) is arranged at the top of the stripping tower 7, the packing supported on a grid is arranged below the hydrogen peroxide feeding distributor, and an air feeding distributor (a groove type distributor) is arranged below the packing; hydrogen peroxide enters the tower from the top of the stripping tower 7, and is in countercurrent contact with air entering from the bottom of the stripping tower 7 for stripping, the ratio of the volumetric flow rate of the hydrogen peroxide entering the stripping tower 7 to the volumetric flow rate of the air entering the stripping tower 7 in a standard state is 1:10, the operating temperature of the stripping tower 7 is 45 ℃, the operating pressure is the same as the oxidation pressure and is 0.21MPaG, and the hydrogen peroxide after stripping is produced from the bottom of the tower.
In addition, the air adopted in the stripping tower is compressed air before entering the oxidation tower 12 in the process of producing hydrogen peroxide by an anthraquinone method, the air is connected with a stripping air pipeline 10 from an air main pipe 9 entering the oxidation tower 12, enters the tower from the bottom of the stripping tower 7 and is in countercurrent contact with hydrogen peroxide in the stripping tower 7, the air returned from an air path 11 at the top of the stripping tower to the air main pipe 9 entering the oxidation tower 12, and the air after being led out by the stripping tower 7 is returned to the oxidation tower 12 and finally enters the oxidation tower 12 to participate in oxidation reaction, and the operation pressure of the stripping tower 7 is the same as the oxidation pressure, so that the process does not need to adjust the air pressure again.
Example 6
A method for improving extraction yield and product quality of hydrogen peroxide produced by an anthraquinone process comprises the following steps:
(1) The anthraquinone working solution for producing hydrogen peroxide is a mixed system consisting of 2-ethyl anthraquinone, heavy aromatic hydrocarbon, trioctyl phosphate and tetrabutyl urea. And extracting the obtained oxidation liquid by the extraction tower 1, and obtaining crude hydrogen peroxide from the bottom of the extraction tower, wherein the total organic carbon content in the crude hydrogen peroxide is 302ppm, and the obtained crude hydrogen peroxide contains the total organic carbon.
(2) Mixing raffinate 17 (400 parts by mass) with phosphoric acid concentrated solution 20 (1 part by mass, phosphoric acid content is 75%) in a mixer 14, then entering a dehydration tank 15 for dehydration treatment, wherein 316L stainless steel filler and PP filler composite coalescence-separation filler are arranged in the dehydration tank 15, and a dehydrated raffinate 18 and a phosphoric acid diluted solution 19 after water absorption are obtained; the phosphoric acid thin solution 19 is concentrated after water absorption, and the obtained concentrated phosphoric acid thick solution 20 is returned to the mixer 14 for recycling.
In addition, after the concentration, the phosphoric acid concentrate 20 contains hydrogen peroxide, and after the hydrogen peroxide reaches a certain concentration, the water for extraction in the preparation step (1) is prepared by entering the extraction water preparation tank 21, and then enters the extraction tower again, so that the hydrogen peroxide contained in the raffinate is brought into the crude hydrogen peroxide.
(3) The crude hydrogen peroxide enters a purifying tower 2 (a filler tower) for purification treatment, heavy aromatic hydrocarbon and hydrogen peroxide are in countercurrent contact for purification, and coalescing separation filler (316L stainless steel filler and PP filler are adopted for compounding) is arranged below a heavy aromatic hydrocarbon inlet of a tower kettle of the purifying tower 2 and at the bottom of the purifying tower 2, wherein the total organic carbon content of the purified hydrogen peroxide is 229ppm.
(4) Hydrogen peroxide which is subjected to purification and coalescence separation treatment to remove part of oil phase substances enters a stripping tower 7 (a packing tower, wherein the packing is pall rings), a hydrogen peroxide feeding distributor (a tubular distributor) is arranged at the top of the stripping tower 7, the packing supported on a grid is arranged below the hydrogen peroxide feeding distributor, and an air feeding distributor (a groove type distributor) is arranged below the packing; hydrogen peroxide enters the tower from the top of the stripping tower 7, and is in countercurrent contact with air entering from the bottom of the stripping tower 7 for stripping, the ratio of the volumetric flow rate of the hydrogen peroxide entering the stripping tower 7 to the volumetric flow rate of the air entering the stripping tower 7 in a standard state is 1:10, the operating temperature of the stripping tower 7 is 45 ℃, the operating pressure is the same as the oxidation pressure and is 0.21MPaG, and the hydrogen peroxide after stripping is produced from the bottom of the tower.
