CN104447629A - Method for by-producing steam from oxidation unit of epoxypropane device - Google Patents
Method for by-producing steam from oxidation unit of epoxypropane device Download PDFInfo
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- CN104447629A CN104447629A CN201410719640.8A CN201410719640A CN104447629A CN 104447629 A CN104447629 A CN 104447629A CN 201410719640 A CN201410719640 A CN 201410719640A CN 104447629 A CN104447629 A CN 104447629A
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- C—CHEMISTRY; METALLURGY
- 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
The invention relates to a method for by-producing steam from an oxidation unit of an epoxypropane device, and the method is used for mainly solving the problem that in the prior art the energy consumption is relatively high. In order to better solve the problem, the technical scheme adopted by the invention is as follows: at least a group of oxidation stations and a concentration tower are adopted, each group of the oxidation stations comprises an oxidation reactor, a steam generator and a cooler, the method comprises the following steps: feeding a raw material isopropylbenzene into the oxidation reactors to react with air, conveying a part of the tower bottom residues of the oxidation reactors to oxidation reactors of a next group of the oxidation station to react continuously, passing another part of the tower bottom residues through the steam generators and the coolers to flow back to the oxidation reactors, and conveying a part of the tower bottom residues of a final group of the oxidation stations into the concentration tower to concentrate, wherein the steam of the steam generator of each group of the oxidation stations is used as a heat source and is conveyed to a reboiler of the concentration tower. The method can be used in production of epoxypropane.
Description
Technical field
The present invention relates to a kind of method of propylene oxide unit oxidation unit byproduct steam.
Background technology
Propylene oxide is one of important intermediate of petrochemicals, prepares urethane plastic in a large number for the production of polyether glycol, and produces unsaturated polyester and tensio-active agent etc.The production technology of current propylene oxide mainly contains: chlorohydrination, propylene oxide/vinylbenzene coproduction, propylene oxide/indirect oxidation method and hydrogen peroxide Direct Epoxidation method such as trimethyl carbinol coproduction, hydrogen phosphide cumene oxidation.
CN201210429266.9 and CN 201110294224.4 relates to the method for producing propylene oxide, describe the processing method that cumene method produces propylene oxide, first the method is obtain hydrogen phosphide cumene CHP by cumene oxidation, then hydrogen phosphide cumene and propylene initial ring oxidizing reaction is generated propylene oxide PO.The technique unit that wherein cumene oxidation obtains hydrogen phosphide cumene is called oxidation unit.CN01806930.4 relates to the preparation method of propylene oxide, and the oxidation operation in the method is under the high temperature conditions, obtains hydrogen phosphide cumene by air or oxygen-containing gas autoxidation isopropyl benzene.CN201120437887.2 relates to the isopropyl benzene continuous oxidation system that heat is moved in a kind of outside, and its oxidation unit comprises oxidizing tower, oxidation outer circulation water cooler and recycle pump.Oxidation unit realizes the circulation of oxidizing tower material by recycle pump, and circulation fluid is with oxidizing reaction Heat of Formation to return oxidizing tower tower top after interchanger cooling is removed.This oxidizing tower high-temperature material adopts circulating cooling water cooling, and waste heat is not recycled, and there is propylene oxide process Energy harvesting unreasonable, the problems such as energy consumption is higher.
All there is the higher problem of energy consumption in prior art, 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 new propylene oxide unit oxidation unit byproduct steam.The method is used for, in the production of propylene oxide, 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 of propylene oxide unit oxidation unit byproduct steam, comprises at least one group of oxidation section, concentration tower, often organizes oxidation section and comprises oxidation reactor, vapour generator, water cooler; The raw material comprising isopropyl benzene enters oxidation reactor and air reaction, the oxidation reactor that next group oxidation section delivered to by a part of material of still liquid at the bottom of oxidation reactor tower continues reaction, and another part material is back to oxidation reactor successively after vapour generator, water 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 concentrate; Wherein, the steam that the vapour generator often organizing oxidation section produces delivers to concentration tower reboiler as thermal source.
In technique scheme, preferably, the heat transferring medium of described vapour generator is oiler feed, and the heat transferring medium of water cooler is that recirculated water supplies water.
In technique scheme, preferably, the connection flow process of described often group oxidation section internal oxidition reactor, vapour generator, water cooler is identical.
