CN202666657U - Facility for collecting carbon dioxide and/or hydrogen sulfide from gas mixture - Google Patents
Facility for collecting carbon dioxide and/or hydrogen sulfide from gas mixture Download PDFInfo
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- CN202666657U CN202666657U CN2012201410527U CN201220141052U CN202666657U CN 202666657 U CN202666657 U CN 202666657U CN 2012201410527 U CN2012201410527 U CN 2012201410527U CN 201220141052 U CN201220141052 U CN 201220141052U CN 202666657 U CN202666657 U CN 202666657U
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Abstract
A facility for collecting carbon dioxide and/or hydrogen sulfide from gas mixture comprises three parts which are an absorption system, a double-tower desorption system and an absorption liquid circulatory system. The absorption system comprises an absorption tower and tower top washing equipment of the absorption tower. The double-tower desorption system comprises two desorption towers which are connected in parallel or in series, reboilers of the desorption towers and tower top backflow equipment of the desorption towers. The absorption liquid circulatory system comprises rich absorption liquid, barren absorption liquid, a rich-barren liquid heat exchanger, a cooler, a filter, a booster pump and a delivery pump. The facility is provided with the double-tower desorption system which comprises the two desorption towers which are connected in parallel or in series, not only are the requirements on carbon dioxide gas products of different concentration satisfied, but also one or two heat media can be used to heat the reboilers according to the situation of a former plant area so that an absorption process and a desorption process are flexible, and energy utilization is reasonable. The facility belongs to the field of gas purification and greenhouse gas emission reduction, not only is greenhouse gas emission is reduced, but also reutilization of energy sources can be distributed reasonably, and accordingly operation cost of a plant can be lowered.
Description
Technical field
The utility model belongs to gas purification and reduction of greenhouse gas discharge field, particularly, relate to containing the admixture of gas of carbon dioxide and/or hydrogen sulfide, as: natural gas, coal bed gas, synthesis gas, refinery gas, coal-fired plant flue gas etc. carry out the facility of carbon dioxide removal and/or hydrogen sulfide.
Background technology
Usually can contain carbon dioxide and/or hydrogen sulfide gas in natural gas, coal bed gas, synthesis gas, refinery gas, the coal-fired plant flue gas.Carbon dioxide and/or hydrogen sulfide are called as acidic components, and carbon dioxide is a kind of greenhouse gases.Contain acidic components can cause e-quipment and pipe in exploitation, storage and transportation corrosion in the gas, especially when carbon dioxide, hydrogen sulfide and water exist simultaneously, can make steel produce hydrogen embrittlement and stress cracking, more serious to the corrosion meeting of steel; If as fuel then can produce sulfur oxide contamination to atmosphere, harm humans is healthy the gas that contains hydrogen sulfide; The gas that contains acidic components then can cause catalyst poisoning as industrial chemicals, affects product yield and quality; If produce the frozen block that contains too high carbon dioxide in the unstripped gas of liquefied natural gas then can cause the visual plants such as downstream ice chest.
Simultaneously, carbon dioxide is one of principal elements that cause global warming as a kind of greenhouse gases, and especially the signing of Kyoto Protocol forces us will change that in the past efficiency of energy utilization is low, the rough mode of production at the cost of the environment.Moreover, too high gas concentration lwevel also can make the nutritive value of crops reduce.Even so, if but with carbon dioxide eliminating and collection, it can have further application in fields such as oil-gas mining, food processings.Many countries are in the world all carrying out the research work that removes and collect carbon dioxide, and therefore, what our nation needs was positive puts in this research field.
To the various ways that removed of acidic components in the admixture of gas, comprise Physical Absorption method, chemical absorption method, physical chemistry absorption process, membrane separation process etc.The Physical Absorption ratio juris is to utilize acidic components from the different of the solubility of other component in some absorption liquid acidic components to be absorbed.Usually utilize organic solvent under high pressure, low temperature acidic components to be absorbed, then solvent discharges the acidic components that absorb under low pressure, high temperature again, makes behind the solvent reclamation recycling.The chemical absorbing ratio juris is that acidic components and some absorption liquid generation chemical reaction generate another kind of compound, and then changes process conditions and make the chemical reaction counter movement, thereby removes absorbed acidic components, makes behind the regeneration of absorption solution recycling.The physical chemistry absorption process is to adopt physical solvent and chemical solvent to form absorption liquid, has the character of Physical Absorption method and chemical absorption method concurrently.Aforesaid way is because all utilizing liquid flux to carry out removing of acidic components, so be called again wet method.Membrane separation process is that the different diactinic difference when utilizing different gas components by permeable membrane is separated acidic components.At present, wet method removes acidic components and obtains extensive concern.But the ubiquity operation energy consumption is higher, the phenomenon that operating cost is higher.In addition, if there is multiple heat medium in former plant area, can effectively utilize multiple heat medium, and only be not limited only to utilize wherein a kind of and cause the problem of energy waste also to have to be solved.And the content of different carbon dioxide can have influence on the calorific value of mist in the mist, so, also have to be solved for the mode of producing simultaneously variable concentrations carbon dioxide product gas.
