CN104478775B - The method reducing phenol-acetone device oxidation reaction unit energy consumption - Google Patents
The method reducing phenol-acetone device oxidation reaction unit energy consumption Download PDFInfo
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- CN104478775B CN104478775B CN201410719776.9A CN201410719776A CN104478775B CN 104478775 B CN104478775 B CN 104478775B CN 201410719776 A CN201410719776 A CN 201410719776A CN 104478775 B CN104478775 B CN 104478775B
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Abstract
The present invention relates to a kind of method reducing phenol-acetone device oxidation reaction unit energy consumption, mainly solve the problem that in prior art, energy consumption is higher.The present invention is by using a kind of method reducing phenol-acetone device oxidation reaction unit energy consumption, including the logistics (1) of isopropylbenzene by reflux stream heat exchange at the bottom of oxidizing tower heat exchanger (2) and oxidizing tower (6) tower after, further enter oxidizing tower (6) after preheating, overhead stream (5) delivers to tail gas treating unit, a part of logistics of tower reactor liquid phase stream enters oxidation product outlet line (9), another part logistics enters the technical scheme of return oxidizing tower (6) after oxidizing tower heat exchanger (2) carries out heat exchange with logistics (1) and preferably solves the problems referred to above, can be used in phenol-acetone device oxidation reaction.
Description
Technical field
The present invention relates to a kind of method reducing phenol-acetone device oxidation reaction unit energy consumption.
Background technology
Phenol is the colourless acicular crystal with special odor, is a kind of multiduty Chemical Manufacture raw material.Acetone is a kind of normal
Chemical solvent that see, highly volatile.Number of patent application US20110301384A1 cumene oxidation system and patent application
The manufacture method of number CN200580006398.9 cumene hydroperoxide, describes in a wet process and dry method carries out isopropylbenzene and contains
Carrier of oxygen carries out oxidation reaction, the technique preparing cumyl hydroperoxide.Number of patent application CN201120437887.2 relates to
A kind of outside isopropylbenzene continuous oxidation system moving heat, its oxidizing tower connects with oxidation outer circulation cooler and circulating pump, oxidation
Product and recirculated cooling water heat exchange react the outer shifting of generation heat to realize cumene oxidation.Number of patent application US6303825B1
Relate to the starting method of a kind of circulating reaction system including at least an exothermic reaction, propose pre-with the reaction heat of exothermic reaction
Hot feed stream stock, reaches heat of reaction and recycles, effectively reduce the purpose of energy consumption.
Prior art generates cumyl hydroperoxide at isopropylbenzene dry process reaction, during preparing phenol-acetone, arranges 1#
With the oxidizing tower of 2# two series connection, making cumene oxidation is cumyl hydroperoxide.The isopropylbenzene charging low pressure of 1# oxidizing tower
Steam preheating each leads into follow outside 1# oxidation outer circulation cooler and 2# oxidation to optimal feeding temperature, two oxidizing tower discharging
Ring cooler, uses circulating cooling water cooling, to realize the outer shifting of cumene oxidation reaction generation heat.Under driving operating mode, two
Oxidation outer circulation cooler is passed through steam to realize preheating function of driving.1# oxidizing tower feeding preheating need to consume a large amount of low pressure and steam
Vapour, and the generation heat of oxidation reaction is removed and is additionally needed a large amount of recirculated cooling waters of consumption, there is the higher problem of energy consumption.
The present invention solves this problem targetedly.
Summary of the invention
The technical problem to be solved is the problem that in prior art, energy consumption is higher, it is provided that a kind of new reduction phenol third
The method of ketone device oxidation reaction unit energy consumption.The method, in the oxidation reaction of phenol-acetone device, has energy consumption relatively low
Advantage.
For solving the problems referred to above, the technical solution used in the present invention is as follows: a kind of reduction phenol-acetone device oxidation reaction unit
The method of energy consumption, the logistics (1) including isopropylbenzene is refluxed at the bottom of oxidizing tower (6) tower by oxidizing tower heat exchanger (2)
After logistics carries out heat exchange, then by the air being passed through in entrance oxidizing tower (6), with tower after preheater (4) further preheating
There is oxidation reaction in logistics (7), oxidizing tower (6) overhead stream (5) delivers to tail gas treating unit, oxidizing tower (6) tower
A part of logistics of still liquid phase stream enters oxidation product outlet line (9), and another part logistics enters oxidizing tower heat exchange
Device (2) and logistics (1) return oxidizing tower (6) after carrying out heat exchange；Wherein, during driving operating mode, oxidizing tower (6) tower reactor
A part of logistics of liquid phase stream enters oxidizing tower driving preheater (3), is then back to oxidizing tower (6), and oxidizing tower heat is handed over
Parallel operation (2) is in parallel with oxidizing tower driving preheater (3).
