CN104478775A - Method for reducing energy consumption of oxidizing reaction unit of phenol-acetone device - Google Patents
Method for reducing energy consumption of oxidizing reaction unit of phenol-acetone device Download PDFInfo
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- CN104478775A CN104478775A CN201410719776.9A CN201410719776A CN104478775A CN 104478775 A CN104478775 A CN 104478775A CN 201410719776 A CN201410719776 A CN 201410719776A CN 104478775 A CN104478775 A CN 104478775A
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Abstract
The invention relates to a method for reducing the energy consumption of an oxidizing reaction unit of a phenol-acetone device in order to mainly solve the problem of relatively high energy consumption caused in the prior art. The method for reducing the energy consumption of the oxidizing reaction unit of the phenol-acetone device comprises the following steps: exchanging the heat of an isopropylbenzene material flow (1) and a bottom backflow material of an oxidation tower (6) by an oxidation tower heat exchanger (2); further preheating the isopropylbenzene material flow (1) and then charging the isopropylbenzene material flow (1) into the oxidation tower (6); conveying a tower top material flow (5) to a tail gas treatment unit; charging a part of a liquid phase material flow at the bottom of the tower into an oxidation product outlet pipeline (9) and charging the other part of the material flow into the oxidation tower heat exchanger (2) to exchange heat with the material flow (1), and then returning to the oxidation tower (6). The method disclosed by the invention can be used for commendably solving the problem and can be applied to an oxidation reaction of the phenol-acetone device.
Description
Technical field
The present invention relates to a kind of method reducing phenol-acetone device oxidizing 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 chemical solvents of common, highly volatile.The manufacture method of number of patent application US20110301384A1 cumene oxidation system and number of patent application CN200580006398.9 Cumene Hydroperoxide 80, describe in a wet process and dry method carries out isopropyl benzene and oxygen-containing gas carries out oxidizing reaction, prepare the technique of hydrogen phosphide cumene.Number of patent application CN201120437887.2 relates to the isopropyl benzene continuous oxidation system that heat is moved in a kind of outside, its oxidizing tower connects with oxidation outer circulation water cooler and recycle pump, and oxidation products and recirculated cooling water heat exchange are reacted the outer of Heat of Formation move to be realized cumene oxidation.Number of patent application US6303825B1 relates to a kind of starting method at least comprising the circulating reaction system of a thermopositive reaction, proposes the reaction heat preheat feed stream stock with thermopositive reaction, reaches heat of reaction and recycles, effectively reduce the object of energy consumption.
Prior art, at isopropyl benzene dry process reaction Hydrogen Peroxide isopropyl benzene, is prepared in the process of phenol-acetone, arranges the oxidizing tower of 1# and 2# two series connection, makes cumene oxidation be hydrogen phosphide cumene.The isopropyl benzene charging low-pressure steam of 1# oxidizing tower is preheated to best feeding temperature, two oxidizing tower dischargings pass into 1# respectively and are oxidized outer circulation water cooler and 2# oxidation outer circulation water cooler, use circulating cooling water cooling, move to realize cumene oxidation reaction the outer of Heat of Formation.Under driving operating mode, two oxidation outer circulation water coolers pass into steam to realize driving preheat function.1# oxidizing tower feeding preheating need consume a large amount of low-pressure steam, and the Heat of Formation of oxidizing reaction is removed and needed in addition to consume a large amount of recirculated cooling water, there is the higher problem of energy consumption.
The present invention solves this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is the problem that in prior art, energy consumption is higher, provides a kind of method of reduction phenol-acetone device oxidizing reaction unit energy consumption newly.The method is used for, in the oxidizing reaction of phenol-acetone device, having the advantage that energy consumption is lower.
For solving the problem, the technical solution used in the present invention is as follows: a kind of method reducing phenol-acetone device oxidizing reaction unit energy consumption, after the logistics (1) comprising isopropyl benzene carries out heat exchange by oxidizing tower heat exchanger (2) and reflux stream at the bottom of oxidizing tower (6) tower, again by entering oxidizing tower (6) after preheater (4) further preheating, oxidizing reaction is there is with the air logistics (7) passed in tower, oxidizing tower (6) overhead stream (5) delivers to tail gas treating unit, a part of logistics of oxidizing tower (6) tower reactor liquid phase stream enters oxidation products outlet line (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 driving preheater (3), then return oxidizing tower (6), oxidizing tower heat exchanger (2) is in parallel with oxidizing tower driving preheater (3).
In technique scheme, preferably, the heat transferring medium of preheater (4), oxidizing tower driving preheater (3) is low-pressure steam.
In technique scheme, preferably, described 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); Described oxidizing tower (6) is provided with quenched water and fire water pipeline.
In technique scheme, preferably, oxidizing tower (6) tower reactor liquid phase stream 10 ~ 50% enters oxidation products outlet line (9) by weight.
In technique scheme, preferably, oxidizing tower (6) service temperature is 20 ~ 200 DEG C, and working pressure is 0.0 ~ 0.8MPaG; Oxidizing tower heat exchanger (2) service temperature is 10 ~ 200 DEG C, and working pressure is 0.01 ~ 1.5MPaG.
In technique scheme, more preferably, oxidizing tower (6) service temperature is 80 ~ 120 DEG C, and working pressure is 0.2 ~ 0.4MPaG; Oxidizing tower heat exchanger (2) service temperature is 30 ~ 110 DEG C, and working pressure is 0.2 ~ 0.8MPaG.
In technique scheme, preferably, the mass content comprising isopropyl benzene in the logistics (1) of isopropyl benzene described in is 65 ~ 99%; .
In technique scheme, preferably, logistics (1) is preheated to 55 ~ 95 DEG C by preheater (4) further.
The present invention is by the heat exchange in oxidizing tower heat exchanger (2) of the oxidation products of isopropyl benzene raw material and oxidizing tower discharging, when heat is 129 kilocalories of/kilogram of phenol, reduce low-pressure steam and consume 245 kgs/tonne of phenol, and reduce circulating cooling water consumption 13.1 tons of/ton of phenol, because oxidizing tower heat exchanger (2) and oxidizing tower driving preheater (3) adopt parallel-connection flow, therefore the resistance of ducting is not increased, do not increase the power consumption of cyclic oxidation liquid transferpump, achieve technique effect preferably yet.
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 preheater; 5 is oxidation top gaseous phase outlet line; 6 is oxidizing tower; 7 is air inlet pipeline; 8 is topping-up pump; 9 is oxidation products outlet line.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
In device flow process as shown in Figure 1, the mass content of isopropyl benzene be 66.1% isopropyl benzene feedstock pipeline (1) carry out heat exchange by oxidizing tower heat exchanger (2) and the oxidizing tower material that refluxes, isopropyl benzene raw material after heating enters oxidizing tower (6), with the air generation oxidizing reaction passed into through air inlet pipeline (7) after being preheated to 55 DEG C by preheater (4); Oxidizing tower (6) tower top is delivered to out-of-bounds containing the tail gas of a small amount of isopropyl benzene and water through gaseous phase outlet pipeline (5); Oxidizing tower (6) tower reactor passes through topping-up pump (8) supercharging containing the liquid phase material of isopropyl benzene and hydrogen phosphide cumene, part liquid phase material is sent outside as oxidation products, part oxidation products (9) enters oxidizing tower heat exchanger (2) by return line and carries out heat exchange with isopropyl benzene raw material, moves the backflow material after heat and gets back to oxidizing tower (6).