The utility model content
The utility model provides a kind of facility of collecting carbon dioxide and/or hydrogen sulfide from admixture of gas, with avoid above-mentioned mention remove energy consumption, high expensive in the acidic components process; Using energy source is unreasonable; And the problem that need to produce simultaneously the carbon dioxide product of variable concentrations specification.
Concrete technical scheme of the present utility model is as follows:
A kind of facility of from admixture of gas, collecting carbon dioxide and/or hydrogen sulfide, described facility comprises three parts: the absorption system that, is comprised of absorption tower and cat head flushing device thereof; Two, the double tower desorption system that is formed by the desorber of two parallel connections or series connection and reboiler thereof, overhead reflux equipment; Three, the absorption liquid circulatory system that is formed by rich absorption liquid and poor absorption liquid and poor rich liquid heat exchanger, cooler, filter, booster pump, delivery pump.
The pending admixture of gas that contains carbon dioxide or hydrogen sulfide or contain simultaneously both enters into the bottom, absorption tower, poor absorption liquid enters into top, absorption tower, admixture of gas in the absorption tower from the bottom to top, poor absorption liquid from top to bottom, gas-liquid is carried out mass exchange and energy exchange in the absorption tower, the admixture of gas that has been absorbed most of carbon dioxide and/or hydrogen sulfide becomes purified gas from absorbing the cat head discharge, and the poor absorption liquid that has absorbed most of carbon dioxide and/or hydrogen sulfide becomes that rich absorption liquid is discharged at the bottom of the absorption tower and through booster pump, poor rich liquid heat exchanger enters into the desorber top of two parallel connections or series connection, two desorbers are respectively arranged with reboiler, the stripping gas that the desorber bottom produces carries out desorb to rich absorption liquid from the bottom to top, rich absorption liquid becomes poor absorption liquid from the discharge of desorber bottom separate sucking-off carbon dioxide and/or hydrogen sulfide in desorber after, and the carbon dioxide that is desorbed out and/or hydrogen sulfide can be discharged (when two desorbers are parallel connection) or only discharge (when two desorbers are series connection) from a desorb cat head from two desorb cats head respectively, and enter into again next processing unit behind the process overhead reflux equipment, and poor absorption liquid is through poor rich liquid heat exchanger, delivery pump, cooler, be back to top, absorption tower behind the filter and finish circulation.
The utility model forms the double tower desorption system by the desorber of two parallel connections or series connection.Each desorber arranges respectively reboiler and overhead reflux equipment, and can move simultaneously or only move one of them tower according to the variation of pending admixture of gas load, make the device operation more flexible, two desorbers are set improve the device reliability of operation, the on-bne repair in can not parking of implement device situation; According to the different requirements to required product air carbon dioxide and/or concentration of hydrogen sulfide, two desorbers can discharge respectively the carbon dioxide of variable concentrations and/or carbon dioxide and/or the hydrogen sulfide of hydrogen sulfide or same concentrations meets the demands, the energy consumption that need to regenerate to rich absorption liquid when the carbon dioxide of generation variable concentrations and/or hydrogen sulfide is not identical, can save energy resource consumption, reduce operating cost by the regeneration amount of two desorbers of reasonable disposition; According to the heat medium that former plant area can provide, the reboiler of two desorbers can respectively by different heat medium heating or the heating of use same heat medium, reasonably be configured the secondary utilization of the energy.
In the utility model, if pending admixture of gas is gases at high pressure, namely the absorption tower operating pressure is in high pressure conditions, then rich absorption liquid enter desorber can lean on self pressure and without booster pump.
The refluxing unit of two desorb cats head is comprised of gas product cooler, knockout drum and reflux pump in the utility model.The gas that cat head produces carries out gas-liquid separation after cooling off through the gas product cooler in knockout drum, gaseous products enters into next processing unit, and liquid phase is sent back to desorber as overhead reflux liquid through reflux pump.The absorption tower cat head need arrange flushing device, and this equipment can be arranged to dual mode: 1) directly introduce flushing water to top, absorption tower by flushing pump and wash; 2) flushing device that is comprised of flushing condenser, dcq buffer tank, flushing pump washes.