In technique scheme, it is preferable that preheater (4), the heat transferring medium of oxidizing tower driving preheater (3) are low pressure
Steam.
In technique scheme, it is preferable that described oxidizing tower (6) tower top is provided with safety valve and emergency discharge pipeline；Described sky
The upper other access nitrogen pipeline of gas suction line (7)；Described oxidizing tower (6) is provided with chilled water (chw) and fire water pipeline.
In technique scheme, it is preferable that oxidizing tower (6) tower reactor liquid phase stream 10～50% enters oxidation product by weight
Thing outlet line (9).
In technique scheme, it is preferable that oxidizing tower (6) operation temperature is 20～200 DEG C, and operation pressure is 0.0～0.8MPaG；
Oxidizing tower heat exchanger (2) operation temperature is 10～200 DEG C, and operation pressure is 0.01～1.5MPaG.
In technique scheme, it is highly preferred that oxidizing tower (6) operation temperature is 80～120 DEG C, operation pressure is
0.2～0.4MPaG；Oxidizing tower heat exchanger (2) operation temperature is 30～110 DEG C, and operation pressure is 0.2～0.8MPaG.
In technique scheme, it is preferable that described in include in the logistics (1) of isopropylbenzene the mass content of isopropylbenzene be 65～
99%；.
In technique scheme, it is preferable that logistics (1) is preheated to 55～95 DEG C by preheater (4) further.
The present invention, by oxidation product heat exchange in oxidizing tower heat exchanger (2) of isopropylbenzene raw material Yu oxidizing tower discharging, is changing
In the case of heat is 129 kilocalorie/kilogram phenol, reduces low-pressure steam and consume 245 kgs/tonne of phenol, and it is cold to reduce circulation
But water consumption 13.1 ton/ton phenol, owing to oxidizing tower heat exchanger (2) uses in parallel with oxidizing tower driving preheater (3)
Flow process, does not the most increase the resistance of ducting, does not the most increase the power consumption of cyclic oxidation liquid delivery pump, achieve preferably technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention.
In Fig. 1,1 is feedstock pipeline；2 is oxidizing tower heat exchanger；3 is oxidizing tower driving preheater；4 is preheating
Device；5 is oxidation top gaseous phase outlet line；6 is oxidizing tower；7 is air inlet pipeline；8 is booster pump；9 is oxidation
Product outlet line.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Detailed description of the invention
[embodiment 1]
In device flow process as shown in Figure 1, the mass content of isopropylbenzene is isopropylbenzene feedstock pipeline (1) of 66.1%
Carrying out heat exchange by oxidizing tower heat exchanger (2) with oxidizing tower backflow material, the isopropylbenzene raw material after heating passes through preheater
(4) enter oxidizing tower (6) after being preheated to 55 DEG C, occur oxidation anti-with the air being passed through through air inlet pipeline (7)
Should；Oxidizing tower (6) tower top is delivered to out-of-bounds through gaseous phase outlet pipeline (5) containing the tail gas of a small amount of isopropylbenzene and water；Oxidizing tower (6)
The tower reactor liquid phase material containing isopropylbenzene and cumyl hydroperoxide is by booster pump (8) supercharging, a part of liquid phase material conduct
Oxidation product is sent outside, and it is former with isopropylbenzene that a part of oxidation product (9) enters oxidizing tower heat exchanger (2) by return line
Material carries out heat exchange, moves the backflow material after heat and returns to oxidizing tower (6).
Oxidizing tower heat exchanger (2) is upper is in parallel with oxidizing tower driving preheater (3), on oxidizing tower heat exchanger (2)
Phegma outlet line be connected with the phegma outlet line on oxidizing tower driving preheater (3) after formed phegma house steward
Line, is then refluxed for liquid main pipe line and is connected with oxidizing tower (6), and described phegma main pipe line is provided with butterfly valve.Oxidizing tower heat is handed over
It is equipped with valve on phegma pipeline before and after parallel operation (2), oxidizing tower driving preheater (3).
