CN103030522B - Method for vaporizing raw materials for styrene preparation through ethylbenzene dehydrogenation - Google Patents
Method for vaporizing raw materials for styrene preparation through ethylbenzene dehydrogenation Download PDFInfo
- Publication number
- CN103030522B CN103030522B CN201110300685.8A CN201110300685A CN103030522B CN 103030522 B CN103030522 B CN 103030522B CN 201110300685 A CN201110300685 A CN 201110300685A CN 103030522 B CN103030522 B CN 103030522B
- Authority
- CN
- China
- Prior art keywords
- ethylbenzene
- water
- logistics
- styrene
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention relates to a method for vaporizing raw materials for styrene preparation through ethylbenzene dehydrogenation and mainly solves the problems that in the prior art, after a styrene device rectification system adopts an azeotropy and energy saving process, when an ethylbenzene dehydrogenation reaction system uses catalysts with low rate ratio, steam is overheated, the outlet temperature is overhigh, the equipment investment is great, and even, the simultaneous application cannot be realized. According to the method, an ethylbenzene/water azeotropic evaporation and ethylbenzene complementary evaporation integral system is adopted for separation, and an independent ethylbenzene complementary evaporation system is arranged for completely evaporating ethylbenzene and water. Through the technical scheme, the problems are perfectly solved, and the method can be used in the industrial production of styrene preparation through ethylbenzene dehydrogenation.
Description
Technical field
The present invention relates to the method for a kind of ethyl benzene dehydrogenation preparation of styrene reaction raw materials vaporization.
Background technology
Vinylbenzene is one of most important basic organic chemical industry raw material, for the manufacture of the copolymer resins such as polystyrene PS and EPS, ABS and SAN, phenylethylene/butadiene copolymer latex SB, styrene-butadiene rubber(SBR) and latex SBR, unsaturated polyester and other is as styrene/methacrylic acid methyl esters latex, methyl methacrylate/butadiene/styrene copolymers MBS, ion exchange resin and medicine etc.
The production technology of industrial ethyl benzene dehydrogenation preparation of styrene has adiabatic dehydrogenation technique, isothermal dehydrogenating technology and dehydrogenation selective oxidation processes.Wherein be most widely used, technology is the most ripe is ethylbenzene negative pressure adiabatic dehydrogenation technique.It is reported, 85% of whole world vinylbenzene output in 2008 adopts ethylbenzene dehydrogenation production technique, only has 15% to be produced by other method.
Ethylbenzene dehydrogenation manufactures cinnamic technological principle: under catalyzer and water vapor existence and 550 ~ 650 DEG C of hot conditionss, ethylbenzene occurs to select dehydrogenation reaction, generate vinylbenzene, this reaction is strong endothermic reaction, ethylbenzene dehydrogenation reaction also needs to add a large amount of superheated vapour, superheated vapour is the thermophore of ethylbenzene dehydrogenation reaction on the one hand, provide the heat needed for reaction, the existence of water vapor on the other hand, reduce reaction dividing potential drop, be conducive to reaction to carry out towards the cinnamic positive dirction of generation, water vapor also can with the carbon distribution generation water gas shift reaction of catalyst surface, the activeconstituents of catalyzer can be prevented to be reduced to metal, be conducive to the extending catalyst life-span, the water ratio (water vapor and ethylbenzene weight ratio) of industrial employing is generally 1 ~ 1.6.
