CN104447629B - The method of propylene oxide unit oxidation unit byproduct steam - Google Patents
The method of propylene oxide unit oxidation unit byproduct steam Download PDFInfo
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- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/02—Synthesis of the oxirane ring
- C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
- C07D301/19—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with organic hydroperoxides
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Abstract
A kind of method that the present invention relates to propylene oxide unit oxidation unit byproduct steam, mainly solves the problem that in prior art, energy consumption is higher.The present invention is by a kind of method using propylene oxide unit oxidation unit byproduct steam, and including least one set oxidation section, concentration tower, often group oxidation section includes oxidation reactor, steam generator, cooler；Raw material including isopropylbenzene enters oxidation reactor and air reaction, a part of material of still liquid at the bottom of oxidation reactor tower is delivered to the oxidation reactor of next group oxidation section and is continued reaction, and another part material is back to oxidation reactor successively after steam generator, cooler；A part of material of still liquid at the bottom of oxidation reactor tower in last group oxidation section is sent into concentration tower and is carried out material concentration；Wherein, the technical scheme that the steam of the steam generator generation often organizing oxidation section delivers to concentration tower reboiler as thermal source preferably solves the problems referred to above, can be used in the production of expoxy propane.
Description
Technical field
A kind of method that the present invention relates to propylene oxide unit oxidation unit byproduct steam.
Background technology
Expoxy propane is one of important intermediate of petrochemicals, is largely used to produce polyether polyol and prepares plasticized polyurethane
Material, and produce unsaturated-resin and surfactant etc..The production technology of expoxy propane mainly has at present: chlorohydrination, ring
Ethylene Oxide/styrene coproduction, expoxy propane/indirect oxidation method and peroxidating such as tert-butyl alcohol coproduction, cumyl hydroperoxide oxidation
Hydrogen Direct Epoxidation method.
CN201210429266.9 and CN 201110294224.4 relates to the method producing expoxy propane, describes cumene method
Producing the process of expoxy propane, first the method is to obtain cumyl hydroperoxide CHP, then by cumene oxidation
Cumyl hydroperoxide is generated expoxy propane PO with propylene initial ring oxidation reaction.Wherein cumene oxidation obtains peroxidating
The technique unit of hydrogen isopropylbenzene is referred to as oxidation unit.CN01806930.4 relates to the preparation method of expoxy propane, in the method
Oxidation operation be under the high temperature conditions, obtain cumyl hydroperoxide by air or oxygen-containing gas autoxidation isopropylbenzene.
CN201120437887.2 relates to a kind of outside isopropylbenzene continuous oxidation system moving heat, its oxidation unit include oxidizing tower,
Oxidation outer circulation cooler and circulating pump.Oxidation unit realizes the circulation of oxidizing tower material by circulating pump, and circulation fluid is carried
Oxidation reaction generates heat and returns oxidizing tower tower top after heat exchanger cooling is removed.This oxidizing tower high-temperature material uses recirculated cooling water
Cooling, the unrecovered utilization of waste heat, there is propylene oxide process Energy harvesting unreasonable, the problems such as energy consumption is higher.
All there is the problem that energy consumption is higher in prior art, 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 expoxy propane dress
The method putting oxidation unit byproduct steam.The method, in the production of expoxy propane, has the advantage that energy consumption is relatively low.
For solving the problems referred to above, the technical solution used in the present invention is as follows: a kind of propylene oxide unit oxidation unit byproduct steam
Method, including least one set oxidation section, concentration tower, often group oxidation section include oxidation reactor, steam generator,
Cooler；Raw material including isopropylbenzene enters oxidation reactor and air reaction, a part of thing of still liquid at the bottom of oxidation reactor tower
Material is delivered to the oxidation reactor of next group oxidation section and is continued reaction, and another part material is successively through steam generator, cooler
After be back to oxidation reactor；At the bottom of oxidation reactor tower in last group oxidation section, concentration sent into by a part of material of still liquid
Tower carries out material concentration；Wherein, the steam of the steam generator generation often organizing oxidation section is delivered to concentration tower as thermal source and is boiled
Device.
In technique scheme, it is preferable that the heat transferring medium of described steam generator is boiler feedwater, the heat exchange of cooler
Medium is that recirculated water supplies water.
