CN202052457U - Novel low-pressure carbon dioxide regeneration tower - Google Patents
Novel low-pressure carbon dioxide regeneration tower Download PDFInfo
- Publication number
- CN202052457U CN202052457U CN2011201322517U CN201120132251U CN202052457U CN 202052457 U CN202052457 U CN 202052457U CN 2011201322517 U CN2011201322517 U CN 2011201322517U CN 201120132251 U CN201120132251 U CN 201120132251U CN 202052457 U CN202052457 U CN 202052457U
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- CN
- China
- Prior art keywords
- carbon dioxide
- monoethanolamine
- export pipeline
- regeneration
- heat exchange
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- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Abstract
The utility model relates to a novel low-pressure carbon dioxide regeneration tower. A steam heating regeneration kettle, a bubble cap gas-liquid dividing section, a temperature rise packing layer, a spray pipe, a gas-liquid tubular heat exchange separator and a carbon dioxide outlet pipeline are arranged in a tower body from bottom to top; the carbon dioxide outlet pipeline is positioned at the top of the tower; the lower portion of a heat separator is provided with an ethanolamine rich liquid outlet pipeline adopting heat exchange for primary temperature rise; the ethanolamine rich liquid outlet pipeline is connected into a heat exchanger and then connected into the spray pipe; another pipeline of the heat exchanger is communicated with a high-temperature ethanolamine lean liquid outlet pipeline; and a self-operated pressure automatic control valve is arranged on the carbon dioxide outlet pipeline. By the aid of the novel low-pressure carbon dioxide regeneration tower, carbon dioxide regeneration effect can be improved, and power consumption can be reduced.
Description
Technical field
The utility model relates to a kind of equipment that reclaims carbon dioxide, particularly a kind of from the ethanolamine solutions that is rich in carbon dioxide the equipment of separating carbon dioxide.
Background technology
From flue gas, reclaim carbon dioxide, usually become the monoethanolamine rich solution with monoethanolamine absorption liquid absorbing carbon dioxide, next step comes out to become the monoethanolamine lean solution with the carbon dioxide thermal regeneration that absorbs in the monoethanolamine rich solution and goes to recycle, the compression of the carbon dioxide that bears is again sealed up for safekeeping or the carbon dioxide that bears is again sent into absorption, rectification and purification, obtain carbon dioxide product, thereby reach reduction of discharging and practical purpose atmosphere.
Reclaim the carbon dioxide regenerator in the carbon dioxide plants in the existing flue gas, be the normal pressure type, structure is: the temperature raising filler interval of the Steam Heating regeneration still at the bottom of the tower, the spray section in the tower and spray section below, the power washing segregation section of cat head constitute, and also are provided with gas flow tube and fluid flow tube separately between temperature raising filler interval and the Steam Heating regeneration still.
From flue gas, be recovered the normal temperature monoethanolamine rich solution behind the carbon dioxide, after the indirect temperature raising of monoethanolamine poor rich liquid heat exchanger, just enter spray liquid temperature raising filler interval, flow downward, rise and the next high further temperature raising of carbon dioxide gas direct heat transfer of temperature with the regeneration of Steam Heating regeneration still, then flow in the thermal regeneration still, reach by Steam Heating under the regeneration temperature of control and regenerate, monoethanolamine lean solution after the regeneration flows into the rich or poor heat exchanger cooling of monoethanolamine, owing to be the normal pressure operation, must send the circulation of carbon dioxide recovery tower as carbon dioxide absorption liquid the monoethanolamine lean solution with pump again.The carbon dioxide regeneration gas that rises in regeneration back packing layer contact with the monoethanolamine rich solution lower the temperature after, rise to top of tower power and wash segregation section, cleaning solution uses out the liquid that carbon dioxide cools and isolates behind the tower, is dynamically washed with cat head by pumping.Isolated carbon dioxide semi-finished product send post processing.
Above-mentioned used carbon dioxide regenerator because of adopting normal pressure regeneration and power washing detached job, must be provided with associated part monoethanolamine lean pump and two power-equipments of washing liquid pump, and to guarantee manipulating of it, then energy consumption is big, complicated operation.The carbon dioxide heat content that bears does not again fully obtain reclaiming in tower yet.Go out the carbon dioxide gas refrigerated separation liquid (being mainly water) behind the tower, in tower, make cleaning solution, can all flow into the regeneration stills and be evaporated once again, increased steam consumption.Simultaneously, rich or poor two solution of monoethanolamine with not regeneration of having regenerated in the Steam Heating regeneration still are obscured easily, have the dead angle, and regeneration effect can be poor.For guaranteeing that good regeneration effect is arranged, it is big that hear rate is wanted, and promptly the heating steam consumption wants many.
Summary of the invention
The present utility model purpose is in order to overcome the defective in the above-mentioned background technology, to provide a kind of and can further improve the carbon dioxide regeneration effect, can saving the novel low pressure CO 2 regenerator of power consumption.