Cinnamic production process is high temperature, needs a large amount of fuel and water vapor, makes this process energy consumption larger.In recent years, along with rising steadily of crude oil and cost of material, the key measure adopting power-saving technology more and more to become styrene device to reduce costs.Both at home and abroad the power saving of styrene device is also conducted extensive research, patent CN1007973B proposes and produces cinnamic improvement dehydrogenating technology by phenylethane, comprise Low Temperature Thermal to reclaim and the improving one's methods of vinylbenzene-water vapour charging, ethylbenzene/styrene separating tower tower top heat is utilized to heat ethylbenzene and water, the part ethylbenzene of reaction needed and water azeotropic vaporization is made to enter reactor, saved the energy consumption of about 10 ~ 20%, the method is applied on full scale plant.Styrene device distillation system adopts azeotropic energy-saving technique, namely, as thermal source, the mixture of heating raw ethylbenzene and water makes it azeotropic vaporization (100kPaA to use ethylbenzene/styrene separating tower overhead gas (pressure 38kPaA, temperature 102 DEG C), 91 DEG C), reach energy-conservation object.Because vinylbenzene is easily polymerized, ethylbenzene styrene separating tower tower top working pressure can not improve again, mean that overhead gas temperature cannot improve again, and the pressure drop of whole ethyl benzene dehydrogenation system determines that the pressure of material ethylbenzene and water azeotropic vaporization also cannot reduce, now for ensureing that ethylbenzene/water azeotropic vaporization device has enough temperature difference impellents, ethylbenzene and water must at minimum azeotrope temperature azeotropic vaporization, the now weight content about 33% of water in ethylbenzene and water mixture, azeotropic temperature 91 DEG C.The heat that ethylbenzene/styrene separating tower overhead gas provides can evaporate the material ethylbenzene of 50 ~ 80%, all the other material ethylbenzenes of 20 ~ 50% supplement evaporator evaporation by the ethylbenzene arranged, ethylbenzene supplements vaporizer and ethylbenzene/water azeotropic vaporization device all adopts ethylbenzene/water by minimum azeotrope temperature proportioning (water accounts for 33 % by weight), is separated ethylbenzene and water enters ethylbenzene/water azeotropic vaporization device respectively and ethylbenzene supplements the evaporation of vaporizer cyclic part by ethylbenzene/water separation tank.This technique emphasis is exactly that the water distribution of ethylbenzene vapo(u)rization system has higher proportion requirement, makes the azeotropic vaporization temperature of ethylbenzene and water under a certain pressure minimum, guarantees that the azeotropic vaporization device of ethylbenzene/styrene separating tower tower top has enough temperature difference heat exchange.
Along with the progress of vinylbenzene technology, the research of low water ratio (weight ratio of water and ethylbenzene) catalyzer in recent years achieves significant progress, water can be reduced to 1.0 ~ 1.25 than from original 1.4 ~ 1.6, the reduction of water ratio can save a large amount of vinylbenzene energy consumptions, according to calculating, water is reduced to 1.1 than by 1.4, and can save vinylbenzene comprehensive energy consumption about 10%, economic benefit is considerable.If but applying low water on the styrene device of former employing azeotropic power-saving technology compares catalyzer, because the water yield of supply ethylbenzene vapo(u)rization system cannot reduce, apply low water must the reduce devaporation process furnace water yield than catalyzer, in the irreducible situation of the temperature of reaction of Ethylbenzene Dehydrogenation Reactor, the temperature out of steam pipe oven must be improved, to provide the heat required for ethylbenzene dehydrogenation.According to calculating, when water is than 1.4, steam pipe oven A and B temperature out only need 850 DEG C and 830 DEG C, when water ratio is reduced to 1.25, steam pipe oven A and B temperature out need be increased to 890 DEG C and 870 DEG C, and when water ratio is reduced to 1.0, steam pipe oven A and B temperature out need be increased to 940 DEG C and 930 DEG C, interchanger and pipeline must adopt high temperature resistant material, when temperature is lower than 880 DEG C, the 800HT material that price is higher can be adopted, temperature is more than 880 DEG C, the high temperature material of more high standard must be adopted, price rises at double, suitable material is not even had to meet processing requirement when temperature is more than 920 DEG C, facility investment is so not only caused to increase, also face the difficult problem that low water can not be applied than catalyzer and azeotropic energy-saving technique simultaneously, device energy-saving effect greatly reduces, have a strong impact on the economic benefit of vinylbenzene enterprise.
For the problem that low water can not be applied than catalyzer and azeotropic energy-saving technique simultaneously, document is not still had to propose to improve one's methods at present.
Summary of the invention
Technical problem to be solved by this invention is after styrene device distillation system adopts azeotropic energy-saving technique in the past, when ethyl benzene dehydrogenation system uses low water than catalyzer, cause that steam superheating heater outlet temperature is too high and facility investment is large, the problem even cannot simultaneously applied, provides a kind of method of new ethyl benzene dehydrogenation preparation of styrene feed vaporization.The method has when styrene device can be made to apply azeotropic energy-saving technique and low water at the same time than catalyzer, reduces steam superheating heater outlet temperature, thus reduces the advantage of facility investment and plant energy consumption.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method of ethyl benzene dehydrogenation preparation of styrene feed vaporization, comprise the following steps: the logistics 1 a) comprising material ethylbenzene and water enters ethylbenzene and supplements vaporizer, be gasified totally and obtain logistics 3, wherein in logistics 1, the weight percentage of water is 0 ~ 20%; B) logistics 2 comprising material ethylbenzene and water enters ethylbenzene/water separation tank, isolated ethylbenzene and water remove ethylbenzene/water azeotropic vaporization device again, gas-liquid mixed logistics 4 is obtained after partial gasification, logistics 4 returns ethylbenzene/water separation tank, obtain gaseous phase outlet logistics 5, wherein in logistics 2, the weight percentage of water is 30 ~ 40%; C) logistics 3 and logistics 5 obtain logistics 6 after mixing, and logistics 6 enters subsequent reactions system.