In technique scheme, it is preferable that described often group oxidation section internal oxidition reactor, steam generator, cooler
Connect flow process identical.
In technique scheme, it is preferable that described propylene oxide unit oxidation unit includes 1～5 group of oxidation section.
In technique scheme, it is preferable that still liquid at the bottom of described oxidation reactor tower is by carrying after circulating pump supercharging.
In technique scheme, it is preferable that described oxidation reactor operation temperature is 0～150 DEG C, operation pressure is
0.0～0.8MpaG；Steam generator operation temperature is 0～150 DEG C, and operation pressure is 0.0～0.8MPaG；Cooler operation temperature
Degree is 0～130 DEG C, and operation pressure is 0.0～0.8MPaG；Circulating pump operation temperature is 0～150 DEG C, and operation pressure is
0.0～0.8MPaG；Concentration tower operation temperature is 0～110 DEG C, and operation pressure is 0.0～0.008MPa (a)；Concentration tower reboiler
Operation temperature is 0～120 DEG C, and operation pressure is 0.0～0.08MPa (a).
In technique scheme, it is highly preferred that described oxidation reactor operation temperature is 30～130 DEG C, operation pressure is
0.0～0.6MPaG；Steam generator operation temperature is 30～130 DEG C, and operation pressure is 0.0～0.6MPaG；Cooler operates
Temperature is 30～120 DEG C, and operation pressure is 0.0～0.6MPaG；Circulating pump operation temperature is 30～130 DEG C, and operation pressure is
0.0～0.6MPaG；Concentration tower operation temperature is 25～100 DEG C, and operation pressure is 0.0～0.006MPa (a)；Concentration tower reboiler
Operation temperature is 20～100 DEG C, and operation pressure is 0.0～0.06MPa (a).
In technique scheme, most preferably, described oxidation reactor operation temperature is for for 50～110 DEG C, and operation pressure is
0.0～0.4MPaG；Steam generator operation temperature is 50～110 DEG C, and operation pressure is 0.0～0.4MPaG；Cooler operates
Temperature is 50～105 DEG C, and operation pressure is 0.0～0.4MPaG；Circulating pump operation temperature is 50～110 DEG C, and operation pressure is
0.0～0.4MPaG；Concentration tower operation temperature is 40～90 DEG C, and operation pressure is 0.0～0.004MPa (a)；Concentration tower reboiler
Operation temperature is 30～90 DEG C, and operation pressure is 0.0～0.04MPa (a).
The present invention carrys out byproduct steam by recovery oxidation reactor circulation fluid waste heat and removes partial oxidation reaction generation heat, is used for
Concentration tower reboiler thermal source, reduces 651.5 kgs/tonne of products of propylene oxide unit steam consumption；Simultaneously because occur steam to move
Walk partial oxidation reaction and generate heat, also reduce the circulating cooling water consumption 35.83 ton/ton product of propylene oxide unit, 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 isopropylbenzene raw material；2,12,22 is air material；3,13,23 is corresponding oxidation reactor tower reactor
Material；4,14,24 is backflow material；5,15,25 is low-pressure steam material；6,16,26 is corresponding oxidation reactor
Kettle material enters next group oxidation section material；7 is the low-pressure steam feeding line of concentration tower reboiler；
201,202,203 is oxidation reactor；301,302,303 is circulating pump；401,402,403 is cooler；
501,502,503 is steam generator；600 is concentration tower reboiler；700 is concentration tower；
LS is low-pressure steam；DW is boiler feedwater；CWS is that recirculated water supplies water；CWR is recirculated water backwater.
In flow process as shown in Figure 1, as a example by 3 groups of oxidation sections, isopropylbenzene raw material 1 is delivered to oxidation reactor 201
In, mix with air material 2, oxidation reaction occurs, generate cumyl hydroperoxide.Oxidation reactor 201 kettle material
The part of 3 is through circulating pump 301 circular flow, and circulation fluid cools down through steam generator 501 and cooler 401, cold
But the material 4 after continues reaction in being back to oxidation reactor 201.Boiler feedwater DW enters steam generator 501, produces
Raw low-pressure steam LS material 5.Recirculated water water supply CWS entrance cooler 401 becomes recirculated water after removing residue reaction heat and returns
Water CWR returns.Another part material of mixed material 3, after circulating pump 301 supercharging, send oxidation anti-as material 6
Answer device 202.
