CN1807377A - Evaporation system for producing ethylene glycol - Google Patents
Evaporation system for producing ethylene glycol Download PDFInfo
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- CN1807377A CN1807377A CN 200510002284 CN200510002284A CN1807377A CN 1807377 A CN1807377 A CN 1807377A CN 200510002284 CN200510002284 CN 200510002284 CN 200510002284 A CN200510002284 A CN 200510002284A CN 1807377 A CN1807377 A CN 1807377A
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- evaporator
- reboiler
- ethylene glycol
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Abstract
The provided evaporation system for glycol production comprises: a multi-effect evaporator system in series with an evaporator and a reboiler, and a heat exchanger with low-pressure steam as heat source to replace the single-effect evaporation system taken much land and investment. This invention comes up to the standard for the water content and fit to apply in prior art.
Description
Technical field
The present invention relates to the vapo(u)rization system in a kind of Chemical Manufacture, say further, relate to produce the vapo(u)rization system in the ethylene glycol technology.
Background technology
Particularly at petrochemical industry, the evaporation flow process of chemical process is to adopt multiple-effect evaporation rationally to utilize to solve energy again in chemical production field.For example in the Production Flow Chart of existing ethylene glycol, vapo(u)rization system is made of multiple-effect evaporation (quadruple effect to six effect).In general, each is imitated evaporation and includes vaporizer and the reboiler composition that is connected with vaporizer.Such evaporator system is together in series and has just formed multiple-effect evaporation.
As shown in Figure 1: conventional evaporation flow process is to be composed in series by the sextuple-effect evaporator system: first single-effect evaporator is T1, and second single-effect evaporator is T2, and third effect evaporator is T3, and fourth evaporator is T4, and quintuple effect evaporator is T5, and sextuple-effect evaporator is T6.One effect is as follows to six pressure sequence of imitating.Reduce to 0.2～0.3MpaG that imitate at the end by a 1.2～1.4MPaG of imitating.
One steam of imitating reboiler E1 is to adopt the about 2.2MPaG of middle pressure steam, its lime set is collected among the lime set jar D1, two thermals source of imitating reboiler E2 are the steam that adopts the 1st effective evaporator top, its lime set is collected among the lime set jar D2, and the steam at each single-effect evaporator top is imitated the thermal source of reboiler to reclaim heat as next successively.Two effects, triple effect, quadruple effect, five are imitated, six lime sets of imitating reboiler are delivered to next effect lime set jar through vacuum flashing successively, finally collect six and imitate among the reboiler lime set jar D6.Be connected with dewatering system after the multiple-effect evaporator system.Finish evaporation, the dehydration of material thus, can rationally utilize each to imitate the steam that evaporates simultaneously.
The multiple-effect evaporator system is the critical process of producing qualified ethylene glycol product, but also is the bottleneck of device volume increase.Because when the ethylene glycol production equipment is extended, oxyethane hydrolysis reaction is also corresponding brings a large amount of water into to satisfy the requirement that throughput improves, bring the dehydration load of these two systems of multiple-effect evaporation and dewatering system to increase very big thus, and pressure gradient was very little between each was imitated at present, and the heat transfer temperature difference between each is imitated is corresponding also little.In order to address this problem, external general terms of settlement is to increase by one group or two groups of evaporator systems, removes the water yield that volume increase brings with this.But for the production equipment of some ethylene glycol, because the problem of place and cost increases very difficulty of evaporator system.
Summary of the invention
When the enlarging of ethylene glycol factory is transformed, owing to limit by conditions such as original device, place, can not increase evaporator system, it is a problem that is difficult to solve that the load that dewaters when solving factory's enlarging again increases.
At problems of the prior art, the purpose of this invention is to provide a kind of vapo(u)rization system, can rationally excavate the potentiality of original equipment, need not to increase again the multiple-effect evaporator system, finally make the product water content up to standard.
A kind of vapo(u)rization system that is used to produce ethylene glycol provided by the invention comprises placed in-line multiple-effect evaporator system.Each single-effect evaporator system comprises vaporizer and reboiler.Be connected with dewatering system after the described multiple-effect evaporator system.Vapo(u)rization system of the present invention also is in series with interchanger after the last evaporator system.Described interchanger is connected with dewatering system.