The main component of absorption liquid can adopt a kind of in following four classes in the utility model: 1) potash; 2) ammonia; 3) sulfolane
4) alcamines comprises: primary amine, secondary amine, tertiary amine, and by one or more absorption liquids that form as main component in these alcamines.Other components in the absorption liquid can comprise the additive of activator, anticorrisive agent, antioxidant, defoamer and similar functions, to improve the assimilation effect of absorption liquid.
Technique effect of the present utility model is:
The utility model is collected carbon dioxide and/or hydrogen sulfide from admixture of gas facility can effectively reduce in the admixture of gas acidic components and greenhouse gases to airborne release; Adopt the desorber of two parallel connections or series connection form the double tower desorption system make the device operation more flexible, improved the device reliability of operation; Simultaneously, can save energy resource consumption, reduce operating cost by the regeneration amount of two desorbers of reasonable disposition; The reboiler of two desorbers can respectively by different heat medium heating or the heating of use same heat medium, reasonably be configured the secondary utilization of the energy.
Description of drawings
Fig. 1 collects the principle schematic of the facility of carbon dioxide and/or hydrogen sulfide from admixture of gas as the utility model, but do not limit protection domain of the present utility model.Simultaneously, Fig. 1 is also as the schematic flow sheet of implementation embodiment one of the present utility model and embodiment two.
Among Fig. 1, T1 is the absorption tower, T2, T3 are desorbers, and M is absorption tower cat head flushing device, the desorber overhead reflux equipment that N1, N2 are comprised of gas product cooler, knockout drum and reflux pump, H1, H2 are reboilers, P3, P4 are booster pumps, and E1, E2 are poor rich liquid heat exchangers, and P1, P2 are delivery pumps, G1, G2 are coolers, and F1, F2 are filters.
The specific embodiment
Below in conjunction with specific embodiment the utility model is described further, but the utility model is not restricted to the following embodiment that sets forth.
Embodiment one:
The pressure of pending admixture of gas is 3.5～5.5MPaG, two desorber parallel runnings, two reboilers all adopt steam to heat, the main component of absorption liquid is N methyldiethanol amine (tertiary amine a kind of), concentration is 35%～45% (mass percent): the admixture of gas that contains carbon dioxide and/or hydrogen sulfide enters the bottom of absorption tower T1 and carries out reverse the contact with the poor absorption liquid that enters from top, absorption tower under the pressure of 3.5～5.5MPaG, gas-liquid is carried out mass exchange and energy exchange in the absorption tower, carbon dioxide and/or hydrogen sulfide are absorbed by liquid absorption, purified gas enters atmosphere or enters next processing unit from absorbing cat head, and the poor absorption liquid that has absorbed carbon dioxide and/or hydrogen sulfide becomes rich absorption liquid and discharges at the bottom of the absorption tower and be divided into two tributary thighs and prepare to enter respectively two desorber T2 in parallel and T3.
Because the pressure ratio of supplied materials admixture of gas is higher, so rich absorption liquid can be without the booster pump supercharging before entering desorber.Two strands of rich absorption liquids pass through respectively the top that poor rich liquid heat exchanger E1 and E2 enter desorber T2 and T3 separately, the stripping gas that produces with reboiler H1 at the bottom of the tower and H2 respectively again carries out the gas-liquid exchange, carbon dioxide in the rich absorption liquid and/or hydrogen sulfide are taken to the desorb cat head and then enter next processing unit through being discharged from behind the overhead reflux equipment with stripping gas, and stripping rich absorption liquid has later removed carbon dioxide and/or hydrogen sulfide and become poor absorption liquid and discharge at the bottom of desorber.
The poor absorption liquid of discharging at the bottom of two desorber T2 and the T3 through being sent respectively back to absorption tower T1 behind poor rich liquid heat exchanger E1 and E2, delivery pump P1 and P2, cooler G1 and G2, filter F 1 and the F2, so far, has been finished the cyclic process of absorption liquid separately.
On top, absorption tower the flushing device M that is comprised of flushing condenser, dcq buffer tank, flushing pump being set washes.
Overhead reflux equipment N1 and the N2 that is comprised of gas product cooler, knockout drum and reflux pump is set respectively at the top of two desorber T2 and T3.The carbon dioxide that is desorbed out and/or hydrogen sulfide is through the cooling of gas product cooler, and after carrying out gas-liquid separation through knockout drum, gas phase is discharged from, and liquid phase is sent respectively back to desorber T2 and T3 as overhead reflux through reflux pump.
