CN104402843B - The method reducing propylene oxide unit oxidation unit energy consumption - Google Patents
The method reducing propylene oxide unit oxidation unit energy consumption Download PDFInfo
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- CN104402843B CN104402843B CN201410719647.XA CN201410719647A CN104402843B CN 104402843 B CN104402843 B CN 104402843B CN 201410719647 A CN201410719647 A CN 201410719647A CN 104402843 B CN104402843 B CN 104402843B
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- oxidizing tower
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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 present invention relates to a kind of method reducing propylene oxide unit oxidation unit energy consumption, mainly solve the problem that in prior art, energy consumption is higher.The present invention is by using a kind of method reducing propylene oxide unit oxidation unit energy consumption, raw material including isopropylbenzene enters oxidizing tower and air contact generation oxidation reaction, generate the logistics including cumyl hydroperoxide, directly being returned at the bottom of oxidizing tower by pipeloop after the cooled device of a part of the liquid phase stream of oxidation tower top, another part enters next stage oxidizing tower or enters next workshop section；Wherein, described pipeloop is not provided with circulating pump, and is dependent on the technical scheme that gas-liquid two-phase logistics and the density contrast of liquid phase stream in pipeloop realize Natural Circulation in oxidizing tower and preferably solves the problems referred to above, can be used in production of propylene oxide.
Description
Technical field
The present invention relates to a kind of method reducing propylene oxide unit oxidation unit energy consumption.
Background technology
Expoxy propane is one of important intermediate of petrochemicals, is largely used to produce PPG 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.
CN20120429266.9 relates to the method for a kind of isopropylbenzene catalysis oxidative synthesis isopropyl benzene hydroperoxide, and the method is by different
Propyl benzene and solid catalyst join in reactor and mix, and are heated to 80～90 DEG C and react 8～10h with oxidant and prepare peroxide
Change hydrogen isopropylbenzene.
CN201120437887.2 relates to a kind of outside isopropylbenzene continuous oxidation system moving heat, and its oxidation unit includes oxidation
Tower, oxidation outer circulation cooler and circulating pump, after isopropylbenzene reacts with the compressed air blasted in tower, by circulation pumping
Inhale, and be back to tower top after cooling and complete the circulation of material.This patented technology can prepare hydrogen peroxide isopropyl by industrially scalable
Benzene, is realized the tower outer circulation of oxidizing tower material, is removed by oxidation reaction heat outside oxidizing tower by circulating pump.Outside oxidizing tower tower
Cyclic process use electrodynamic pump supercharging to realize, circulating pump needs power consumption, underuse compressed-air actuated kinetic energy, deposit
In the problem that cyclic process energy consumption is higher.
The present invention solves this problem targetedly.
Summary of the invention
The technical problem to be solved is the problem that in prior art, energy consumption is higher, it is provided that a kind of new reduction epoxy third
The method of alkane device oxidation unit energy consumption.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 reduction propylene oxide unit oxidation unit energy consumption
Method, the raw material including isopropylbenzene enters oxidizing tower and air contact generation oxidation reaction, generates and include hydrogen peroxide isopropyl
The logistics of benzene, is directly returned at the bottom of oxidizing tower, separately by pipeloop after the cooled device of a part of the liquid phase stream of oxidation tower top
It is partly into next stage oxidizing tower or enters next workshop section；Wherein, described pipeloop is not provided with circulating pump, but
In relying on oxidizing tower, gas-liquid two-phase logistics realizes Natural Circulation with the density contrast of liquid phase stream in pipeloop.
In technique scheme, it is preferable that described oxidizing tower operation temperature is 0～150 DEG C, and operation pressure is 0.0～0.8MPaG；
Cooler operation temperature is 0～150 DEG C, and operation pressure is 0.0～0.8MPaG.
In technique scheme, it is highly preferred that described oxidizing tower operation temperature be 50～110 DEG C, operation pressure for for
0.0～0.4MPaG；Cooler operation temperature is 50～110 DEG C, and operation pressure is 0.0～0.4MPaG.
In technique scheme, it is preferable that gas-liquid two-phase logistics and the density of liquid phase stream in pipeloop in described oxidizing tower
Difference is more than 6.9.
In technique scheme, it is preferable that described oxidation unit oxidizing tower is provided with three, and each oxidizing tower is provided with pipeloop
And cooler, the overhead stream of last oxidizing tower be partly into next workshop section.
In technique scheme, it is preferable that the 50 of the liquid phase stream of described oxidation tower top～90% after cooled device by circulation
Pipeline directly returns at the bottom of oxidizing tower.
