CN104447214A - Method for reducing energy consumption by employing phenol-acetone device oxidation reaction unit - Google Patents
Method for reducing energy consumption by employing phenol-acetone device oxidation reaction unit Download PDFInfo
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- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/08—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by decomposition of hydroperoxides, e.g. cumene hydroperoxide
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- C07C407/00—Preparation of peroxy compounds
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- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/51—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition
- C07C45/53—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition of hydroperoxides
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Abstract
The invention relates to a method for reducing energy consumption by employing a phenol-acetone device oxidation reaction unit and is mainly used for solving the problem of relatively high energy consumption in the prior art. According to the technical scheme, the method for reducing energy consumption by employing the phenol-acetone device oxidation reaction unit, disclosed by the invention, comprises the following steps: firstly, enabling a cumin material flow to exchange heat with a bottom reflux material flow (21) of a 2# oxidation tower (16), then exchanging heat with a bottom reflux material flow (9) of a 1# oxidation tower (6), and then preheating and feeding into the 1# oxidation tower (6); conveying an overhead material flow to a tail gas treatment unit, feeding one part of tower bottom material flow to the 2# oxidation tower (16), returning the other part back to the 1# oxidation tower (6) after passing through a 1# oxidation tower heat exchanger (2); conveying the overhead material flow of the 2# oxidation tower (16) to the tail gas treatment unit; and sending one part of the tower bottom material flow to a subsequent oxidation unit, and returning the other part of the material flow back to the 2# oxidation tower (16) after passing through the 2# oxidation tower heat exchanger, thus the problem is relatively well solved; and the method can be applied to the phenol-acetone device oxidation reaction unit.
Description
Technical field
The present invention relates to a kind of method that phenol-acetone device oxidizing reaction unit reduces 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 new phenol-acetone device oxidizing reaction unit to reduce the method for energy consumption.The method is used for, in phenol-acetone device oxidizing reaction unit, 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 phenol-acetone device oxidizing reaction unit reduces the method for energy consumption, after the logistics (1) comprising isopropyl benzene carries out heat exchange by 2# oxidizing tower heat exchanger (20) and reflux stream (21) at the bottom of 2# oxidizing tower (16) tower, heat exchange is carried out again by 1# oxidizing tower heat exchanger (2) and reflux stream (9) at the bottom of 1# oxidizing tower (6) tower, cumene stream (3) after heating is by oxidation feed preheater (4) preheating further, feed stream (5) after preheating enters 1# oxidizing tower (6), oxidizing reaction is there is with the air logistics (11) passed in tower, 1# oxidizing tower (6) overhead stream (12) delivers to tail gas treating unit, a part of logistics (13) of 1# oxidizing tower (6) tower reactor liquid phase stream (7) enters 2# oxidizing tower (16), and another part logistics (15) enters after 1# oxidizing tower heat exchanger (2) carries out heat exchange with logistics (1) and returns 1# oxidizing tower (6), there is oxidizing reaction further in the air logistics (22) passed in the logistics (13) passing into 2# oxidizing tower (16) and tower, 2# oxidizing tower (16) overhead stream (23) delivers to tail gas treating unit, subsequent oxidation unit is sent in a part of logistics (19) of 2# oxidizing tower (16) tower reactor logistics (17), and another part logistics (16) returns 2# oxidizing tower (16) after entering 2# oxidizing tower heat exchanger (20) and logistics (1) heat exchange.
In technique scheme, preferably, be parallel with 1# oxidizing tower driving preheater (14) with logistics (15), be parallel with 2# oxidizing tower driving preheater (26) with logistics (16), the heating of backflow material when realizing driving.
In technique scheme, preferably, described 1# oxidizing tower (6) service temperature is 20 ~ 200 DEG C, and working pressure is 0.1 ~ 0.8MPaG; 1# oxidizing tower heat exchanger (2) service temperature is 10 ~ 200 DEG C, and working pressure is 0.1 ~ 1.5MPaG; 2# oxidizing tower (16) service temperature is 20 ~ 200 DEG C, and working pressure is 0.1 ~ 0.8MPaG; 2# oxidizing tower heat exchanger (20) service temperature is 10 ~ 200 DEG C, and working pressure is 0.1 ~ 1.5MPaG.
In technique scheme, more preferably, described 1# oxidizing tower (6) service temperature is 80 ~ 120 DEG C, and working pressure is 0.2 ~ 0.4MPaG; 1# oxidizing tower heat exchanger (2) service temperature is 60 ~ 110 DEG C, and working pressure is 0.2 ~ 0.8MPaG; 2# oxidizing tower (16) service temperature is 80 ~ 120 DEG C, and working pressure is 0.2 ~ 0.4MPaG; 2# oxidizing tower heat exchanger (20) service temperature is 30 ~ 110 DEG C, and working pressure is 0.2 ~ 0.8MPaG.
In technique scheme, preferably, described logistics (13) is 1:1 ~ 10 with the ratio of the mass rate of logistics (15), and logistics (19) is 1:1 ~ 10 with the ratio of the mass rate of logistics (16).
In technique scheme, preferably, the mass content comprising isopropyl benzene in the logistics (1) of isopropyl benzene described in is 50 ~ 99%; Logistics (5) is 1 ~ 10:1 with the ratio of the mass rate of logistics (11), and logistics (13) is 1 ~ 10:1 with the ratio of the mass rate of logistics (22).
In technique scheme, preferably, the cumene stream (3) after described heating is preheated to 60 ~ 98 DEG C further by oxidation feed preheater (4).
In technique scheme, preferably, the heat transferring medium of described oxidation feed preheater (4), 1# oxidizing tower driving preheater (14), 2# oxidizing tower driving preheater (26) is low-pressure steam.
The reflux stream successively heat exchange in 2# oxidizing tower heat exchanger (20) and 1# oxidizing tower heat exchanger (2) that the feed stream (1) of 1# oxidizing tower (6) charging and 2# oxidizing tower (16) tower reactor and 1# oxidizing tower (6) tower reactor export by the present invention, be 39.6 kilocalories of/kilogram of phenol in 1# oxidizing tower heat exchanger (20) heat, 2# oxidizing tower heat exchanger (20) heat is 89.6 kilocalories of/kilogram of phenol, when total heat is 129.2 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, achieve technique effect preferably.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention.
In Fig. 1,1 is the feed stream comprising isopropyl benzene; 2 is 1# oxidizing tower heat exchanger; 3 is the cumene stream after heating; 4 is oxidation feed preheater; 5 is the feed stream after preheating; 6 is 1# oxidizing tower; 7 is 1# oxidizing tower (6) tower reactor liquid phase stream; 8 is 1# oxidizing tower (6) tower reactor pump; 9 for entering the reflux stream of 1# oxidizing tower heat exchanger; 10 is 1# oxidizing tower (6) tower reactor reflux stream; 11 is air logistics; 12 is 1# oxidizing tower overhead stream; 13 is the part of 1# oxidizing tower (6) tower reactor liquid phase stream (7); 14 is 1# oxidizing tower driving preheater; 15 is another part of tower reactor liquid phase stream (7); 16 is 2# oxidizing tower; 17 is 2# oxidizing tower (16) tower reactor logistics; 18 is low-pressure steam; 19 is 2# oxidizing tower (16) tower reactor logistics) a part; 20 is 2# oxidizing tower heat exchanger; 21 for entering the reflux stream of 2# oxidizing tower heat exchanger; 22 is air logistics; 23 is 2# oxidation overhead stream; 24 is 2# oxidizing tower tower reactor pump; 25 is low-pressure steam; 26 is 2# oxidizing tower driving preheater; 27 is low-pressure steam; 28 is the logistics of 2# oxidizing tower tower reactor; 29 is the gas disposal that truncates; 30 is air main.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
