CN105294605A - Circulating method for preparation of propylene oxide from hydrogen peroxide ethylbenzene and propene - Google Patents
Circulating method for preparation of propylene oxide from hydrogen peroxide ethylbenzene and propene Download PDFInfo
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- CN105294605A CN105294605A CN201410355428.8A CN201410355428A CN105294605A CN 105294605 A CN105294605 A CN 105294605A CN 201410355428 A CN201410355428 A CN 201410355428A CN 105294605 A CN105294605 A CN 105294605A
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Abstract
The invention relates to a circulating method for preparation of propylene oxide from hydrogen peroxide ethylbenzene and propene, and mainly solves the problem that in the prior art, the molar ratio of propene to hydrogen peroxide ethylbenzene is required to be relatively large in order to maintain higher reaction temperature rise and higher reaction efficiency. According to the method, adopted raw materials of hydrogen peroxide ethylbenzene and propene enter at least two tandem adiabatic reactors in a liquid-phase manner, under the condition that the reaction temperature is 15-160 DEG C, the pressure is 1.0-12.0 MPa, and the total molar ratio of propene to hydrogen peroxide ethylbenzene is 1-20, propene and hydrogen peroxide ethylbenzene are in contact with a Ti-silicon dioxide catalyst to realize an epoxidation reaction to generate propylene epoxide, wherein according to the technical scheme, part of the hydrogen peroxide ethylbenzene raw material and part of epoxidized reaction products containing propylene oxide proportionally enter inlets of the all reactors in a circulating manner, so that the problem in the prior art is well solved, and the method can be used in industries for production of propylene oxide through epoxidation of hydrogen peroxide ethylbenzene and propene.
Description
Technical field
The present invention relates to the circulation means of a kind of hydrogen peroxide ethylbenzene and propylene propylene oxide.
Background technology
Propylene oxide is important basic chemical industry raw material, is the third-largest propylene analog derivative being only second to polypropylene and vinyl cyanide, mainly for the production of polyethers, propylene glycol etc.It is also the main raw material of forth generation washing composition nonionogenic tenside, oil field demulsifier, farm chemical emulgent etc.The derivative of propylene oxide is widely used in the industries such as automobile, building, food, tobacco, medicine and makeup.The derived product of having produced nearly hundred kinds is the important source material of fine chemical product.
The traditional processing technology of propylene oxide is chlorohydrination technique, and process comprises the chlorohydrination of propylene and hypochlorite solution, propylene chlorohydrin and milk of lime saponification and product purification three steps.The feature of this method is that flow process is shorter, and construction investment is few, technical maturity, not high to raw material propylene purity requirement.But owing to using chlorine in production process, produce the waste water of a large amount of chloride containing calcium, have corrosion to equipment, there is serious problem of environmental pollution.
For the problem of environmental pollution that chlorohydrination technique exists, the companies such as Lyondell develop co-oxidation propylene oxide green synthesis process.Conjugated oxidation is divided into Trimethylmethane conjugated oxidation and ethylbenzene conjugated oxidation two kinds of joint process, the former coproduction trimethyl carbinol, the latter's coproduction vinylbenzene, and its basic step is: (1) Trimethylmethane or ethylbenzene oxidation are corresponding superoxide; (2) propylene is produced propylene oxide and corresponding alcohol by superoxide epoxidation; (3) propylene oxide is refined; (4) be converted into can product sold for coproduction alcohol.Compared with chlorohydrination, conjugated oxidation overcomes environmental pollution, the equipment corrosion of chlorohydrination existence and consumes the shortcomings such as chlorine, but this method weak point is that technical process is long, investment cost is high (being about 2 times of chlorohydrination), and a large amount of joint product (joint product output is about 2 ~ 3 times of PO) need be balanced, the economic benefit certain degree of therefore conjugated oxidation depends on the sale of joint product.