In technique scheme, the water-content of logistics 2 is 31 ~ 35% (weight), ethylbenzene/water azeotropic vaporization device adopts ethylbenzene/styrene separating tower overhead gas heating evaporation, the material ethylbenzene of 65 ~ 75% (weight) needed for evaporation reaction, working pressure is 80 ~ 120kPaA, and temperature is 85 ~ 97 DEG C; The water-content of logistics 1 is 5 ~ 15% (weight), ethylbenzene supplements vapo(u)rization system and adopts steam heating evaporation, the material ethylbenzene of 25 ~ 35% (weight) needed for evaporation reaction, working pressure is 80 ~ 120kPaA, and temperature is 100 ~ 140 DEG C; Ethylbenzene supplements the mixture that vaporizer shell side is ethylbenzene and water, and tube side is heating steam; Ethylbenzene supplement vaporizer be gasified totally after ethylbenzene and the mixed pressure of gas phase portion of water and ethylbenzene/water azeotropic vaporization components of system as directed gasified raw material ethylbenzene and water be 80 ~ 120kpaA, temperature is 90 ~ 130 DEG C.
In subsequent reactions system, the water of Ethylbenzene Dehydrogenation Reactor and the weight ratio of ethylbenzene are 0.9 ~ 1.3: 1, and pressure is 50 ~ 75kpaA, and temperature is 580 DEG C ~ 650 DEG C; Steam heating system comprises steam pipe oven A and steam pipe oven B, and the temperature out of steam pipe oven A is 800 ~ 880 DEG C, and the temperature out of steam pipe oven B is 800 ~ 860 DEG C.
Original ethylbenzene/water azeotropic vaporization and ethylbenzene are supplemented evaporating integrated system and are separated by the present invention, arrange independently ethylbenzene and supplement vapo(u)rization system.It take water vapor as thermal source that the ethylbenzene separated supplements vapo(u)rization system, adopt all evaporation ethylbenzene or minimizing water distribution ratio to be gasified totally and evaporate the method for ethylbenzene and water, break away from water weight content when integral type is evaporated and be necessary for the restriction of 33%, the weight content of water can be reduced to 0 ~ 20% by original 33%; Ethylbenzene/former processing condition of water azeotropic vaporization system held, partial gasification material ethylbenzene and water, wherein the weight content of water is about 33%, which reduce ethylbenzene vapo(u)rization system about 25 ~ 35% water distribution total amount, when applying low water than catalyzer, the water vapor amount of steam pipe oven is corresponding to be increased, the heat of enough reactions just can be provided under lower temperature out, thus reduce the application of high-temperature material, reduce facility investment, apply low water simultaneously and also significantly can reduce energy consumption increase economic benefit than catalyzer and azeotropic energy-saving technique.
Adopting technical solution of the present invention, when applying azeotropic energy-saving technique, ethylbenzene vapo(u)rization system water distribution quantity about 25 ~ 35% can be reduced, thus increase the water vapor amount of steam pipe oven, reduce furnace outlet temperature.Catalyzer is compared at the low water of application, when water ratio is 1.25, steam pipe oven A and B temperature out are reduced to 850 DEG C and 835 DEG C by 890 DEG C that originally needed and 870 DEG C, high-temperature pipe and resuperheater facility investment can reduce 50%, when water ratio is 1.0, steam pipe oven A and B temperature out are reduced to 880 DEG C and 860 DEG C by 940 DEG C that originally needed and 930 DEG C, high-temperature pipe and resuperheater material became can meet processing requirement from originally meeting the demands, low water is applied than while catalyzer and azeotropic power-saving technology, vinylbenzene comprehensive energy consumption can by originally energy-conservation 15% being increased to energy-conservation 20 ~ 25%, achieve good technique effect.
Accompanying drawing explanation
Fig. 1 is the ethyl benzene dehydrogenation preparation of styrene typical method adopting existing azeotropic energy-saving technique.
Fig. 2 is the ethyl benzene dehydrogenation preparation of styrene method adopting technical solution of the present invention.