Material 6 mixes at oxidation reactor 202 with air material 12, occurs oxidation reaction to generate cumyl hydroperoxide.
Oxidation reactor 202 kettle material 13 part is through circulating pump 302 circular flow, and circulation fluid is through steam generator 502
After cooling down with cooler 402, material 14 continues reaction in being back to oxidation reactor 202.Boiler feedwater DW enters steaming
Vapour generator 502, produces low-pressure steam LS material 15.Recirculated water water supply CWS enters cooler 402 and removes residue instead
Become recirculated water backwater CWR after answering heat to return.Another part material 16 of oxidation reactor 202 outlet is through circulating pump
After 302 superchargings, send oxidation reactor 203.
Material 16 mixes at oxidation reactor 203 with air material 22, occurs oxidation reaction to generate hydrogen peroxide further different
Propyl benzene.Oxidation reactor 203 kettle material 23 part is through circulating pump 303 circular flow, and circulation fluid is sent out through steam
After raw device 503 and cooler 403 cooling, material 24 continues reaction in being back to oxidation reactor 203.Boiler feedwater DW
Enter steam generator 503, produce low-pressure steam LS material 25.Recirculated water water supply CWS enters cooler 403 and removes
Become recirculated water backwater CWR after residue reaction heat to return.Another part material 26 of oxidation reactor 203 outlet is through following
After ring pump 303 supercharging, deliver to concentration tower 700 and carry out material concentration.Thing merged into by low-pressure steam LS material 5,15,25
Material 7 is as concentration tower reboiler 600 thermal source, needed for meeting the heat of concentration tower reboiler 600.
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]
Production of propylene oxide scale is 100,000 tons/year, arranges 2 groups of oxidation sections.Oxidation reactor operation temperature 105 DEG C；
Operation pressure is 0.25MPaG；Steam generator operation temperature 105 DEG C；Operation pressure is 0.25MPaG；Cooler operates
Temperature 97 DEG C；Operation pressure is 0.25MPaG；Circulating pump operation temperature 105 DEG C；Operation pressure is 0.25MPaG；Concentration
Tower operation temperature 70 C；Operation pressure is 0.0035MPa (a)；Concentration tower reboiler duty temperature 81 DEG C；Operation pressure is
0.042MPa(a)；By-product specification is 80.0 DEG C, the steam 8144 kgs/hour of 0.04736MPa (a), it may be assumed that reduce technique dress
Put steam consumption 8144 kgs/hour；Reduce process unit circulating cooling water consumption 447.9 ton hour simultaneously.Concrete data
It is shown in Table 1.
Table 1
| Material number | 4 | 6 | 24 | 26 | 5 | 15 | 25 | 7 |
| Mass fraction % | ||||||||
| Hexane | 91.1 | 91.1 | 75.2 | 75.2 | 0.0 | 0.0 | 0.0 | 0.0 |
| Nonane | 8.2 | 8.2 | 23.4 | 23.4 | 0.0 | 0.0 | 0.0 | 0.0 |
| Isopropylbenzene | 0.4 | 0.4 | 1.0 | 1.0 | 0.0 | 0.0 | 0.0 | 0.0 |
| Cumyl hydroperoxide | 0.0 | 0.0 | 0.1 | 0.1 | 0.0 | 0.0 | 0.0 | 0.0 |
| Nitrogen | 0.1 | 0.1 | 0.1 | 0.1 | 0.0 | 0.0 | 0.0 | 0.0 |
| Water | 0.1 | 0.1 | 0.1 | 0.1 | 100.0 | 100.0 | 100.0 | 100.0 |
| Styrene oligomer | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 |
| Carbon nine | 0.1 | 0.1 | 0.1 | 0.1 | 0.0 | 0.0 | 0.0 | 0.0 |
| Add up to | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 |
[embodiment 2]
According to the condition described in embodiment 1 and step, simply production of propylene oxide scale becomes 150,000 tons/year, arranges 3 groups
Oxidation section.Oxidation reactor operation temperature 105 DEG C；Operation pressure is 0.25MPaG；Steam generator operation temperature 105 DEG C；
Operation pressure is 0.25MPaG；Cooler operation temperature 97 DEG C；Operation pressure is 0.25MPaG；Circulating pump operation temperature
105℃；Operation pressure is 0.25MPaG；Concentration tower operation temperature 70 C；Operation pressure is 0.0035MPa (a)；Concentration
Tower reboiler duty temperature 81 DEG C；Operation pressure is 0.042MPa (a)；By-product specification is 80.0 DEG C, 0.04736MPa (a)
Steam 12216 kgs/hour, it may be assumed that reduce process unit steam consumption 12216 kgs/hour；Reduce technique dress simultaneously
Put circulating cooling water consumption 671.9 ton hour.Concrete data are shown in Table 2.
