CN105042880B - Butylene oxidation-dehydrogenation reaction generation gas heat recovery technique - Google Patents
Butylene oxidation-dehydrogenation reaction generation gas heat recovery technique Download PDFInfo
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- CN105042880B CN105042880B CN201510570031.5A CN201510570031A CN105042880B CN 105042880 B CN105042880 B CN 105042880B CN 201510570031 A CN201510570031 A CN 201510570031A CN 105042880 B CN105042880 B CN 105042880B
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Abstract
The present invention relates to butylene oxidation-dehydrogenation field, and in particular to a kind of butylene oxidation-dehydrogenation reaction generation gas heat recovery technique.Three sections of recovery of heat point of generation gas will be reacted：Reaction generation gas is exchanged heat with middle pressure steam, reaction generation temperature degree is down to 430 460 DEG C after heat exchange, and Returning reactor utilizes as reaction vapor after middle pressure steam heating；Reaction generation gas enters back into waste heat boiler and carries out second segment recovery, and the temperature of reaction generation gas is down to 135 180 DEG C after recovery, and the low-pressure steam of waste heat boiler by-product reuses as reaction vapor；Reaction generation gas, which enters in rear heat exchanger, carries out the 3rd section of recovery, remaining hot water reclaims the heat of reaction generation gas in rear heat exchanger, the preheating that the waste heat water section after heat is used for raw material butylene is absorbed, another part enters in heat pump, and reaction generation temperature degree is down to 75 80 DEG C.The present invention is high by the three sections of recovery of heat point of reaction generation gas, the effectively heat of recovery reaction generation gas, heat recovery rate.
Description
Technical field
The present invention relates to butylene oxidation-dehydrogenation field, and in particular to a kind of butylene oxidation-dehydrogenation reaction generation gas heat recovery
Technique.
Background technology
Oxidative Dehydrogenation of Butene into Butadiene is one of main method of butadiene production, and butylene oxidation-dehydrogenation reaction release is big
Calorimetric amount, the heat of effectively recovery reaction generation gas is to reduce process energy consumption, the important means of lifting device benefit, in the field
Existing Patents are seen in report.
A kind of method of two sections of energy regeneratings of the patent disclosure of Patent No. " CN201110359476.0 "：One section be by
The 370-420 DEG C of reaction generation gas heat exchange that 100-120 DEG C of mixed material gas obtains with reaction so that mixed material gas is warming up to
300-350℃；Another section is oxidative dehydrogenation process by 280-300 DEG C of vapor in the shell of reactor with butylene
Caused heat is exchanged heat.But this method has the following disadvantages：After reaction generation gas and material mixed gas energy exchange, its heat
Amount is not fully utilized further, but is directly cooled by heat exchanger, causes energy loss.
Using thermal medium recovery heat is removed in the patent of Patent No. " CN201310034287.5 ", in addition, the technology is led to
Cross steam superheater, waste heat boiler recovery first-stage reactor outlets products heat；Patent No. " CN201110334864.3 "
Patent is with medium waste heat boiler and reaction generation gas waste heat boiler recovery heat and byproduct steam.Both approaches employ isothermal
The shortcomings of complicated, high to catalyst requirement and dismounting is difficult be present, limit its application in shell-and-tube reactor, the reactor
Property.In addition, the two patents do not illustrate the further utilization of low grade heat energy.
The patent of Patent No. " CN201220745072.5 " discloses a kind of using butylene catalytic dehydrogenation preparation 1,3- fourths
The device of diene, the technology reclaim heat with waste heat boiler.But this method reclaims heat, its heat recovery only with waste heat boiler
Rate is low.In addition, coming into operation for the equipment such as heating furnace, steam superheater, air-heating furnace further increases plant energy consumption.