Fig. 1, in Fig. 2, 1 is process furnace A, 2 is intermediate heat, 3 is process furnace B, 4 is the first dehydrogenation reactor, 5 is the second dehydrogenation reactor, 6 is ethylbenzene superheater, 7 is ethylbenzene/water separation tank, 8 is ethylbenzene/water azeotropic vaporization device, 9 supplement vaporizer for ethylbenzene, 10 is ethylbenzene/styrene separating tower, 101 is the water vapor into steam pipe oven A, 102 is steam pipe oven A outlet water vapor, 103 is the water vapor resuperheater, 104 is the water vapor steam pipe oven, 105 is material ethylbenzene, 106 is water distribution, 107 is the ethylbenzene into ethylbenzene/water azeotropic vaporization device, 108 is the water into ethylbenzene/water azeotropic vaporization device, 109 is the ethylbenzene supplementing vaporizer into ethylbenzene, 110 is the water supplementing vaporizer into ethylbenzene, 111 supplement evaporator outlet gas for ethylbenzene, 112 is ethylbenzene/styrene separating tower overhead gas, 113 is ethylbenzene/water azeotropic vaporization organ pipe journey outlet material, 114 is ethylbenzene/water separation tank gas phase discharging, 115 remove the ethylbenzene material of the first dehydrogenation reactor for ethylbenzene superheater, 116 is the first dehydrogenation reactor outlet material, 117 is the second dehydrogenation reactor outlet material, 118 is the reaction mass through the cooling of ethylbenzene superheater, 119 is the ethylbenzene into ethylbenzene/water separation tank, 120 is the water into ethylbenzene/water separation tank, 121 is the ethylbenzene supplementing vaporizer into ethylbenzene, 122 is the water supplementing vaporizer into ethylbenzene, 123 supplement evaporator outlet gas for ethylbenzene, 124 is the ethylbenzene that ethylbenzene/water separation tank removes ethylbenzene/water azeotropic vaporization device, 125 is the water that ethylbenzene/water separation tank removes ethylbenzene/water azeotropic vaporization device, 127 is ethylbenzene/water azeotropic vaporization organ pipe journey outlet material, 128 is ethylbenzene/water separation tank gas phase discharging.
In Fig. 1, material ethylbenzene 105 and water distribution 106 enter ethylbenzene/water separation tank 7 jointly, the isolated ethylbenzene of ethylbenzene/water separation tank 7 and water are all divided into 2 strands, wherein ethylbenzene 107 and water 108 enter ethylbenzene/water azeotropic vaporization device 8 partial gasification, adopt ethylbenzene/styrene separating tower 10 overhead gas 112 to be thermal source, the gas-liquid mixture 113 after partial gasification returns ethylbenzene/water separation tank 7, ethylbenzene 109 and water 110 enter ethylbenzene and supplement vaporizer 9 partial gasification, gas-liquid mixture 111 after partial gasification returns ethylbenzene/water separation tank 7, the material 115 of gaseous phase outlet material 114 after ethylbenzene superheater 6 heats of ethylbenzene/water separation tank 7 enters the first dehydrogenation reactor 4 and reacts, reaction mass 116 enters the second dehydrogenation reactor 5 and reacts after resuperheater 2 reheating, reacting rear material 117 obtains material 118 after ethylbenzene superheater 6 cools, the logistics 102 of water vapour 101 after steam pipe oven A heats, logistics 103 is obtained again after resuperheater heat exchange, after steam pipe oven B heats, logistics 104 enters the first dehydrogenation reactor 4 after mixing with logistics 115.
In Fig. 2, material ethylbenzene 105 is divided into 2 bursts of logistics 119 and 121, water distribution 106 is also divided into 2 strand 120 and 122, wherein logistics 119 and 120 enters ethylbenzene/water separation tank jointly, the isolated ethylbenzene 124 of ethylbenzene/water separation tank 7 and water 125 enter ethylbenzene/water azeotropic vaporization device 8 partial gasification, adopt ethylbenzene/styrene separating tower 10 overhead gas 112 to be thermal source, the gas-liquid mixture 127 after partial gasification returns ethylbenzene/water separation tank 7, logistics 121 and 122 jointly enters ethylbenzene and supplements vaporizer 9, supplement in vaporizer 9 at ethylbenzene and be gasified totally, logistics 123 after gasification and the gaseous phase outlet material 128 of ethylbenzene/water separation tank 7 mix, material 115 after ethylbenzene superheater 6 heats enters the first dehydrogenation reactor 4 and reacts, reaction mass 116 enters the second dehydrogenation reactor 5 and reacts after resuperheater 2 reheating, reacting rear material 117 obtains material 118 after ethylbenzene superheater 6 cools, the logistics 102 of water vapour 101 after steam pipe oven A heats, logistics 103 is obtained again after resuperheater heat exchange, after steam pipe oven B heats, logistics 104 enters the first dehydrogenation reactor 4 after mixing with logistics 115.