The present invention utilize 0.66MPaG compressed air raw material that oxidizing tower inputs as kinetic energy, with thermal siphon as principle, it is achieved
Oxidizing tower outer circulation liquid Natural Circulation, reduces device power consumption 6.36～7.26 kilowatt hours/ton product, and compressed air consumption still keeps
Constant, its consumption is 3.00～3.26 ton/ton products, achieves preferable technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention.
1 is isopropylbenzene raw material；2 is compressed air；3 is oxidation tower top liquid phase stream；4 is pipeloop；5 is circulation fluid；
6 enter the pipeline of next stage oxidizing tower for tower top liquid phase stream；7 is pneumatic manifold；8 is exhaust pipe；9 is compression
Air；10 is circulation fluid；11 is the pipeloop of second level oxidizing tower；12 enter for second level oxidation tower top liquid phase stream
The pipeline of next stage oxidizing tower；13 is compressed air；14 enter the pipeline of cooler for third level oxidation tower top liquid phase stream；
15 is the pipeloop of third level oxidizing tower；16 for entering the discharging pipeline of next workshop section；201,202,203 is oxidizing tower；
301,302,303 is cooler.
In flow process as shown in Figure 1, as a example by 3 oxidizing towers, isopropylbenzene raw material 1 is delivered in oxidizing tower 201, compression
One shunting 2 in air 7 is sent into bottom oxidizing tower 201 and is mixed with isopropylbenzene raw material 1, at certain temperature and pressure
Under, occur oxidation reaction, part to generate cumyl hydroperoxide 3 and tail gas 8, tail gas 8 is sent outside；Isopropylbenzene raw material 1 He
Compressed air 2 is mixed into two phase materials in oxidizing tower 201, and density is relatively low, and this material divides in oxidizing tower 201 top gas-liquid
Being liquid phase after device separates, density is relatively big, and one material 5 in the material 3 of gas-liquid separator overfall enters circulation pipe
Line, removes oxidation reaction heat in cooler 301, and the material after cooling returns oxidizing tower 201 through pipeloop 4 Natural Circulation
Bottom；Oxidizing tower 201 pushes up another strand of material 6 in liquid phase stream 3 and enters bottom next oxidizing tower 202.
The most unreacted isopropylbenzene raw material 6 continues reaction with compressed air 9 in oxidizing tower 202, utilizes density contrast, circulation
Oxidation reaction heat removed by the cooled device of liquid 10 302, and the material after cooling returns oxidizing tower 202 through pipeloop 11 Natural Circulation
Bottom, oxidizing tower 202 pushes up another strand of material 12 of liquid phase stream and enters bottom next oxidizing tower 203.
The most unreacted isopropylbenzene raw material 12 continues reaction with compressed air 13 in oxidizing tower 203, utilizes density contrast, follows
Oxidation reaction heat removed by the cooled device of ring liquid 303, and the material after cooling returns oxidizing tower 203 through pipeloop 15 Natural Circulation
Bottom, another strand of material that oxidizing tower 203 pushes up in liquid phase stream 14 enters next workshop section through pipeline 16.
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 oxidizing towers.Oxidizing tower 201 operates temperature 110 DEG C；Behaviour
It is 0.30MPaG as pressure；Cooler 301 operates temperature 110 DEG C；Operation pressure is 0.30MPaG；Oxidizing tower 202 is grasped
Make temperature 105 DEG C；Operation pressure is 0.20MPaG；Cooler 302 operates temperature 105 DEG C；Operation pressure is 0.20MPaG；
Circulation fluid pipeloop is not provided with circulating pump, relies on gas-liquid two-phase logistics and liquid phase stream in pipeloop in oxidizing tower
Density contrast realizes Natural Circulation.In described oxidizing tower, gas-liquid two-phase logistics is 7.5 with the density contrast of liquid phase stream in pipeloop.
Directly returned at the bottom of oxidizing tower by pipeloop after 70% cooled device of the liquid phase stream of oxidation tower top.Reduce power consumption 72.59
Ten thousand kilowatt hours/year.
[embodiment 2]
According to the condition described in embodiment 1 and step, production of propylene oxide scale becomes 150,000 tons/year, arranges 3 oxidations
Reactor.Oxidizing tower 201 operates temperature 110 DEG C；Operation pressure is 0.30MPaG；Cooler 301 operates temperature 110 DEG C；
Operation pressure is 0.30MPaG；Oxidizing tower 202 operates temperature 108 DEG C；Operation pressure is 0.25MPaG；Cooler 302
Operation temperature 108 DEG C；Operation pressure is 0.25MPaG；Oxidizing tower 203 operates temperature 105 DEG C；Operation pressure is
0.20MPaG；Cooler 303 operates temperature 105 DEG C；Operation pressure is 0.20MPaG；Gas-liquid two-phase in described oxidizing tower
Logistics is 7.5 with the density contrast of liquid phase stream in pipeloop.Pass through after 70% cooled device of the liquid phase stream of oxidation tower top
Pipeloop directly returns at the bottom of oxidizing tower.Reduce power consumption 109.04 ten thousand kilowatt hours/year.