In technique scheme, preferably, described propylene oxide unit oxidation unit comprises 1 ~ 5 group of oxidation section.
In technique scheme, preferably, still liquid at the bottom of described oxidation reactor tower is by carrying after recycle pump supercharging.
In technique scheme, preferably, described oxidation reactor service temperature is 0 ~ 150 DEG C, and working pressure is 0.0 ~ 0.8MpaG; Vapour generator service temperature is 0 ~ 150 DEG C, and working pressure is 0.0 ~ 0.8MPaG; Water cooler service temperature is 0 ~ 130 DEG C, and working pressure is 0.0 ~ 0.8MPaG; Recycle pump service temperature is 0 ~ 150 DEG C, and working pressure is 0.0 ~ 0.8MPaG; Concentration tower service temperature is 0 ~ 110 DEG C, and working pressure is 0.0 ~ 0.008MPa (a); Concentration tower reboiler duty temperature is 0 ~ 120 DEG C, and working pressure is 0.0 ~ 0.08MPa (a).
In technique scheme, more preferably, described oxidation reactor service temperature is 30 ~ 130 DEG C, and working pressure is 0.0 ~ 0.6MPaG; Vapour generator service temperature is 30 ~ 130 DEG C, and working pressure is 0.0 ~ 0.6MPaG; Water cooler service temperature is 30 ~ 120 DEG C, and working pressure is 0.0 ~ 0.6MPaG; Recycle pump service temperature is 30 ~ 130 DEG C, and working pressure is 0.0 ~ 0.6MPaG; Concentration tower service temperature is 25 ~ 100 DEG C, and working pressure is 0.0 ~ 0.006MPa (a); Concentration tower reboiler duty temperature is 20 ~ 100 DEG C, and working pressure is 0.0 ~ 0.06MPa (a).
In technique scheme, most preferably, described oxidation reactor service temperature is for being 50 ~ 110 DEG C, and working pressure is 0.0 ~ 0.4MPaG; Vapour generator service temperature is 50 ~ 110 DEG C, and working pressure is 0.0 ~ 0.4MPaG; Water cooler service temperature is 50 ~ 105 DEG C, and working pressure is 0.0 ~ 0.4MPaG; Recycle pump service temperature is 50 ~ 110 DEG C, and working pressure is 0.0 ~ 0.4MPaG; Concentration tower service temperature is 40 ~ 90 DEG C, and working pressure is 0.0 ~ 0.004MPa (a); Concentration tower reboiler duty temperature is 30 ~ 90 DEG C, and working 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 Heat of Formation, for concentration tower reboiler thermal source, reduces propylene oxide unit steam consumption 651.5 kgs/tonne of products; Remove partial oxidation reaction Heat of Formation owing to there is steam simultaneously, also reduce circulating cooling water consumption 35.83 tons of/ton of products of propylene oxide unit, achieve good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention.
In Fig. 1,1 is isopropyl benzene raw material; 2,12,22 is air material; 3,13,23 is corresponding oxidation reactor kettle material; 4,14,24 is backflow material; 5,15,25 is low-pressure steam material; 6,16,26 oxidation section material is organized for corresponding oxidation reactor kettle material enters next; 7 is the low-pressure steam feeding line of concentration tower reboiler;
201,202,203 is oxidation reactor; 301,302,303 is recycle pump; 401,402,403 is water cooler; 501,502,503 is vapour generator; 600 is concentration tower reboiler; 700 is concentration tower;
LS is low-pressure steam; DW is oiler feed; CWS is that recirculated water supplies water; CWR is recirculated water backwater.
In flow process as shown in Figure 1, for 3 groups of oxidation sections, isopropyl benzene raw material 1 is delivered in oxidation reactor 201, mixes with air material 2, oxidizing reaction occurs, Hydrogen Peroxide isopropyl benzene.A part for oxidation reactor 201 kettle material 3 is through recycle pump 301 circular flow, and circulation fluid cools through vapour generator 501 and water cooler 401, and cooled material 4 is back in oxidation reactor 201 and continues reaction.Oiler feed DW enters vapour generator 501, produces low-pressure steam LS material 5.Recirculated water water supply CWS enters after residue reaction heat removed by water cooler 401 to be become recirculated water backwater CWR and returns.Another part material of mixture 3, after recycle pump 301 supercharging, send oxidation reactor 202 as material 6.