In addition, the air adopted in the stripping tower is compressed air before entering the oxidation tower 12 in the process of producing hydrogen peroxide by an anthraquinone method, the air is connected with a stripping air pipeline 10 from an air main pipe 9 entering the oxidation tower 12, enters the tower from the bottom of the stripping tower 7 and is in countercurrent contact with hydrogen peroxide in the stripping tower 7, the air returned from an air path 11 at the top of the stripping tower to the air main pipe 9 entering the oxidation tower 12, and the air after being led out by the stripping tower 7 is returned to the oxidation tower 12 and finally enters the oxidation tower 12 to participate in oxidation reaction, and the operation pressure of the stripping tower 7 is the same as the oxidation pressure, so that the process does not need to adjust the air pressure again.
Example 7
A method for improving extraction yield and product quality of hydrogen peroxide produced by an anthraquinone process comprises the following steps:
(1) The anthraquinone working solution for producing hydrogen peroxide is a mixed system consisting of 2-amyl anthraquinone, heavy aromatic hydrocarbon, trioctyl phosphate and tetrabutyl urea. And extracting the obtained oxidation liquid by the extraction tower 1, and obtaining crude hydrogen peroxide from the bottom of the extraction tower, wherein the total organic carbon content in the crude hydrogen peroxide is 318ppm, and the obtained crude hydrogen peroxide is the crude hydrogen peroxide.
(2) Mixing raffinate 17 (400 parts by mass) with phosphoric acid concentrated solution 20 (1 part by mass, phosphoric acid content is 75%) in a mixer 14, then entering a dehydration tank 15 for dehydration treatment, wherein 316L stainless steel filler and PP filler composite coalescence-separation filler are arranged in the dehydration tank 15, and a dehydrated raffinate 18 and a phosphoric acid diluted solution 19 after water absorption are obtained; the phosphoric acid thin liquid 19 after water absorption enters the concentration tank 16 for concentration, and the obtained concentrated phosphoric acid thick liquid 20 returns to the mixer 14 for recycling.
In addition, after the concentration, the phosphoric acid concentrate 20 contains hydrogen peroxide, and after the hydrogen peroxide reaches a certain concentration, the water for extraction in the preparation step (1) is prepared by entering the extraction water preparation tank 21, and then enters the extraction tower again, so that the hydrogen peroxide contained in the raffinate is brought into the crude hydrogen peroxide.
(3) The crude hydrogen peroxide enters a purifying tower 2 (a filler tower) for purification treatment, heavy aromatic hydrocarbon and hydrogen peroxide are in countercurrent contact for purification, a hydrogen peroxide coalescer 5 is arranged at the tower bottom of the purifying tower 2, coalescing separation filler (316L stainless steel filler and PP filler are adopted for compounding) is arranged, and the total organic carbon content in the purified hydrogen peroxide is 243ppm.
(4) Hydrogen peroxide which is subjected to purification and coalescence separation treatment to remove part of oil phase substances enters a stripping tower 7 (a packing tower, wherein the packing is pall rings), a hydrogen peroxide feeding distributor (a tubular distributor) is arranged at the top of the stripping tower 7, the packing supported on a grid is arranged below the hydrogen peroxide feeding distributor, and an air feeding distributor (a groove type distributor) is arranged below the packing; hydrogen peroxide enters the tower from the top of the stripping tower 7, and is in countercurrent contact with air entering from the bottom of the stripping tower 7 for stripping, the ratio of the volumetric flow rate of the hydrogen peroxide entering the stripping tower 7 to the volumetric flow rate of the air entering the stripping tower 7 in a standard state is 1:10, the operating temperature of the stripping tower 7 is 45 ℃, the operating pressure is the same as the oxidation pressure and is 0.21MPaG, and the hydrogen peroxide after stripping is produced from the bottom of the tower.