Table 2
| Material number | 4 | 6 | 14 | 16 | 24 | 26 | 5 | 15 | 25 | 7 |
| Mass fraction % | ||||||||||
| Hexane | 91.1 | 91.1 | 79.5 | 79.5 | 74.8 | 74.8 | 0.0 | 0.0 | 0.0 | 0.0 |
| Nonane | 8.2 | 8.2 | 19.5 | 19.5 | 23.8 | 23.8 | 0.0 | 0.0 | 0.0 | 0.0 |
| Isopropylbenzene | 0.4 | 0.4 | 0.7 | 0.7 | 1.0 | 1.0 | 0.0 | 0.0 | 0.0 | 0.0 |
| Cumyl hydroperoxide | 0.0 | 0.0 | 0.1 | 0.1 | 0.1 | 0.1 | 0.0 | 0.0 | 0.0 | 0.0 |
| Nitrogen | 0.1 | 0.1 | 0.0 | 0.0 | 0.1 | 0.1 | 0.0 | 0.0 | 0.0 | 0.0 |
| Water | 0.1 | 0.1 | 0.1 | 0.1 | 0.1 | 0.1 | 100.0 | 100.0 | 100.0 | 100.0 |
| Styrene oligomer | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 |
| Carbon nine | 0.1 | 0.1 | 0.1 | 0.1 | 0.1 | 0.1 | 0.0 | 0.0 | 0.0 | 0.0 |
| Add up to | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 |
[embodiment 3]
According to the condition described in embodiment 1 and step, production of propylene oxide scale is 100,000 tons/year, arranges 2 groups of oxidation works
Section.Oxidation reactor operation temperature 96 DEG C；Operation pressure is 0.22MPaG；Steam generator operation temperature 96 DEG C；Operation
Pressure is 0.22MPaG；Cooler operation temperature 88 DEG C；Operation pressure is 0.22MPaG；Circulating pump operation temperature 96 DEG C；
Operation pressure is 0.22MPaG；Concentration tower operation temperature 70 C；Operation pressure is 0.0035MPa (a)；Concentration tower reboiler
Operation temperature 81 DEG C；Operation pressure is 0.042MPa (a)；By-product specification is 80.0 DEG C, the steam 8144 of 0.04736MPa (a)
Kg/hour, it may be assumed that reduce process unit steam consumption 8144 kgs/hour；Reduce process unit recirculated cooling water to disappear simultaneously
Consume 447.9 ton hour.Concrete data are shown in Table 3.