[embodiment 3]
According to the condition described in embodiment 1 and step, production of propylene oxide scale is 100,000 tons/year, arranges 2 oxidations anti-
Answering device, simply operating condition changes.Oxidizing tower 201 operates temperature 120 DEG C；Operation pressure is 0.35MPaG；Cooler
301 operation temperature 120 DEG C；Operation pressure is 0.35MPaG；Oxidizing tower 202 operates temperature 105 DEG C；Operation pressure is
0.20MPaG；Cooler 302 operates temperature 105 DEG C；Operation pressure is 0.20MPaG；Gas-liquid two-phase in described oxidizing tower
Logistics is 8.8 with the density contrast of liquid phase stream in pipeloop.Pass through after 64% cooled device of the liquid phase stream of oxidation tower top
Pipeloop directly returns at the bottom of oxidizing tower.Reduce power consumption 73.72 ten thousand kilowatt hours/year.
[embodiment 4]
According to the condition described in embodiment 1 and step, production of propylene oxide scale becomes 200,000 tons/year, arranges 4 oxidations
Reactor.Oxidizing tower 201 operates temperature 120 DEG C；Operation pressure is 0.35MPaG；Cooler 301 operates temperature 120 DEG C；
Operation pressure is 0.35MPaG；Oxidizing tower 202 operates temperature 115 DEG C；Operation pressure is 0.31MPaG；Cooler 302
Operation temperature 115 DEG C；Operation pressure is 0.31MPaG；Oxidizing tower 203 operates temperature 110 DEG C；Operation pressure is
0.25MPaG；Cooler 303 operates temperature 110 DEG C；Operation pressure is 0.25MPaG；4th oxidizing tower operation temperature
105℃；Operation pressure is 0.20MPaG；4th cooler operation temperature 105 DEG C；Operation pressure is 0.20MPaG；
In described oxidizing tower, gas-liquid two-phase logistics is 8.8 with the density contrast of liquid phase stream in pipeloop.The liquid phase stream of oxidation tower top
64% cooled device after directly returned at the bottom of oxidizing tower by pipeloop.Reduce power consumption 147.44 ten thousand kilowatt hours/year.
[embodiment 5]
According to the condition described in embodiment 1 and step, production of propylene oxide scale becomes 200,000 tons/year, arranges 3 oxidations
Reactor.Oxidizing tower 201 operates temperature 150 DEG C；Operation pressure is 0.8MPaG；Cooler 301 operates temperature 150 DEG C；
Operation pressure is 0.8MPaG；Oxidizing tower 202 operates temperature 140 DEG C；Operation pressure is 0.7MPaG；Cooler 302 is grasped
Make temperature 140 DEG C；Operation pressure is 0.7MPaG；Oxidizing tower 203 operates temperature 130 DEG C；Operation pressure is 0.6MPaG；
Cooler 303 operates temperature 130 DEG C；Operation pressure is 0.6MPaG；Gas-liquid two-phase logistics and circulation pipe in described oxidizing tower
In line, the density contrast of liquid phase stream is 10.5.Pipeloop is passed through direct after 50% cooled device of the liquid phase stream of oxidation tower top
Return at the bottom of oxidizing tower.Reduce power consumption 151.41 ten thousand kilowatt hours/year.
[embodiment 6]
According to the condition described in embodiment 1 and step, production of propylene oxide scale becomes 200,000 tons/year, arranges 3 oxidations
Reactor.Oxidizing tower 201 operates temperature 70 C；Operation pressure is 0.2MPaG；Cooler 301 operates temperature 70 C；
Operation pressure is 0.2MPaG；Oxidizing tower 202 operates temperature 65 DEG C；Operation pressure is 0.15MPaG；Cooler 302 is grasped
Make temperature 65 DEG C；Operation pressure is 0.15MPaG；Oxidizing tower 203 operates temperature 60 C；Operation pressure is 0.1MPaG；
Cooler 303 operates temperature 60 C；Operation pressure is 0.1MPaG；Gas-liquid two-phase logistics and circulation pipe in described oxidizing tower
In line, the density contrast of liquid phase stream is 6.9.Pipeloop is passed through direct after 90% cooled device of the liquid phase stream of oxidation tower top
Return at the bottom of oxidizing tower.Reduce power consumption 142.17 ten thousand kilowatt hours/year.