In addition, the air adopted in the stripping tower is compressed air before entering the oxidation tower 12 in the process of producing hydrogen peroxide by an anthraquinone method, the air is connected with a stripping air pipeline 10 from an air main pipe 9 entering the oxidation tower 12, enters the tower from the bottom of the stripping tower 7 and is in countercurrent contact with hydrogen peroxide in the stripping tower 7, the air returned from an air path 11 at the top of the stripping tower to the air main pipe 9 entering the oxidation tower 12, and the air after being led out by the stripping tower 7 is returned to the oxidation tower 12 and finally enters the oxidation tower 12 to participate in oxidation reaction, and the operation pressure of the stripping tower 7 is the same as the oxidation pressure, so that the process does not need to adjust the air pressure again.
Example 8
The difference from example 2 is that: the operating temperature of the stripper 7 was 55 ℃.
Example 9
The difference from example 2 is that: the operating pressure of the stripper 7 was 0.45MPaG.
Example 10
The difference from example 5 is that: the operating temperature of the stripper 7 was 55 ℃.
Comparative example 1
The difference from example 2 is that: the mass ratio of raffinate 17 to phosphoric acid concentrate 20 was 800:1.
Comparative example 2
The difference from example 2 is that: the mass ratio of raffinate 17 to phosphoric acid concentrate 20 was 400:1, with a sulfuric acid content of 30 wt.% in the phosphoric acid concentrate used.
Comparative example 3
The difference from example 2 is that: the ratio of the volumetric flow rate of hydrogen peroxide into the stripping column 7 to the volumetric flow rate of air into the stripping column 7 in the standard state is 1:2.
Comparative example 4
The difference from example 5 is that: the ratio of the volumetric flow rate of hydrogen peroxide into the stripping column 7 to the volumetric flow rate of air into the stripping column 7 in the standard state is 1:4.
Comparative example 5
The difference from example 2 is that: no purification tower and no hydrogen peroxide coalescer are provided.
Comparative example 6
The difference from example 5 is that: no purification tower and no hydrogen peroxide coalescer are provided.
The total organic carbon in the hydrogen peroxide is measured by a total organic carbon analyzer, and the total organic carbon content in the hydrogen peroxide produced in the examples and comparative examples is shown in table 1.
TABLE 1
(1) As can be seen from examples 1-7 and comparative examples 1-2, after the raffinate is dehydrated by the phosphoric acid concentrate, the hydrogen peroxide content is greatly reduced, wherein the water content can be reduced to below 0.25%, the raffinate is reduced to below 0.1g/L, and the control value of the raffinate is obviously lower than the control value of not more than 0.3g/L required in production. If the mass ratio of the raffinate to the phosphoric acid concentrate is too large or the phosphoric acid content in the phosphoric acid concentrate is too low, the reduction degree of the hydrogen peroxide content in the raffinate is obviously reduced.
(2) It can be seen from examples 1-10 and comparative examples 3-6 that the total organic carbon content of the crude hydrogen peroxide extracted from the extraction column is gradually reduced in sequence after passing through the purification column and the hydrogen peroxide coalescer and the stripping column. Compared with crude hydrogen peroxide obtained by extraction, the removal rate of the total organic carbon can reach more than 47 percent. If the crude hydrogen peroxide from the extraction tower does not pass through the purification tower and the hydrogen peroxide coalescer, the crude hydrogen peroxide directly enters the stripping tower, and the total organic carbon content can be reduced by about 30 percent through the stripping, but the hydrogen peroxide product is faintly yellow in color, which indicates that trace anthraquinone substances are not removed.
(3) It can be seen from examples 2, 5 and comparative examples 3 to 4 that when the volumetric flow rate of hydrogen peroxide entering the stripping tower and the volumetric flow rate of air in the standard state reach a certain ratio, the effect of increasing the air amount on removing the total organic carbon is very small, but the stripping effect is remarkably affected when the air amount is too small.
The foregoing description is only of the preferred embodiments of the present invention, and is not intended to limit the scope of the invention, but rather is intended to cover any equivalents of the structures disclosed herein or modifications in the equivalent processes, or any application of the structures disclosed herein, directly or indirectly, in other related arts.