Table 3
| Material number | 4 | 6 | 24 | 26 | 5 | 15 | 25 | 7 |
| Mass fraction % | ||||||||
| Hexane | 91.2 | 91.2 | 75.3 | 75.3 | 0.0 | 0.0 | 0.0 | 0.0 |
| Nonane | 8.1 | 8.1 | 23.3 | 23.3 | 0.0 | 0.0 | 0.0 | 0.0 |
| Isopropylbenzene | 0.4 | 0.4 | 1.0 | 1.0 | 0.0 | 0.0 | 0.0 | 0.0 |
| Cumyl hydroperoxide | 0.0 | 0.0 | 0.1 | 0.1 | 0.0 | 0.0 | 0.0 | 0.0 |
| Nitrogen | 0.1 | 0.1 | 0.1 | 0.1 | 0.0 | 0.0 | 0.0 | 0.0 |
| Water | 0.1 | 0.1 | 0.1 | 0.1 | 100.0 | 100.0 | 100.0 | 100.0 |
| Styrene oligomer | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 | 0.0 |
| Carbon nine | 0.1 | 0.1 | 0.1 | 0.1 | 0.0 | 0.0 | 0.0 | 0.0 |
| Add up to | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 | 100.0 |
[embodiment 4]
According to the condition described in embodiment 1 and step, simply production of propylene oxide scale becomes 200,000 tons/year, arranges 4 groups
Oxidation section.Oxidation reactor operation temperature 96 DEG C；Operation pressure is 0.22MPaG；Steam generator operation temperature 96 DEG C；
Operation pressure is 0.22MPaG；Cooler operation temperature 88 DEG C；Operation pressure is 0.22MPaG；Circulating pump operation temperature
96℃；Operation pressure is 0.22MPaG；Concentration tower operation temperature 70 C；Operation pressure is 0.0035MPa (a)；Concentration tower
Reboiler duty temperature 81 DEG C；Operation pressure is 0.042MPa (a)；By-product specification is 80.0 DEG C, the steaming of 0.04736MPa (a)
Vapour 16288 kgs/hour, it may be assumed that reduce process unit steam consumption 16288 kgs/hour；Reduce process unit to follow simultaneously
Ring cooling-water consumption 895.8 ton hour.Concrete data are shown in Table 4.
Table 4
[embodiment 5]
According to the condition described in embodiment 1 and step, oxidation reactor operation temperature 150 DEG C；Operation pressure is 0.8MPaG；
Steam generator operation temperature 150 DEG C；Operation pressure is 0.8MPaG；Cooler operation temperature 130 DEG C；Operation pressure is
0.8MPaG；Circulating pump operation temperature 150 DEG C；Operation pressure is 0.8MPaG；Concentration tower operation temperature 110 DEG C；Operation
Pressure is 0.008MPa (a)；Concentration tower reboiler duty temperature 120 DEG C；Operation pressure is 0.08MPa (a)；By-product specification is
80.0 DEG C, the steam 8144 kgs/hour of 0.04736MPa (a), it may be assumed that minimizing process unit steam consumption 8144 kilograms/little
Time；Reduce process unit circulating cooling water consumption 447.9 ton hour simultaneously.
[embodiment 6]
According to the condition described in embodiment 1 and step, oxidation reactor operation temperature 65 DEG C；Operation pressure is 0.1MPaG；
Steam generator operation temperature 65 DEG C；Operation pressure is 0.1MPaG；Cooler operation temperature 50 C；Operation pressure is
0.1MPaG；Circulating pump operation temperature 65 DEG C；Operation pressure is 0.1MPaG；Concentration tower operation temperature 55 DEG C；Operation pressure
Power is 0.001MPa (a)；Concentration tower reboiler duty temperature 58 DEG C；Operation pressure is 0.01MPa (a)；By-product specification is
50.0 DEG C, the steam 8282 kgs/hour of 0.01234MPa (a), it may be assumed that minimizing process unit steam consumption 8282 kilograms/little
Time；Reduce process unit circulating cooling water consumption 455.5 ton hour simultaneously.
[embodiment 7]
According to the condition described in embodiment 1 and step, oxidation reactor operation temperature 140 DEG C；Operation pressure is 0.6MPaG；
Steam generator operation temperature 140 DEG C；Operation pressure is 0.6MPaG；Cooler operation temperature 120 DEG C；Operation pressure is
0.6MPaG；Circulating pump operation temperature 140 DEG C；Operation pressure is 0.6MPaG；Concentration tower operation temperature 102 DEG C；Operation
Pressure is 0.0055MPa (a)；Concentration tower reboiler duty temperature 110 DEG C；Operation pressure is 0.065MPa (a)；By-product specification
It is 80.0 DEG C, the steam 8144 kgs/hour of 0.04736MPa (a), it may be assumed that minimizing process unit steam consumption 8144 kilograms/
Hour；Reduce process unit circulating cooling water consumption 447.9 ton hour simultaneously.