The patent of Patent No. " CN201310360727.6 " discloses a kind of used heat of oxidative dehydrogenation butadiene product equipment
Recovery method：The circulation washings that water-cooling tower tower reactor is discharged in oxidation unit are added before cooled as in device using hot water
Again by circulating cooling water cooling after the reboiler of thermal medium and the thermal source progress heat recovery of heat exchanger.This method is mainly by water
Circulated in cold tower after washings add alkali and be used as heating medium, it is limited to the castering action of device heat utilization ratio.
The content of the invention
In view of the shortcomings of the prior art, generation gas heat is reacted it is an object of the invention to provide a kind of butylene oxidation-dehydrogenation to return
Knock off skill, can effectively reclaim the heat of more than 80 DEG C of reaction generation gas, heat recovery rate height.
Butylene oxidation-dehydrogenation reaction generation gas heat recovery technique of the present invention, will react the heat point three of generation gas
Duan Huishou：
(1) reaction generation gas exchanges heat with middle pressure steam, and reaction generation temperature degree is down to 430-460 DEG C after heat exchange, and middle pressure is steamed
Returning reactor utilizes as reaction vapor after vapour heating；
(2) the reaction generation gas after step (1) heat exchange, which enters, carries out second segment recovery in waste heat boiler, after recovery, instead
The temperature that gas should be generated is down to 135-180 DEG C, and the low-pressure steam of waste heat boiler by-product reuses as reaction vapor；
(3) the reaction generation gas after step (2) recovery, which enters in rear heat exchanger, carries out the 3rd section of recovery, and remaining hot water is rear
The heat of recovery reaction generation gas in heat exchanger, absorbs the remaining hot water after heat and enters in heat pump, and reaction generation temperature degree is down to
75-80℃。
Wherein：
The initial temperature of reaction generation gas is 570-600 DEG C in step (1).
Temperature in step (1) before middle pressure steam heat exchange is 200-250 DEG C.
In step (1) 400-420 DEG C is warming up to after middle pressure steam heat exchange.
The low-pressure steam of waste heat boiler by-product is 0.25-0.35MPa low-pressure steams in step (2).
Waste heat boiler and flash tank use out-of-bounds desalted water moisturizing.
Step (3) is preferably：Reaction generation gas after step (2) recovery enters to be carried out the 3rd section time in rear heat exchanger
Receive, remaining hot water reclaims the heat of reaction generation gas in rear heat exchanger, absorbs the waste heat water section after heat and is used for raw material butylene
Preheating, another part enter heat pump in, reaction generation temperature degree be down to 75-80 DEG C.
Remaining hot water reclaims the heat of reaction generation gas in rear heat exchanger in step (3), absorbs the remaining hot water portion after heat
Divide and enter in heat pump, transfer heat to heat pump, then return in rear heat exchanger.
The heat of the remaining hot water of absorption is converted into high-grade heat energy by heat pump by low grade heat energy in step (3), for adding
The hot water from flash tank, the water after being heated return to generation 0.2-0.25MPa steam in flash tank, and caused steam is as anti-
Steam Returning reactor is answered to reuse.
As a kind of preferred scheme, step (3) is：Reaction generation gas after step (2) recovery enters in rear heat exchanger
The 3rd section of recovery is carried out, remaining hot water reclaims the heat of reaction generation gas in rear heat exchanger, and remaining hot water initial temperature is 70-78
DEG C, absorb the remaining hot water after heat and be warming up to 90-103 DEG C, the partly preheating for raw material butylene, another part enters heat pump
In, heat pump is transferred heat to, is then returned in rear heat exchanger, reaction generates the heat of gas in heat exchanger after then reabsorbing
Amount, carries out next circulation；Water in flash tank enters in heat pump, and the water initial temperature in flash tank is 125-130 DEG C, heat pump
The heat of the remaining hot water of absorption is converted into high-grade heat energy by low grade heat energy, for heating the water from flash tank, added
Coolant-temperature gage after heat rises to 135-145 DEG C, returns to generation 0.2-0.25MPa steam in flash tank, caused steam is as reaction
Steam Returning reactor reuses；Water in flash tank is entered back into heat pump, carries out next circulation；Reaction generation gas passes through
Temperature is down to 75-80 DEG C by reaction generation tracheae discharge after three sections of recovery.