Claims (10)
1. A method for improving extraction yield and product quality of hydrogen peroxide produced by an anthraquinone process is characterized by comprising the following steps:
(1) Extracting the oxidation liquid by an extraction tower, obtaining raffinate from the tower top and obtaining crude hydrogen peroxide from the tower bottom;
(2) Mixing the raffinate with the phosphoric acid concentrated solution, and then carrying out dehydration treatment to obtain a phosphoric acid solution containing hydrogen peroxide, wherein the hydrogen peroxide contained in the raffinate is brought into the crude hydrogen peroxide by preparing water for extraction in the step (1) and then entering the extraction tower again;
(3) And (3) sequentially carrying out purification treatment and coalescence separation treatment on the crude hydrogen peroxide, entering the tower from the top of the stripping tower, carrying out countercurrent contact with air entering from the bottom of the stripping tower to carry out stripping, and finally producing hydrogen peroxide from the bottom of the stripping tower to obtain a hydrogen peroxide finished product.
2. The method for improving the extraction yield and the product quality of hydrogen peroxide produced by an anthraquinone process according to claim 1, wherein in the step (2), the mass fraction of phosphoric acid in the phosphoric acid concentrate is 40-80%; the mass ratio of the raffinate to the phosphoric acid concentrated solution is 200-500: 1.
3. the method for improving the extraction yield and the product quality of the anthraquinone process hydrogen peroxide production according to claim 1 or 2, wherein in the step (2), a dehydration tank is adopted for dehydration treatment, and a coalescing separation filler compounded by 316L stainless steel filler and PP filler is arranged in the dehydration tank; and the phosphoric acid solution containing hydrogen peroxide enters a concentration tank for concentration, and the phosphoric acid concentrate is obtained again for recycling.
4. The method for improving the extraction yield and the product quality of the production of hydrogen peroxide by the anthraquinone process according to claim 1, wherein in the step (3), the purification treatment is as follows: purifying by countercurrent contact of heavy aromatic hydrocarbon and hydrogen peroxide, arranging a hydrogen peroxide coalescer at the bottom of the purifying tower, and discharging purified hydrogen peroxide from the bottom of the tower after coalescence and separation; the purifying tower is a plate tower or a filler tower, and the separation filler in the hydrogen peroxide coalescer is formed by compounding 316L stainless steel filler and PP filler or compounding 316L stainless steel filler and PTFE filler.
5. The method for improving the extraction yield and the product quality of hydrogen peroxide produced by an anthraquinone process according to claim 1, wherein in the step (3), the stripping tower is a packing tower, a hydrogen peroxide feeding distributor is arranged at the top of the stripping tower, a packing supported on a grid is arranged below the hydrogen peroxide feeding distributor, and an air feeding distributor is arranged below the packing.
6. The method for improving the extraction yield and the product quality of the anthraquinone process hydrogen peroxide production according to claim 1 or 5, wherein in the step (3), the hydrogen peroxide feeding distributor is one of a tubular distributor, a trough distributor or a disk distributor; the air feeding distributor is a tubular distributor or a trough distributor; the filler is one of a pall ring, a ladder ring, a conjugate ring or a saddle ring.
7. The method for improving the extraction yield and the product quality of hydrogen peroxide produced by an anthraquinone process according to claim 1, wherein in the step (3), the steam stripping is as follows: the ratio of the volumetric flow rate of hydrogen peroxide to the volumetric flow rate of air entering the stripping tower is 1:6-45, the operating temperature of the stripping tower is 20-60 ℃, the pressure of air is 0.05-0.60 MPaG, and the operating pressure of the stripping tower does not need to be regulated after the stripping tower enters the stripping tower.
8. The method for improving the extraction yield and the product quality of the production of the hydrogen peroxide by the anthraquinone process according to claim 7, wherein in the step (3), the air entering from the bottom of the stripping tower is the compressed air before entering the oxidation tower in the process of producing the hydrogen peroxide by the anthraquinone process, and the air containing a small amount of organic matters and the hydrogen peroxide after being discharged from the stripping tower returns to the oxidation tower and finally enters the oxidation tower to participate in the oxidation reaction.
9. The method for improving the extraction yield and the product quality of hydrogen peroxide produced by an anthraquinone process according to claim 1, wherein the total organic carbon substances in the hydrogen peroxide produced by the anthraquinone process comprise anthraquinone, heavy aromatic hydrocarbon and polar solvent.
10. The method for improving the extraction yield and the product quality of hydrogen peroxide produced by an anthraquinone process according to claim 9, wherein the anthraquinone is at least one of 2-ethylanthraquinone, 2-butylanthraquinone and 2-pentylalnthraquinone; the polar solvent is at least one of trioctyl phosphate, 2-methylcyclohexyl acetate, tetrabutyl urea and diisobutyl methanol.
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