Below by embodiment, the present invention is further elaborated.
Embodiment
[embodiment 1]
Certain 100,000 tons/year of ethyl benzene dehydrogenation preparation of styrene device, adopt and press the ethyl benzene dehydrogenation preparation of styrene technology shown in Fig. 2, material ethylbenzene flow is 21 tons/hour, be divided into 2 strands, the flow entering ethylbenzene/water separation tank is 14.5 tons/hour, entering the flow that ethylbenzene supplements vaporizer is 6.5 tons/hour, and water distribution total flux 7.3 tons/hour, all enters ethylbenzene/water separation tank.In ethylbenzene/water separation tank, the weight content of water is 33.4%, 145 tons/hour, isolated ethylbenzene and 73 tons/hour, water enter ethylbenzene/water azeotropic vaporization device partial gasification, the operational condition of ethylbenzene/water azeotropic vaporization device is pressure 100kPaA, vaporization temperature 91 DEG C, ethylbenzene/styrene separating tower overhead gas is adopted to be thermal source, tower top pressure 38kPaA, temperature 102 DEG C, the gas-liquid mixture after partial gasification returns ethylbenzene/water separation tank.Ethylbenzene supplements vaporizer and adopts autoclave heat exchanger structure, ethylbenzene material is gasified totally at shell side, tube side is the heating steam of 0.6MPaG, pressure after gasification is 100kPaA, temperature 132 DEG C, the gaseous phase outlet mixing of materials of the material after gasification and ethylbenzene/water separation tank, mixed temperature of charge is 104 DEG C, through ethylbenzene superheater be heated to 500 DEG C and from steam pipe oven water vapour mixing enter the first dehydrogenation reactor (temperature of reaction 615 DEG C successively, pressure 60kPaA), resuperheater and the second dehydrogenation reactor (temperature of reaction 617 DEG C, pressure 50kPaA), the vapor flow entering steam pipe oven is 15.8 tons/hour, steam pipe oven A temperature out 860 DEG C, steam pipe oven B temperature out 840 DEG C.
This device water ratio is 1.1, and high-temperature pipe and resuperheater gross investment are 7,000,000 Renminbi, and device total energy consumption is 295 kilograms of mark oil/ton vinylbenzene.
[embodiment 2]
Certain 100,000 tons/year of ethyl benzene dehydrogenation preparation of styrene device, adopt and press the ethyl benzene dehydrogenation preparation of styrene technology shown in Fig. 2, material ethylbenzene flow is 21 tons/hour, be divided into 2 strands, the flow entering ethylbenzene/water separation tank is 14.5 tons/hour, entering the flow that ethylbenzene supplements vaporizer is 6.5 tons/hour, and water distribution total flux 7.3 tons/hour, all enters ethylbenzene/water separation tank.In ethylbenzene/water separation tank, the weight content of water is 33.4%, 145 tons/hour, isolated ethylbenzene and 73 tons/hour, water enter ethylbenzene/water azeotropic vaporization device partial gasification, the operational condition of ethylbenzene/water azeotropic vaporization device is pressure 100kPaA, vaporization temperature 91 DEG C, ethylbenzene/styrene separating tower overhead gas is adopted to be thermal source, tower top pressure 38kPaA, temperature 102 DEG C, the gas-liquid mixture after partial gasification returns ethylbenzene/water separation tank.Ethylbenzene supplements vaporizer and adopts autoclave heat exchanger structure, ethylbenzene material is gasified totally at shell side, tube side is the heating steam of 0.6MPaG, pressure after gasification is 100kPaA, temperature 132 DEG C, the gaseous phase outlet mixing of materials of the material after gasification and ethylbenzene/water separation tank, mixed temperature of charge is 104 DEG C, through ethylbenzene superheater be heated to 500 DEG C and from steam pipe oven water vapour mixing enter the first dehydrogenation reactor (temperature of reaction 615 DEG C successively, pressure 60kPaA), resuperheater and the second dehydrogenation reactor (temperature of reaction 617 DEG C, pressure 50kPaA), the vapor flow entering steam pipe oven is 13.5 tons/hour, steam pipe oven A temperature out 880 DEG C, steam pipe oven B temperature out 860 DEG C.
This device water ratio is 1.0, and high-temperature pipe and resuperheater gross investment are 8,000,000 Renminbi, and device total energy consumption is 285 kilograms of mark oil/ton vinylbenzene.