The technical solution of the utility model is: a kind of carbon dioxide recovery tower, comprise tower body, the Steam Heating of tower body bottom regeneration still with and still at the bottom of high temperature monoethanolamine lean solution export pipeline, temperature raising packing layer in the tower, shower on the temperature raising packing layer, the segregation section of cat head and carbon dioxide export pipeline, be provided with bubble-cap gas-liquid shunting section between wherein said Steam Heating regeneration still and the temperature raising packing layer, the segregation section of cat head is gas-liquid shell and tube heat exchange segregator, this heat exchange segregator top is provided with normal temperature monoethanolamine rich solution inlet ductwork, the heat separator bottom is provided with the monoethanolamine rich solution export pipeline through the first temperature raising of heat exchange, this export pipeline inserts a heat exchanger and inserts above-mentioned shower then, another pipeline of this heat exchanger is communicated with above-mentioned high temperature monoethanolamine lean solution export pipeline, and the carbon dioxide export pipeline is provided with the self-operated type pressure automatic valve.
The force value of described self-operated type pressure automatic valve is set to 0.14～0.15MPa.
Described Steam Heating regeneration still is divided into the regeneration sub-district of four polyphones by steam-heating pipe, three vertical plate washers and the import and export pipeline of steam is formed.
The beneficial effects of the utility model are: with respect to traditional carbon dioxide regenerator, saved monoethanolamine lean pump and two power-equipments of washing liquid pump, saved electric power.Steam Heating regeneration still is divided into the regeneration sub-district of four polyphones by three vertical plate washers, like this ethanolamine solutions can one distinguish ground, contact, the heating at, no dead angle mixed mutually with the monoethanolamine liquid of having regenerated, improved the separative efficiency of carbon dioxide.
Description of drawings
Fig. 1 is the utility model structural representation;
Wherein: 1, Steam Heating regeneration still, 2, high temperature monoethanolamine lean solution export pipeline, 3, bubble-cap gas-liquid shunting section, 4, packing layer, 5, the plate-like spray head, 6, gas-liquid tubulation heat exchange segregator, 7, normal temperature monoethanolamine rich solution inlet ductwork, 8, monoethanolamine rich solution export pipeline, 9, hot ethanol amine rich solution entrance pipe, 10, carbon dioxide export pipeline, 11, self-operated type pressure automatic valve, 12, heat exchanger, 13, cooler, 14, carbon dioxide cooler, 15, gas-liquid separator.
The specific embodiment
The utility model as shown in Figure 1, regenerator bottom part body are Steam Heating regeneration still (1), and this Steam Heating regeneration still is made up of the import and export pipeline that steam-heating pipe, three vertical plate washers are divided into four polyphone regeneration sub-districts and steam; Be provided with high temperature monoethanolamine lean solution export pipeline (2) at the bottom of this Steam Heating regeneration still still.Steam Heating regeneration still top in the tower body is provided with bubble-cap gas-liquid shunting section (3).The top of bubble-cap gas-liquid shunting section is provided with packing layer (4), this packing layer is equipped with stainless steel cloth ripple dish type, one to one, the structured packing of cross filling, packing layer top is plate-like spray head (5), plate-like spray head top is provided with and can carries out further heat recovery and can be to the gas-liquid tubulation heat exchange segregator (6) with gas-liquid separating function of the normal temperature monoethanolamine rich solution that enters heating to carbon dioxide, this heat exchange segregator top is provided with normal temperature monoethanolamine rich solution inlet ductwork (7), the heat separator bottom is provided with the monoethanolamine rich solution export pipeline (8) through the first temperature raising of heat exchange, this export pipeline inserts a heat exchanger and inserts above-mentioned shower through hot ethanol amine rich solution entrance pipe (9) then, and another pipeline of this heat exchanger is communicated with above-mentioned high temperature monoethanolamine lean solution export pipeline.The regenerator cat head is provided with carbon dioxide export pipeline (10), and the carbon dioxide export pipeline is provided with self-operated type pressure automatic valve (11).
The utility model course of work is:
From the next normal temperature monoethanolamine rich solution of carbon dioxide recovery tower, enter the shell of gas-liquid tubulation heat exchange segregator (6) by the normal temperature monoethanolamine rich solution inlet ductwork (7) of top of tower, carbon dioxide by the heat that rises in the tower also enters gas-liquid tubulation heat exchange segregator, gas-liquid is after heat exchange, the monoethanolamine rich solution obtains elementary temperature raising, then enter the further temperature raising of the outer heat exchanger (12) of regenerator, inserting plate-like spray head (5) then evenly sprays and descends, at bigger serface, stainless steel cloth corrugated filler layer (4) lining of porous, with the high-temperature that rises from Steam Heating regeneration still (1) lining and through time temperature raising of winning the third place of the direct contact heat-exchanging of carbon dioxide gas at the even upper reaches of side opening of bubble-cap gas-liquid shunting section (3), then flow into 1 district of Steam Heating regeneration still (1) by the side lower part fluid flow tube of bubble-cap gas-liquid shunting section (3), go into 2 districts by the overflow of 1 district again, flow into 3 districts from 2 district's bottom outlets, 4 districts are gone in overflow again from 3 districts, and such one distinguishes ground, polyphone ground, do not mix mutually with the monoethanolamine liquid of having regenerated, no dead angle, channelization fluidly, and temperature control is regenerated under regeneration temperature and is emitted carbon dioxide gas.The monoethanolamine rich solution is become carbon dioxide-lean in nearly zero monoethanolamine lean solution by the regeneration of one-level one-level ground, lean on tower self pressure by bottom, 4 districts, be pressed into the outer heat exchanger (12) of regenerator, through heat exchange cooling back and access cooler (13) reduce to normal temperature, send the carbon dioxide recovery tower to recycle as carbon dioxide recovery liquid.After the high carbon dioxide rising gas of temperature that 4 districts of Steam Heating regeneration still produce again compiles, by side opening current-sharing around the bubble-cap gas-liquid shunting section (3) upwards, evenly spray the direct contact heat-exchanging of monoethanolamine rich solution that flows down with packing layer (4) lining, lowered the temperature for the first time, after continue to rise in the tubulation of gas-liquid tubulation heat exchange segregator (6) of cat head with shell normal temperature monoethanolamine rich solution material liquid indirect heat exchange after discharge by the carbon dioxide export pipeline (10) of cat head after cooling for the second time and the gas-liquid separation, and control through self-operated type pressure automatic valve (11), carbon dioxide enters carbon dioxide cooler (14), gas-liquid separator (15) is handled, obtain 99.5% carbon dioxide semi-finished product, send down operation.
Claims (3)
1. novel low pressure CO 2 regenerator, comprise tower body, the Steam Heating of tower body bottom regeneration still with and still at the bottom of high temperature monoethanolamine lean solution export pipeline, temperature raising packing layer in the tower, shower on the temperature raising packing layer, the segregation section of cat head and carbon dioxide export pipeline, it is characterized in that being provided with bubble-cap gas-liquid shunting section between described Steam Heating regeneration still and the temperature raising packing layer, the segregation section of cat head is gas-liquid shell and tube heat exchange segregator, this heat exchange segregator top is provided with normal temperature monoethanolamine rich solution inlet ductwork, this heat exchange segregator bottom is provided with the monoethanolamine rich solution export pipeline through the first temperature raising of heat exchange, this export pipeline inserts a heat exchanger and inserts above-mentioned shower then, another pipeline of this heat exchanger is communicated with above-mentioned high temperature monoethanolamine lean solution export pipeline, and the self-operated type pressure automatic valve is arranged on the carbon dioxide export pipeline.
2. novel low pressure CO 2 regenerator as claimed in claim 1 is characterized in that the force value of described self-operated type pressure automatic valve is set to 0.14～0.15MPa.
3. novel low pressure CO 2 regenerator as claimed in claim 1, four the polyphone regeneration sub-districts that it is characterized in that described Steam Heating regeneration still is divided into by steam-heating pipe, three vertical plate washers and the import and export pipeline of steam are formed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201322517U CN202052457U (en) | 2011-04-29 | 2011-04-29 | Novel low-pressure carbon dioxide regeneration tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201322517U CN202052457U (en) | 2011-04-29 | 2011-04-29 | Novel low-pressure carbon dioxide regeneration tower |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202052457U true CN202052457U (en) | 2011-11-30 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011201322517U Expired - Lifetime CN202052457U (en) | 2011-04-29 | 2011-04-29 | Novel low-pressure carbon dioxide regeneration tower |
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| Country | Link |
|---|---|
| CN (1) | CN202052457U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107812445A (en) * | 2016-09-14 | 2018-03-20 | 中国石油化工股份有限公司 | Thermal regeneration condensation separation integrated device and renovation process for hot potash method decarbonization process |
| WO2021202627A1 (en) * | 2020-04-01 | 2021-10-07 | Huntsman Petrochemical Llc | Process for conversion of bis(hydroxyethylethoxy)-urea to dga |
-
2011
- 2011-04-29 CN CN2011201322517U patent/CN202052457U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107812445A (en) * | 2016-09-14 | 2018-03-20 | 中国石油化工股份有限公司 | Thermal regeneration condensation separation integrated device and renovation process for hot potash method decarbonization process |
| WO2021202627A1 (en) * | 2020-04-01 | 2021-10-07 | Huntsman Petrochemical Llc | Process for conversion of bis(hydroxyethylethoxy)-urea to dga |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: 221000 West Side of Xingang Road, Xinyi Economic Development Zone, Xuzhou City, Jiangsu Province (South Side of Shifu Road) Patentee after: Xuzhou Jinhong Gas Co., Ltd. Address before: 221400 West Side of Xingang Road, Xinyi Economic Development Zone, Xuzhou City, Jiangsu Province (South Side of Shifu Road) Patentee before: Xuzhou Jinhong Carbon Dioxide Technology Development Co., Ltd. |
|
| CP03 | Change of name, title or address | ||
| CX01 | Expiry of patent term |
Granted publication date: 20111130 |
|
| CX01 | Expiry of patent term |