CN104555935A - Hydrogenation process for producing hydrogen peroxide by anthraquinone method - Google Patents
Hydrogenation process for producing hydrogen peroxide by anthraquinone method Download PDFInfo
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- CN104555935A CN104555935A CN201310496104.1A CN201310496104A CN104555935A CN 104555935 A CN104555935 A CN 104555935A CN 201310496104 A CN201310496104 A CN 201310496104A CN 104555935 A CN104555935 A CN 104555935A
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- reactor
- hydrogenation
- hydrogen
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- 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
Abstract
The invention discloses a hydrogenation process for producing a hydrogen peroxide by an anthraquinone method. The hydrogenation process comprises the following steps that: (1) two reactors are arranged in the hydrogenation process for producing the hydrogen peroxide by the anthraquinone method; a first current of fresh hydrogen and a working liquid serve as a feeding material I and perform hydrogenation in the first reactor; the reacted material is subjected to gas-liquid separation to obtain a gas phase and a liquid phase, wherein part of the liquid phase is recycled back to the first reactor; the rest of the liquid phase is reasonably optimized and modulated; the phenomenon that the reaction hydrogen is deficient or excessive is avoided; the hydrogenation completeness is realized; the liquid phase and the gas phase are mixed to serve as feeding material II and enter the second reactor; (2) a second current of fresh hydrogen and the feeding material II perform the hydrogenation in the second reactor; the reacted material is subjected to the gas-liquid separation to obtain a gas phase and a liquid phase, wherein part of the liquid phase is recycled back to the second reactor, and the rest of the liquid phase enters an oxidation process. According to the process disclosed by the invention, a hydrogenation process is optimized, and meanwhile, side effects are reduced, so that the hydrogenation is more uniform, and the service life of a catalyst is prolonged.
Description
Technical field
The present invention relates to a kind of method for hydrogenation of Hydrogen Peroxide Production, particularly a kind of hydrogenation process of hydrogen dioxide solution production by anthraquinone process.
Background technology
Hydrogen dioxide solution production by anthraquinone process is generally with 2-ethyl-anthraquinone (EAQ) for working material, is made into working fluid, through operations such as over hydrogenation, oxidation, extraction and working fluid aftertreatments, obtains hydrogen peroxide product with heavy aromatics (Ar) and trioctyl phosphate (TOP) for solvent.Wherein hydrogenation process refers to that the EAQ in working fluid is under the existence of palladium catalyst, generates 2-ethyl hydrogen anthraquinone (HEAQ) with hydrogen generation hydrogenation reaction.
Existing hydrogen dioxide solution production by anthraquinone process hydrogenation process generally adopts fixed-bed reactor, and inner filling catalyzer, reaction pressure is generally 0.15 ~ 0.3MPa, and temperature of reaction is 40 ~ 70 DEG C.The initial temperature that anthraquinone hydrogenation reaction needed is certain, but due to this reaction be thermopositive reaction, in reaction process, temperature constantly raises.In normal operation condition, anthraquinone hydrogenation main reaction is not only accelerated in the rising of bed temperature, also can accelerate side reaction.If temperature rise is too high, easily there is side reaction, make anthraquinone occur significantly degraded.The heat that general work liquid hydrogenation in hydrogenation reactor produces will make working fluid discharging temperature rise 6 ~ 12 DEG C, therefore hydrogenation degree and beds temperature rise to strictly be controlled in anthraquinone hydrogenation reaction process, should requirements hydrogenation be reached, reduce side reaction again.
Disclose a kind of method controlling fixed bed temperature in CN1335256A, the method adds water cooler before mixing liquid enters fixed bed, removes the partial reaction heat that circulation hydride is taken out of, to make into a fluid temperature within the scope of 35 ~ 60 DEG C.The method suppresses DeR by controlling hydrogenation reactor temperature in, extending catalyst life cycle, but the method is the ordinary method of current industrial hydriding process, and strictly unrealized or accurately control hydriding process, bed temperature rise cannot be regulated in time.
The temperature control loop of a kind of 201183752Y fixed-bed palladium catalysts, hydrogen dioxide solution production by anthraquinone process device is disclosed in CN202201708U, in this loop, pneumatic adjusting valve one end connects interchanger, the other end connects return piping and low-pressure steam pipeline by Y-tube, and return piping is provided with stopping valve.Recirculated water no longer directly arrives return piping after interchanger, but reenters recovery line after pneumatic adjusting valve throttling.The object of the method accurately controls working fluid to go out the temperature that namely interchanger enters hydrogenation reactor, realize controlling hydrogenation, similar to the method described in CN1335256A patent, same strictly unrealized or accurately control hydriding process, bed temperature rise cannot be regulated in time.