[embodiment 3]
Certain 100,000 tons/year of ethyl benzene dehydrogenation preparation of styrene device, adopt and press the ethyl benzene dehydrogenation preparation of styrene technology shown in Fig. 2, water distribution total flux 8.0 tons/hour, be divided into 2 strands, wherein 7.3 tons/hour enter ethylbenzene/water separation tank, 0.7 ton/hour enters ethylbenzene and supplements vaporizer, and the weight content supplementing ethylbenzene evaporator water is 10.7%, and all the other operational conditions are identical with embodiment 1.Supplement ethylbenzene and water in ethylbenzene vaporizer be gasified totally after temperature be 116 DEG C, the gaseous phase outlet mixing of materials of the material after gasification and ethylbenzene/water separation tank, mixed temperature of charge is 99 DEG C, the vapor flow entering steam pipe oven is 17.2 tons/hour, steam pipe oven A temperature out 850 DEG C, steam pipe oven B temperature out 830 DEG C.
This device water ratio is 1.2, and high-temperature pipe and resuperheater gross investment are 6,000,000 Renminbi, and device total energy consumption is 310 kilograms of mark oil/ton vinylbenzene.
[embodiment 4]
Certain 100,000 tons/year of ethyl benzene dehydrogenation preparation of styrene device, adopt and press the ethyl benzene dehydrogenation preparation of styrene technology shown in Fig. 2, material ethylbenzene is divided into 2 strands, the flow entering ethylbenzene/water separation tank is 12 tons/hour, entering the flow that ethylbenzene supplements vaporizer is 9 tons/hour, water distribution total flux 8.2 tons/hour, be divided into 2 strands, wherein 6.0 tons/hour enter ethylbenzene/water separation tank, 2.2 tons/hour enter ethylbenzene and supplement vaporizer, the weight content supplementing ethylbenzene evaporator water is 20%, and all the other operational conditions are identical with embodiment 1.Supplement ethylbenzene and water in ethylbenzene vaporizer be gasified totally after temperature be 105 DEG C, the gaseous phase outlet mixing of materials of the material after gasification and ethylbenzene/water separation tank, mixed temperature of charge is 98 DEG C, the vapor flow entering steam pipe oven is 18 tons/hour, steam pipe oven A temperature out 845 DEG C, steam pipe oven B temperature out 825 DEG C.
This device water ratio is 1.25, and high-temperature pipe and resuperheater gross investment are 5,800,000 Renminbi, and device total energy consumption is 325 kilograms of mark oil/ton vinylbenzene.
[comparative example 1]
Certain 100,000 tons/year of ethyl benzene dehydrogenation preparation of styrene device, adopt and press the ethyl benzene dehydrogenation preparation of styrene technology shown in Fig. 1, material ethylbenzene flow is 21 tons/hour, and water distribution quantity 10.5 tons/hour, enters ethylbenzene/water separation tank jointly.In ethylbenzene/water separation tank, the weight content of water is 33%, isolated ethylbenzene and moisture 2 strands, wherein 140 tons/hour, ethylbenzene and 70 tons/hour, water enter ethylbenzene/water azeotropic vaporization device partial gasification, 65 tons/hour, ethylbenzene and 33 tons/hour, water enter ethylbenzene/water azeotropic vaporization device partial gasification, ethylbenzene supplements vaporizer and adopts vertical heat exchanger structure, ethylbenzene material is at tube side partial gasification, shell side is the heating steam of 0.35MPaG, material after partial gasification returns ethylbenzene/water separation tank, ethylbenzene/water separation tank gaseous phase materials working pressure 100kPaA, temperature 91 DEG C, through ethylbenzene superheater be heated to 500 DEG C and from steam pipe oven water vapour mixing enter the first dehydrogenation reactor (temperature of reaction 615 DEG C successively, pressure 60kPaA), resuperheater and the second dehydrogenation reactor (temperature of reaction 617 DEG C, pressure 50kPaA), the vapor flow entering steam pipe oven is 12.6 tons/hour, steam pipe oven A temperature out 915 DEG C, steam pipe oven B temperature out 900 DEG C.
This device water ratio is 1.1, and high-temperature pipe and resuperheater gross investment are 1,200 ten thousand Renminbi, and device total energy consumption is 300 kilograms of mark oil/ton vinylbenzene.