In summary, the present invention has advantages below：
The present invention is for the shortcomings of energy recovery rate existing for prior art is low, application performance is poor, there is provided a kind of new
Butylene oxidation-dehydrogenation reaction generation gas heat recovery technique, reaction is generated into three sections of recovery of heat point in gas, effectively recovery reaction
The heat that more than 80 DEG C of generation gas, heat recovery rate are high.
Brief description of the drawings
Fig. 1 is the process chart of butylene oxidation-dehydrogenation of the present invention reaction generation gas heat recovery technique；
In figure：1-1：Reaction generation tracheae, 1-2：Reaction generation tracheae, 1-3：Reaction generation tracheae, 1-4：Reaction generation
Tracheae, 2：Middle pressure steam inlet pipe, 3：Middle pressure steam outlet pipe, 4：Heat exchanger, 5：Waste heat boiler, 6：Low-pressure steam outlet pipe, 7：Waste heat
Water backwater line, 8：Heat exchanger afterwards, 9：High-temperature-hot-water backwater line, 10：Heat pump, 11：Flash tank, 12：Flash tank low pressure steam pipe,
13：Waterline on remaining hot water, 14：Waterline on high-temperature-hot-water.
Embodiment
With reference to embodiment, the present invention will be further described.
Embodiment 1
A kind of butylene oxidation-dehydrogenation reaction generation gas heat recovery technique, as shown in figure 1, the heat point for generating gas will be reacted
Three sections of recovery：
(1) 600 DEG C of reaction generation gas is changed by the reaction generation tracheae 1-1 middle pressure steams entered in heat exchanger 4 with 250 DEG C
Heat, reaction generation temperature degree is down to 450 DEG C after heat exchange, and the reaction generation gas after heat exchange enters used heat by reaction generation tracheae 1-2
In boiler 5, Returning reactor is utilized as reaction vapor after caused middle pressure steam is warming up to 420 DEG C in heat exchanger 4, and middle pressure is steamed
Vapour enters heat exchanger 4 by middle pressure steam inlet pipe 2, and the middle pressure steam after heating is by the Returning reactor of middle pressure steam outlet pipe 3 as anti-
Answer steam utilization；
(2) the reaction generation gas after step (1) heat exchange is entered in waste heat boiler 5 by reaction generation tracheae 1-2 carries out the
Two sections of recovery, after recovery, the temperature of reaction generation gas is down to 170 DEG C, and the 0.35MPa low-pressure steams of waste heat boiler by-product are by low pressure
Steam outlet pipe 6 is discharged to be reused as reaction vapor；Waste heat boiler 5 is using out-of-bounds desalted water by extraneous desalting pipe to used heat
The moisturizing of boiler 5；
(3) the reaction generation gas after step (2) recovery is entered in rear heat exchanger 8 by reaction generation tracheae 1-3 carries out the
Three sections of recovery, remaining hot water reclaim the heat of reaction generation gas in rear heat exchanger 8, and remaining hot water initial temperature is 75 DEG C, absorbs heat
Remaining hot water after amount is warming up to 100 DEG C, partly the preheating for raw material butylene, and another part enters heat transfer in heat pump 10
To heat pump 10, then return in rear heat exchanger 8, reaction generates the heat of gas in heat exchanger 8 after then reabsorbing, and carries out next
Individual circulation；Remaining hot water is entered in heat pump 10 by waterline on remaining hot water 13 from rear heat exchanger 8；Changed after being returned to by return afterheat-water line 7
In hot device 8；Water in flash tank 11 enters in heat pump 10, and the water initial temperature in flash tank 11 is 125 DEG C, and heat pump 10 will absorb
The heat of remaining hot water high-grade heat energy is converted into by low grade heat energy, for heating the water from flash tank 11, after being heated
Coolant-temperature gage rise to 135 DEG C, return in flash tank 11 generation 0.25MPa steam, caused steam is as reaction vapor by flashing
The Returning reactor of tank low pressure steam pipe 12 reuses；Water in flash tank 11 is entered back into heat pump 10, carries out next circulation；
Reaction generation gas temperature after three sections of recovery is down to 75 DEG C by reaction generation tracheae 1-4 discharges；Water in flash tank 11 is by height
Warm water's backwater line 9 enters in heat pump 10 from flash tank 11；Returned to by waterline on high-temperature-hot-water 14 in flash tank 11；Wherein：Dodge
Steaming pot 11 is using out-of-bounds desalted water by extraneous desalting pipe moisturizing.