Under driving operating mode, close the backflow material pipeline of oxidizing tower heat exchanger (2), open oxidizing tower driving preheater
(14) backflow material pipeline, the backflow material of booster pump (8) supercharging passes through oxidizing tower driving preheater (14), real
Heating when now driving.
Preheater (4), oxidizing tower driving preheater (3) are provided with low-pressure steam feeding line, and oxidizing tower (6) tower top is provided with
Safety valve and emergency discharge pipeline, the upper other access nitrogen pipeline of described air inlet pipeline (7), on described oxidizing tower (6)
Being provided with chilled water (chw) and fire water pipeline, described oxidizing tower heat exchanger (2) is provided with cross-line, booster pump (8) outlet line
That road pipeline being connected with oxidizing tower heat exchanger (2) strides across oxidizing tower heat exchanger (2) directly and oxidizing tower (6) phase
Even.
Phenol-acetone production scale is 100,000 tons/year.Oxidizing tower (6) tower reactor liquid phase stream 11% enters oxidation by weight
Product outlet line (9).Oxidizing tower operation temperature 105 DEG C；Operation pressure is 0.27MPaG；Oxidizing tower heat exchanger is grasped
It it is 100 DEG C as temperature；Operation pressure is 0.27MPaG.Be computed, the method can reduce low-pressure steam consume 1.905 tons/
Hour, and reduce circulating cooling water consumption 101.5 ton hour.
[embodiment 2]
According to the condition described in embodiment 1 and step, phenol-acetone production scale changes 200,000 tons/year into.Low pressure can be reduced steam
Vapour consumes 3.80 ton hour, and reduces circulating cooling water consumption 203 ton hour.
[embodiment 3]
According to the condition described in embodiment 1 and step, simply phenol-acetone production scale changes 350,000 tons/year into.Can reduce low
Pressure steam consumption 6.65 ton hour, and reduce circulating cooling water consumption 354 ton hour.
[embodiment 4]
According to the condition described in embodiment 1 and step, in charging (1), the mass content of isopropylbenzene is 70.3%；After heating
Isopropylbenzene raw material by preheater (4) be preheated to 60 DEG C after enter oxidizing tower (6)；Oxidizing tower (6) tower reactor liquid phase thing
Stream 26% enters oxidation product outlet line (9) by weight；Oxidizing tower operation temperature 105 DEG C；Operation pressure is
0.27MPaG；Oxidizing tower heat exchanger operation temperature is 60 DEG C；Operation pressure is 0.2MPaG.Being computed, the method can
Reduce low-pressure steam and consume 1.865 ton hour, and reduce circulating cooling water consumption 99.5 ton hour.
[embodiment 5]
According to the condition described in embodiment 1 and step, in charging (1), the mass content of isopropylbenzene is 75.6%；After heating
Isopropylbenzene raw material enters oxidizing tower (6) after being preheated to 68 DEG C by preheater (4)；Oxidizing tower (6) tower reactor liquid phase stream
32% enter oxidation product outlet line (9) by weight；Oxidizing tower operation temperature 105 DEG C；Operation pressure is 0.27MPaG；
Oxidizing tower heat exchanger operation temperature is 70 DEG C；Operation pressure is 0.3MPaG.Being computed, the method can reduce low pressure and steam
Vapour consumes 1.885 ton hour, and reduces circulating cooling water consumption 100.5 ton hour.
[embodiment 6]
According to the condition described in embodiment 1 and step, in charging (1), the mass content of isopropylbenzene is 89.2%；After heating
Isopropylbenzene raw material enters oxidizing tower (6) after being preheated to 79 DEG C by preheater (4)；Oxidizing tower (6) tower reactor liquid phase stream
47% enter oxidation product outlet line (9) by weight；Oxidizing tower operation temperature 105 DEG C；Operation pressure is 0.27MPaG；
Oxidizing tower heat exchanger operation temperature is 80 DEG C；Operation pressure is 0.5MPaG.Being computed, the method can reduce low pressure and steam
Vapour consumes 1.925 ton hour, and reduces circulating cooling water consumption 102.5 ton hour.
[embodiment 7]
According to the condition described in embodiment 1 and step, in charging (1), the mass content of isopropylbenzene is 98.9%；After heating
Isopropylbenzene raw material enters oxidizing tower (6) after being preheated to 95 DEG C by preheater (4)；Oxidizing tower (6) tower reactor liquid phase stream
50% enter oxidation product outlet line (9) by weight；Oxidizing tower operation temperature 105 DEG C；Operation pressure is 0.27MPaG；
Oxidizing tower heat exchanger operation temperature is 100 DEG C；Operation pressure is 0.8MPaG.Being computed, the method can reduce low pressure and steam
Vapour consumes 1.945 ton hour, and reduces circulating cooling water consumption 103.5 ton hour.
Claims (8)
1. the method reducing phenol-acetone device oxidation reaction unit energy consumption, oxidizing tower is passed through in the logistics (1) including isopropylbenzene
After reflux stream at the bottom of heat exchanger (2) and oxidizing tower (6) tower carries out heat exchange, then preheated further by preheater (4)
There is oxidation reaction, oxidizing tower (6) tower top in the air inlet pipeline (7) being passed through in rear entrance oxidizing tower (6), with tower
Tail gas treating unit is delivered in logistics (5), and a part of logistics of oxidizing tower (6) tower reactor liquid phase stream enters oxidation product outlet
Pipeline (9), another part logistics enters after oxidizing tower heat exchanger (2) carries out heat exchange with logistics (1) and returns oxidizing tower
(6)；Wherein, during driving operating mode, a part of logistics of oxidizing tower (6) tower reactor liquid phase stream enters oxidizing tower and drives to preheat
Device (3), is then back to oxidizing tower (6), and oxidizing tower heat exchanger (2) is in parallel with oxidizing tower driving preheater (3).
The method reducing phenol-acetone device oxidation reaction unit energy consumption the most according to claim 1, it is characterised in that preheater
(4), the heat transferring medium of oxidizing tower driving preheater (3) is low-pressure steam.
The method reducing phenol-acetone device oxidation reaction unit energy consumption the most according to claim 1, it is characterised in that described oxygen
Change tower (6) tower top and be provided with safety valve and emergency discharge pipeline；The upper other access nitrogen pipeline of described air inlet pipeline (7)；
Described oxidizing tower (6) is provided with chilled water (chw) and fire water pipeline.
The method reducing phenol-acetone device oxidation reaction unit energy consumption the most according to claim 1, it is characterised in that oxidizing tower
(6) tower reactor liquid phase stream 10～50% enters oxidation product outlet line (9) by weight.
The method reducing phenol-acetone device oxidation reaction unit energy consumption the most according to claim 1, it is characterised in that oxidizing tower
(6) operation temperature is 20～200 DEG C, and operation gauge pressure is 0.0～0.8MPa；Oxidizing tower heat exchanger (2) operation temperature is
10～200 DEG C, operation gauge pressure is 0.01～1.5MPa.
The method reducing phenol-acetone device oxidation reaction unit energy consumption the most according to claim 5, it is characterised in that oxidizing tower
(6) operation temperature is 80～120 DEG C, and operation gauge pressure is 0.2～0.4MPa；Oxidizing tower heat exchanger (2) operation temperature is
30～110 DEG C, operation gauge pressure is 0.2～0.8MPa.
The method reducing phenol-acetone device oxidation reaction unit energy consumption the most according to claim 1, it is characterised in that described bag
Including the mass content of isopropylbenzene in the logistics (1) of isopropylbenzene is 65～99%.
The method reducing phenol-acetone device oxidation reaction unit energy consumption the most according to claim 1, it is characterised in that preheater
(4) further logistics (1) is preheated to 55～95 DEG C.
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| CN201410719776.9A CN104478775B (en) | 2014-12-01 | 2014-12-01 | The method reducing phenol-acetone device oxidation reaction unit energy consumption |
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| CN201410719776.9A CN104478775B (en) | 2014-12-01 | 2014-12-01 | The method reducing phenol-acetone device oxidation reaction unit energy consumption |
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| CN104478775B true CN104478775B (en) | 2016-09-07 |
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| CN105237374A (en) * | 2015-10-12 | 2016-01-13 | 中石化上海工程有限公司 | Phenol-acetone device acetone refining system waste heat recovery method |
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| DE19911024B4 (en) * | 1999-03-12 | 2005-09-08 | Phenolchemie Gmbh & Co. Kg | Process for starting up loop reactor systems in which at least one exothermic reaction is to be carried out |
| CN202315861U (en) * | 2011-11-08 | 2012-07-11 | 太仓塑料助剂厂有限公司 | Isopropylbenzene continuous oxidation system with external heat transfer |
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