CN1232500C - Method for recovering regeneration tower heat quantity - Google Patents
Method for recovering regeneration tower heat quantity Download PDFInfo
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- CN1232500C CN1232500C CN 200310109090 CN200310109090A CN1232500C CN 1232500 C CN1232500 C CN 1232500C CN 200310109090 CN200310109090 CN 200310109090 CN 200310109090 A CN200310109090 A CN 200310109090A CN 1232500 C CN1232500 C CN 1232500C
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Abstract
The present invention discloses a method for recovering heat of a regeneration tower for regenerating chemical absorption liquid. The present invention fully exerts the advantages of low rich fluid boiling point and high vaporization heat, and recovers heat energy by a parallel shunting mode. The present invention breaks through the traditional thinking mode in the existing 'equal heat capacity exchange' field, and the heat energy consumption keeps as low as possible in a regeneration process.
Description
Technical field
The present invention relates to a kind of chemical absorption liquid regenerated regenerator column heat recovery method that is applied to.
Background technology
It is technology commonly used in the Chemical Manufacture that the solution washing tower removes one or more components in the unstripped gas, and its scope of application is extensive, and solution is application capable of circulation after regenerating.For chemical absorption, rich solution must be heated to boiling point usually, thereby the component that just solution is absorbed desorbs and obtains regeneration, so regenerator column need consume more heat energy.
The steam latent heat that sensible heat that the regenerator column heat-energy losses is mainly taken out of by regeneration back high-temperature barren liquor at the bottom of the tower and cat head resurgent gases are taken out of is constituted.(Kohl A.L. and Riesenfeld F.C.GasPurification, thirded.P39), its rich solution that goes out the absorption tower only is used to reclaim out the sensible heat of regenerator column high-temperature barren liquor to traditional reclaiming process.This traditional reclaiming process, its shortcoming is: the temperature of the resurgent gases that exports from the regenerator column top is very high, carries a large amount of steam secretly, and its entrained heat is not done to reclaim and is lost to the external world, thereby causes the hear rate of regenerator column too high.In order to reduce the hear rate of regenerator column, a kind of polyphone reclaiming technology had once appearred, and the rich solution of self-absorption tower lower part outlet at first enters the resurgent gases interchanger, makes partial regeneration air cooling but, reclaims by the entrained part heat of resurgent gases.Rich solution temperature behind the recovery heat raises, and enters solution heat exchanger, reclaims by the entrained part heat of the hot lean solution of regenerator column lower part outlet.This polyphone reclaiming technology though reclaimed the latent heat of partial regeneration gas steam, rises because rich solution is gone into the temperature of solution heat exchanger, cause the effect of solution heat exchanger significantly to reduce, lean solution outlet sensible heat loss increases suddenly, and therefore, its energy-conservation whole structure is still undesirable.
Summary of the invention
The object of the invention is, proposes a kind of rich solution method that reclaims lean solution sensible heat and resurgent gases latent heat in parallel of utilizing, and makes the calorific loss of regeneration system rapidly reduce to minimum state.
Theoretical foundation of the present invention is that to utilize the boiling point of rich solution be low characteristic than lean solution, even if the rich solution amount is less, it is after temperature rises to boiling point in heat transfer process, because volatile components is partly vaporized in the rich solution, temperature can not significantly improve yet again, make it and hot lean solution generally keep 10～30 ℃ the temperature difference, therefore it is enough only to reclaim the sensible heat of lean solution with the part rich solution, just become possibility and extract the latent heat that the rest part rich solution reclaims resurgent gases out, so just can fully reclaim the sensible heat of hot lean solution and the latent heat of resurgent gases with enough heat transfer temperature difference impellents with method in parallel.
According to above-mentioned design, the contriver proposes the method for a kind of rich solution distributary recovery regeneration tower in parallel heat, it is characterized in that: the rich solution parallel connection of self-absorption tower lower part outlet is split into two-way, wherein one road rich solution enters solution heat exchanger, with the hot lean solution partition heat exchange of regenerator column bottom outlet, reclaim the sensible heat in the lean solution; Another road rich solution enters the resurgent gases interchanger, and with the hot resurgent gases partition heat exchange of regenerator column top outlet, the latent heat of reclaiming gas, the rich solution that leaves the rich solution of solution heat exchanger and leave the resurgent gases interchanger respectively or enter regenerator column regeneration after merging.