Embodiment two:
The pressure of pending admixture of gas is 0.05～0.15MPaG, two desorber series operations, reboiler H1 adopts steam to heat, reboiler H2 adopts conduction oil to heat, the main component of absorption liquid is monoethanolamine (primary amine a kind of), concentration is 15%～25% (mass percent): the admixture of gas that contains carbon dioxide and/or hydrogen sulfide enters the bottom of absorption tower T1 and carries out reverse the contact with the poor absorption liquid that enters from top, absorption tower under the pressure of 0.05～0.15MPaG, gas-liquid is carried out mass exchange and energy exchange in the absorption tower, carbon dioxide and/or hydrogen sulfide are absorbed by liquid absorption, purified gas enters atmosphere or enters next processing unit from absorbing cat head, and the poor absorption liquid that has absorbed carbon dioxide and/or hydrogen sulfide becomes rich absorption liquid and discharge and prepare to enter desorber T2 at the bottom of the absorption tower.
Because the pressure ratio of supplied materials admixture of gas is lower, so rich absorption liquid needs through the booster pump supercharging before entering desorber.The rich absorption liquid of discharging from absorption tower T1 bottom enters the top of desorber T2 after through booster pump P3 supercharging, the stripping gas that produces with reboiler H1 at the bottom of the tower again carries out the gas-liquid exchange, then the top that the partial CO 2 that is gone out by stripping in the rich absorption liquid and/or hydrogen sulfide together are taken to T2 with stripping gas and the carbon dioxide of sending here from the T3 top and/or hydrogen sulfide also enters next processing unit through being discharged from behind the T2 overhead reflux equipment N1, and stripping rich absorption liquid has later removed partial CO 2 and/or hydrogen sulfide and discharged at the bottom of desorber T2.
The absorption liquid of discharging from desorber T2 bottom is through booster pump P4 supercharging, then after heating up through poor rich liquid heat exchanger E2, enter the top of desorber T3, the stripping gas that produces with reboiler H2 at the bottom of the tower again carries out the gas-liquid exchange, carbon dioxide in the absorption liquid and/or hydrogen sulfide are taken to desorber T3 top with stripping gas and are transported to the bottom of desorber T2 through overhead line, and the stripping gas that produces with reboiler H1 and carbon dioxide and/or hydrogen sulfide together are taken to the top of T2.The absorption liquid that has been removed carbon dioxide and/or hydrogen sulfide among the T3 becomes poor absorption liquid and discharges at the bottom of desorber T3.
The poor absorption liquid of discharging at the bottom of the desorber T3 is sent back to absorption tower T1 after through poor rich liquid heat exchanger E2, delivery pump P2, cooler G2, filter F 2, so far, has finished the cyclic process of absorption liquid.
On top, absorption tower the flushing device M that is comprised of flushing condenser, dcq buffer tank, flushing pump being set washes.
The overhead reflux equipment N1 that is comprised of gas product cooler, knockout drum and reflux pump is set at desorber T2 top.The carbon dioxide that is desorbed out and/or hydrogen sulfide is through the cooling of gas product cooler, and after carrying out gas-liquid separation through knockout drum, gas phase is discharged from, and liquid phase is sent back to desorber T2 as overhead reflux through reflux pump.
Claims (6)
1. from admixture of gas, collect the facility of carbon dioxide and/or hydrogen sulfide, it is characterized in that described facility comprises three parts: the absorption system that, is comprised of absorption tower and cat head flushing device thereof; Two, the double tower desorption system that is formed by the desorber of two parallel connections or series connection and reboiler thereof, overhead reflux equipment; Three, the absorption liquid circulatory system that is formed by rich absorption liquid and poor absorption liquid and poor rich liquid heat exchanger, cooler, filter, booster pump, delivery pump;
The pending admixture of gas that contains carbon dioxide or hydrogen sulfide or contain simultaneously both enters into the bottom, absorption tower, poor absorption liquid enters into top, absorption tower, admixture of gas in the absorption tower from the bottom to top, poor absorption liquid from top to bottom, gas-liquid is carried out mass exchange and energy exchange in the absorption tower, the admixture of gas that has been absorbed most of carbon dioxide and/or hydrogen sulfide becomes purified gas from absorbing the cat head discharge, and the poor absorption liquid that has absorbed most of carbon dioxide and/or hydrogen sulfide becomes that rich absorption liquid is discharged at the bottom of the absorption tower and through booster pump, poor rich liquid heat exchanger enters into the desorber top of two parallel connections or series connection, two desorbers are respectively arranged with reboiler, the stripping gas that the desorber bottom produces carries out desorb to rich absorption liquid from the bottom to top, rich absorption liquid becomes poor absorption liquid from the discharge of desorber bottom separate sucking-off carbon dioxide and/or hydrogen sulfide in desorber after, and the carbon dioxide that is desorbed out and/or hydrogen sulfide can be discharged (when two desorbers are parallel connection) or only discharge (when two desorbers are series connection) from a desorb cat head from two desorb cats head respectively, and enter into again next processing unit behind the process overhead reflux equipment, and poor absorption liquid is through poor rich liquid heat exchanger, delivery pump, cooler, be back to top, absorption tower behind the filter and finish circulation.