Along with developing rapidly of green chemical synthesis industry in recent years, the demand of hydrogen peroxide is grown with each passing day, optimizing hydrogenation by improving fixed bed hydrogenation reaction process, reducing degraded, reduction consumes, the work-ing life of extending catalyst is significant.
Summary of the invention
For the deficiency of currently available technology, the invention provides a kind of hydrogenation process of hydrogen dioxide solution production by anthraquinone process, this technique is by the reasonably optimizing of hydrogenation process and modulation, avoid reactive hydrogen tolerance deficiency or amounts of hydrogen excess phenomenon, realize hydrogenation simultaneously completely, reduce side reaction to occur, make hydrogenation more even, extending catalyst work-ing life.
The hydrogenation process of hydrogen dioxide solution production by anthraquinone process of the present invention, comprises following content:
(1) in the hydrogenation process of hydrogen dioxide solution production by anthraquinone process, two reactors are set, first burst of fresh hydrogen and working fluid as charging I after the first reactor generation hydrogenation, reacted material is through gas-liquid separation, obtain gas phase (hydrogen) and liquid phase (hydrogenated work liquid), Partial Liquid Phase loops back the first reactor, enters the second reactor after residue liquid phase mixes with gas phase as charging II;
After there is hydrogenation in (2) second bursts of fresh hydrogen and charging II in the second reactor, reacted material is through gas-liquid separation, obtain gas phase (hydrogen) and liquid phase (hydrogenated work liquid), Partial Liquid Phase loops back the second reactor, and residue liquid phase enters oxidation operation.
In present invention process, preferably the 3rd reactor is set after the second reactor, after in step (2) there is hydrogenation as charging III in residue liquid phase and the 3rd burst of fresh hydrogen in the 3rd reactor, reacted material is through gas-liquid separation, Partial Liquid Phase loops back the 3rd anti-device, and residue liquid phase enters oxidation operation.
In present invention process, also can set gradually along Flow of Goods and Materials direction according to actual needs the 4th, the 5th or the 6th etc. more multiple reactor carry out hydrogenation, the same step of reaction process (2), one fresh hydrogen charging corresponding of each reactor.
In present invention process, containing hydrogenation catalyst bed layer in reactor, the noble metal catalyst that hydrogenation catalyst is is active ingredient with palladium or platinum.
In present invention process, the total liquid-gas ratio (Nm in each reactor
3/ m
3) be 1:1 ~ 1:5.5, preferred 1:1.5 ~ 1:3.
In present invention process, by Flow of Goods and Materials direction, the entrance amounts of hydrogen between adjacent reactor increases successively, and with the first reactor inlet amounts of hydrogen for benchmark, increasing degree is 0.5% ~ 10%, and preferably 4% ~ 8%.
In present invention process, by Flow of Goods and Materials direction, the working fluid internal circulating load between adjacent reactor increases successively, and the increasing degree ratio of the fresh working fluid of the first reactor inlet (each reactor cycles work liquid measure with) is 1% ~ 10%, and preferably 3% ~ 6%.
In present invention process, the reaction pressure of reactor is 0.1 ~ 0.5MPa, preferably successively decreases successively by the reaction pressure between Flow of Goods and Materials orienting response device, and wherein between adjacent reactor, the reaction pressure amplitude of successively decreasing is 0.01 ~ 0.15MPa, preferably 0.03 ~ 0.06MPa.
In present invention process, the temperature of reaction of reactor is 30 ~ 70 DEG C, preferably increases progressively successively by the temperature of reaction between the adjacent reactor of Flow of Goods and Materials direction, and wherein between adjacent reactor, temperature of reaction increasing degree is 3 ~ 12 DEG C, preferably 4 ~ 8 DEG C.Wherein, preferably arrange three reactors, wherein the temperature range of the first reactor is 35 ~ 53 DEG C, and the temperature range of the second reactor is 38 ~ 60 DEG C, and the temperature range of the 3rd reactor is 43 ~ 70 DEG C.
Present invention process compared with prior art, has the following advantages:
(1) hydrogen gradation is added each reactor, the strict degree of depth controlling generation hydrogenation reaction in each reactor, both can avoid excessive hydrogenation reaction occurs in each reactor, the phenomenon of hydrogen deficient can be prevented again.