Above-mentioned said rich solution parallel connection splits into: the amount that enters the solution heat exchanger rich solution accounts for 30～90% of total rich solution weight, and surplus enters the resurgent gases interchanger; Preferred shunting mode in parallel is: the amount that enters the solution heat exchanger rich solution accounts for 50～80% of total rich solution weight, and surplus enters the resurgent gases interchanger.
Description of drawings
Fig. 1 is the schematic flow sheet of the said regenerator column heat recuperation of the present invention
Wherein: the 1-absorption tower; The 2-solution cooler; The 3-solution heat exchanger; The 4-regenerator column; 5-resurgent gases interchanger; 6-resurgent gases water cooler; The 7-reboiler.
Embodiment
Below in conjunction with accompanying drawing the present invention is set forth:
The rich solution of self-absorption tower 1 lower part outlet is divided into two-way.Wherein one road rich solution enters solution heat exchanger 3, with the hot lean solution partition heat exchange of regenerator column 4 bottom outlets, reclaims the sensible heat in the lean solution, and rich solution reaches its corresponding boiling point at last, and rich solution is partly vaporized, and temperature no longer obviously raises, thereby keeps certain driving force of heat transfer.Another road rich solution removes resurgent gases interchanger 5, hot resurgent gases partition heat exchange with the outlet of regenerator column top, the latent heat of main reclaiming gas, the rich solution temperature rise is until the boiling point that reaches under this pressure, this moment, rich solution was partly vaporized, temperature no longer obviously raises, and has kept enough drivings force of heat transfer, and heat transfer is steadily advanced.The rich solution that leaves solution heat exchanger 3 all is the gas-liquid two-phase state with the rich solution that leaves resurgent gases interchanger 5, can respectively or enter regenerator column 4 regeneration after merging.
The present invention gives full play to the low and higher advantage of vaporization heat of rich solution boiling point, adopt shunting mode in parallel to carry out energy recovery, broken through the traditional thinking mode of existing in this field " etc. thermal capacity exchange ", made the heat energy consumption of regenerative process be retained to low as much as possible.Usually, have many thermals source to be utilized, for example steam, hot charge gas, heat technologic gas, burning gas, hot exhaust gas or hot waste gas all can be used as thermal source of the present invention.
Be better understanding content of the present invention, the invention will be further described below by embodiment, but the cited case does not limit protection scope of the present invention:
Embodiment 1
Present embodiment has adopted rich solution shown in Figure 1 shunting in parallel flow process for Monoethanolamine MEA BASF solution reclaims carbon dioxide process in the stack gas.Unstripped gas is a stack gas, and the carbonic acid gas of intending reclaiming wherein is used for acetic acid production, flue tolerance 6000m
3/ h contains CO
210%, gas enters native system after desulfurization and dedusting cooling.Absorption agent is for containing the 15% Monoethanolamine MEA BASF aqueous solution, internal circulating load L=210m
3/ h.Rich solution by the absorption tower outlet at bottom is shunted, bypass flow: send solution heat exchanger 0.6L, send resurgent gases interchanger 0.4L.
Result of implementation is as follows:
Leave 60 ℃ of the lean solution temperature of solution heat exchanger
Leave 78 ℃ of the resurgent gases temperature of resurgent gases interchanger
Rich solution enters 91 ℃ of the temperature of regenerator column
Thermal source steam consumption (every 1000Nm
3CO
2) 2.6t
Adopt existing carbon dioxide recovery technology, the about 4.5t/1000Nm of its thermal source steam consumption
3CO
2, both compare, and the present invention has saved thermal source steam about 42.2%.