Material 6 mixes at oxidation reactor 202 with air material 12, and oxidizing reaction Hydrogen Peroxide isopropyl benzene occurs.Oxidation reactor 202 kettle material 13 part is through recycle pump 302 circular flow, and circulation fluid is after vapour generator 502 and water cooler 402 cool, and material 14 is back in oxidation reactor 202 and continues reaction.Oiler feed DW enters vapour generator 502, produces low-pressure steam LS material 15.Recirculated water water supply CWS enters after residue reaction heat removed by water cooler 402 to be become recirculated water backwater CWR and returns.Another part material 16 that oxidation reactor 202 exports, after recycle pump 302 supercharging, send oxidation reactor 203.
Material 16 mixes at oxidation reactor 203 with air material 22, and the further Hydrogen Peroxide isopropyl benzene of oxidizing reaction occurs.Oxidation reactor 203 kettle material 23 part is through recycle pump 303 circular flow, and circulation fluid is after vapour generator 503 and water cooler 403 cool, and material 24 is back in oxidation reactor 203 and continues reaction.Oiler feed DW enters vapour generator 503, produces low-pressure steam LS material 25.Recirculated water water supply CWS enters after residue reaction heat removed by water cooler 403 to be become recirculated water backwater CWR and returns.Another part material 26 that oxidation reactor 203 exports, after recycle pump 303 supercharging, is delivered to concentration tower 700 and is carried out material concentrate.Low-pressure steam LS material 5,15,25 merges into material 7 as concentration tower reboiler 600 thermal source, needed for the heat meeting concentration tower reboiler 600.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
Production of propylene oxide scale is 100,000 tons/year, arranges 2 groups of oxidation sections.Oxidation reactor service temperature 105 DEG C; Working pressure is 0.25MPaG; Vapour generator service temperature 105 DEG C; Working pressure is 0.25MPaG; Water cooler service temperature 97 DEG C; Working pressure is 0.25MPaG; Recycle pump service temperature 105 DEG C; Working pressure is 0.25MPaG; Concentration tower service temperature 70 DEG C; Working pressure is 0.0035MPa (a); Concentration tower reboiler duty temperature 81 DEG C; Working pressure is 0.042MPa (a); By-product specification is 80.0 DEG C, the steam 8144 kgs/hour of 0.04736MPa (a), that is: reduce process unit steam consumption 8144 kgs/hour; Reduce process unit circulating cooling water consumption 447.9 tons/hour simultaneously.Concrete data are 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 |
| Isopropyl benzene | 0.4 | 0.4 | 1.0 | 1.0 | 0.0 | 0.0 | 0.0 | 0.0 |
| Hydrogen phosphide cumene | 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, just production of propylene oxide scale becomes 150,000 tons/year, arranges 3 groups of oxidation sections.Oxidation reactor service temperature 105 DEG C; Working pressure is 0.25MPaG; Vapour generator service temperature 105 DEG C; Working pressure is 0.25MPaG; Water cooler service temperature 97 DEG C; Working pressure is 0.25MPaG; Recycle pump service temperature 105 DEG C; Working pressure is 0.25MPaG; Concentration tower service temperature 70 DEG C; Working pressure is 0.0035MPa (a); Concentration tower reboiler duty temperature 81 DEG C; Working pressure is 0.042MPa (a); By-product specification is 80.0 DEG C, the steam 12216 kgs/hour of 0.04736MPa (a), that is: reduce process unit steam consumption 12216 kgs/hour; Reduce process unit circulating cooling water consumption 671.9 tons/hour simultaneously.Concrete data are 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 |
| Isopropyl benzene | 0.4 | 0.4 | 0.7 | 0.7 | 1.0 | 1.0 | 0.0 | 0.0 | 0.0 | 0.0 |
| Hydrogen phosphide cumene | 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 sections.Oxidation reactor service temperature 96 DEG C; Working pressure is 0.22MPaG; Vapour generator service temperature 96 DEG C; Working pressure is 0.22MPaG; Water cooler service temperature 88 DEG C; Working pressure is 0.22MPaG; Recycle pump service temperature 96 DEG C; Working pressure is 0.22MPaG; Concentration tower service temperature 70 DEG C; Working pressure is 0.0035MPa (a); Concentration tower reboiler duty temperature 81 DEG C; Working pressure is 0.042MPa (a); By-product specification is 80.0 DEG C, the steam 8144 kgs/hour of 0.04736MPa (a), that is: reduce process unit steam consumption 8144 kgs/hour; Reduce process unit circulating cooling water consumption 447.9 tons/hour simultaneously.Concrete data are 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 |