[embodiment 7]
According to the condition described in embodiment 1 and step, production of propylene oxide scale becomes 200,000 tons/year, arranges 3 oxidations
Reactor.Oxidizing tower 201 operates temperature 135 DEG C；Operation pressure is 0.6MPaG；Cooler 301 operates temperature 135 DEG C；
Operation pressure is 0.6MPaG；Oxidizing tower 202 operates temperature 130 DEG C；Operation pressure is 0.5MPaG；Cooler 302 is grasped
Make temperature 130 DEG C；Operation pressure is 0.5MPaG；Oxidizing tower 203 operates temperature 120 DEG C；Operation pressure is 0.4MPaG；
Cooler 303 operates temperature 120 DEG C；Operation pressure is 0.4MPaG；Gas-liquid two-phase logistics and circulation pipe in described oxidizing tower
In line, the density contrast of liquid phase stream is 9.2.Pipeloop is passed through direct after 60% cooled device of the liquid phase stream of oxidation tower top
Return at the bottom of oxidizing tower.Reduce power consumption 150.16 ten thousand kilowatt hours/year.
Claims (5)
1. the method reducing propylene oxide unit oxidation unit energy consumption, the raw material including isopropylbenzene enters oxidizing tower
With air contact generation oxidation reaction, generate the logistics including cumyl hydroperoxide, the liquid phase thing of oxidation tower top
Directly being returned at the bottom of oxidizing tower by pipeloop after the cooled device of a part of stream, another part enters next stage oxygen
Change tower or enter next workshop section；Wherein, described pipeloop is not provided with circulating pump, and is dependent on oxidizing tower
Interior gas-liquid two-phase logistics realizes Natural Circulation, gas in described oxidizing tower with the density contrast of liquid phase stream in pipeloop
Liquid two-phase logistics and the density contrast of liquid phase stream in pipeloop are more than 6.9, with input in described oxidizing tower
0.66MPaG compressed air raw material is as kinetic energy.
The method reducing propylene oxide unit oxidation unit energy consumption the most according to claim 1, it is characterised in that institute
Stating oxidizing tower operation temperature is 0～150 DEG C, and operation pressure is 0.0～0.8MPaG；Cooler operation temperature is
0～150 DEG C, operation pressure is 0.0～0.8MPaG.
The method reducing propylene oxide unit oxidation unit energy consumption the most according to claim 2, it is characterised in that institute
Stating oxidizing tower operation temperature is 50～110 DEG C, and operation pressure is 0.0～0.4MPaG；Cooler operation temperature is
50～110 DEG C, operation pressure is 0.0～0.4MPaG.
The method reducing propylene oxide unit oxidation unit energy consumption the most according to claim 1, it is characterised in that institute
Stating oxidation unit oxidizing tower and be provided with three, each oxidizing tower is provided with pipeloop and cooler, last oxidation
The overhead stream of tower be partly into next workshop section.
The method reducing propylene oxide unit oxidation unit energy consumption the most according to claim 1, it is characterised in that institute
State 50～90% directly being returned at the bottom of oxidizing tower after cooled device of liquid phase stream of oxidation tower top by pipeloop.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040059162A1 (en) * | 2002-07-29 | 2004-03-25 | Dyckman Arkady Samuilovich | Method of producing cumene hydroperoxide |
| CN1873853A (en) * | 2006-06-13 | 2006-12-06 | 上海科宏变电设备有限公司 | Heat elimination of transformer by using separate type heat-pipes |
| 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 |
| CN202338891U (en) * | 2011-11-03 | 2012-07-18 | 中国石油天然气股份有限公司 | Natural circulation waste heat boiler |
| CN102911096A (en) * | 2012-10-31 | 2013-02-06 | 华南理工大学 | Method for synthetizing cumene hydroperoxide by catalytic oxidation of cumene |
| CN103030611A (en) * | 2011-09-30 | 2013-04-10 | 中国石油化工股份有限公司 | Method for production of propylene oxide |
-
2014
- 2014-12-01 CN CN201410719647.XA patent/CN104402843B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040059162A1 (en) * | 2002-07-29 | 2004-03-25 | Dyckman Arkady Samuilovich | Method of producing cumene hydroperoxide |
| CN1873853A (en) * | 2006-06-13 | 2006-12-06 | 上海科宏变电设备有限公司 | Heat elimination of transformer by using separate type heat-pipes |
| CN103030611A (en) * | 2011-09-30 | 2013-04-10 | 中国石油化工股份有限公司 | Method for production of propylene oxide |
| CN202338891U (en) * | 2011-11-03 | 2012-07-18 | 中国石油天然气股份有限公司 | Natural circulation waste heat boiler |
| 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 |
| CN102911096A (en) * | 2012-10-31 | 2013-02-06 | 华南理工大学 | Method for synthetizing cumene hydroperoxide by catalytic oxidation of cumene |
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