To this, many companies are devoted to develop the propylene oxide Green Manufacturing Technology without coproduction.The company such as Degussa and KruppUnde and BASF and Dow is " HPPO " production technology of oxygenant with hydrogen peroxide in cooperative development.This method for raw material, take methyl alcohol as solvent with chemical grade propylene and hydrogen peroxide, adopts tubular reactor, reacts at the temperature and low pressure of gentleness in liquid phase.Hydrogen peroxide transforms completely, and propylene is Quantitative yield almost, only generates propylene oxide and water in production process, unreacting propylene can be used for other process or recycles, and technical process is simple, and product yield is high, there is no other joint product, substantially pollution-free, belong to eco-friendly process for cleanly preparing.The shortcoming of this technique is that hydrogen peroxide consumption is large, and propylene oxide per ton consumes hydrogen peroxidase 10 .7 ton.
SUMITOMO CHEMICAL chemical company develops the conjugated oxidation technique without by-product.This technique adopts isopropyl benzene to substitute Trimethylmethane or ethylbenzene, cumene oxidation is become hydrogen phosphide cumene (CHP), epoxidation of propylene is made to become propylene oxide with CHP again, the dimethyl benzyl alcohol simultaneously obtained can obtain alpha-methyl styrene after dewatering, and then hydrogenation becomes isopropyl benzene for recycling.
Compared with PO/SM co-production method, CHP method is without coproduction chemical, though the market risk because a large amount of by-product of coproduction brings can be reduced, but two kinds of explained hereafter devices, capital construction investments are more or less the same, have the market requirement to obtain countries and regions for propylene oxide and vinylbenzene, PO/SM co-production method generating apparatus economic benefit is better.
Some patents are had to relate to the conjugated oxidation technique of PO/SM co-production method.EP323663 discloses a kind of hydrogen peroxide ethylbenzene and epoxidation of propylene obtains technique, and under the condition of temperature of reaction 100 DEG C, hydrogen peroxide ethylbenzene and propylene enter reactor, with Ti/SiO with the mol ratio of 16.7
2catalyst exposure reacts, and generates propylene oxide, reactor outlet pressure 26bar, and volatile components (as propylene) vaporization absorption epoxidation reaction heat, to maintain the temperature of reaction of reactor.US6153153 discloses a kind of epoxidation processes be made up of multiple adiabatic reaction district, raw material hydrogen peroxide ethylbenzene and propylene are with the mixed in molar ratio of 4.65:1, be divided into the reactant flow that multiple logistics cools each reaction zone respectively, reactor is entered to 80 ~ 107 DEG C with the hot reacting by heating raw material of epoxidation reaction, the outlet reactant decompression vaporization of last reaction zone, reduce temperature, the logistics of vaporization cools the inlet streams of last reaction zone, the temperature rise of each reaction zone keeps 6 ~ 28 DEG C, and reaction pressure is carried out in the liquid phase to keep reaction.US5883268 discloses the treatment process of ethylbenzene oxidation product.Hydrogen peroxide ethylbenzene disclosed in US5849937 and epoxidation of propylene technique and USUS6153153 different, epoxidation reaction is divided into 6 catalytic reaction zones, and wherein last reaction zone is for subsequent use.Raw material hydrogen peroxide ethylbenzene and propylene are divided into the outlet material that four strands of materials cool front four reaction areas respectively, the first reaction zone is entered to 38 ~ 101 DEG C with the hot reacting by heating raw material of epoxidation reaction, reaction zone temperature out 121 DEG C, reaction pressure keeps reaction zone entirety to be liquid phase.When the catalyst activity of the first reaction zone is reduced to a certain degree, close the valve of the turnover pipeline of the first reaction zone, switch out regeneration or replacing that reactive system carries out catalyzer, the 6th reaction zone of simultaneously coming into operation, steady with retaining ring oxidizing reaction.Epoxidation technique disclosed in US5760253, reaction is divided into multiple reaction zone, material between each reaction zone and charging heat exchange, remove the reaction heat of 25 ~ 75%, remaining reaction heat promotes the temperature of reaction mass, and the component that vaporization is easily vaporized, the temperature rise of each reaction zone is generally 20 ~ 100.