Embodiment 2
A kind of butylene oxidation-dehydrogenation reaction generation gas heat recovery technique, as shown in figure 1, the heat point for generating gas will be reacted
Three sections of recovery：
(1) 570 DEG C of reaction generation gas is entered to the middle pressure steam in heat exchanger 4 with 200 DEG C by reaction generation tracheae 1-1
Heat exchange, reaction generation temperature degree is down to 430 DEG C after heat exchange, and the reaction generation gas after heat exchange is entered useless by reaction generation tracheae 1-2
In heat boiler 5, Returning reactor utilizes as reaction vapor after caused middle pressure steam is warming up to 400 DEG C in heat exchanger 4, middle pressure
Steam enters heat exchanger 4 by middle pressure steam inlet pipe 2, and the middle pressure steam after heating is by the Returning reactor conduct of middle pressure steam outlet pipe 3
Reaction vapor utilizes；
(2) the reaction generation gas after step (1) heat exchange is entered in waste heat boiler 5 by reaction generation tracheae 1-2 carries out the
Two sections of recovery, after recovery, the temperature of reaction generation gas is down to 135 DEG C, and the 0.25MPa low-pressure steams of waste heat boiler by-product are by low pressure
Steam outlet pipe 6 is discharged to be reused as reaction vapor；Waste heat boiler 5 is using out-of-bounds desalted water by extraneous desalting pipe to used heat
The moisturizing of boiler 5；
(3) the reaction generation gas after step (2) recovery is entered in rear heat exchanger 8 by reaction generation tracheae 1-3 carries out the
Three sections of recovery, remaining hot water reclaim the heat of reaction generation gas in rear heat exchanger 8, and remaining hot water initial temperature is 70 DEG C, absorbs heat
Remaining hot water after amount is warming up to 90 DEG C, and heat pump 10 is transferred heat into heat pump 10, then returns in rear heat exchanger 8,
Then reaction generates the heat of gas in heat exchanger 8 after reabsorbing, and carries out next circulation；Remaining hot water by waterline on remaining hot water 13 from
Heat exchanger 8 enters in heat pump 10 afterwards；Returned to by return afterheat-water line 7 in rear heat exchanger 8；Water in flash tank 11 enters heat pump 10
In, the water initial temperature in flash tank 11 is 130 DEG C, and the heat of the remaining hot water of absorption is converted into by heat pump 10 by low grade heat energy
High-grade heat energy, for heating the water from flash tank 11, the coolant-temperature gage after being heated rises to 145 DEG C, returns in flash tank 11
0.2MPa steam is produced, caused steam is reused as reaction vapor by the Returning reactor of flash tank low pressure steam pipe 12；
Water in flash tank 11 is entered back into heat pump 10, carries out next circulation；Reaction generation gas temperature after three sections of recovery is down to
80 DEG C by reaction generation tracheae 1-4 discharges；Water in flash tank 11 enters heat pump 10 by high-temperature-hot-water backwater line 9 from flash tank 11
In；Returned to by waterline on high-temperature-hot-water 14 in flash tank 11；Wherein：Flash tank 11 is using out-of-bounds desalted water by extraneous desalting pipe
Moisturizing.
Claims (1)
- A kind of 1. butylene oxidation-dehydrogenation reaction generation gas heat recovery technique, it is characterised in that：The heat point of generation gas will be reacted Three sections of recovery：（1）The middle pressure steam that 600 DEG C of reaction generation gas is entered in heat exchanger with 250 DEG C by reaction generation tracheae exchanges heat, heat exchange Reaction generation temperature degree is down to 450 DEG C afterwards, and the reaction generation gas after heat exchange is entered in waste heat boiler by reaction generation tracheae, heat exchange Returning reactor utilizes as reaction vapor after caused middle pressure steam is warming up to 420 DEG C in device, and middle pressure steam is by middle pressure steam Inlet pipe enters heat exchanger, and the middle pressure steam after heating is utilized by middle pressure steam outlet pipe Returning reactor as reaction vapor；（2）Through step（1）Reaction generation gas after heat exchange is entered by reaction generation tracheae carries out second segment recovery in waste heat boiler, After recovery, the temperature of reaction generation gas is down to 170 DEG C, and the 0.35MPa low-pressure steams of waste heat boiler by-product are by low-pressure steam outlet pipe Discharge reuses as reaction vapor；Waste heat boiler gives waste heat boiler moisturizing using out-of-bounds desalted water by extraneous desalting pipe；（3）Through step（2）Reaction generation gas after recovery is entered in rear heat exchanger by reaction generation tracheae carries out the 3rd section of recovery, Remaining hot water reclaims the heat of reaction generation gas in rear heat exchanger, and remaining hot water initial temperature is 75 DEG C, absorbs the waste heat after heat Water is warming up to 100 DEG C, partly the preheating for raw material butylene, and another part, which enters in heat pump, transfers heat to heat pump, then Return in rear heat exchanger, reaction generates the heat of gas in heat exchanger after then reabsorbing, and carries out next circulation；Remaining hot water by Waterline enters in heat pump from rear heat exchanger on remaining hot water；Returned to by return afterheat-water line in rear heat exchanger；Water in flash tank enters Enter in heat pump, the water initial temperature in flash tank is 125 DEG C, and heat pump is converted the heat of the remaining hot water of absorption by low grade heat energy For high-grade heat energy, for heating the water from flash tank, the coolant-temperature gage after being heated rises to 135 DEG C, returns in flash tank and produces Raw 0.25MPa steam, caused steam reuse as reaction vapor Returning reactor；Water in flash tank enters back into heat pump In, carry out next circulation；Reaction generation gas temperature after three sections of recovery is down to 75 DEG C by reaction generation tracheae discharge；Flash distillation Water in tank is entered in heat pump by high-temperature-hot-water backwater line from flash tank；Returned to by waterline on high-temperature-hot-water in flash tank；Wherein： Flash tank is using out-of-bounds desalted water by extraneous desalting pipe moisturizing.
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| DE2602895B2 (en) * | 1976-01-27 | 1978-06-15 | Davy Powergas Gmbh, 5000 Koeln | Process for utilizing the heat of reaction resulting from the catalytic oxidation of o-xylene to phthalic anhydride |
| CN101367702B (en) * | 2008-09-26 | 2012-06-13 | 淄博齐翔腾达化工股份有限公司 | Method for preparing butadiene with butylene oxo-dehydrogenation of axially-located bed |
| CN202280490U (en) * | 2011-10-31 | 2012-06-20 | 淄博齐翔腾达化工股份有限公司 | Device for converting heat energy of remained hot water |
| CN202516539U (en) * | 2012-03-10 | 2012-11-07 | 中石油东北炼化工程有限公司锦州设计院 | Low-temperature heat utilization system of reaction gas waste heat from fluidized bed for preparing butadiene by oxidative dehydrogenation of butene |
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