| Isopropyl benzene | 0.4 | 0.4 | 1.0 | 1.0 | 0.0 | 0.0 | 0.0 | 0.0 |
| Hydrogen phosphide cumene | 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, just production of propylene oxide scale becomes 200,000 tons/year, arranges 4 groups of oxidation sections.Oxidation reactor service temperature 96 DEG C; Working pressure is 0.22MPaG; Vapour generator service temperature 96 DEG C; Working pressure is 0.22MPaG; Water cooler service temperature 88 DEG C; Working pressure is 0.22MPaG; Recycle pump service temperature 96 DEG C; Working pressure is 0.22MPaG; Concentration tower service temperature 70 DEG C; Working pressure is 0.0035MPa (a); Concentration tower reboiler duty temperature 81 DEG C; Working pressure is 0.042MPa (a); By-product specification is 80.0 DEG C, the steam 16288 kgs/hour of 0.04736MPa (a), that is: reduce process unit steam consumption 16288 kgs/hour; Reduce process unit circulating cooling water consumption 895.8 tons/hour simultaneously.Concrete data are in table 4.
Table 4
[embodiment 5]
According to the condition described in embodiment 1 and step, oxidation reactor service temperature 150 DEG C; Working pressure is 0.8MPaG; Vapour generator service temperature 150 DEG C; Working pressure is 0.8MPaG; Water cooler service temperature 130 DEG C; Working pressure is 0.8MPaG; Recycle pump service temperature 150 DEG C; Working pressure is 0.8MPaG; Concentration tower service temperature 110 DEG C; Working pressure is 0.008MPa (a); Concentration tower reboiler duty temperature 120 DEG C; Working pressure is 0.08MPa (a); By-product specification is 80.0 DEG C, the steam 8144 kgs/hour of 0.04736MPa (a), that is: reduce process unit steam consumption 8144 kgs/hour; Reduce process unit circulating cooling water consumption 447.9 tons/hour simultaneously.
[embodiment 6]
According to the condition described in embodiment 1 and step, oxidation reactor service temperature 65 DEG C; Working pressure is 0.1MPaG; Vapour generator service temperature 65 DEG C; Working pressure is 0.1MPaG; Water cooler service temperature 50 DEG C; Working pressure is 0.1MPaG; Recycle pump service temperature 65 DEG C; Working pressure is 0.1MPaG; Concentration tower service temperature 55 DEG C; Working pressure is 0.001MPa (a); Concentration tower reboiler duty temperature 58 DEG C; Working pressure is 0.01MPa (a); By-product specification is 50.0 DEG C, the steam 8282 kgs/hour of 0.01234MPa (a), that is: reduce process unit steam consumption 8282 kgs/hour; Reduce process unit circulating cooling water consumption 455.5 tons/hour simultaneously.
[embodiment 7]
According to the condition described in embodiment 1 and step, oxidation reactor service temperature 140 DEG C; Working pressure is 0.6MPaG; Vapour generator service temperature 140 DEG C; Working pressure is 0.6MPaG; Water cooler service temperature 120 DEG C; Working pressure is 0.6MPaG; Recycle pump service temperature 140 DEG C; Working pressure is 0.6MPaG; Concentration tower service temperature 102 DEG C; Working pressure is 0.0055MPa (a); Concentration tower reboiler duty temperature 110 DEG C; Working pressure is 0.065MPa (a); By-product specification is 80.0 DEG C, the steam 8144 kgs/hour of 0.04736MPa (a), that is: reduce process unit steam consumption 8144 kgs/hour; Reduce process unit circulating cooling water consumption 447.9 tons/hour simultaneously.
[embodiment 8]
According to the condition described in embodiment 1 and step, oxidation reactor service temperature 130 DEG C; Working pressure is 0.5MPaG; Vapour generator service temperature 130 DEG C; Working pressure is 0.5MPaG; Water cooler service temperature 110 DEG C; Working pressure is 0.5MPaG; Recycle pump service temperature 130 DEG C; Working pressure is 0.5MPaG; Concentration tower service temperature 95 DEG C; Working pressure is 0.0045MPa (a); Concentration tower reboiler duty temperature 105 DEG C; Working pressure is 0.055MPa (a); By-product specification is 80.0 DEG C, the steam 8144 kgs/hour of 0.04736MPa (a), that is: reduce process unit steam consumption 8144 kgs/hour; Reduce process unit circulating cooling water consumption 447.9 tons/hour simultaneously.
