CN1204099C - Cooling and heat recovery method for high temperature discharging of ethyl benzene dehydrogenation system - Google Patents
Cooling and heat recovery method for high temperature discharging of ethyl benzene dehydrogenation system Download PDFInfo
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Abstract
The present invention relates to a cooling and heat recovering method for the high-temperature discharging of an ethylbenzene dehydrogenation reaction system, which mainly solves the problems in the previous documents that connection pipe lines between every two heat exchangers used for material discharging and heat supply by a high-temperature reactor are long so that the loss of pressure reduction and the heat loss are high. The feeding superheater of a reactor at a high-temperature section in a heat recovering system for the high-temperature discharging of an ethylbenzene dehydrogenation reactor is connected with a steam generator arranged at a moderate-temperature section horizontally through a short cylinder with a wave-shaped expansion joint having at least one wave, and the central lines of the feeding superheater and the steam generator form an included angle of 90 to 135 DEG; the steam generator arranged at the moderate-temperature section horizontally is connected with an ethylbenzene evaporator at a low-temperature section by the short cylinder, and the central lines of the steam generator and the ethylbenzene evaporator form an included angle of 135 to 180 DEG. The method solves the two problems in the prior art that three heat exchangers are separated independently so that the pressure is greatly reduced and the heat loss is large. The method is suitable for styrene industrial production by the negative-pressure dehydrogenation of ethylbenzene.
Description
Technical field
The present invention relates to the cooling and the heat recovery method of high temperature discharging of ethyl benzene dehydrogenation system.Specifically, relate to a kind of method that is used for ethylbenzene negative pressure adiabatic catalytic dehydrogenation preparation of styrene reactor high temperature discharging cooling and heat recuperation.
Background technology
As everyone knows, vinylbenzene is a kind of important chemical material commodity, is used to make polystyrene PS, engineering plastics ABS and AS, styrene butadiene rubber sbr and latex SBR-latex, styrene/butadiene/styrene block copolymers SBS, methyl methacrylate/butadiene/styrene copolymers MBS, phenylethylene/maleic anhydride copolymer SMA, styrene/methacrylic acid methyl esters latex and unsaturated polyester, ion-exchange resin and medicine etc.
In view of vinylbenzene purposes and to its growing demand widely, since World War II, its industrial production has obtained to develop rapidly.Whole world production of styrene ability reached 2,288 ten thousand tons/year in 2000.
In all multi-styrene industrial processes, be most widely used, technology is the most ripe, the most rational operational path of economy is that vinylbenzene is made in ethylbenzene dehydrogenation.The statistic data of nineteen ninety shows that 90.2% of whole world vinylbenzene output was to adopt the ethylbenzene dehydrogenation production technique at that time, has only 9.8% by other method production (as producing propylene oxide and vinylbenzene by the ethylbenzene co-oxidation).
The ethyl benzene dehydrogenation preparation of styrene production technology is continually developed research through for many years, from paying attention to Study of Catalyst in early days, transfer to improvement catalyzer and installation optimization and lay equal stress on, and especially payes attention to reducing the material consumption and the energy consumption of unit styrene product, improves competitiveness.At present, the vinylbenzene industrial production generally adopts the negative pressure adiabatic dehydrogenation technology with inter-stage second-heating two-stage series connection reactor, and device is tending towards maximizing, automatization, and raw material consumption and energy consumption descend significantly.
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---reaction heat in the formula.When reacting down for 627 ℃, Δ Hr=124.9 kj/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 is Chinese cock (E.G.Hancock) [English] chief editor " benzene and industrial derivative thereof " (Benzene And Its IndustrialDerivatives) Chinese translation (Chemical Industry Press, November nineteen eighty-two, Beijing) a kind of general flow chart of dehydrogenation of ethylbenzene to styrene device in the 319th page.Because present patent application does not relate to the separation and purification and the recovery of dehydrogenation reactor discharging, so separation and purification and recovery part are only summarized expression with dashed rectangle, with the outstanding related theme of present patent application---the technology of reactor discharging cooling and heat recuperation and the improvement of heat-exchange equipment thereof.
Consult Fig. 1 as can be known, usually drawing one so-called batching steam from the water vapor 8 of steam pipe system converges with charging ethylbenzene, its major portion then enters the shell side of interchanger 4, with tube side from the reactor discharging heat exchange of interchanger 3 and heat up, enter then in the boiler tube of steam superheater 1, by directly fire heating and be warmed up to 720～850 ℃ in the burner hearth, as the main steam of ethylbenzene dehydrogenation technology.After fresh ethylbenzene 9 (liquid state) converged with circulation ethylbenzene 10 (liquid state), one batching vapor mixing of telling with water vapor 8 just entered interchanger 5 shell sides again, with the reactor discharging heat exchange from interchanger 4 tube sides of tube side, makes the liquid ethylbenzene vaporization.Gained ethylbenzene/water vapor gas phase mixture and then be imported into the shell side of interchanger 3, heat exchange is carried out in the discharging from dehydrogenation reactor system 2 with tube side, and be heated to 450～520 ℃, then with converging from 720～850 ℃ of hyperthermia and superheating main steams of steam superheater 1, the two mixes the back temperature and reaches 570～650 ℃, just together enters reactor assembly 2.In reactor assembly 2, 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, himself temperature also reduces simultaneously.Comprise that effusive temperature is 500～600 ℃ in the reactor discharging autoreaction system 2 of various reaction product and water vapor and unconverted ethylbenzene, its will flow through successively tube side of interchanger 3,4,5, reaction feed heat exchange with shell side, realize heat recovery and utilization and self cooling, the temperature that derives from interchanger 5 tube sides is 100～150 ℃ at last, enters then to continue cooling and separation and purification and recovery zone 6.In with the cooling of dashed rectangle 6 representatives, separation, refining and recovery process, the various components that the reactor discharging comprises obtain separating, and gained coagulates water 11 after stripping is handled, and can be used as oiler feed and recycle; Gained dehydrogenated tail gas and 12 can be sent to steam superheater 1 and act as a fuel or recover hydrogen; The not reacted ethylbenzene 10 circulation Returning reacting systems of gained are once more as dehydrogenation feed; Gained is respectively the major product and the byproduct of this Ethyl Benzene Dehydrogenation Plant through purified vinylbenzene 15, benzene 13, toluene 14; Gained tar 16 can be sent to steam superheater 1 and act as a fuel and burn, and also can be used as a kind of byproduct and transports to out-of-bounds, as the raw material of further comprehensive utilization.
Investigate 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 high temperature and low pressure help this reversible reaction and carries out to generating cinnamic direction.This adiabatic radial reactor of two-stage series connection negative pressure system that has the inter-stage second-heating just obtains the reason place of widespread usage in the ethyl benzene dehydrogenation preparation of styrene industrial production.Because the beds of this radial adiabatic reactor is thinner relatively, under the identical prerequisite of the air speed of reaction mass by beds, the pressure drop of radial adiabatic reactor is starkly lower than the pressure drop of the thicker relatively calandria type fixed bed equitemperature reactor of beds.So the radial adiabatic reactor more helps forming the negative pressure operating mode of condition of high vacuum degree.In addition, the interchanger that is provided with between two placed in-line adiabatic radial reactors of this reactor assembly can be reduced to 500～570 ℃ material and implements to heat for the second time carry out adiabatic dehydrogenation reaction back temperature in first step reactor, make material be warmed up to 580～650 ℃ again, enter second stage radial reactor, carry out the adiabatic dehydrogenation reaction once more, thereby charging ethylbenzene can be realized higher transformation efficiency.
As mentioned above, the advantage of this negative pressure adiabatic dehydrogenation reactive system is mathematical, but also produce the problem that must face thereupon: the one, how reasonably the heat of the high-temperature reactor discharging that is in negative pressure to be recycled, and make it to cool down, to reduce the comprehensive energy consumption of product; The 2nd, how to make to be used to the type selecting that reclaims reactor discharging heat and make it the refrigerative heat-exchange equipment and to arrange the negative pressure operating mode of adaptive response system better.
Make the heat recuperation and the utilization of styrene device about ethylbenzene dehydrogenation, U.S. Pat 4628136 has proposed a kind of overhead condenser from ethylbenzene/styrene separating tower and has reclaimed low warm, be used for heating raw ethylbenzene/water vapor charging, thereby reduce the steam superheater heat supplied, reach the method for energy-saving effect; German patent DE 3147323 is devoted to effectively to utilize in the ethylbenzene dehydrogenation technology heat energy, propose with being cooled to 90～120 ℃, and the reactor discharging gas of locating 0.4～1.2 barometric point go to add hot water make it the vaporization, the gained water vapor pressure is reduced to 1.4～2.5 normal atmosphere, again with this steam deallocation system ethylbenzene/water vapor incoming mixture; The method that U.S. Pat 3515767 reclaims dehydrogenation reactor discharging heat is to utilize this heat to remove to produce subatmospheric water vapor, this low-pressure steam is compressed with compressor again, reclaims the reboiler heat supply of fractionation plant as product separation; English Patent GB1122857 then proposes to obtain heat and is used to produce water vapor from the dehydrogenation reactor discharging, and this steam is compressed, as the heating medium of ethyl benzene/styrene separation column reboiler.More than the improvement project that proposes of each piece patent about the Ethyl Benzene Dehydrogenation Plant heat recovery and utilization, dispose compressor mostly.Obviously, its facility investment and working cost all are very important expenditures.
Summary of the invention
Technical problem to be solved by this invention is that three interchanger that utilize reactor discharging high temperature sensible heat that exist in the technology of document in the past are owing to separately independently place, pipeline is long to cause droop loss bigger, the calorific loss that pipeline causes is bigger, floor space is big, and interchanger itself is owing to the thermal expansion reason easily causes the problem of leakage, and a kind of cooling and heat recovery method of new high temperature discharging of ethyl benzene dehydrogenation system is provided.It is little that this method has the interchanger floor space, and the droop loss that pipeline causes is little, and calorific loss is few, can effectively solve the characteristics of heat exchanger leakage problem.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of cooling of high temperature discharging of ethyl benzene dehydrogenation system and heat recovery method may further comprise the steps:
A) the dehydrogenation reaction zone temperature is 500～650 ℃.Pressure is that high temperature section reactor feed superheater tube side is at first passed through in the reactor discharging of 10～100KPa, after reactor feed heat exchange with shell side, temperature is a warm area section vapour generator tube side during 300～410 ℃ reactor discharging enters, after oiler feed heat exchange with shell side, temperature is that 140～280 ℃ reactor discharging enters low temperature section ethylbenzene vaporizer 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 30～90KPa;
B) temperature is that 95～120 ℃ the material ethylbenzene and the vapor mixing of preparing burden become reactor feed, at first enter low temperature section ethylbenzene vaporizer shell side, after the reactor discharging heat exchange with tube side, temperature is that 95～220 ℃ reactor feed directly enters high temperature section reactor feed superheater shell side, after reactor discharging heat exchange with tube side, the reactor feed temperature is 400～570 ℃, and pressure is 80～140KPa, enters the dehydrogenation reaction zone reaction;
C) warm area section vapour generator shell side during oiler feed enters after the reactor discharging heat exchange with tube side, produces the saturation steam of pressure 150～1100KPa;
Wherein on the housing between two of high temperature section reactor feed superheater retaining plates the major diameter corrugated-type expansion joint is set, the middle warm area section vapour generator of high temperature section reactor feed superheater and horizontal positioned is at least one the short tube of corrugated-type expansion joint and is connected by wave number is set, and the angle α that both medullary rays form is 90～135 °; The middle warm area section vapour generator of horizontal positioned is connected by short tube with low temperature section ethylbenzene vaporizer, and the angle β that their both medullary rays form is 135～180 °.
High temperature section reactor feed superheater adopts the thin tubesheet structure in the technique scheme, and wave number is set on the shell side between two tube sheets is at least one major diameter corrugated-type expansion joint.The preferred value of the angle α that the medullary ray of the middle warm area section vapour generator of high temperature section reactor feed superheater and horizontal positioned forms is 90 °, and the preferred value of the angle β that the middle warm area section vapour generator of horizontal positioned and the medullary ray of low temperature section ethylbenzene vaporizer form is 180 °.
In Fig. 1, if what number 2 representatives is a cover negative dehydrogenation reactor assembly, resemble so as shown in Figure 1, with pipeline the interchanger of interchanger 3, interchanger 4, interchanger 5 three platform independent is together in series, the dehydrogenation reactor high temperature discharging is successively by the tube side of these three interchanger and the connection line between them, it is long then to be the distance that the high temperature discharging of gas phase not only flows through, and heat lost by radiation is big, and will experience repeatedly the long-pending drastic change of cross section of fluid channel.Or rather, its flow velocity changes repeatedly with suddenly big or suddenly small, certainly will cause meaningless power loss, and the pipeline of in addition flowing through is long, these two reasons will form bigger resistance, thereby increase the difficulty that vacuumizing device (using screw vacuum pump usually) is extracted into reactor assembly 2 enough vacuum tightness.Advancing in order to reduce reactor/resistance (being reduced to less than 10KPa) of discharging heat-exchange system, and these three interchanger are fused, cancel the elongated connecting tube between them, obviously is a kind of selection of wisdom.
In the vinylbenzene full scale plant, in order to reduce the resistance of negative dehydrogenation reactive system, interchanger 3, interchanger 4,5 three interchanger of interchanger are selected the one way tube and shell heat exchanger mostly for use, and the reactor discharging are passed through by tube side among Fig. 1.When this three one way tube and shell heat exchanger vertically after the end to end one-tenth yi word pattern of the tube side integral body, this inner tubulation is divided into the yi word pattern buster of three sections vertically, no matter horizontally-arranged still erecting put, though all can reach the purpose that reduces the tube side resistance, but occur new problem again, i.e. thermal expansion causes tube side with the internal leakage between the shell side thereupon.Trace it to its cause, the one, enter running status after, tubulation is with the temperature contrast between the housing, makes the joint of tubulation end and tube sheet and tube sheet all bear big stress with the weld seam of housing and ruptures; The 2nd, the axial length of this unitized exchanger that is formed by connecting along the axial yi word pattern of tubulation is very long, and tubulation is difficult to obtain compensation with the two thermal dilation difference of housing.This internal leakage mainly betides the high temperature section (being equivalent to interchanger 3 among Fig. 1) of yi word pattern unitized exchanger, and horizontal placement is even more serious than vertical placement.Certainly, the perpendicular floor space of putting of horizontally-arranged ratio is much bigger, and also being one is worth improved problem.
For making aforesaid combination formula interchanger more become perfect, at its two principal contradictions---realize the leakage problem between low pressure drop (less than 10KPa) and solution temperature compensation and the pipe/shell side, the present invention proposes the unitized exchanger technical scheme.
Consult technical scheme Fig. 2 of the present invention as can be known, after fresh ethylbenzene 109 (liquid state) converges with circulation ethylbenzene 110 (liquid state), mix with batching steam 108 again, the reactor feed temperature that forms reaches 90～110 ℃, just enter the shell side of the low temperature section ethylbenzene vaporizer 105 of unitized exchanger, ethylbenzene is realized vaporization, and is warmed up to 95～220 ℃, then enter the shell side of unitized exchanger high temperature section feed superheater 103, pressure is 80～140KPa therebetween.At this, flow out after reactor feed is heated to 400～570 ℃, and converge with 720～850 ℃ of hyperthermia and superheating steam 101A from steam superheater.The two is behind thorough mixing, and temperature is 570～650 ℃, just enters the 1st grade of dehydrogenation reactor 102A, and reaction mass radially flows through beds, and temperature drops to 500～570 ℃ gradually in carrying out dehydrogenation reaction process.Then, the discharging of 102A is imported into the tube side of intermediate heat 102C, by 720～860 ℃ of hyperthermia and superheating steam 101B heating from steam superheater of shell side, be warmed up to 580～650 ℃ once more, enter the 2nd grade of dehydrogenation reactor 102B, the beds of the 102B that radially flows through continues to take place dehydrogenation reaction, the reactor drop temperature of deriving from 102B is 500～600 ℃ at last, and pressure is 40～100KPa.The discharging of this strand pyritous reactor enters the tube side of unitized exchanger high temperature section feed superheater 103 then, after ethylbenzene/water vapor charging heat exchange with shell side, when it entered the tube side of warm area section vapour generator 104 in the unitized exchanger, temperature had dropped to 300～410 ℃.At this, the feedwater of its heating shell side, producing gauge pressure is the steam of 150～1100KPa.When the reactor discharging enters unitized exchanger low temperature section ethylbenzene vaporizer 105 tube sides then, its temperature has been reduced to 140～280 ℃, continue to utilize its sensible heat, the vaporization of the reactor feed ethylbenzene of shell side and heat up (temperature is 95～220 ℃), and himself temperature drops to 110～140 ℃ gradually, and pressure then drops to 30～90KPa.This stock-traders' know-how has gone through that unitized exchanger is implemented heat recovery and utilization to its and the reactor discharging that cools down just is sucked and the separation and purification and the recovery system that flow to the downstream done further processing, obtain the various products and the by product of ethylbenzene dehydrogenation technology, ethylbenzene 110 Returning reacting systems that wherein circulate are once more as dehydrogenation feed.
From above analysis as can be known the present invention because housing between two blocks of stationary tubesheets of high temperature section reactor feed superheater is provided with the major diameter corrugated-type expansion joint, and between high temperature section reactor feed superheater and middle warm area section vapour generator, corrugated-type expansion joint is set also, can solves the reactor feed superheater and be connected the damage that short tube causes because of thermal expansion because of thermal expansion causes between leakage problem between the tube side shell side and feed superheater and the vapour generator.To be connected with short tube between high-temperature zone reactor feed superheater, middle warm area vapour generator and the cold zone ethylbenzene vaporizer, and reactor feed superheater in high-temperature zone becomes 90～135 ° of angles with middle warm area vapour generator medullary ray, middle warm area vapour generator becomes the technical scheme of 135～180 ° of angles with cold zone ethylbenzene vaporizer medullary ray, saved floor space on the one hand, reduce droop loss and calorific loss that a large amount of connection lines cause on the other hand, obtained better technical effect.
Description of drawings
Fig. 1 is the reactive system general flow chart of dehydrogenation of ethylbenzene to styrene device.In Fig. 1,1 is steam superheater; 2 are dehydrogenation reactor (its representative can be the separate unit reactor, also can be the adiabatic radial reactor of the two-stage series connection negative pressure system with inter-stage interchanger second-heating); 3,4,5 be interchanger, the setting of these three interchanger is in order to recycle the heat of reactor high temperature discharging, simultaneously it to be cooled down, to carry out following process; 6 represented the reactor discharging continue to be cooled off, numerous equipment of separation and purification and the various products of recovery; The 7th, the fuel gas of steam superheater is or/and oil; The 8th, water vapor; The 9th, as the fresh ethylbenzene of dehydrogenation feed; The 10th, circulation ethylbenzene (the reactor discharging through separate, the refining and not reacted ethylbenzene Returning reacting system that reclaims, after converging with fresh ethylbenzene, once more as reactor feed); The 11st, the water with fixed attention that the reactor discharging obtains through cooling, separation; The 12nd, dehydrogenated tail gas; The 13rd, through separation and purification and ethylbenzene dehydrogenation byproduct benzene; The 14th, byproduct toluene; The 15th, through the major product benzene ethylbenzene of separation and purification gained ethylbenzene dehydrogenation; The 16th, the heavy byproduct tar that after the separation and purification operation, obtains.
Fig. 2 is an improvement project simplified schematic diagram of the present invention.Wherein the left side is the adiabatic radial reactor of the two-stage series connection negative pressure system that typically has the inter-stage second-heating; Right-hand part then is the L type unitized exchanger that improved three heat exchangers in series are formed.For the ease of comparing with Fig. 1, the numbering among Fig. 2 is basic corresponding with Fig. 1, just the numbering among Fig. 1 is added that " 100 " are as corresponding numbers among Fig. 2.For example the numbering 103 among Fig. 2 is just corresponding to the numbering among Fig. 13, and surplus person analogizes.
In Fig. 2,102A is a first step dehydrogenation reactor; 102B is a second stage dehydrogenation reactor; 102C is heated the intermediate heat that heats up and be provided with for the second time for the realization response material; The 103rd, the high temperature section of unitized exchanger is as the reactor feed superheater; The 104th, the middle warm area section of unitized exchanger is as the vapour generator that produces steam; The 105th, the low temperature section of unitized exchanger is as the ethylbenzene vaporizer that liquid ethylbenzene is vaporized; The 107th, the drum of vapour generator 104.101A is the main steam from steam superheater (do not draw among the figure, can referring to Fig. 1); 101B is the second-heating hyperthermia and superheating steam that feeds the intermediate heat shell side; 101C is the superheated vapour that returns steam superheater after the cooling; The 106th, separation and purification and recovery system (do not draw among the figure, can referring to Fig. 1) be sent in the reactor discharging of lowering the temperature after unitized exchanger reclaims heat; The 108th, batching steam; The 109th, fresh ethylbenzene; The 110th, circulation ethylbenzene; The 111st, oiler feed; The 112nd, the steam (being sent to the factory steam pipe network) that vapour generator 104 produces; 113 is corrugated-type expansion joint, and 114 for connecting short tube.
The present invention is further elaborated below by embodiment.
Embodiment
[embodiment 1]
According to the present invention, have 60,000 tons of/year styrene device Ethylbenzene Dehydrogenation Reactor high temperature discharging coolings of negative pressure adiabatic catalytic dehydrogenating technology of inter-stage second-heating two-stage series connection reactor and L type unitized exchanger that heat recovery and utilization designs for a certain employing as shown in Figure 2, α=90 ° wherein, β=180 ° form a L type unitized exchanger.
The perpendicular arm of this L type unitized exchanger is a reactor feed superheater 103, and it is one section one way tube and shell heat exchanger, and its housing internal diameter is 1500 millimeters of φ, and tubulation length is 7000 millimeters, has 749 tubulations, and heat interchanging area is 626 meters
2The transverse arm of L type unitized exchanger is vapour generator 104 and ethylbenzene vaporizer 105 successively.These two sections also all is the one way tube and shell heat exchanger, and wherein the housing internal diameter of vapour generator 104 is 1500 millimeters of φ, and tubulation length is 3000 millimeters, and the tubulation radical is 749, and heat interchanging area is 268 meters
2The housing internal diameter of ethylbenzene vaporizer 105 is 1500 millimeters of φ, and tubulation length is 9000 millimeters, and the tubulation radical is 749, and heat interchanging area is 805 meters
2
Reactor feed (108+109+110) flow by ethylbenzene vaporizer 105 shell sides and feed superheater 103 shell sides is 16733 kilograms/hour successively; The flow of reactor discharging 106 is 27412 kilograms/hour.
The temperature that the discharging of reactor high temperature gas phase enters reactor feed superheater 103 tube sides is 564 ℃, and pressure is 45KPa; The temperature that the reactor discharging is flowed out superheater 103 tube sides and entered vapour generator 104 tube sides is 392 ℃; The reactor discharging is 269 ℃ from the temperature that vapour generator 104 tube sides flow out into ethylbenzene vaporizer 105 tube sides; Dropped to 125 ℃ from the effusive reactor drop temperature of ethylbenzene vaporizer 105 tube sides at last, pressure is 36KPa.The stagnation pressure that L type unitized exchanger is flow through in the reactor discharging is reduced to 9KPa, heat dissipation capacity be 20 megajoules/hour.
The temperature that charging liquid phase ethylbenzene and batching vapour mixture enter ethylbenzene vaporizer 105 shell sides is 104 ℃, and it is 210 ℃ from the temperature that 105 shell sides flow out into superheater 103 shell sides, has reached 505 ℃ from the effusive temperature of superheater 103 shell sides at last
The gauge pressure that vapour generator 104 shell sides produce is that the flow of 350KPa low-pressure steam 112 is 10 tons/hour.
[comparative example 1]
According to each Step By Condition of embodiment 1, just change the array mode of interchanger, adopt Fig. 1 mode to arrange, three independent respectively arrangements of heat exchange equipments, its result is, pressure drop is more than the 30KPa, heat dissipation capacity 500 megajoules/hour.
Claims (4)
1, a kind of cooling of high temperature discharging of ethyl benzene dehydrogenation system and heat recovery method may further comprise the steps:
A) the dehydrogenation reaction zone temperature is 500～650 ℃, pressure is that high temperature section reactor feed superheater tube side is at first passed through in the reactor discharging of 40～100KPa, after reactor feed heat exchange with shell side, temperature is a warm area section vapour generator tube side during 300～410 ℃ reactor discharging enters, after oiler feed heat exchange with shell side, temperature is that 140～280 ℃ reactor discharging enters low temperature section ethylbenzene vaporizer 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 30～90KPa;
B) temperature is that 95～120 ℃ the material ethylbenzene and the vapor mixing of preparing burden become reactor feed, at first enter low temperature section ethylbenzene vaporizer shell side, after the reactor discharging heat exchange with tube side, temperature is that 95～220 ℃ reactor feed directly enters high temperature section reactor feed superheater shell side, after reactor discharging heat exchange with tube side, the reactor feed temperature is 400～570 ℃, and pressure is 80～140KPa, enters the dehydrogenation reaction zone reaction;
C) warm area section vapour generator shell side during oiler feed enters after the reactor discharging heat exchange with tube side, produces the saturation steam of pressure 150～1100KPa;
It is characterized in that on the housing between two retaining plates of high temperature section reactor feed superheater the major diameter corrugated-type expansion joint being set, the middle warm area section vapour generator of high temperature section reactor feed superheater and horizontal positioned is at least one the short tube of corrugated-type expansion joint and is connected by wave number is set, and the angle α that both medullary rays form is 90～135 °; The middle warm area section vapour generator of horizontal positioned is connected by short tube with low temperature section ethylbenzene vaporizer, and the angle β that their both medullary rays form is 135～180 °.
2, according to the cooling and the heat recovery method of the described high temperature discharging of ethyl benzene dehydrogenation system of claim 1, it is characterized in that high temperature section reactor feed superheater adopts the thin tubesheet structure, and wave number is set on the shell side between two tube sheets is at least one major diameter expansion joint.
3,, it is characterized in that the angle α that the medullary ray of the middle warm area section vapour generator of high temperature section reactor feed superheater and horizontal positioned forms is 90 ° according to the cooling and the heat recovery method of the described high temperature discharging of ethyl benzene dehydrogenation system of claim 1.
4,, it is characterized in that the angle β that the medullary ray of the middle warm area vapour generator of horizontal positioned and cold zone ethylbenzene vaporizer forms is 180 ° according to the cooling and the heat recovery method of the described high temperature discharging of ethyl benzene dehydrogenation system of claim 1.
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| CN1329353C (en) * | 2004-10-29 | 2007-08-01 | 中国石油化工股份有限公司 | Reaction device for ethylbenzene dehydrogenation for making styrene |
| CN107973763A (en) * | 2017-12-08 | 2018-05-01 | 河南心连心化肥有限公司 | A kind of process units and method for preparing 2- methylfurans |
| 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 |
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|---|---|
| CN1467188A (en) | 2004-01-14 |
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