In existing document or report, how the reaction process problem of shorter mention hydrogen peroxide ethylbenzene and propylene to prepare epoxy propane, particularly effectively reduce reaction temperature rising, the raising propylene of reaction bed and the problem of the mol ratio of hydrogen peroxide ethylbenzene.
Summary of the invention
Technical problem to be solved by this invention is in prior art, it is higher and for keep higher reaction efficiency to need the problems such as the mol ratio of higher propylene and hydrogen peroxide ethylbenzene to there is reaction temperature rising in the reaction process of hydrogen peroxide ethylbenzene and propylene to prepare epoxy propane, the circulation technology of a kind of new hydrogen peroxide ethylbenzene and propylene propylene oxide is provided, the method, under the prerequisite of total mol ratio not increasing propylene and hydrogen peroxide ethylbenzene, effectively can reduce reaction temperature rising, improve the reaction propylene of beds and the mol ratio of hydrogen peroxide ethylbenzene.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: the circulation means of a kind of hydrogen peroxide ethylbenzene and propylene propylene oxide, hydrogen peroxide ethylbenzene and propylene carry out epoxidation reaction and generate product propene oxide under contacting with Ti-SiO 2 catalyst, the product generated is divided into extraction logistics and recycle stream, wherein recycle stream is divided into (n-1) individual logistics, be circulated to each beds entrance, adiabatic reactor is divided into N section, wherein, n be more than or equal to 1 positive integer; N is that its step of positive integer being greater than 1 comprises:
1) raw material I 1 segmentation containing hydrogen peroxide ethylbenzene enters the multiple adiabatic reactors being at least two series connection;
2) raw material I a2 of the first part of raw material I 1 namely containing hydrogen peroxide ethyl benzene mixtures is mixed into the first reactor with the raw material II 5 containing propylene;
3) namely the second section of raw material I 1 contains raw material I b3 and the first reactor outlet product of hydrogen peroxide ethyl benzene mixtures and is mixed into the second reactor containing the recycle stream I 7 in the epoxidation reaction product of propylene oxide;
4) namely the n-th part of raw material I 1 contains raw material I n4 and the (n-1)th reactor outlet product of hydrogen peroxide ethyl benzene mixtures and is mixed into N reactor containing the recycle stream N8 in the epoxidation reaction product of propylene oxide;
Wherein, epoxidation reaction temperature is 15 ~ 160 DEG C, pressure is 1.0 ~ 12.0MPa, total mol ratio of propylene and hydrogen peroxide ethylbenzene is 1 ~ 20.In technique scheme, preferably, the extraction logistics of epoxidation reaction product and the part by weight of recycle stream are 0.1 ~ 10.
In technique scheme, preferably, entering second to the epoxidation reaction product circulation logistics of N reactor and the part by weight of global cycle logistics is 0.01 ~ 0.99.
In technique scheme, preferably, described multiple adiabatic reactor is made up of 2 ~ 10 reactors in series.More preferably, described multiple adiabatic reactor is preferably made up of 2 ~ 4 reactors in series.
In technique scheme, in the adiabatic reactor of described multiple series connection, beds is single bed and/or multistage bed; Wherein, in each reactor above-mentioned, logistics flows to as upflowing or downflow system.
In technique scheme, the propylene in described raw material II is fresh propylene, the Propylene recovery of follow-up system or its mixture.Hydrogen peroxide ethylbenzene in described raw material I obtains with ethylbenzene oxidation, and be the mixture of ethylbenzene, hydrogen peroxide ethylbenzene, hydrogen peroxide ethylbenzene concentration is 5 ~ 65wt%.
In technique scheme, step 2) in, raw material I a2 mixes with the raw material II 5 containing propylene outward at the first reactor or mixes in the first reactor; Step 3) in raw material I b3 and the first reactor outlet thing containing hydrogen peroxide ethyl benzene mixtures and the recycle stream I 7 contained in the epoxidation reaction product of propylene oxide mix outward at the second reactor or mix in the second reactor; Step 4) in raw material I n4 and (n-1) reactor outlet thing containing hydrogen peroxide ethyl benzene mixtures and the recycle stream N8 contained in the epoxidation reaction product of propylene oxide mix outward at N reactor or mix in N reactor; In the middle of adopting between each reactor, between the beds of each reactor, heat collector removes reaction heat.Each section of hydrogen peroxide ethyl benzene mixtures both can mix outward at reactor with reaction mass, also can mix in reactor.Middle heat collector can be adopted between each reactor, between each beds where necessary to remove reaction heat.In technique scheme, described epoxidation reaction is carried out in the liquid phase using solvent.Be liquid under the temperature and pressure of this solvent when reacting, and do not react with reactant and product.Hydrogen peroxide ethylbenzene in raw material I does not add solvent containing the mixture as the ethylbenzene of its raw material, replaces solvent by hydrogen peroxide ethyl benzene mixtures.
In technique scheme, preferably, epoxidation reaction temperature is 30 ~ 130 DEG C, and pressure is 1.5 ~ 6.0MPa, total mol ratio of propylene and hydrogen peroxide ethylbenzene is 2 ~ 15.
Epoxidation reaction temperature is generally 15 ~ 160 DEG C, considers economic utilization and the reaction preference of speed of reaction and catalyzer, preferably 30 ~ 130 DEG C.When the temperature is too low, speed of reaction is too low, and the amount therefore obtaining the catalyzer needed for required reacting weight increases.On the contrary, when temperature is too high, selectivity reduces, and catalyst regeneration cycle shortens.Particularly, when the amount of the compound with 4 carbon atoms increases, loss and the energy required when removing compound of valuable constituent increase.Pressure can be enough to keep reaction mixture to be in the pressure of liquid state, is generally 1.0 ~ 12.0MPa, preferential 1.5 ~ 6.0MPa.
The mol ratio propylene of propylene/hydrogen peroxide ethylbenzene and the total mol ratio of hydrogen peroxide ethylbenzene that are supplied to epoxidation step are generally 1 ~ 20, preferential 2 ~ 15, override 3 ~ 12.When this ratio is too low, speed of reaction reduces, and reaction preference is deteriorated, and the yield of object product will reduce.When this ratio is too high, the quantitative change of the propylene of recirculation obtains and excessively increases, and therefore in recycling step, needs many energy, and the energy consumption of device is increased.
Owing to adopting the insulation fix bed reaction process of multiple series connection of the intersegmental cooling of raw material hydrogen peroxide ethylbenzene and the circulation of epoxidation reaction product section in the present invention, can partly or entirely absorption reaction heat, effectively control reaction temperature rising, improve the propylene of beds and the ratio of hydrogen peroxide ethylbenzene, ensure that epoxidation reaction is carried out under the reaction conditions of the best, the selectivity of object product propene oxide can be improved, delay the coking and deactivation of catalyzer, the regeneration period of extending catalyst.Meanwhile, by the ratio of feed product flow and every section of propylene and hydrogen peroxide ethylbenzene between adjustment reaction number, reactor, reach the propylene circulation ratio reducing epoxidation reaction system, reduce energy consumption, reduce the object of investment.Prove to adopt technical scheme of the present invention through test, the insulation fix bed reaction process of individual reactors in series series connection tandem, epoxidised reaction temperature rising is only 12.8 DEG C, lower than 32.1 in comparative example DEG C, under total propylene and hydrogen peroxide ethylbenzene mol ratio are the condition of 11.52, the mol ratio of beds is up to 27.46, and hydrogen peroxide ethylbenzene almost all transforms, the selectivity of object product propene oxide reaches 99.08%, achieves good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of the circulation technology of hydrogen peroxide ethylbenzene of the present invention and propylene propylene oxide.
In Fig. 1, 1 is the raw material I containing hydrogen peroxide ethylbenzene, 2 is raw material I a containing hydrogen peroxide ethyl benzene mixtures, 3 is raw material I b containing hydrogen peroxide ethyl benzene mixtures, 4 is raw material I n containing hydrogen peroxide ethyl benzene mixtures, 5 is the raw material II containing propylene, 6 for containing the extraction logistics of the peroxidation reaction product of propylene oxide, 7 for containing the recycle stream I in the epoxidation reaction product of propylene oxide, 8 for containing the recycle stream N in the epoxidation reaction product of propylene oxide, 1a is adiabatic reactor, 2a is the beds of the first reactor, 3a is the beds of the second reactor, 4a is the beds of the n-th reactor.
In Fig. 1, raw material I 1 is divided into raw material I a2, raw material I b3, raw material I n4 at the temperature, pressure of regulation, enter the first reactor catalyst bed 2a of the multiple insulation fix bed reactor 1a of liquid-solid phase, the second reactor catalyst bed 3a, the n-th reactor catalyst bed 4a respectively, raw material II 5 enters the first reactor catalyst bed 2a of multiple insulation fix bed reactor.Propylene and hydrogen peroxide ethylbenzene to contact with Ti-SiO 2 catalyst with certain proportion and carry out epoxidation reaction, epoxidation reaction product is divided into extraction logistics 6 containing the reaction product of propylene oxide and recycle stream, wherein, recycle stream is divided into recycle stream 7, recycle stream 8 loops back second of reactor to N reactor inlet.Extraction logistics 6 containing the reaction product of propylene oxide goes follow-up separation and purification unit to carry out separation and purification to obtain qualified product propylene.
Below by embodiment, the present invention is further elaborated.
Embodiment
In order to make object of the present invention, technical scheme and advantage clearly understand, the present invention is described with following specific embodiment further, but the present invention is limited to absolutely not these examples.
[embodiment 1]
By the technical scheme shown in Fig. 1, raw material is containing the hydrogen peroxide ethyl benzene mixtures of 19.34% weight concentration, flow is 162367.5 kgs/hr, be divided into two strands in proportion, enter the insulation fix bed reactor of many bed catalyst of two series connection respectively, raw material propylene 10987.6 kgs/hr, circulation propylene 103863.5 kgs/hr, mix with the hydrogen peroxide ethyl benzene mixtures entering the first reactor catalyst bed, temperature of reaction 76 DEG C, under the condition of reaction pressure 2.9MPaG, with Ti/SiO
2catalyst exposure, liquid phase epoxidation reaction generates propylene oxide and xylyl alcohol and other by product; The reactant flowing out the first reactor catalyst bed mixes with the hydrogen peroxide ethyl benzene mixtures entering the second reactor catalyst bed, recycle stream, and control temperature 76 DEG C, enters the second reactor catalyst bed, with Ti/SiO
2catalyst exposure, liquid phase epoxidation reaction generates propylene oxide and xylyl alcohol and other by product.Hydrogen peroxide ethylbenzene weight air speed 4.1hr
-1the mol ratio of total propylene and hydrogen peroxide ethylbenzene is 11.52, the propylene of the first reactor catalyst bed and the second reactor catalyst bed inlet and the mol ratio of hydrogen peroxide ethylbenzene then reach 27.43 and 27.46, the temperature out of the first reactor catalyst bed and the second beds is respectively 88.8 DEG C, 87.5 DEG C, the total conversion rate of hydrogen peroxide ethylbenzene is 99.2%, and the molar selectivity of propylene oxide is 99.08%.
