CN101279883A - Method for heating ethylbenzene by ethylbenzene dehydrogenation reaction - Google Patents
Method for heating ethylbenzene by ethylbenzene dehydrogenation reaction Download PDFInfo
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Abstract
The invention relates to a heating method of ethyl benzene of an ethyl benzene dehydrogenation reaction material, which mainly solves the problems of frequent accidents of the combined heat exchanger, difficult long-period and stable running, large pressure drop in the pipeline of a reactive system and inadequate heat recovery of a reactor charging/discharging three-level combined heat exchanger in the traditional styrene device due to the unreasonable flow for heating the ethyl benzene by utilizing the discharging of the high temperature reactor. The invention adopts the technical proposals that a liquid phase ethyl benzene material and ingredient water vapor are firstly vaporized to a gas phase with a temperature of between 90 and 110 DEG C through an independently arranged evaporator, and then enter the third level shell pass of the reactor charging/discharging combined heat exchanger to be preheated to a temperature of between 200 and 250 DEG C and then enter the first level shell pass of the reactor charging/discharging combined heat exchanger for being super-heated to a temperature of between 450 and 550 DEG C by the discharging of the high temperature reactor, and the second level shell pass of the reactor charging/discharging combined heat exchanger is used for generating saturated water vapor with a pressure of between 400KPaA and 1000KPaA; and the reactor charging/discharging three-level combined heat exchanger adopts the horizontal or vertical straight-line type arrangement mode, a linear type pipeline expansion joint is disposed between an exit of a dehydrogenation reactor and a material inlet of the first level in the reactor charging super-heater, namely the three-level combined heat exchanger to maintain the shortest distance for allowing installation between the dehydrogenation reactor and the charging super-heater, thereby reducing the tube shell pass thermal expansion difference of the first level heat exchanger.
Description
Technical field
The present invention relates to a kind of heating means of ethylbenzene by ethylbenzene dehydrogenation reaction.Specifically, relate to a kind of method of utilizing ethylbenzene negative pressure adiabatic catalytic dehydrogenation preparation of styrene reactor high temperature discharging heating raw ethylbenzene.
Background technology
Vinylbenzene is one of most important basic Organic Chemicals, is used to make copolymer resin (accounting for 11.5%), phenylethylene/butadiene copolymer latex SB (accounting for 5.3%), styrene-butadiene rubber(SBR) and latex SBR (accounting for 5.3%), unsaturated polyesters (accounting for 4.1%) such as polystyrene PS and EPS (accounting for 66.7%), ABS and SAN and other is as (accounting for 5.6%) such as styrene/methacrylic acid methyl esters latex, methyl methacrylate/butadiene/styrene copolymers MBS, ion exchange resin and medicines.
Because the strong growth of vinylbenzene derived product such as polystyrene and ABS resin consumption, the cinnamic production development in the world in recent years is very fast.The cinnamic throughput in the world was increased to about 2,588 ten thousand tons in 2004, and the throughput of its Middle and North America/South American region accounts for 28.7% of world's vinylbenzene overall throughput; The throughput of European Region accounts for 27.2% of world's overall throughput; The geographic throughput in Asia accounts for 39.5% of world's overall throughput.Expect 2006, the cinnamic overall throughput in the world will be above 3,000 ten thousand tons, and wherein the geographic consumption growth in Asia is the fastest, will be increased to 1218.7 ten thousand tons/year in 2006 from 1028.2 ten thousand tons/year in 2002.
The production technology of industrial ethyl benzene dehydrogenation preparation of styrene has adiabatic dehydrogenation technology, isothermal dehydrogenating technology and dehydrogenation selective oxidation processes.Wherein be most widely used, technology is the most sophisticated is ethylbenzene negative pressure adiabatic dehydrogenation technology.It is reported that 89% of whole world vinylbenzene output in 2004 is to adopt the ethylbenzene dehydrogenation production technique, have only 11% by other method production (as producing propylene oxide and vinylbenzene) by the ethylbenzene co-oxidation.
Cinnamic technological principle is made in ethylbenzene dehydrogenation: catalyzer and water vapor exist and 550～650 ℃ of hot conditionss under, dehydrogenation reaction takes place to select in ethylbenzene, generation vinylbenzene.
Δ Hr is a reaction heat in the formula.When reacting down for 627 ℃, Δ Hr=124.9KJ/mol (thermo-negative reaction).
Except generating polynomial (1) main reaction, side reactions such as thermo-cracking, hydrocracking and steam cracking take place also in reactor, by product mainly contains: hydrogen, benzene, toluene, methane, ethane, carbon monoxide, carbonic acid gas etc.
In ethylbenzene dehydrogenation technology, impurity atom in the material ethylbenzene also reacts, the resultant of major and minor reaction also can further react, so end product also comprises other by products, as alpha-methyl styrene, dimethylbenzene, propyl benzene, diethylbenzene, triethylbenzene, triphenyl methane, diphenylethlene, polystyrene and tar etc.
Fig. 1 and Fig. 2 are respectively the typical material ethylbenzene heating means of present vinylbenzene full scale plant sketch.
Among Fig. 1, material ethylbenzene and water vapor mixture 1a through evaporator evaporation, temperature is 90～120 ℃, the shell side that directly enters the first step ethylbenzene superheater 101a of three-stage combined interchanger is superheated to 450 ℃～550 ℃, mixing the back temperature with main steam 11a is 580～650 ℃, enter the first dehydrogenation reactor 104a, in reactor, the adiabatic ethylbenzene dehydrogenation reaction takes place in the ethylbenzene and the water vapor hot mixture that are gas phase in the process that flows through the fixed bed catalyst bed, generate principal product vinylbenzene and the preceding various by products of having addressed, simultaneously himself temperature also reduces, the logistics 3a temperature of outflow reactor 104a is 500～550 ℃, enters second dehydrogenation reactor 106a continuation reaction after the heat again through resuperheater.The reactor discharging 5a temperature that comprises various reaction product and water vapor and unconverted ethylbenzene is 500～600 ℃, its unitized exchanger 101a that will flow through, 102a, the tube side of 103a, this unitized exchanger is horizontal yi word pattern structure, in first step interchanger 101a, reactor discharging and the heat exchange of low temperature feedstock ethylbenzene, make it overheated, in the interchanger 102a of the second stage, with feedwater heat exchange generation pressure be the low-pressure steam of 300～500KpaA, in third stage interchanger 103a, with feedwater heat exchange generation pressure be the low low-pressure steam of 130～150KpaA, the reactant gases 6a temperature that derives from the tube side of interchanger 103a is reduced to 100～140 ℃ at last, continues cooling and separation and purification and recovery then.
Among Fig. 2, liquid phase feed ethylbenzene 1b mixes with batching water vapor 2b, temperature is 100～110 ℃, be the shell side that the vapour-liquid two-phase enters the third stage 103b of unitized exchanger, with the heat exchange of reactor discharging gas, preheating temperature to 200～250 ℃, the shell side that enters the first step 101b of three-stage combined interchanger then is superheated to 450 ℃～550 ℃, mixing the back temperature with main steam 11b is 580～650 ℃, enter the first dehydrogenation reactor 104b, in reactor, the adiabatic ethylbenzene dehydrogenation reaction takes place in the ethylbenzene and the water vapor hot mixture that are gas phase in the process that flows through the fixed bed catalyst bed, generate principal product vinylbenzene and various by product, simultaneously himself temperature also reduces, the logistics 5b temperature of outflow reactor 104b is 500～550 ℃, enters second dehydrogenation reactor 106b continuation reaction after the heat again through being arranged in two reactor intermediary resuperheaters.Comprise that effusive temperature is 500～600 ℃ among the reactor discharging autoreactor 106b of various reaction product and water vapor and unconverted ethylbenzene, its unitized exchanger 101b that will flow through, 102b, the tube side of 103b, this unitized exchanger is the perpendicular yi word pattern structure of putting, in first step interchanger 101b, material ethylbenzene heat exchange after reactor discharging and the preheating, make it overheated, in the interchanger 102b of the second stage, with feedwater heat exchange generation pressure be the middle pressure steam of 800～1200KpaA, in third stage interchanger 103b, the material ethylbenzene heat exchange makes it preheating, the reactant gases temperature that derives from the tube side of interchanger 103b is reduced to 100～140 ℃ at last, continues cooling and separation and purification and recovery then.
By main reaction formula (1) as can be known, it is the reversible reaction that a strong heat absorption increases molecule that ethylbenzene dehydrogenation generates vinylbenzene, and therefore, high temperature, negative pressure help this reversible reaction and carry out to generating cinnamic direction.For realizing higher conversion of ethylbenzene, industrial common employing has the placed in-line adiabatic radial reactor of two of resuperheater system, and this reactive system requires pressure drop little, and thermosteresis is little, to guarantee the high temperature and the negative pressure operating mode of reaction needed.
Up to 500～600 ℃, this part caloric requirement is rationally recycled from the reaction gas typical temperature of reactive system discharging, to reduce the comprehensive energy consumption of device.For this reason, be provided with three-stage combined interchanger mostly on the full scale plant at present, utilize pyroreaction gas superheated feedstock ethylbenzene, and steam takes place.This method is very rational on technology, can fully reclaim heat on the one hand, cuts down the consumption of energy, and owing to the unitized exchanger compact construction, pressure drop is little, the negative pressure operating mode that helps reacting on the other hand.This technology mainly contains Fig. 1 and two kinds of flow processs of Fig. 2 on full scale plant.
But find in the actual production, adopt the three-stage combined interchanger first step of Fig. 1 flow process because the shell journey temperature difference causes thermal dilation difference big too greatly, low-temperature end slip tube sheet is subjected to conduct oneself with dignity to influence and is difficult to slide and the drawing crack heat transfer tube, cause the shell side raw material to leak and the repairing of can only stopping, also there is the problem that is difficult to utilize in the low low-pressure steam 10a that third stage interchanger takes place in Fig. 1 flow process simultaneously; And adopt the three-stage combined interchanger of Fig. 2 flow process to have a narrow range of temperature owing to the shell journey, first step interchanger slip tube sheet miles of relative movement is short, heat transfer tube is difficult for drawing crack, but the third stage of combination exchanger is because shell side ethylbenzene raw material and the charging of batching vapor mixing are vapour-liquid two-phase state, the exchange heat pipe causes and washes away easily, thereby also there is the shortcoming of easy leakage in the third stage heat transfer tube of unitized exchanger, simultaneously owing to adopted the perpendicular yi word pattern structure of putting, pipeline between the reactor is compared obviously and will be grown with Fig. 1 flow process, the consequence of bringing is that pressure drop is big, thermosteresis is big, and this is to negative pressure, the pyritous ethylbenzene dehydrogenation reaction is quite disadvantageous.
Therefore, for long period is stably carried out industrial production, we need and arrange and be improved in the technology of this system and lectotype selection.
At the problem that this system exists, more existing patents have proposed different improving one's methods.The three-stage combined interchanger method for arranging that is " L " type as Chinese patent ZL102112454.x proposition; " ∏ " type reactor that CN1765858A proposes connects the method for " Γ " type unitized exchanger; Ethylbenzene catalytic dehydrogenation reactor that ZL03132028.7 proposes and the method for attachment between the interchanger etc.
Summary of the invention
Technical problem to be solved by this invention be in traditional styrene device the three-stage combined interchanger of reactor input and output material owing to utilize the flow process of high-temperature reactor discharging heating ethylbenzene unreasonable, accidents happened repeatly to cause this combination exchanger existence, be difficult to long-period stable operation, and the pipeline pressure drop is big in the reactive system, the inadequate problem of heat recuperation provides a kind of heating means of new ethylbenzene dehydrogenation material ethylbenzene.This method has the shell journey thermal dilation difference that can reduce first step interchanger, eliminate third stage interchanger material inlet washing away to tube side, solve the problem that they leak easily preferably, and the entire reaction system pressure drop is little, thermosteresis is little, and high temperature sensible heat energy has obtained the advantage of abundant recycling.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of heating means of ethylbenzene by ethylbenzene dehydrogenation reaction may further comprise the steps:
A) temperature is that 30 ℃～50 ℃ liquid phase feed ethylbenzene at first enters the ethylbenzene vaporizer of independent setting, be evaporated to 90 ℃～120 ℃ of temperature together with batching steam, the material of pressure 100～150kpaA, be preheated to 200～250 ℃ after entering the shell side of the third stage of reactor input and output material unitized exchanger and reactor discharging heat exchange then, enter the first step shell side of reactor input and output material unitized exchanger again, be superheated to 450～550 ℃ of temperature by the high-temperature reactor discharging, the ethylbenzene steam of pressure 60～120kpaA enters the dehydrogenation reaction zone reaction;
B) second stage of reactor input and output material unitized exchanger is used for taking place the saturated vapor that pressure is 500kpaA～1000kpaA;
C) the dehydrogenation reaction zone temperature is 550～600 ℃, pressure is that unitized exchanger first step feed superheater tube side is at first passed through in the reactor discharging of 40～120KPaA, after reactor feed heat exchange with shell side, temperature is that 300～410 ℃ reactor discharging enters warm area section vapour generator tube side in the unitized exchanger second stage, after oiler feed heat exchange with shell side, temperature is that 200～300 ℃ reactor discharging enters unitized exchanger third stage low temperature section tube side, after reactor feed heat exchange with shell side, temperature is 110～140 ℃, and pressure is that separation and purification and recovery system are sent in the reactor discharging of 30～110KPaA;
Wherein reactor input and output material three-stage combined interchanger employing level or the perpendicular yi word pattern decoration form of putting, the outlet of dehydrogenation reactor and reactor feed superheater are that linear pattern pipe expansion joint is installed between the material inlet of the first step in the three-stage combined interchanger, keep having between dehydrogenation reactor and the feed superheater allowing the shortest distance of installing.
In the technique scheme, the liquid phase ethylbenzene raw material is independent the setting with batching vapor mixing vaporizer, and ethylbenzene vaporizer preferred version is a still formula vaporizer pattern, and raw material evaporates at shell side, and tube side is heating steam, and tube side adopts U type tubular construction.The three-stage combined interchanger preferred version of reactor input and output material is horizontal yi word pattern structure.
Among Fig. 1, as preceding analysis, because the material ethylbenzene temperature of ethylbenzene superheater 101a shell side heating is low, only be 90～120 ℃, the shell side mean wall temperature is about 300 ℃, and the tube side mean wall temperature up to 450 ℃ about, the temperature difference reaches 150 ℃, the low-temperature end shell journey temperature difference of ethylbenzene superheater 101a is especially up to more than 250 ℃, cause the axial thermal expansion amount difference of shell journey to reach more than the 20mm, often this interchanger low-temperature end is designed to slide construction on the full scale plant for this reason, poor by its axial thermal expansion that is free to slide the offsetting pipe shell side.But in the actually operating, because slide construction is subjected to the influence of interchanger deadweight and polymkeric substance, slippage is very limited, makes tubulation be difficult to obtain effectively compensate and rupture with the two thermal dilation difference of housing.Be subjected to process technology limit simultaneously, the steam 10a pressure that third stage interchanger takes place is too low, is difficult to utilize, and has increased the energy consumption of device.
Though and Fig. 2 technology has solved the leakage problem of ethylbenzene superheater 101b, be not difficult to the low low-pressure steam utilized yet, but the third stage 103b of combination exchanger is because shell side ethylbenzene raw material and the charging of batching vapor mixing are vapour-liquid two-phase state, the exchange heat pipe causes and washes away easily, thereby also there is the shortcoming of easy leakage in the third stage heat transfer tube of unitized exchanger, simultaneously owing to adopted the perpendicular yi word pattern structure of putting, pipeline between the reactor is compared obviously and will be grown with Fig. 1 flow process, the consequence of bringing is that pressure drop is big, thermosteresis is big, and this is to negative pressure, the pyritous ethylbenzene dehydrogenation reaction is quite disadvantageous.
For making above-mentioned technology more become perfect, at its several principal contradictions, realize that promptly low pressure drop (less than 10KPa), solution ethylbenzene superheater tube/shell side thermal expansion amount difference leak raw material greatly easily, and the energy that fully reclaims pyroreaction gas, the present invention proposes the technical scheme of the heating means of ethyl benzene dehydrogenation system material ethylbenzene.
Consult technical scheme Fig. 3 of the present invention as can be known, temperature is the ethylbenzene vaporizer 108 that 30 ℃～50 ℃ liquid phase feed ethylbenzene 1 at first enters independent setting, be evaporated to 90 ℃～120 ℃ of temperature together with batching steam 2, the material 3 of pressure 100～150kpaA, enter shell side and the reactor discharging heat exchange of the third stage 103 of reactor input and output material unitized exchanger then, material 4 is preheated to 200～250 ℃, enter the shell side of the first step 101 of reactor input and output material unitized exchanger again, be superheated to 450～550 ℃ of temperature by high-temperature reactor discharging 8, the ethylbenzene steam 5 of pressure 60～120kpaA, enter dehydrogenation reaction zone first dehydrogenation reactor 104, in reactor, the adiabatic ethylbenzene dehydrogenation reaction takes place in the ethylbenzene and the water vapor hot mixture that are gas phase in the process that flows through the fixed bed catalyst bed, generate principal product vinylbenzene and the preceding various by products of having addressed, simultaneously himself temperature also reduces, logistics 6 temperature of outflow reactor 104 are 500～550 ℃, enter the 106 continuation reactions of second dehydrogenation reactor after the heat again through resuperheater 105, reactor discharging 8 temperature that comprise various reaction product and water vapor and unconverted ethylbenzene are 500～600 ℃, its unitized exchanger 101 of will flowing through, 102,103 tube side, this unitized exchanger is horizontal yi word pattern structure, linear pattern pipe expansion joint 107 is installed between the material inlet of the outlet of dehydrogenation reactor and reactor feed superheater (the three-stage combined interchanger first step), keep having between dehydrogenation reactor and the feed superheater shortest distance of the installation of allowing, in first step interchanger 101, material ethylbenzene heat exchange after reactor discharging and the preheating, make it overheated, in second stage interchanger 102, with feedwater heat exchange generation pressure be the water vapor of 500～1000KpaA, in third stage interchanger 103, preheater preheating ethylbenzene as the ethylbenzene raw material, reactant gases 9 temperature that derive from the tube side of interchanger 103 are reduced to 100～140 ℃ at last, continue cooling and separation and purification and recovery then.
From above analysis as can be known, at first, the present invention is owing to be provided with ethylbenzene vaporizer 108 separately, make the material 3 that enters the three-stage combined interchanger third stage be gas phase state, reduced washing away to 103 equipment tube sides, while ethylbenzene vaporizer 108 is still formula vaporizer preferably, heat transfer tube is a U type pipe, material ethylbenzene and batching steam can be respectively many mouthfuls enter the ethylbenzene vaporizer, do not have washing away of exchange heat pipe, and Fig. 2 flow process because being the single tube journey, the 103b interchanger enters interchanger after ethylbenzene and batching steam generally can only mix again, be vapour-liquid two-phase state owing to mix the back material, aggravated washing away of exchange heat pipe.
Secondly, for first step interchanger (ethylbenzene superheater 101), because the ethylbenzene raw material that enters heat exchanger shell pass has passed through the preheating of ethylbenzene preheater 103, ethylbenzene temperature after the preheating can reach 200～250 ℃, the shell side mean wall temperature of ethylbenzene superheater 101 is about 380 ℃ like this, the tube side mean wall temperature is about 450 ℃, the temperature difference is reduced to 70 ℃, the low-temperature end shell journey temperature difference of ethylbenzene superheater 101a is also reduced to about 150 ℃, the axial thermal expansion amount that has effectively reduced the shell journey is poor, the sliding distance of this interchanger low-temperature end slide construction shortens more than 50%, the suffered tensile stress of heat transfer tube greatly alleviates, technology of the present invention also can fully reclaim heat simultaneously, and the low low-pressure steam 10a that avoids Fig. 1 flow process is owing to the too low problem that is difficult to utilize of pressure.
At last, because in the technical program, the three-stage combined interchanger of reactor input and output material adopts horizontal yi word pattern decoration form, linear pattern pipe expansion joint is installed between the material inlet of the outlet of dehydrogenation reactor and reactor feed superheater (the three-stage combined interchanger first step), guarantee to have between dehydrogenation reactor and the feed superheater shortest distance of the installation of allowing, reduce droop loss and the calorific loss that a large amount of connection lines cause in Fig. 2 technology between the reactor and between reactor and three grades of combination exchangers, obtained better technical effect.
Description of drawings
Fig. 1 is the sketch of the typical material ethylbenzene heating means 1 of vinylbenzene full scale plant.
Fig. 2 is the sketch of the typical material ethylbenzene heating means 2 of vinylbenzene full scale plant.
Fig. 3 is that the present invention improves the process technology scheme sketch.
In Fig. 1,101a is the first step interchanger-ethylbenzene superheater of three-stage combined interchanger, 102a and 103a are respectively the second stage and the third stage interchanger of three-stage combined interchanger, 104a is first dehydrogenation reactor, 105a is a resuperheater, 106a is second dehydrogenation reactor, 107a is the linear pattern pipe expansion joint of installing between the outlet of dehydrogenation reactor 106a and the reactor feed superheater material inlet, material 1a is the material ethylbenzene of 101a shell side into, 2a is 101a shell side outlet ethylbenzene, 3a is first reactor outlet material, 4a is the resuperheater outlet material, 5a is second reactor outlet material, 6a is three grades of combination exchanger tube side outlet materials, and 7a is the feedwater of 102a shell side into, and 8a is the evaporation low pressure water vapor of 102a shell side, 9a is the feedwater of 103a shell side into, and 10a is the low low pressure water vapor of the evaporation of 103a shell side.
In Fig. 2,101b is the first step interchanger-ethylbenzene superheater of three-stage combined interchanger, 102b and 103b are respectively the second stage and the third stage interchanger of three-stage combined interchanger, 104b is first dehydrogenation reactor, 105b is a resuperheater, 106b is second dehydrogenation reactor, material 1b is the material ethylbenzene of 103b shell side into, 2b is batching water vapour, 3b is 103b shell side outlet ethylbenzene, 4b exports overheated ethylbenzene for the 101b shell side, and 5b is first reactor outlet material, and 6b is the resuperheater outlet material, 7b is second reactor outlet material, 8b is three grades of combination exchanger tube side outlet materials, and 9b is the feedwater of 102b shell side into, and 10b is the vaporize water steam of 102b shell side.
In Fig. 3,101 is the first step interchanger-ethylbenzene superheater of three-stage combined interchanger, 102 and 103 are respectively the second stage and the third stage interchanger of three-stage combined interchanger, 104 is first dehydrogenation reactor, 105 is resuperheater, 106 is second dehydrogenation reactor, 107 are the linear pattern pipe expansion installed between the outlet of dehydrogenation reactor 106 and reactor feed superheater material inlet joint, material 1 is the material ethylbenzene of 108 shell sides into, material 2 is the batching steam of into 108 shell sides, 3 is the phase feed ethylbenzene of into ethylbenzene preheater 103,4 is the ethylbenzene that after the 103 shell side preheatings, 5 is the superheated feedstock ethylbenzene of first dehydrogenation reactor 104 into, and 6 is first reactor outlet material, and 7 is the resuperheater outlet material, 8 is second reactor outlet material, 9 is three grades of combination exchanger tube side outlet materials, and 10 is the feedwater of 102 shell sides into, and 11 is the vaporize water steam of 102 shell sides.
The present invention is further elaborated below by embodiment.
Embodiment
[embodiment 1]
According to the present invention, the heat recovery and utilization technology that has the heating of 80,000 tons of/year styrene device ethyl benzene dehydrogenation system material ethylbenzenes of negative pressure adiabatic catalytic dehydrogenating technology of inter-stage second-heating two-stage series connection reactor and high temperature discharging for a certain employing as shown in Figure 3.
The first step ethylbenzene feed superheater 101 of three-stage combined interchanger in this technical process, it is one section one way tube and shell heat exchanger, its housing internal diameter is
Millimeter, tubulation length is 7000 millimeters, has 1600 tubulations, heat interchanging area is 1337 meters
2The second stage vapour generator 102 of unitized exchanger and ethylbenzene preheater 103, these two sections also all is the one way tube and shell heat exchanger, wherein the housing internal diameter of vapour generator 102 is
Millimeter, tubulation length is 8000 millimeters, and the tubulation radical is 1730, and heat interchanging area is 1652 meters
2The housing internal diameter of ethylbenzene preheater 103 is
Millimeter, tubulation length is 6000 millimeters, and the tubulation radical is 1730, and heat interchanging area is 1240 meters
2
The liquid phase ethylbenzene raw material 1 that temperature is 40 ℃ enters ethylbenzene vaporizer 108 respectively with batching steam 2, be evaporated to 92 ℃ of temperature, the gas phase of pressure 100kpaA, flow is 26041 kilograms/hour, the temperature that flows out into superheater 101 shell sides through the shell side of ethylbenzene preheater 103 is 200 ℃, reach 520 ℃ from the effusive temperature of superheater 101 shell sides at last, enter dehydrogenation reactor after mixing with main steam, the flow of dehydrogenation reactor discharging 8 is 38045 kilograms/hour.
The temperature that the discharging of reactor high temperature gas phase enters ethylbenzene superheater 101 tube sides is 567 ℃, and pressure is 45KPaA; The temperature that the reactor discharging is flowed out superheater 101 tube sides and entered vapour generator 102 tube sides is 365 ℃; The reactor discharging is 230 ℃ from the temperature that vapour generator 102 tube sides flow out into ethylbenzene preheater 103 tube sides; Dropped to 130 ℃ from the effusive reactor drop temperature of ethylbenzene preheater 103 tube sides at last, pressure is 39KPaA.
The gauge pressure that vapour generator 102 shell sides produce is that the flow of 350KPaG low-pressure steam 11 is 8 tons/hour.
Ethylbenzene superheater shell side medial temperature is 360 ℃, 465 ℃ of tube side medial temperatures, 160 ℃ of the low-temperature end temperature difference, entire reaction system (exporting from first dehydrogenation reactor, 104 imports to the three-stage combined interchanger third stage 103) stagnation pressure is reduced to 22Kpa, heat dissipation capacity 30 megajoules/hour.
[comparative example 1]
According to each Step By Condition of embodiment 1, the heating means of charging ethylbenzene adopt Fig. 1 mode, and its result is:
The gauge pressure that vapour generator 102a shell side produces is that the flow of 350KPaG low-pressure steam 8a is 5.6 tons/hour, and the gauge pressure that vapour generator 103a shell side produces is that the flow of the low low-pressure steam 10a of 40KPaG is 1.2 tons/hour.
Ethylbenzene superheater shell side medial temperature is 295 ℃, 460 ℃ of tube side medial temperatures, 250 ℃ of the low-temperature end temperature difference, entire reaction system (exporting from the first dehydrogenation reactor 104a import to three-stage combined interchanger third stage 103a) stagnation pressure is reduced to 25Kpa, heat dissipation capacity 31 megajoules/hour.
[comparative example 2]
Each Step By Condition according to embodiment 1, the heating means of charging ethylbenzene adopt Fig. 2 mode, its result is: the gauge pressure that vapour generator 102b shell side produces is that the flow of 1100KPaG low-pressure steam 10b is 4 tons/hour, entire reaction system (exporting from the first dehydrogenation reactor 104a import to three-stage combined interchanger third stage 103a) stagnation pressure is reduced to 45Kpa, heat dissipation capacity 120 megajoules/hour.
Claims (3)
1. the heating means of an ethylbenzene by ethylbenzene dehydrogenation reaction may further comprise the steps:
A) temperature is that 30 ℃～50 ℃ liquid phase feed ethylbenzene at first enters the ethylbenzene vaporizer of independent setting, be evaporated to 90 ℃～120 ℃ of temperature together with batching steam, the material of pressure 100～150kpaA, be preheated to 200～250 ℃ after entering the shell side of the third stage of reactor input and output material unitized exchanger and reactor discharging heat exchange then, enter the first step shell side of reactor input and output material unitized exchanger again, be superheated to 450～550 ℃ of temperature by the high-temperature reactor discharging, the ethylbenzene steam of pressure 60～120kpaA enters the dehydrogenation reaction zone reaction;
B) second stage of reactor input and output material unitized exchanger is used for taking place the saturated vapor that pressure is 500kpaA～1000kpaA;
C) the dehydrogenation reaction zone temperature is 550～600 ℃, pressure is that unitized exchanger first step feed superheater tube side is at first passed through in the reactor discharging of 40～120KPaA, after reactor feed heat exchange with shell side, temperature is that 300～410 ℃ reactor discharging enters warm area section vapour generator tube side in the unitized exchanger second stage, after oiler feed heat exchange with shell side, temperature is that 200～300 ℃ reactor discharging enters unitized exchanger third stage low temperature section tube side, after reactor feed heat exchange with shell side, temperature is 110～140 ℃, and pressure is that separation and purification and recovery system are sent in the reactor discharging of 30～110KPaA;
Wherein reactor input and output material three-stage combined interchanger employing level or the perpendicular yi word pattern decoration form of putting, the outlet of dehydrogenation reactor and reactor feed superheater are that linear pattern pipe expansion joint is installed between the material inlet of the first step in the three-stage combined interchanger, keep having between dehydrogenation reactor and the feed superheater allowing the shortest distance of installing.
2. according to the heating means of the described ethyl benzene dehydrogenation system material ethylbenzene of claim 1, it is characterized in that the ethylbenzene vaporizer is a still formula vaporizer pattern, raw material evaporates at shell side, and tube side is heating steam, and tube side adopts U type tubular construction.
3. according to the heating means of the described ethyl benzene dehydrogenation system material ethylbenzene of claim 1, it is characterized in that the three-stage combined interchanger of reactor input and output material is horizontal yi word pattern structure.
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| CNA2007100390939A CN101279883A (en) | 2007-04-04 | 2007-04-04 | Method for heating ethylbenzene by ethylbenzene dehydrogenation reaction |
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| CNA2007100390939A CN101279883A (en) | 2007-04-04 | 2007-04-04 | Method for heating ethylbenzene by ethylbenzene dehydrogenation reaction |
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| CN101279883A true CN101279883A (en) | 2008-10-08 |
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| CNA2007100390939A Pending CN101279883A (en) | 2007-04-04 | 2007-04-04 | Method for heating ethylbenzene by ethylbenzene dehydrogenation reaction |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102258877A (en) * | 2011-05-24 | 2011-11-30 | 徐志刚 | Method and device for evaporating ethylbenzene and water azeotrope |
| CN103030522A (en) * | 2011-09-29 | 2013-04-10 | 中国石油化工股份有限公司 | Method for vaporizing raw materials for styrene preparation through ethylbenzene dehydrogenation |
| CN104826567A (en) * | 2015-05-07 | 2015-08-12 | 中石化南京工程有限公司 | Apparatus utilizing heat energy generated during platinum catalytic hydrogenation in cyclohexanone production for dehydrogenation technology |
| 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 |
| CN110740984A (en) * | 2017-08-30 | 2020-01-31 | 特殊设计和工程局卡塔利扎托尔股份公司 | Process layout (variants) of a plant for the dehydrogenation of C3-C5 paraffins |
| CN111848323A (en) * | 2020-05-26 | 2020-10-30 | 常州瑞华化工工程技术股份有限公司 | Process method for producing styrene by low-water-ratio ethylbenzene dehydrogenation |
| CN112880456A (en) * | 2021-01-26 | 2021-06-01 | 上海蓝滨石化设备有限责任公司 | Multi-module series heat exchanger |
| CN113620771A (en) * | 2020-05-08 | 2021-11-09 | 中国石油化工股份有限公司 | Reaction system and reaction method for preparing divinylbenzene through dehydrogenation of diethylbenzene |
| CN114456027A (en) * | 2020-10-21 | 2022-05-10 | 中国石油化工股份有限公司 | Device and method for preparing styrene through ethylbenzene dehydrogenation |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102258877A (en) * | 2011-05-24 | 2011-11-30 | 徐志刚 | Method and device for evaporating ethylbenzene and water azeotrope |
| CN102258877B (en) * | 2011-05-24 | 2013-08-28 | 徐志刚 | Method and device for evaporating ethylbenzene and water azeotrope |
| CN103030522A (en) * | 2011-09-29 | 2013-04-10 | 中国石油化工股份有限公司 | Method for vaporizing raw materials for styrene preparation through ethylbenzene dehydrogenation |
| CN103030522B (en) * | 2011-09-29 | 2015-02-11 | 中国石油化工股份有限公司 | Method for vaporizing raw materials for styrene preparation through ethylbenzene dehydrogenation |
| CN104826567A (en) * | 2015-05-07 | 2015-08-12 | 中石化南京工程有限公司 | Apparatus utilizing heat energy generated during platinum catalytic hydrogenation in cyclohexanone production for dehydrogenation technology |
| CN104826567B (en) * | 2015-05-07 | 2016-06-15 | 中石化南京工程有限公司 | A kind of Cyclohexanone Production platinum catalysis hydrogenation heat energy is for the device of dehydrogenating technology |
| 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 |
| CN110740984A (en) * | 2017-08-30 | 2020-01-31 | 特殊设计和工程局卡塔利扎托尔股份公司 | Process layout (variants) of a plant for the dehydrogenation of C3-C5 paraffins |
| CN113620771A (en) * | 2020-05-08 | 2021-11-09 | 中国石油化工股份有限公司 | Reaction system and reaction method for preparing divinylbenzene through dehydrogenation of diethylbenzene |
| CN111848323A (en) * | 2020-05-26 | 2020-10-30 | 常州瑞华化工工程技术股份有限公司 | Process method for producing styrene by low-water-ratio ethylbenzene dehydrogenation |
| CN114456027A (en) * | 2020-10-21 | 2022-05-10 | 中国石油化工股份有限公司 | Device and method for preparing styrene through ethylbenzene dehydrogenation |
| CN112880456A (en) * | 2021-01-26 | 2021-06-01 | 上海蓝滨石化设备有限责任公司 | Multi-module series heat exchanger |
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