[comparative example 2]
Certain 100,000 tons/year of ethyl benzene dehydrogenation preparation of styrene device, adopt and press the ethyl benzene dehydrogenation preparation of styrene technology shown in Fig. 1, the vapor flow entering steam pipe oven is 16.8 tons/hour, steam pipe oven A temperature out 865 DEG C, steam pipe oven B temperature out 850 DEG C, all the other operational conditions are identical with comparative example 1.
This device water ratio is 1.3, and high-temperature pipe and resuperheater gross investment are 6,000,000 Renminbi, and device total energy consumption is 325 kilograms of mark oil/ton vinylbenzene.
Claims (7)
1. a method for ethyl benzene dehydrogenation preparation of styrene feed vaporization, comprises the following steps:
A) logistics 1 comprising material ethylbenzene and water enters ethylbenzene and supplements vaporizer, and vaporization obtains logistics 3 completely, and wherein in logistics 1, the weight percentage of water is 0 ~ 20%;
B) logistics 2 comprising material ethylbenzene and water enters ethylbenzene/water separation tank, isolated liquid phase ethylbenzene and water remove ethylbenzene/water azeotropic vaporization device, gas-liquid mixed logistics 4 is obtained after components vaporize, logistics 4 returns ethylbenzene/water separation tank, obtain gaseous phase outlet logistics 5, wherein in logistics 2, the weight percentage of water is 30 ~ 40%;
C) logistics 3 and logistics 5 obtain logistics 6 after mixing, and logistics 6 enters subsequent reactions system.
2. the method for ethyl benzene dehydrogenation preparation of styrene feed vaporization according to claim 1, it is characterized in that the weight percentage of water in logistics 1 is 5 ~ 15%, in logistics 2, the weight percentage of water is 31 ~ 35%.
3. the method for ethyl benzene dehydrogenation preparation of styrene feed vaporization according to claim 1, it is characterized in that the material ethylbenzene of 50 ~ 80 % by weight needed for ethylbenzene/water azeotropic vaporization device evaporation reaction, ethylbenzene supplements the material ethylbenzene of 20 ~ 50 % by weight needed for evaporator evaporation reaction.
4. the method for ethyl benzene dehydrogenation preparation of styrene feed vaporization according to claim 3, it is characterized in that the material ethylbenzene of 65 ~ 75 % by weight needed for ethylbenzene/water azeotropic vaporization device evaporation reaction, ethylbenzene supplements the material ethylbenzene of 25 ~ 35 % by weight needed for evaporator evaporation reaction.
5. the method for ethyl benzene dehydrogenation preparation of styrene feed vaporization according to claim 1, it is characterized in that ethylbenzene/water azeotropic vaporization device working pressure is 80 ~ 120kPaA, temperature is 85 ~ 97 DEG C; It is 80 ~ 120kPaA that ethylbenzene supplements evaporator operation pressure, and temperature is 100 ~ 140 DEG C.
6. the method for ethyl benzene dehydrogenation preparation of styrene feed vaporization according to claim 1, it is characterized in that the pressure of logistics 6 is 80 ~ 120kPaA, temperature is 90 ~ 130 DEG C.
7. the method for ethyl benzene dehydrogenation preparation of styrene feed vaporization according to claim 1, it is characterized in that ethylbenzene/water azeotropic vaporization device adopts styrene rectification system ethylbenzene/styrene separating tower overhead gas to be thermal source, ethylbenzene supplements vaporizer and adopts steam heating.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110300685.8A CN103030522B (en) | 2011-09-29 | 2011-09-29 | Method for vaporizing raw materials for styrene preparation through ethylbenzene dehydrogenation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110300685.8A CN103030522B (en) | 2011-09-29 | 2011-09-29 | Method for vaporizing raw materials for styrene preparation through ethylbenzene dehydrogenation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103030522A CN103030522A (en) | 2013-04-10 |
| CN103030522B true CN103030522B (en) | 2015-02-11 |
Family
ID=48017976
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110300685.8A Active CN103030522B (en) | 2011-09-29 | 2011-09-29 | Method for vaporizing raw materials for styrene preparation through ethylbenzene dehydrogenation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103030522B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107540508A (en) * | 2016-06-29 | 2018-01-05 | 中石化上海工程有限公司 | The method and its equipment of a kind of producing phenyl ethylene by ethyl benzene catalytic dehydrogenation |
| CN114436744B (en) * | 2020-10-20 | 2024-06-28 | 中国石油化工股份有限公司 | Method and system for preparing styrene by ethylbenzene dehydrogenation |