In technical process as shown in Figure 1, after the logistics (1) comprising isopropyl benzene carries out heat exchange by 2# oxidizing tower heat exchanger (20) and reflux stream (21) at the bottom of 2# oxidizing tower tower, heat exchange is carried out again by 1# oxidizing tower heat exchanger (2) and reflux stream (9) at the bottom of 1# oxidizing tower tower, cumene stream (3) after heating is preheated to feeding temperature further by oxidation feed preheater (4), isopropyl benzene incoming flow stock (5) after preheating enters 1# oxidizing tower (6), oxidizing reaction is there is with the air logistics (11) passed in tower, 1# oxidizing tower (6) tower top delivers to tail gas treating unit process containing the tail gas (12) of a small amount of isopropyl benzene and water, 1# oxidizing tower (6) tower reactor is got by 1# oxidizing tower tower reactor pump (8) containing the liquid phase stream (7) of isopropyl benzene and hydrogen phosphide cumene, part oxidation products (13) enters 2# oxidizing tower (16) and is oxidized further, another part oxidation products enters 1# oxidizing tower heat exchanger (2) and isopropyl benzene raw material by return line through bypass (15) to carry out heat exchange and removes reaction Heat of Formation, moves the reflux stream after heat and gets back to 1# oxidizing tower (6) through return line (10).There is oxidizing reaction further in the air logistics (22) passed in the oxidation products (13) passing into 2# oxidizing tower (16) and tower; 2# oxidizing tower (16) tower top delivers to tail gas treating unit process containing the tail gas (23) of a small amount of isopropyl benzene and water; 2# oxidizing tower (16) tower reactor is got by 2# oxidizing tower tower reactor pump (24) containing the further oxidation products (17) of isopropyl benzene and hydrogen phosphide cumene, part oxidation products (19) sends subsequent oxidation unit, another part oxidation products enters 2# oxidizing tower heat exchanger (20) and isopropyl benzene raw material by return line through bypass (16) to carry out heat exchange and removes reaction Heat of Formation, moves the reflux stream after heat and gets back to 2# oxidizing tower (16) through return line (28).
Be parallel with 1# oxidizing tower driving preheater (14) with logistics (15), be parallel with 2# oxidizing tower driving preheater (26) with logistics (16), the heating of backflow material when realizing driving.Driving operating mode, bypass duct (15) and (16) are closed, the reflux stream that 1# oxidizing tower tower reactor pump (8) and 2# oxidizing tower tower reactor pump (24) are got enters 1# oxidizing tower driving preheater (14) respectively and preheating is carried out in 2# oxidizing tower driving preheater (26), the heating of reflux stream when realizing driving.
Logistics (13) is 1:2 with the ratio of the mass rate of logistics (15), and logistics (19) is 1:2 with the ratio of the mass rate of logistics (16).The described mass content comprising isopropyl benzene in the logistics (1) of isopropyl benzene is 50.2%; Logistics (5) is 7:1 with the ratio of the mass rate of logistics (11), and logistics (13) is 7:1 with the ratio of the mass rate of logistics (22).Cumene stream (3) after described heating is preheated to 61 DEG C further by oxidation feed preheater (4).
Phenol-acetone industrial scale is 100,000 tons/year.1# oxidizing tower (6) service temperature 105 DEG C, working pressure is 0.27MPaG; 2# oxidizing tower (16) service temperature 101 DEG C, working pressure is 0.27MPaG; 1# oxidizing tower heat exchanger (2) service temperature is 105 DEG C; Working pressure is 0.8MPaG; 2# oxidizing tower heat exchanger (2) service temperature is 101 DEG C, and working pressure is 0.8MPaG.The composition distribution of each logistics is in table 1.As calculated, the method can reduce low-pressure steam and consume 1.86 tons/hour, and reduces circulating cooling water consumption 99 tons/hour.