Oxidizing tower heat exchanger (2) is upper is in parallel with oxidizing tower driving preheater (3), phegma main pipe line is formed after phegma outlet line on oxidizing tower heat exchanger (2) is connected with the phegma outlet line on oxidizing tower driving preheater (3), then phegma main pipe line is connected with oxidizing tower (6), and described phegma main pipe line is provided with butterfly valve.Phegma pipeline before and after oxidizing tower heat exchanger (2), oxidizing tower driving preheater (3) is equipped with valve.
Under driving operating mode, close the backflow material pipeline of oxidizing tower heat exchanger (2), open the backflow material pipeline of oxidizing tower driving preheater (14), the backflow material of topping-up pump (8) supercharging to be driven preheater (14) by oxidizing tower, heating when realizing driving.
Preheater (4), oxidizing tower driving preheater (3) are provided with low-pressure steam feeding line, 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), described oxidizing tower (6) is provided with quenched water and fire water pipeline, described oxidizing tower heat exchanger (2) is provided with cross-line, and that road pipeline that topping-up pump (8) outlet line is connected with oxidizing tower heat exchanger (2) strides across oxidizing tower heat exchanger (2) and is directly connected with oxidizing tower (6).
Phenol-acetone industrial scale is 100,000 tons/year.Oxidizing tower (6) tower reactor liquid phase stream 11% enters oxidation products outlet line (9) by weight.Oxidizing tower service temperature 105 DEG C; Working pressure is 0.27MPaG; Oxidizing tower heat exchanger operation temperature is 100 DEG C; Working pressure is 0.27MPaG.As calculated, the method can reduce low-pressure steam and consume 1.905 tons/hour, and reduces circulating cooling water consumption 101.5 tons/hour.
[embodiment 2]
According to the condition described in embodiment 1 and step, phenol-acetone industrial scale changes 200,000 tons/year into.Low-pressure steam can be reduced and consume 3.80 tons/hour, and reduce circulating cooling water consumption 203 tons/hour.
[embodiment 3]
According to the condition described in embodiment 1 and step, just phenol-acetone industrial scale changes 350,000 tons/year into.Low-pressure steam can be reduced and consume 6.65 tons/hour, and reduce circulating cooling water consumption 354 tons/hour.
[embodiment 4]
According to the condition described in embodiment 1 and step, in charging (1), the mass content of isopropyl benzene is 70.3%; Isopropyl benzene raw material after heating enters oxidizing tower (6) after being preheated to 60 DEG C by preheater (4); Oxidizing tower (6) tower reactor liquid phase stream 26% enters oxidation products outlet line (9) by weight; Oxidizing tower service temperature 105 DEG C; Working pressure is 0.27MPaG; Oxidizing tower heat exchanger operation temperature is 60 DEG C; Working pressure is 0.2MPaG.As calculated, the method can reduce low-pressure steam and consume 1.865 tons/hour, and reduces circulating cooling water consumption 99.5 tons/hour.
[embodiment 5]
According to the condition described in embodiment 1 and step, in charging (1), the mass content of isopropyl benzene is 75.6%; Isopropyl benzene raw material after heating enters oxidizing tower (6) after being preheated to 68 DEG C by preheater (4); Oxidizing tower (6) tower reactor liquid phase stream 32% enters oxidation products outlet line (9) by weight; Oxidizing tower service temperature 105 DEG C; Working pressure is 0.27MPaG; Oxidizing tower heat exchanger operation temperature is 70 DEG C; Working pressure is 0.3MPaG.As calculated, the method can reduce low-pressure steam and consume 1.885 tons/hour, and reduces circulating cooling water consumption 100.5 tons/hour.
[embodiment 6]
According to the condition described in embodiment 1 and step, in charging (1), the mass content of isopropyl benzene is 89.2%; Isopropyl benzene raw material after heating enters oxidizing tower (6) after being preheated to 79 DEG C by preheater (4); Oxidizing tower (6) tower reactor liquid phase stream 47% enters oxidation products outlet line (9) by weight; Oxidizing tower service temperature 105 DEG C; Working pressure is 0.27MPaG; Oxidizing tower heat exchanger operation temperature is 80 DEG C; Working pressure is 0.5MPaG.As calculated, the method can reduce low-pressure steam and consume 1.925 tons/hour, and reduces circulating cooling water consumption 102.5 tons/hour.
[embodiment 7]
According to the condition described in embodiment 1 and step, in charging (1), the mass content of isopropyl benzene is 98.9%; Isopropyl benzene raw material after heating enters oxidizing tower (6) after being preheated to 95 DEG C by preheater (4); Oxidizing tower (6) tower reactor liquid phase stream 50% enters oxidation products outlet line (9) by weight; Oxidizing tower service temperature 105 DEG C; Working pressure is 0.27MPaG; Oxidizing tower heat exchanger operation temperature is 100 DEG C; Working pressure is 0.8MPaG.As calculated, the method can reduce low-pressure steam and consume 1.945 tons/hour, and reduces circulating cooling water consumption 103.5 tons/hour.
Claims (8)
1. one kind is reduced the method for phenol-acetone device oxidizing reaction unit energy consumption, after the logistics (1) comprising isopropyl benzene carries out heat exchange by oxidizing tower heat exchanger (2) and reflux stream at the bottom of oxidizing tower (6) tower, again by entering oxidizing tower (6) after preheater (4) further preheating, oxidizing reaction is there is with the air logistics (7) passed in tower, oxidizing tower (6) overhead stream (5) delivers to tail gas treating unit, a part of logistics of oxidizing tower (6) tower reactor liquid phase stream enters oxidation products outlet line (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 driving preheater (3), then return oxidizing tower (6), oxidizing tower heat exchanger (2) is in parallel with oxidizing tower driving preheater (3).
2. reduce the method for phenol-acetone device oxidizing reaction unit energy consumption according to claim 1, it is characterized in that preheater (4), the heat transferring medium of oxidizing tower driving preheater (3) is low-pressure steam.
3. reduce the method for phenol-acetone device oxidizing reaction unit energy consumption according to claim 1, it is characterized in that described 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); Described oxidizing tower (6) is provided with quenched water and fire water pipeline.
4. reduce the method for phenol-acetone device oxidizing reaction unit energy consumption according to claim 1, it is characterized in that oxidizing tower (6) tower reactor liquid phase stream 10 ~ 50% enters oxidation products outlet line (9) by weight.
5. reduce the method for phenol-acetone device oxidizing reaction unit energy consumption according to claim 1, it is characterized in that oxidizing tower (6) service temperature is 20 ~ 200 DEG C, working pressure is 0.0 ~ 0.8MPaG; Oxidizing tower heat exchanger (2) service temperature is 10 ~ 200 DEG C, and working pressure is 0.01 ~ 1.5MPaG.
6. reduce the method for phenol-acetone device oxidizing reaction unit energy consumption according to claim 5, it is characterized in that oxidizing tower (6) service temperature is 80 ~ 120 DEG C, working pressure is 0.2 ~ 0.4MPaG; Oxidizing tower heat exchanger (2) service temperature is 30 ~ 110 DEG C, and working pressure is 0.2 ~ 0.8MPaG.
7. reduce the method for phenol-acetone device oxidizing reaction unit energy consumption according to claim 1, the mass content comprising isopropyl benzene in the logistics (1) of isopropyl benzene described in it is characterized in that is 65 ~ 99%; .
8. reduce the method for phenol-acetone device oxidizing reaction unit energy consumption according to claim 1, it is characterized in that logistics (1) is preheated to 55 ~ 95 DEG C by preheater (4) further.
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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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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6303825B1 (en) * | 1999-03-12 | 2001-10-16 | Phenolchemie Gmbh & Co. Kg | Method of 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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2014
- 2014-12-01 CN CN201410719776.9A patent/CN104478775B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6303825B1 (en) * | 1999-03-12 | 2001-10-16 | Phenolchemie Gmbh & Co. Kg | Method of 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 |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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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