[embodiment 8]
According to the condition described in embodiment 1 and step, oxidation reactor operation temperature 130 DEG C；Operation pressure is 0.5MPaG；
Steam generator operation temperature 130 DEG C；Operation pressure is 0.5MPaG；Cooler operation temperature 110 DEG C；Operation pressure is
0.5MPaG；Circulating pump operation temperature 130 DEG C；Operation pressure is 0.5MPaG；Concentration tower operation temperature 95 DEG C；Operation pressure
Power is 0.0045MPa (a)；Concentration tower reboiler duty temperature 105 DEG C；Operation pressure is 0.055MPa (a)；By-product specification is
80.0 DEG C, the steam 8144 kgs/hour of 0.04736MPa (a), it may be assumed that minimizing process unit steam consumption 8144 kilograms/little
Time；Reduce process unit circulating cooling water consumption 447.9 ton hour simultaneously.
Claims (6)
1. a method for propylene oxide unit oxidation unit byproduct steam, including least one set oxidation section, concentration tower,
Often group oxidation section includes oxidation reactor, steam generator, cooler；Raw material including isopropylbenzene enters oxygen
Changing reactor and air reaction, next group oxidation section delivered to by a part of material of still liquid at the bottom of oxidation reactor tower
Oxidation reactor continues reaction, and it is anti-that another part material is back to oxidation successively after steam generator, cooler
Answer device；A part of material of still liquid at the bottom of oxidation reactor tower in last group oxidation section is sent into concentration tower and is carried out
Material concentration；Wherein, the steam of the steam generator generation often organizing oxidation section delivers to concentration tower again as thermal source
Boiling device；
Wherein, still liquid at the bottom of described oxidation reactor tower is by carrying after circulating pump supercharging；
Wherein, described oxidation reactor operation temperature is 0～150 DEG C, and operation pressure is 0.0～0.8MpaG；Steam
Vapour generator operation temperature is 0～150 DEG C, and operation pressure is 0.0～0.8MPaG；Cooler operation temperature
Being 0～130 DEG C, operation pressure is 0.0～0.8MPaG；Circulating pump operation temperature is 0～150 DEG C, operation
Pressure is 0.0～0.8MPaG；Concentration tower operation temperature be 0～110 DEG C, operation pressure be 0.0～
0.008MPa(a)；Concentration tower reboiler duty temperature is 0～120 DEG C, operation pressure be 0.0～
0.08MPa(a)。
The method of propylene oxide unit oxidation unit byproduct steam the most according to claim 1, it is characterised in that described
The heat transferring medium of steam generator be boiler feedwater, the heat transferring medium of cooler is that recirculated water supplies water.
The method of propylene oxide unit oxidation unit byproduct steam the most according to claim 1, it is characterised in that described
Often group oxidation section internal oxidition reactor, steam generator, cooler connection flow process identical.
The method of propylene oxide unit oxidation unit byproduct steam the most according to claim 1, it is characterised in that described
Propylene oxide unit oxidation unit includes 1～5 group of oxidation section.
The method of propylene oxide unit oxidation unit byproduct steam the most according to claim 1, it is characterised in that described
Oxidation reactor operation temperature is 30～130 DEG C, and operation pressure is 0.0～0.6MPaG；Steam generator is grasped
Being 30～130 DEG C as temperature, operation pressure is 0.0～0.6MPaG；Cooler operation temperature be 30～
120 DEG C, operation pressure is 0.0～0.6MPaG；Circulating pump operation temperature is 30～130 DEG C, operates pressure
It is 0.0～0.6MPaG；Concentration tower operation temperature be 25～100 DEG C, operation pressure be 0.0～
0.006MPa(a)；Concentration tower reboiler duty temperature is 20～100 DEG C, operation pressure be 0.0～
0.06MPa(a)。
The method of propylene oxide unit oxidation unit byproduct steam the most according to claim 5, it is characterised in that described
Oxidation reactor operation temperature is for for 50～110 DEG C, and operation pressure is 0.0～0.4MPaG；Steam generator
Operation temperature is 50～110 DEG C, and operation pressure is 0.0～0.4MPaG；Cooler operation temperature be 50～
105 DEG C, operation pressure is 0.0～0.4MPaG；Circulating pump operation temperature is 50～110 DEG C, operates pressure
It is 0.0～0.4MPaG；Concentration tower operation temperature be 40～90 DEG C, operation pressure be 0.0～
0.004MPa(a)；Concentration tower reboiler duty temperature is 30～90 DEG C, operation pressure be 0.0～
0.04MPa(a)。
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