(2) each reactor strictly controls working fluid internal circulating load, and the effect of this cycle working fluid can regulate the reactor temperature difference on the one hand, prevents hot localised points and produces side reaction; The linear velocity of catalyst surface working fluid can be improved on the other hand, be conducive to accelerating hydrogenation; The working fluid circulation of catalyst surface can also be made to upgrade, prevent excessive hydrogenation.
(3) each temperature of reactor raises gradually along material direction, reactor pressure successively decreases gradually along material direction, make initial hydrogenation react on the one hand to carry out under certain pressure and lesser temps, maintaining certain pressure is to improve speed of reaction, and controlling low temperature is produce a large amount of side reaction to prevent initial reaction too violent; Subsequent reactions is made on the other hand to react under high-temperature at permission minimal pressure with slightly, the degradation product generated due to initial reaction is few, control slightly high-temperature and both can increase substantially hydrogenation reaction rate, while improving hydrogen effect, be less likely to occur again the depth degradation of degradation product, and the lower pressure maintaining reaction is not only conducive to the generation reducing side reaction, facility investment and energy consumption can be reduced again.
(4) the inventive method effectively can control the temperature rise of each reactor below 6 DEG C, ensure that effectively carrying out of hydrogenation.
Accompanying drawing explanation
Fig. 1 is present invention process method flow schematic diagram (for 2 hydrogenation reactors).
Wherein, 1 is hydrogen manifold, and 2 is working fluid, and 3 is the first hydrogenation reactor hydrogen, 4 is the first hydrogenation reactor charging, 5 is the second hydrogenation reactor hydrogen, and 6 is the second hydrogenation reactor charging, 7-first hydrogenation reactor, 8-first hydrogenation reactor beds, 9-second hydrogenation reactor, 10-second hydrogenation reactor beds, 11-first hydrogenation reactor effluent; 12-first gas-liquid separator; 13-first hydrogenation reactor recycle pump, 14-first heating/cooling device; 15-second heating/cooling device; 16-second hydrogenation reactor effluent; 17-second gas-liquid separator; 18-second hydrogenation reactor recycle pump.
Embodiment
Illustrate that the present invention is described in detail with embodiment below in conjunction with accompanying drawing, but therefore do not limit the present invention.
The inventive method is realized by such mode: be divided into two-way from the hydrogen of hydrogen manifold 1, and a road is the first hydrogenation reactor hydrogen 3, and another road is the second hydrogenation reactor hydrogen 5.First, first hydrogenation reactor hydrogen 3 is mixed into the first hydrogenation reactor charging 4 with working fluid 2, enter from the top of the first hydrogenation reactor 7, flowed out by bottom after the first hydrogenation reactor beds 8, effluent 11 enters the first gas-liquid separator 12 and carries out gas-liquid separation, some work liquid after separation turns back to the entrance of the first hydrogenation reactor 7 through the first hydrogenation reactor recycle pump 13, after the first heating/cooling device 14 regulates temperature, the first hydrogenation reactor is entered after mixing with 2, the gas phase that another part working fluid and the first gas-liquid separator separate and the second hydrogenation reactor hydrogen 5 are mixed into the second hydrogenation reactor charging 6, enter from the top of the second hydrogenation reactor 9, flowed out by bottom after the second hydrogenation reactor beds 10, effluent carries out gas-liquid separation through the second gas-liquid separator 17, some work liquid after separation turns back to the entrance of the second hydrogenation reactor 9 through the second hydrogenation reactor recycle pump 18, after the second heating/cooling device 15 regulates temperature, the second hydrogenation reactor is entered after mixing with the first hydrogenation reactor discharging, another part working fluid enters next operation.
The embodiment of the present invention adopts anthraquinone as working material, and heavy aromatics and trioctyl phosphate, as solvent composition working fluid, adopt Pd/Al
2o
3as working fluid hydrogenation catalyst, the character of catalyzer is as follows: Ф 3 ~ 4mm's is spherical, and bulk density is 0.58 ± 0.02g/ml; Anti-crushing power>=40N/cm; Palladium content is 0.3 ± 0.02wt%; Active kg (H
2o
2100%)/kg catalyst sky:>=3.3.In working fluid, anthraquinone content is 72g/L, and tetrahydro-anthraquinone content is 48g/L.