Table 1
| Mass fraction | Logistics 1 | Logistics 5 | Logistics 7 | Logistics 10 | Logistics 17 | Logistics 19 |
| Methyl phenyl ketone | 0.000 | 0.000 | 0.001 | 0.001 | 0.001 | 0.001 |
| Phenol | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Acetone | 0.497 | 0.497 | 0.436 | 0.436 | 0.873 | 0.873 |
| Isopropyl benzene | 0.502 | 0.502 | 0.560 | 0.560 | 0.120 | 0.120 |
| Hydrogen phosphide cumene | 0.000 | 0.000 | 0.003 | 0.003 | 0.005 | 0.005 |
| Formic acid | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Water | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Nitrogen | 0.001 | 0.001 | 0.000 | 0.000 | 0.000 | 0.000 |
| Methane | 0.000 | 0.000 | 0.000 | 0.000 | 0.001 | 0.001 |
| Dimethylphenylcarbinol | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Subtotal | 1.000 | 1.000 | 1.000 | 1.000 | 1.000 | 1.000 |
[embodiment 2]
According to the condition described in embodiment 1 and step, 1# oxidizing tower (6) service temperature 195 DEG C, working pressure is 0.75MPaG; 2# oxidizing tower (16) service temperature 180 DEG C, working pressure is 0.70MPaG; 1# oxidizing tower heat exchanger (2) service temperature is 195 DEG C, and working pressure is 0.8MPaG; 2# oxidizing tower heat exchanger (20) service temperature is 180 DEG C; Working pressure is 0.8MPaG.Logistics (13) is 1:3 with the ratio of the mass rate of logistics (15), and logistics (19) is 1:3 with the ratio of the mass rate of logistics (16).The described mass content comprising isopropyl benzene in the logistics (1) of isopropyl benzene is 61.2%; Logistics (5) is 6:1 with the ratio of the mass rate of logistics (11), and logistics (13) is 6:1 with the ratio of the mass rate of logistics (22).Cumene stream (3) after described heating is preheated to 75 DEG C further by oxidation feed preheater (4).The composition distribution of each logistics is in table 2.As calculated, the method can reduce low-pressure steam and consume 1.88 tons/hour, and reduces circulating cooling water consumption 100 tons/hour.
Table 2
| Mass fraction | Logistics 1 | Logistics 5 | Logistics 7 | Logistics 10 | Logistics 17 | Logistics 19 |
| Methyl phenyl ketone | 0.000 | 0.000 | 0.001 | 0.001 | 0.001 | 0.001 |
| Phenol | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Acetone | 0.387 | 0.387 | 0.826 | 0.826 | 0.843 | 0.843 |
| Isopropyl benzene | 0.612 | 0.612 | 0.170 | 0.170 | 0.120 | 0.120 |
| Hydrogen phosphide cumene | 0.000 | 0.000 | 0.003 | 0.003 | 0.035 | 0.035 |
| Formic acid | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Water | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Nitrogen | 0.001 | 0.001 | 0.000 | 0.000 | 0.000 | 0.000 |
| Methane | 0.000 | 0.000 | 0.000 | 0.000 | 0.001 | 0.001 |
| Dimethylphenylcarbinol | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Subtotal | 1.000 | 1.000 | 1.000 | 1.000 | 1.000 | 1.000 |
[embodiment 3]
According to the condition described in embodiment 1 and step, 1# oxidizing tower (6) service temperature 65 DEG C, working pressure is 0.15MPaG; 2# oxidizing tower (16) service temperature 60 DEG C, working pressure is 0.10MPaG; 1# oxidizing tower heat exchanger (2) service temperature is 65 DEG C; Working pressure is 0.1MPaG; 2# oxidizing tower heat exchanger (20) service temperature is 60 DEG C; Working pressure is 0.1MPaG.Logistics (13) is 1:8 with the ratio of the mass rate of logistics (15), and logistics (19) is 1:8 with the ratio of the mass rate of logistics (16).The described mass content comprising isopropyl benzene in the logistics (1) of isopropyl benzene is 85.2%; Logistics (5) is 3:1 with the ratio of the mass rate of logistics (11), and logistics (13) is 3:1 with the ratio of the mass rate of logistics (22).Cumene stream (3) after described heating is preheated to 86 DEG C further by oxidation feed preheater (4).The composition distribution of each logistics is in table 3.As calculated, the method can reduce low-pressure steam and consume 1.92 tons/hour, and reduces circulating cooling water consumption 102 tons/hour.
Table 3
| Mass fraction | Logistics 1 | Logistics 5 | Logistics 7 | Logistics 10 | Logistics 17 | Logistics 19 |
| Methyl phenyl ketone | 0.000 | 0.000 | 0.001 | 0.001 | 0.001 | 0.001 |
| Phenol | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Acetone | 0.147 | 0.147 | 0.739 | 0.739 | 0.862 | 0.862 |
| Isopropyl benzene | 0.852 | 0.852 | 0.257 | 0.257 | 0.109 | 0.109 |
| Hydrogen phosphide cumene | 0.000 | 0.000 | 0.003 | 0.003 | 0.005 | 0.005 |
| Formic acid | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Water | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Nitrogen | 0.001 | 0.001 | 0.000 | 0.000 | 0.000 | 0.000 |
| Methane | 0.000 | 0.000 | 0.000 | 0.000 | 0.001 | 0.001 |
| Dimethylphenylcarbinol | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Subtotal | 1.000 | 1.000 | 1.000 | 1.000 | 1.000 | 1.000 |
[embodiment 4]
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 5]
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 6]
According to the condition described in embodiment 1 and step, 1# oxidizing tower (6) service temperature 20 DEG C, working pressure is 0.4MPaG; 2# oxidizing tower (16) service temperature 20 DEG C, working pressure is 0.40MPaG; 1# oxidizing tower heat exchanger (2) service temperature is 155 DEG C; Working pressure is 0.4MPaG; 2# oxidizing tower heat exchanger (20) service temperature is 145 DEG C; Working pressure is 0.4MPaG.Logistics (13) is 1:4 with the ratio of the mass rate of logistics (15), and logistics (19) is 1:7 with the ratio of the mass rate of logistics (16).The described mass content comprising isopropyl benzene in the logistics (1) of isopropyl benzene is 90.5%; Logistics (5) is 7:1 with the ratio of the mass rate of logistics (11), and logistics (13) is 2:1 with the ratio of the mass rate of logistics (22).Cumene stream (3) after described heating is preheated to 97 DEG C further by oxidation feed preheater (4).The composition distribution of each logistics is in table 4.As calculated, the method can reduce low-pressure steam and consume 1.94 tons/hour, and reduces circulating cooling water consumption 103 tons/hour.
Table 4
| Mass fraction | Logistics 1 | Logistics 5 | Logistics 7 | Logistics 10 | Logistics 17 | Logistics 19 |
| Methyl phenyl ketone | 0.000 | 0.000 | 0.001 | 0.001 | 0.001 | 0.001 |
| Phenol | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Acetone | 0.085 | 0.085 | 0.739 | 0.739 | 0.862 | 0.862 |
| Isopropyl benzene | 0.905 | 0.905 | 0.257 | 0.257 | 0.109 | 0.109 |
| Hydrogen phosphide cumene | 0.000 | 0.000 | 0.003 | 0.003 | 0.005 | 0.005 |
| Formic acid | 0.010 | 0.010 | 0.000 | 0.000 | 0.000 | 0.000 |
| Water | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Nitrogen | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Methane | 0.000 | 0.000 | 0.000 | 0.000 | 0.001 | 0.001 |
| Dimethylphenylcarbinol | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Subtotal | 1.000 | 1.000 | 1.000 | 1.000 | 1.000 | 1.000 |
Claims (8)
1. the method for a phenol-acetone device oxidizing reaction unit reduction energy consumption, after the logistics (1) comprising isopropyl benzene carries out heat exchange by 2# oxidizing tower heat exchanger (20) and reflux stream (21) at the bottom of 2# oxidizing tower (16) tower, heat exchange is carried out again by 1# oxidizing tower heat exchanger (2) and reflux stream (9) at the bottom of 1# oxidizing tower (6) tower, cumene stream (3) after heating is by oxidation feed preheater (4) preheating further, feed stream (5) after preheating enters 1# oxidizing tower (6), oxidizing reaction is there is with the air logistics (11) passed in tower, 1# oxidizing tower (6) overhead stream (12) delivers to tail gas treating unit, a part of logistics (13) of 1# oxidizing tower (6) tower reactor liquid phase stream (7) enters 2# oxidizing tower (16), and another part logistics (15) enters after 1# oxidizing tower heat exchanger (2) carries out heat exchange with logistics (1) and returns 1# oxidizing tower (6), there is oxidizing reaction further in the air logistics (22) passed in the logistics (13) passing into 2# oxidizing tower (16) and tower, 2# oxidizing tower (16) overhead stream (23) delivers to tail gas treating unit, subsequent oxidation unit is sent in a part of logistics (19) of 2# oxidizing tower (16) tower reactor logistics (17), and another part logistics (16) returns 2# oxidizing tower (16) after entering 2# oxidizing tower heat exchanger (20) and logistics (1) heat exchange.
2. phenol-acetone device oxidizing reaction unit reduces the method for energy consumption according to claim 1, it is characterized in that being parallel with 1# oxidizing tower driving preheater (14) with logistics (15), 2# oxidizing tower driving preheater (26) is parallel with, the heating of backflow material when realizing driving with logistics (16).
3. phenol-acetone device oxidizing reaction unit reduces the method for energy consumption according to claim 1, and it is characterized in that described 1# oxidizing tower (6) service temperature is 20 ~ 200 DEG C, working pressure is 0.1 ~ 0.8MPaG; 1# oxidizing tower heat exchanger (2) service temperature is 10 ~ 200 DEG C, and working pressure is 0.1 ~ 1.5MPaG; 2# oxidizing tower (16) service temperature is 20 ~ 200 DEG C, and working pressure is 0.1 ~ 0.8MPaG; 2# oxidizing tower heat exchanger (20) service temperature is 10 ~ 200 DEG C, and working pressure is 0.1 ~ 1.5MPaG.
4. phenol-acetone device oxidizing reaction unit reduces the method for energy consumption according to claim 3, and it is characterized in that described 1# oxidizing tower (6) service temperature is 80 ~ 120 DEG C, working pressure is 0.2 ~ 0.4MPaG; 1# oxidizing tower heat exchanger (2) service temperature is 60 ~ 110 DEG C, and working pressure is 0.2 ~ 0.8MPaG; 2# oxidizing tower (16) service temperature is 80 ~ 120 DEG C, and working pressure is 0.2 ~ 0.4MPaG; 2# oxidizing tower heat exchanger (20) service temperature is 30 ~ 110 DEG C, and working pressure is 0.2 ~ 0.8MPaG.
5. phenol-acetone device oxidizing reaction unit reduces the method for energy consumption according to claim 1, it is characterized in that described logistics (13) is 1:1 ~ 10 with the ratio of the mass rate of logistics (15), logistics (19) is 1:1 ~ 10 with the ratio of the mass rate of logistics (16).
6. phenol-acetone device oxidizing reaction unit reduces the method for energy consumption according to claim 1, and the mass content comprising isopropyl benzene in the logistics (1) of isopropyl benzene described in it is characterized in that is 50 ~ 99%; Logistics (5) is 1 ~ 10:1 with the ratio of the mass rate of logistics (11), and logistics (13) is 1 ~ 10:1 with the ratio of the mass rate of logistics (22).
7. phenol-acetone device oxidizing reaction unit reduces the method for energy consumption according to claim 1, it is characterized in that the cumene stream (3) after described heating is preheated to 60 ~ 98 DEG C further by oxidation feed preheater (4).
8. according to claim 1,2, phenol-acetone device oxidizing reaction unit reduces the method for energy consumption, it is characterized in that described oxidation feed preheater (4), 1# oxidizing tower driving preheater (14), 2# oxidizing tower driving preheater (26) heat transferring medium be low-pressure steam.
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| DE19946888A1 (en) * | 1999-09-30 | 2001-04-05 | Phenolchemie Gmbh & Co Kg | Process for the production of phenol, acetone and methyl ethyl ketone |
| CN104151144A (en) * | 2014-07-16 | 2014-11-19 | 常州大学 | Method for preparing phenol/acetone by decomposing cumene hydroperoxide |
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2014
- 2014-12-01 CN CN201410719763.1A patent/CN104447214B/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106117018A (en) * | 2016-07-05 | 2016-11-16 | 中石化上海工程有限公司 | The method of phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery |
| CN106117018B (en) * | 2016-07-05 | 2018-12-04 | 中石化上海工程有限公司 | The method of phenol-acetone device cumyl hydroperoxide upgrading system waste heat recycling |
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| CN104447214B (en) | 2016-02-24 |
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