[embodiment 2]
With [embodiment 1], only change the flow of circulation propylene: circulation propylene flow is 69242.4 kgs/hr, other [embodiment 1].Hydrogen peroxide ethylbenzene weight air speed 4.1hr
-1the mol ratio of total propylene and hydrogen peroxide ethylbenzene is 8.03, the propylene of the first beds and the second beds entrance and the mol ratio of hydrogen peroxide ethylbenzene then reach 19.13 and 18.70, the temperature out of the first beds and the second beds is respectively 90.8 DEG C, 89.1 DEG C, the total conversion rate of hydrogen peroxide ethylbenzene is 99.2%, and the molar selectivity of propylene oxide is 99.05%.
[embodiment 3]
With [embodiment 1], an altering reactor form: two single bed insulation fix bed reactor series connection, other is with [embodiment 1].Hydrogen peroxide ethylbenzene weight air speed 4.1hr
-1the mol ratio of total propylene and hydrogen peroxide ethylbenzene is 11.52, the propylene of the first reactor catalyst bed and the second reactor catalyst bed inlet and the mol ratio of hydrogen peroxide ethylbenzene then reach 27.43 and 27.46, the temperature out of the first reactor catalyst bed and the second reactor catalyst bed is respectively 88.8 DEG C, 87.5 DEG C, the total conversion rate of hydrogen peroxide ethylbenzene is 99.2%, and the molar selectivity of propylene oxide is 99.08%.
[embodiment 4]
With [embodiment 1], only change beds temperature in: the first reactor catalyst bed inlet temperatures is 79 DEG C, and the second reactor catalyst bed inlet temperatures is 79 DEG C, other is with [embodiment 1].Hydrogen peroxide ethylbenzene weight air speed 4.1hr
-1the mol ratio of total propylene and hydrogen peroxide ethylbenzene is 11.52, the propylene of the first reactor catalyst bed and the second reactor catalyst bed inlet and the mol ratio of hydrogen peroxide ethylbenzene then reach 27.43 and 27.46, the temperature out of the first reactor catalyst bed and the second reactor catalyst bed is respectively 91.8 DEG C, 90.5 DEG C, the total conversion rate of hydrogen peroxide ethylbenzene is 99.21%, and the molar selectivity of propylene oxide is 99.06%.
[comparative example]
Epoxidation reactor is single stage adiabatic fixed-bed reactor, and epoxidation reaction product does not circulate.Raw material is containing the hydrogen peroxide ethyl benzene mixtures of 19.4% weight concentration, flow is 162367.5 kgs/hr, mixes with raw material propylene 10987.6 kgs/hr, circulation propylene 155795.5 kgs/hr, entrance temperature of reaction 76 DEG C, under the condition of reaction pressure 2.9MPaG, with Ti/SiO
2catalyst exposure, liquid phase epoxidation reaction generates propylene oxide and xylyl alcohol and other by product, hydrogen peroxide ethylbenzene weight air speed 4.1hr
-1, the mol ratio of total propylene and hydrogen peroxide ethylbenzene is 16.75, and the temperature out of reactor is 108.1 DEG C, and the total conversion rate of hydrogen peroxide ethylbenzene is 99.2%, and the molar selectivity of propylene oxide is 98.3%.
Claims (10)
1. the circulation means of a hydrogen peroxide ethylbenzene and propylene propylene oxide, hydrogen peroxide ethylbenzene and propylene carry out epoxidation reaction and generate product propene oxide under contacting with Ti-SiO 2 catalyst, the product generated is divided into extraction logistics and recycle stream, wherein recycle stream is circulated to each beds entrance, individual logistics that recycle stream is divided into (n-1), multiple adiabatic reactor is divided into N section, wherein, n be more than or equal to 1 positive integer; N be more than or equal to 1 positive integer; Its step comprises:
1) raw material I (1) segmentation containing hydrogen peroxide ethylbenzene enters the adiabatic reactor being at least two series connection;
2) raw material I a (2) of the first part of raw material I (1) namely containing hydrogen peroxide ethyl benzene mixtures is mixed into the first reactor with the raw material II (5) containing propylene;
3) raw material I b (3) of the second section of raw material I (1) namely containing hydrogen peroxide ethyl benzene mixtures is mixed into the second reactor with the first reactor outlet product with containing the recycle stream I (7) in the epoxidation reaction product of propylene oxide;
4) raw material I n (4) of the n-th part of raw material I (1) namely containing hydrogen peroxide ethyl benzene mixtures is mixed into N reactor with (N-1) reactor outlet product with containing the recycle stream N (8) in the epoxidation reaction product of propylene oxide;
Wherein, epoxidation reaction temperature is 15 ~ 160 DEG C, pressure is 1.0 ~ 12.0MPa, total mol ratio of propylene and hydrogen peroxide ethylbenzene is 1 ~ 20.
2. the circulating reaction method of hydrogen peroxide ethylbenzene and propylene propylene oxide according to claim 1, is characterized in that the extraction logistics of epoxidation reaction product and the part by weight of recycle stream are 0.1 ~ 10.
3. the circulating reaction method of hydrogen peroxide ethylbenzene and propylene propylene oxide according to claim 1, is characterized in that entering second to the epoxidation reaction product circulation logistics of N reactor and the part by weight of global cycle logistics is 0.01 ~ 0.99.
4. the circulating reaction method of hydrogen peroxide ethylbenzene and propylene propylene oxide according to claim 1, is characterized in that multiple adiabatic reactor is made up of 2 ~ 10 reactors in series.
5. the circulation means of hydrogen peroxide ethylbenzene and propylene propylene oxide according to claim 1, is characterized in that in the adiabatic reactor of described multiple series connection, beds is single bed and/or multiple bed; Wherein, in each reactor above-mentioned, logistics flows to as upflowing or downflow system.
6. the circulation means of hydrogen peroxide ethylbenzene and propylene propylene oxide according to claim 1, the propylene that it is characterized in that in described raw material II is fresh propylene, the Propylene recovery of follow-up system or its mixture; Hydrogen peroxide ethylbenzene in described raw material I obtains with ethylbenzene oxidation, and be the mixture of ethylbenzene, hydrogen peroxide ethylbenzene, hydrogen peroxide ethylbenzene concentration is 5 ~ 65wt%.
7. the circulation means of hydrogen peroxide ethylbenzene and propylene propylene oxide according to claim 1, it is characterized in that step 2) in, raw material I a (2) mixes with the raw material II (5) containing propylene outward at the first reactor or mixes in the first reactor; Step 3) in raw material I b (3) and the first reactor outlet thing containing hydrogen peroxide ethyl benzene mixtures and the recycle stream I (7) contained in the epoxidation reaction product of propylene oxide mix outward at the second reactor or mix in the second reactor; Step 4) in raw material I n (4) and (n-1) reactor outlet thing containing hydrogen peroxide ethyl benzene mixtures and the recycle stream N (8) contained in the epoxidation reaction product of propylene oxide mix outward at N reactor or mix in N reactor.
8. the circulation means of hydrogen peroxide ethylbenzene and propylene propylene oxide according to claim 1, is characterized in that described epoxidation reaction is carried out in the liquid phase using solvent; Liquid under the temperature and pressure of this solvent when reacting.
9. the circulation means of hydrogen peroxide ethylbenzene and propylene propylene oxide according to claim 1, is characterized in that hydrogen peroxide ethylbenzene contains the mixture of the ethylbenzene as its raw material, does not add solvent and replaces solvent by hydrogen peroxide ethyl benzene mixtures.
10. the circulation means of hydrogen peroxide ethylbenzene and propylene propylene oxide according to claim 1, it is characterized in that, epoxidation reaction temperature is 30 ~ 130 DEG C, and pressure is 1.5 ~ 6.0MPa, total mol ratio of propylene and hydrogen peroxide ethylbenzene is 2 ~ 15.
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