Interchanger between last evaporator system and dewatering system of the present invention mainly plays the effect to material heating revaporization here.Described interchanger is already present various forms of interchanger in the prior art, as long as can reach above-mentioned effect, and shell and tube heat exchanger etc. for example.General preferred horizontal heat exchanger.
Because the rich amount of the low-pressure steam of device is bigger, and price is low, and the middle pressure steam surplus of general device is very little, and price is expensive more a lot of than low pressure.So the thermal source of above-mentioned interchanger preferably uses low-pressure steam.The temperature of described low-pressure steam is 120～140 ℃.
The present invention uses the interchanger of a routine, plays the effect of revaporization, and it acts on alternative 1st effective evaporator of the prior art system.In ethylene glycol Production Flow Chart enlarging, by common way, need to increase two-effect evaporation device system, utilize vapo(u)rization system of the present invention, only need to add an interchanger than original increase 1st effective evaporator system; Needs increase the 1st effective evaporator system, only need can make the water content of product reach standard than interchanger of original increase.
Thus, vapo(u)rization system of the present invention compared with prior art has following outstanding feature.
A. process simplification, take up an area of less, conserve space, reduce investment outlay;
B. operation easily, the water-content of product ethylene glycol is up to standard always, has satisfactorily resolved the bottleneck of ethylene glycol volume increase.
Description of drawings
Accompanying drawing 1 is the schema of conventional vapo(u)rization system in the ethylene glycol production process.Among the figure:
T1, T2, T3, T4, T5-each single-effect evaporator
E1, E2, E3, E4, E5-respectively imitate reboiler
D1, D2, D3, D4, D5-respectively imitate condensate drum
T6, E6, D6---newly-increased 1st effective evaporator system
E6a-condenser
T7-dehydration tower
W-material.
Accompanying drawing 2 is the schema of vapo(u)rization system in the ethylene glycol production process of the present invention.Among the figure:
T1, T2, T3, T4, T5-each single-effect evaporator
E1, E2, E3, E4, E5-respectively imitate reboiler
D1, D2, D3, D4, D5-respectively imitate condensate drum
E5a-condenser
EF-newly-increased horizontal heat exchanger
The condensate drum of DF-horizontal heat exchanger
T7-dehydration tower
W-material.
Embodiment
Be that embodiment further describes the present invention with accompanying drawing 2 below.Scope of the present invention is not subjected to the restriction of embodiment, and scope of the present invention proposes in claims.
As shown in Figure 2: vapo(u)rization system of the present invention is by comprising that a quintuple effect evaporator system and a horizontal heat exchanger EF etc. are composed in series.Wherein horizontal heat exchanger adopts horizontal shell and tube heat exchanger; The first single-effect evaporator system comprises 1st effective evaporator T1, an effect reboiler E1 and a lime set jar D1; The second single-effect evaporator system comprises 2nd effect evaporator T2, two effect reboiler E2 and two effect lime set jar D2; The third effect evaporator system comprises triple-effect evaporator T3, triple effect reboiler E3 and triple effect lime set jar D3; The fourth evaporator system comprises quadruple effect evaporator T4, quadruple effect reboiler E4 and quadruple effect lime set jar D4; The quintuple effect evaporator system comprises quintuple effect evaporator T5, five effect reboiler E5 and five effect lime set jar D5.One imitate to the pressure sequence of quintuple effect evaporator as follows: reduce to the 0.2MpaG that imitate at the end by a 1.3MPaG of imitating.