Comparative example 1
A hydrogenation reactor, the agent of inner filling two-stage catalytic, amounts to 0.3m
3, hydrogenation reactor temperature in is 48 DEG C, and hydrogenation pressure is 0.25 ~ 0.3MPa, and whole working fluid and hydrogen autoreactor top also flow to into reactor, pass through first, second beds generation hydrogenation reaction successively.After this method process, hydrogenation reactor stagnation temperature is upgraded to 8.7 ~ 10.6 DEG C, and hydrogen effect is 5.11 ~ 5.26g/L, is 94 ~ 98 g/L by the total anthraquinones content measured in working fluid after the oxidation of hydrogen anthraquinone.
Embodiment 1
Two hydrogenation reactors, each hydrogenation reactor loads one section of catalyzer 0.15m
3.First hydrogenation reactor reaction conditions is as follows: temperature in is 40 DEG C, and top pressure is 0.28 ~ 0.34MPa, and fresh working fluid flow is 7.08m
3/ h, cycle operation flow quantity is 8.7m
3/ h, amounts of hydrogen is 39.9 Nm
3/ h.Second hydrogenation reactor reaction conditions is as follows: temperature in is 46.7 DEG C, and top pressure is 0.23 ~ 0.28MPa, and cycle operation flow quantity is 9.1m
3/ h, amounts of hydrogen is 46.8Nm
3/ h.
After this method process, first hydrogenation reactor temperature rise is 4.6 ~ 4.7 DEG C, second hydrogenation reactor temperature rise is 4.8 DEG C ~ 4.9 DEG C, measuring the second hydrogenation reactor outlet hydrogen effect is 7.8 ~ 8.0g/L, is 118 ~ 125 g/L by the total anthraquinones content measured in working fluid after the second hydrogenation reactor outlet hydrogen anthraquinone oxidation.
Embodiment 2
Two hydrogenation reactors, each hydrogenation reactor loads one section of catalyzer 0.15m
3.First hydrogenation reactor reaction conditions is as follows: temperature in is 55 DEG C, and top pressure is 0.25 ~ 0.30MPa, and fresh working fluid flow is 7.08m
3/ h, cycle operation flow quantity is 9.2m
3/ h, amounts of hydrogen is 41.2 Nm
3/ h.Second hydrogenation reactor reaction conditions is as follows: temperature in is 62.3 DEG C, and top pressure is 0.23 ~ 0.25MPa, and cycle operation flow quantity is 10.5m
3/ h, amounts of hydrogen is 45.3Nm
3/ h.
After this method process, first hydrogenation reactor temperature rise is 5.0 ~ 5.2 DEG C, second hydrogenation reactor temperature rise is 5.3 DEG C ~ 5.5 DEG C, measuring the second hydrogenation reactor outlet hydrogen effect is 8.0 ~ 8.2g/L, is 122 ~ 128 g/L by the total anthraquinones content measured in working fluid after the second hydrogenation reactor outlet hydrogen anthraquinone oxidation.
Embodiment 3
Three hydrogenation reactors, each hydrogenation reactor loads one section of catalyzer 0.1m
3, the first hydrogenation reactor reaction conditions is as follows: temperature in is 40 DEG C, and top pressure is 0.30 ~ 0.34MPa, and fresh working fluid flow is 4.78m
3/ h, cycle operation flow quantity is 2.68m
3/ h, amounts of hydrogen is 26.6 Nm
3/ h.Second hydrogenation reactor reaction conditions is as follows: temperature in is 44.1 DEG C, and top pressure is 0.25 ~ 0.28MPa, and cycle operation flow quantity is 2.79m
3/ h, amounts of hydrogen is 29.5Nm
3/ h.3rd hydrogenation reactor reaction conditions is as follows: temperature in is 47.5 DEG C, and top pressure is 0.2 ~ 0.23MPa, and cycle operation flow quantity is 2.92m
3/ h, amounts of hydrogen is 30.6Nm
3/ h.
After this method process, each hydrogenation reactor temperature rise is 3.3 ~ 3.4 DEG C, and measuring the 3rd hydrogenation reactor outlet hydrogen effect is 8.2 ~ 8.5g/L, is 123 ~ 133 g/L by the total anthraquinones content measured in working fluid after the second hydrogenation reactor outlet hydrogen anthraquinone oxidation.
Claims (9)
1. the hydrogenation process of a hydrogen dioxide solution production by anthraquinone process, it is characterized in that comprising following content: in the hydrogenation process of (1) hydrogen dioxide solution production by anthraquinone process, arrange two reactors, first burst of fresh hydrogen and working fluid as charging I after the first reactor generation hydrogenation, reacted material is through gas-liquid separation, obtain gas phase (hydrogen) and liquid phase (hydrogenated work liquid), Partial Liquid Phase loops back the first reactor, enters the second reactor after residue liquid phase mixes with gas phase as charging II; After there is hydrogenation in (2) second bursts of fresh hydrogen and charging II in the second reactor, reacted material is through gas-liquid separation, obtain gas phase (hydrogen) and liquid phase (hydrogenated work liquid), Partial Liquid Phase loops back the second reactor, and residue liquid phase enters oxidation operation.
2. according to technique according to claim 1, it is characterized in that: the 3rd reactor is set after the second reactor, after in step (2) there is hydrogenation as charging III in residue liquid phase and the 3rd burst of fresh hydrogen in the 3rd reactor, reacted material is through gas-liquid separation, Partial Liquid Phase loops back the 3rd anti-device, and residue liquid phase enters oxidation operation.
3. according to technique according to claim 2, it is characterized in that: set gradually the 4th, the 5th or the 6th reactor along Flow of Goods and Materials direction and carry out hydrogenation, the same step of reaction process (2), one fresh hydrogen charging corresponding of each reactor.
4. according to technique according to claim 1, it is characterized in that: containing hydrogenation catalyst bed layer in reactor, the noble metal catalyst that hydrogenation catalyst is is active ingredient with palladium or platinum.
5. according to the technique described in claim 1 or 2, it is characterized in that: the total liquid-gas ratio (Nm in each reactor
3/ m
3) be 1:1 ~ 1:5.5.
6. according to technique according to claim 1, it is characterized in that: by Flow of Goods and Materials direction, the entrance amounts of hydrogen between adjacent reactor increases successively, and with the first reactor inlet amounts of hydrogen for benchmark, increasing degree is 0.5% ~ 10%.
7. according to technique according to claim 1, it is characterized in that: by Flow of Goods and Materials direction, the working fluid internal circulating load between adjacent reactor increases successively, and increasing degree is 1% ~ 10%.
8. according to technique according to claim 1, it is characterized in that: the reaction pressure of reactor is 0.1 ~ 0.5MPa, successively decreases successively by the reaction pressure between Flow of Goods and Materials orienting response device, and wherein between adjacent reactor, the reaction pressure amplitude of successively decreasing is 0.01 ~ 0.15MPa.
9. according to technique according to claim 1, it is characterized in that: the temperature of reaction of reactor is 30 ~ 70 DEG C, increases progressively successively by the temperature of reaction between the adjacent reactor of Flow of Goods and Materials direction, and wherein between adjacent reactor, temperature of reaction increasing degree is 3 ~ 12 DEG C.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109678120A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of hydrogenation reactor and method for hydrogenation of hydrogen dioxide solution production by anthraquinone process |
| CN110013758A (en) * | 2018-01-09 | 2019-07-16 | 中国石油化工股份有限公司 | Hydrogenated tail gas safe reuse and processing method in hydrogenation apparatus |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102009960A (en) * | 2010-11-18 | 2011-04-13 | 清华大学 | Hydrogenation method for production of hydrogen peroxide by anthraquinone process |
| CN202201708U (en) * | 2011-09-19 | 2012-04-25 | 傅骐 | Fixed-bed hydrogenating device for producing H2O2 by anthraquinone process |
-
2013
- 2013-10-22 CN CN201310496104.1A patent/CN104555935B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102009960A (en) * | 2010-11-18 | 2011-04-13 | 清华大学 | Hydrogenation method for production of hydrogen peroxide by anthraquinone process |
| CN202201708U (en) * | 2011-09-19 | 2012-04-25 | 傅骐 | Fixed-bed hydrogenating device for producing H2O2 by anthraquinone process |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109678120A (en) * | 2017-10-19 | 2019-04-26 | 中国石油化工股份有限公司 | A kind of hydrogenation reactor and method for hydrogenation of hydrogen dioxide solution production by anthraquinone process |
| CN109678120B (en) * | 2017-10-19 | 2020-06-09 | 中国石油化工股份有限公司 | Hydrogenation reactor and hydrogenation method for producing hydrogen peroxide by anthraquinone process |
| CN110013758A (en) * | 2018-01-09 | 2019-07-16 | 中国石油化工股份有限公司 | Hydrogenated tail gas safe reuse and processing method in hydrogenation apparatus |
| CN110013758B (en) * | 2018-01-09 | 2022-05-03 | 中国石油化工股份有限公司 | Safe recycling and treating method for hydrogenation tail gas in hydrogenation reaction device |
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