2. the facility of collecting carbon dioxide and/or hydrogen sulfide from admixture of gas according to claim 1, it is characterized in that: the desorber by two parallel connections or series connection forms the double tower desorption system.
3. the facility of collecting carbon dioxide and/or hydrogen sulfide from admixture of gas according to claim 1 and 2 is characterized in that:
1) two desorbers can move or only move one of them tower simultaneously;
2) according to the different requirements of required product air carbon dioxide and/or concentration of hydrogen sulfide, two desorbers can discharge respectively the carbon dioxide of variable concentrations and/or carbon dioxide and/or the hydrogen sulfide of hydrogen sulfide or same concentrations meets the demands;
3) reboiler of two desorber bottoms can be respectively by different heat medium heating or the heating of use same heat medium.
4. the facility of from admixture of gas, collecting carbon dioxide and/or hydrogen sulfide according to claim 1, it is characterized in that: if pending admixture of gas is gases at high pressure, be that the absorption tower operating pressure is in high pressure conditions, then rich absorption liquid can be without booster pump before entering desorber.
5. the facility of collecting carbon dioxide and/or hydrogen sulfide from admixture of gas according to claim 1 and 2, it is characterized in that: two desorber tops arrange respectively the overhead reflux equipment that is comprised of gas product cooler, knockout drum and reflux pump.
6. the facility of from admixture of gas, collecting carbon dioxide and/or hydrogen sulfide according to claim 1, it is characterized in that: the absorption tower cat head need arrange flushing device, and this equipment can be arranged to dual mode:
1) directly introducing flushing water to top, absorption tower by flushing pump washes;
2) flushing device that is comprised of flushing condenser, dcq buffer tank, flushing pump washes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012201410527U CN202666657U (en) | 2012-04-06 | 2012-04-06 | Facility for collecting carbon dioxide and/or hydrogen sulfide from gas mixture |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012201410527U CN202666657U (en) | 2012-04-06 | 2012-04-06 | Facility for collecting carbon dioxide and/or hydrogen sulfide from gas mixture |
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| CN202666657U true CN202666657U (en) | 2013-01-16 |
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| CN2012201410527U Expired - Fee Related CN202666657U (en) | 2012-04-06 | 2012-04-06 | Facility for collecting carbon dioxide and/or hydrogen sulfide from gas mixture |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103357250A (en) * | 2012-04-06 | 2013-10-23 | 李志远 | Facility and process for collecting carbon dioxide and/or hydrogen sulfide from gas mixture |
| CN103752133A (en) * | 2014-01-03 | 2014-04-30 | 南京工业大学 | Method for removing CO under medium-high pressure by adopting methyl cyclosiloxane2Process and apparatus for the production of |
| CN106943848A (en) * | 2015-12-14 | 2017-07-14 | 株式会社东芝 | The method of carbon dioxide capture systems and operation carbon dioxide capture systems |
-
2012
- 2012-04-06 CN CN2012201410527U patent/CN202666657U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103357250A (en) * | 2012-04-06 | 2013-10-23 | 李志远 | Facility and process for collecting carbon dioxide and/or hydrogen sulfide from gas mixture |
| CN103752133A (en) * | 2014-01-03 | 2014-04-30 | 南京工业大学 | Method for removing CO under medium-high pressure by adopting methyl cyclosiloxane2Process and apparatus for the production of |
| CN103752133B (en) * | 2014-01-03 | 2016-01-27 | 南京工业大学 | Method for removing CO under medium-high pressure by adopting methyl cyclosiloxane2Process and apparatus for the production of |
| CN106943848A (en) * | 2015-12-14 | 2017-07-14 | 株式会社东芝 | The method of carbon dioxide capture systems and operation carbon dioxide capture systems |
| US10864478B2 (en) | 2015-12-14 | 2020-12-15 | Kabushiki Kaisha Toshiba | Carbon dioxide capture system and a method of operating a carbon dioxide capture system |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130116 Termination date: 20180406 |
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| CF01 | Termination of patent right due to non-payment of annual fee |