One steam of imitating reboiler E1 is to adopt the about 2.2MPaG of middle pressure steam, and its lime set is collected among the lime set jar D1.The material that need evaporate enters among the 1st effective evaporator T1 and evaporates, and steam is discharged from the vaporizer top, and material is discharged from base of evaporator.Part material is imitated through one and is got back in the 1st effective evaporator after reboiler E1 heats once more, plays material and is heated effect.Rest materials enters revaporization among the 2nd effect evaporator T2, and two thermals source of imitating reboiler E2 are the steam that adopts 1st effective evaporator T1 top, and its lime set is collected in two and imitates among the lime set jar D2.The material that each single-effect evaporator is discharged enters the vaporizer of reboiler and next effect respectively again, carries out multiple-effect evaporation.The steam at each single-effect evaporator top is imitated the thermal source of reboiler to reclaim heat as next successively.The lime set of two effects, triple effect, quadruple effect, five effect reboilers is delivered to next effect lime set jar through vacuum flashing successively, finally collects five and imitates among the reboiler lime set jar D5.From the material that quintuple effect evaporator T5 discharges, a part is imitated through five and is got back among the quintuple effect evaporator T5 after reboiler E5 evaporates once more, and rest materials enters among the horizontal heat exchanger EF of the present invention, heats revaporization.The low-pressure steam that the thermal source of horizontal heat exchanger EF is about 120～140 ℃.The lime set of interchanger is sent into lime set jar DF, then with being pumped in the system other interchanger as thermal source.Through the material behind the described interchanger revaporization, with the water content unanimity of the material behind the sextuple-effect evaporation in the prior art, can reach fully and produce the water content requirement of going up material, the dewatering system that can import thereafter to be connected carries out next step dewatering process flow.
The interchanger of vapo(u)rization system utilization occupation of land of the present invention, less investment has been replaced and has been taken up an area of 1st effective evaporator system big, that investment is high, has also realized the effect that material moisture is up to standard simultaneously.Be well suited in existing ethylene glycol production enlarging, using.
Claims (3)
1. vapo(u)rization system that is used to produce ethylene glycol comprises placed in-line multiple-effect evaporator system, and each single-effect evaporator system comprises vaporizer and reboiler, it is characterized in that being in series with interchanger after the last evaporator system.
2. vapo(u)rization system according to claim 1 is characterized in that described interchanger is a horizontal heat exchanger, and thermal source uses low-pressure steam.
3. vapo(u)rization system according to claim 2 is characterized in that described low-pressure steam temperature is 120～140 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100022849A CN100343212C (en) | 2005-01-20 | 2005-01-20 | Evaporation system for producing ethylene glycol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100022849A CN100343212C (en) | 2005-01-20 | 2005-01-20 | Evaporation system for producing ethylene glycol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1807377A true CN1807377A (en) | 2006-07-26 |
| CN100343212C CN100343212C (en) | 2007-10-17 |
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ID=36839495
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005100022849A Expired - Fee Related CN100343212C (en) | 2005-01-20 | 2005-01-20 | Evaporation system for producing ethylene glycol |
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| Country | Link |
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| CN (1) | CN100343212C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108325227A (en) * | 2018-04-10 | 2018-07-27 | 上海优华系统集成技术股份有限公司 | A kind of system and its processing method to heat recovery and utilization in multi-effect evaporation system |
| CN109847394A (en) * | 2019-03-28 | 2019-06-07 | 湖北三宁化工股份有限公司 | A kind of system and method that ethylene glycol rectifier unit process waste recycles |
| CN113683484A (en) * | 2020-05-18 | 2021-11-23 | 北京诺维新材科技有限公司 | Method and device for distilling ethylene glycol aqueous solution |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3143734A1 (en) * | 1981-11-04 | 1983-05-11 | Hoechst Ag, 6230 Frankfurt | METHOD FOR THE CONTINUOUS RECTIFICATION OF AN ALCOHOL-CONTAINING LIQUID MIXTURE " |
| KR20000048902A (en) * | 1996-10-04 | 2000-07-25 | 그레이스 스티븐 에스. | A method for producing glycols |
-
2005
- 2005-01-20 CN CNB2005100022849A patent/CN100343212C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108325227A (en) * | 2018-04-10 | 2018-07-27 | 上海优华系统集成技术股份有限公司 | A kind of system and its processing method to heat recovery and utilization in multi-effect evaporation system |
| CN108325227B (en) * | 2018-04-10 | 2024-04-16 | 上海优华系统集成技术股份有限公司 | System for recycling heat in multi-effect evaporation system and treatment method thereof |
| CN109847394A (en) * | 2019-03-28 | 2019-06-07 | 湖北三宁化工股份有限公司 | A kind of system and method that ethylene glycol rectifier unit process waste recycles |
| CN113683484A (en) * | 2020-05-18 | 2021-11-23 | 北京诺维新材科技有限公司 | Method and device for distilling ethylene glycol aqueous solution |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100343212C (en) | 2007-10-17 |
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