Claims (8)
1. a method for propylene oxide unit oxidation unit byproduct steam, comprises at least one group of oxidation section, concentration tower, often organizes oxidation section and comprises oxidation reactor, vapour generator, water cooler; The raw material comprising isopropyl benzene enters oxidation reactor and air reaction, the oxidation reactor that next group oxidation section delivered to by a part of material of still liquid at the bottom of oxidation reactor tower continues reaction, and another part material is back to oxidation reactor successively after vapour generator, water 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 concentrate; Wherein, the steam that the vapour generator often organizing oxidation section produces delivers to concentration tower reboiler as thermal source.
2. the method for propylene oxide unit oxidation unit byproduct steam according to claim 1, is characterized in that the heat transferring medium of described vapour generator is oiler feed, and the heat transferring medium of water cooler is that recirculated water supplies water.
3. the method for propylene oxide unit oxidation unit byproduct steam according to claim 1, it is characterized in that described often organize oxidation section internal oxidition reactor, vapour generator, water cooler connection flow process identical.
4. the method for propylene oxide unit oxidation unit byproduct steam according to claim 1, is characterized in that described propylene oxide unit oxidation unit comprises 1 ~ 5 group of oxidation section.
5. the method for propylene oxide unit oxidation unit byproduct steam according to claim 1, is characterized in that at the bottom of described oxidation reactor tower, still liquid is by carrying after recycle pump supercharging.
6. the method for propylene oxide unit oxidation unit byproduct steam according to claim 1,5, it is characterized in that described oxidation reactor service temperature is 0 ~ 150 DEG C, working pressure is 0.0 ~ 0.8MpaG; Vapour generator service temperature is 0 ~ 150 DEG C, and working pressure is 0.0 ~ 0.8MPaG; Water cooler service temperature is 0 ~ 130 DEG C, and working pressure is 0.0 ~ 0.8MPaG; Recycle pump service temperature is 0 ~ 150 DEG C, and working pressure is 0.0 ~ 0.8MPaG; Concentration tower service temperature is 0 ~ 110 DEG C, and working pressure is 0.0 ~ 0.008MPa (a); Concentration tower reboiler duty temperature is 0 ~ 120 DEG C, and working pressure is 0.0 ~ 0.08MPa (a).
7. the method for propylene oxide unit oxidation unit byproduct steam according to claim 6, it is characterized in that described oxidation reactor service temperature is 30 ~ 130 DEG C, working pressure is 0.0 ~ 0.6MPaG; Vapour generator service temperature is 30 ~ 130 DEG C, and working pressure is 0.0 ~ 0.6MPaG; Water cooler service temperature is 30 ~ 120 DEG C, and working pressure is 0.0 ~ 0.6MPaG; Recycle pump service temperature is 30 ~ 130 DEG C, and working pressure is 0.0 ~ 0.6MPaG; Concentration tower service temperature is 25 ~ 100 DEG C, and working pressure is 0.0 ~ 0.006MPa (a); Concentration tower reboiler duty temperature is 20 ~ 100 DEG C, and working pressure is 0.0 ~ 0.06MPa (a).
8. the method for propylene oxide unit oxidation unit byproduct steam according to claim 7, it is characterized in that described oxidation reactor service temperature is for being 50 ~ 110 DEG C, working pressure is 0.0 ~ 0.4MPaG; Vapour generator service temperature is 50 ~ 110 DEG C, and working pressure is 0.0 ~ 0.4MPaG; Water cooler service temperature is 50 ~ 105 DEG C, and working pressure is 0.0 ~ 0.4MPaG; Recycle pump service temperature is 50 ~ 110 DEG C, and working pressure is 0.0 ~ 0.4MPaG; Concentration tower service temperature is 40 ~ 90 DEG C, and working pressure is 0.0 ~ 0.004MPa (a); Concentration tower reboiler duty temperature is 30 ~ 90 DEG C, and working pressure is 0.0 ~ 0.04MPa (a).
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| CN104447629B (en) | 2017-01-04 |
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