Present embodiment is that diethanolamine solution removes the sour gas in the ethylene raw material gas.Present embodiment has adopted Fig. 1 rich solution shunting in parallel flow process, remove carbonic acid gas and sulfide in the ethylene raw material gas with large-scale ethylene plant at home, absorption agent adopts diethanolamine, solution circulated amount L=35000kg/h, bypass flow: rich solution advances solution heat exchanger 0.75L, and rich solution advances resurgent gases interchanger 0.25L.Result of implementation is compared as follows:
| Before the enforcement | After the enforcement | |
| Lean solution is advanced the solution heat exchanger temperature | 110℃ | 110℃ |
| Lean solution goes out the solution heat exchanger temperature | 73℃ | 63℃ |
| Resurgent gases goes out the regenerator column temperature | 107℃ | 107℃ |
| Resurgent gases goes out the regeneration actuator temperature | 107℃ | 92℃ |
| The thermal source steam consumption quantity | 4300kg/h | 2735kg/h |
With implement before compare, the present invention has saved thermal source steam about 36.4%
The regeneration system rapidly of the present invention's carbonic acid gas in being applicable to above-mentioned recovery stack gas and removing the regeneration system rapidly of sour gas in the unstripped gas still can be applicable to other any solution regeneration systems that all gases scavenging process of obvious heat exhaustion is arranged.
Claims (3)
1, a kind of chemical absorption liquid regenerated regenerator column heat recovery method that is applied to, it is characterized in that: the rich solution parallel connection of self-absorption tower (1) lower part outlet is split into two-way, wherein one road rich solution enters solution heat exchanger (3), with the hot lean solution partition heat exchange of regenerator column (4) lower part outlet, reclaim the sensible heat in the lean solution; Another road rich solution enters resurgent gases interchanger (5), hot resurgent gases partition heat exchange with regenerator column (4) top exit, the latent heat of reclaiming gas, the rich solution that leaves the rich solution of solution heat exchanger (3) and leave resurgent gases interchanger (5) are respectively or enter regenerator column (4) regeneration after merging;
Wherein said rich solution parallel connection splits into: the amount that enters solution heat exchanger (3) rich solution accounts for 30～90% of total rich solution weight, and surplus enters resurgent gases interchanger (5).
As the said heat recovery method of claim 1, it is characterized in that 2, the amount that wherein enters solution heat exchanger (3) rich solution accounts for 50～80% of total rich solution weight, surplus enters resurgent gases interchanger (5).
As claim 1 or 2 said heat recovery methods, it is characterized in that 3, wherein the thermal source of regenerator column (4) comprises steam, hot charge gas, heat technologic gas, burning gas, hot exhaust gas or hot waste gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310109090 CN1232500C (en) | 2003-12-04 | 2003-12-04 | Method for recovering regeneration tower heat quantity |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200310109090 CN1232500C (en) | 2003-12-04 | 2003-12-04 | Method for recovering regeneration tower heat quantity |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1546459A CN1546459A (en) | 2004-11-17 |
| CN1232500C true CN1232500C (en) | 2005-12-21 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200310109090 Expired - Fee Related CN1232500C (en) | 2003-12-04 | 2003-12-04 | Method for recovering regeneration tower heat quantity |
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| CN (1) | CN1232500C (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102225297B (en) * | 2011-05-18 | 2013-04-10 | 成都华西工业气体有限公司 | Heat pump regeneration process for desulphurization solvent used in flue gas desulphurization by solvent cyclic absorption method |
| CN102784545B (en) * | 2011-05-20 | 2015-12-16 | 中国科学院大连化学物理研究所 | A kind of microchannel gas desorption system |
| CN102872680B (en) * | 2012-09-26 | 2016-08-17 | 中国恩菲工程技术有限公司 | Flue gas desulphurization system and fume desulphurization method |
| CN102895860B (en) * | 2012-09-29 | 2015-01-07 | 华北电力大学 | Method and system for reducing consumption in capturing process of CO2 through chemical absorption |
| CN103463955B (en) * | 2013-09-16 | 2015-10-28 | 湖南大学 | A kind of technique of separation and recovery carbon dioxide from industrial tail gas |
| CN107149865A (en) * | 2017-05-24 | 2017-09-12 | 华中农业大学 | CO based on vapor mass transfer enhancement waste heat recovery2Chemical absorbing System and method for |
| CN108744932A (en) * | 2018-06-20 | 2018-11-06 | 北京化工大学 | One kind removing from industrial smoke or tail gas and recycle SO2Device and technique |
| CN111467940B (en) * | 2019-01-24 | 2022-02-01 | 中石化南京化工研究院有限公司 | Method and system for removing carbon dioxide in reaction gas and application of method and system |
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2003
- 2003-12-04 CN CN 200310109090 patent/CN1232500C/en not_active Expired - Fee Related
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|---|---|
| CN1546459A (en) | 2004-11-17 |
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