| CN114456027B (en) * | 2020-10-21 | 2024-06-28 | 中国石油化工股份有限公司 | Device and method for preparing styrene by ethylbenzene dehydrogenation |
| CN114456037B (en) * | 2020-10-21 | 2024-06-28 | 中国石油化工股份有限公司 | Raw material gasification method for preparing styrene by ethylbenzene dehydrogenation |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4479025A (en) * | 1982-11-22 | 1984-10-23 | Uop Inc. | Alkylaromatic hydrocarbon dehydrogenation process |
| US4695664A (en) * | 1986-04-17 | 1987-09-22 | The Badger Company, Inc. | Method of recovering heat from low temperature effluent |
| CN1587242A (en) * | 2004-07-09 | 2005-03-02 | 华东理工大学 | Improved method for producing styrene by ethyl benzene catalyzed dehydrogenation |
| CN101279883A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for heating ethylbenzene by ethylbenzene dehydrogenation reaction |
| CN101734999A (en) * | 2008-11-21 | 2010-06-16 | 中国石油化工股份有限公司 | Method for sequential separation and azeotropic recovery of ethyl benzene/styrene |
-
2011
- 2011-09-29 CN CN201110300685.8A patent/CN103030522B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4479025A (en) * | 1982-11-22 | 1984-10-23 | Uop Inc. | Alkylaromatic hydrocarbon dehydrogenation process |
| US4695664A (en) * | 1986-04-17 | 1987-09-22 | The Badger Company, Inc. | Method of recovering heat from low temperature effluent |
| CN1587242A (en) * | 2004-07-09 | 2005-03-02 | 华东理工大学 | Improved method for producing styrene by ethyl benzene catalyzed dehydrogenation |
| CN101279883A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for heating ethylbenzene by ethylbenzene dehydrogenation reaction |
| CN101734999A (en) * | 2008-11-21 | 2010-06-16 | 中国石油化工股份有限公司 | Method for sequential separation and azeotropic recovery of ethyl benzene/styrene |
Non-Patent Citations (1)
| Title |
|---|
| 苯乙烯生产工艺节能技术的研究;沈江;《化学世界》;20101231(第2期);全文 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103030522A (en) | 2013-04-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109503326B (en) | Process for indirectly producing ethanol by dimethyl ether | |
| CN103030522B (en) | Method for vaporizing raw materials for styrene preparation through ethylbenzene dehydrogenation | |
| CN101734999B (en) | Method for sequential separation and azeotropic recovery of ethyl benzene/styrene | |
| JP6216824B2 (en) | Process for producing styrene from ethylbenzene using azeotropic vaporization and low water to ethylbenzene total ratio | |
| CN101279883A (en) | Method for heating ethylbenzene by ethylbenzene dehydrogenation reaction | |
| CN102060664B (en) | High-efficiency and energy-saving reaction process for preparing ethylene glycol through hydrogenation of oxalate | |
| US20240238694A1 (en) | Method for refining styrene by using combined falling film reboilers and heat pump technology to provide heat source of separation column | |
| CN103664497B (en) | Method for producing styrene employing catalytic dehydrogenation of ethylbenzene | |
| CN103965001B (en) | Butylene oxidation-dehydrogenation reaction heat recovery method | |
| CN114436744B (en) | Method and system for preparing styrene by ethylbenzene dehydrogenation | |
| CN105669353B (en) | Ethylbenzene styrene separation process | |
| CN107603659A (en) | One kind alkylation fractional method | |
| EP4302853A1 (en) | Low-pressure drop ethylbenzene evaporator and energy-saving process for ethylbenzene vaporization in styrene dehydrogenation reaction system | |
| CN101955407A (en) | Preparation method and reaction device of acenaphthylene | |
| CN114456037B (en) | Raw material gasification method for preparing styrene by ethylbenzene dehydrogenation | |
| CN106631663A (en) | Energy-saving styrene production device | |
| CN107540508A (en) | The method and its equipment of a kind of producing phenyl ethylene by ethyl benzene catalytic dehydrogenation | |
| Geng et al. | Study on the process of producing crotonaldehyde from acetaldehyde catalyzed by Zr-β zeolite | |
| CN115582076A (en) | Device and production method for continuous production of dimethyl sebacate by solid acid catalyzed esterification | |
| CN202754919U (en) | 1, 4-butynediol stripping tower top steam latent heat recycle device | |
| CN105669354B (en) | ethylbenzene dehydrogenation reaction product separation method | |
| CN206375840U (en) | Styrene production energy-saving device | |
| CN216170035U (en) | Rectifying device | |
| CN105669352B (en) | Ethylbenzene styrene energy-saving separation method | |
| CN114349589B (en) | Method for preparing p-methyl ethylbenzene by using toluene and ethylene |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |