CN217367848U - Desorption system for regenerable amine process desulfurization - Google Patents
Desorption system for regenerable amine process desulfurization Download PDFInfo
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- CN217367848U CN217367848U CN202221458495.9U CN202221458495U CN217367848U CN 217367848 U CN217367848 U CN 217367848U CN 202221458495 U CN202221458495 U CN 202221458495U CN 217367848 U CN217367848 U CN 217367848U
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Abstract
The utility model relates to a desulfurization desorption device specifically discloses a desorption system for amine method desulfurization can regenerate, including rich liquid storage tank, desorber and barren liquor storage tank, still include steam precooler and reboiler, the rich liquid storage tank communicates with the inlet of steam precooler, and the liquid outlet of steam precooler communicates with the last feed inlet of desorber, and the bottom discharge gate of desorber communicates with the inlet of reboiler, and the liquid outlet of reboiler communicates with the barren liquor storage tank; an upper exhaust port of the desorption tower is communicated with an air inlet of a steam precooler, and a sulfur-containing gas is discharged from an air outlet of the steam precooler; and the gas outlet of the reboiler is communicated with the lower feed inlet of the desorption tower. The desorption system has low energy consumption in integral operation, high energy utilization rate and high sulfur dioxide recovery efficiency.
Description
Technical Field
The utility model relates to a desulfurization desorption device, concretely relates to a desorption system for desulfurization of regenerable amine method.
Background
In several mainstream wet flue gas desulfurization technologies at present, calcium desulfurization is adopted to produce sulfur gypsum, the utilization value of sulfur is extremely low, and a proper solution is not found for the problem of secondary pollution; and the ammonium sulfate fertilizer is produced by adopting ammonia desulphurization, so the sale price is low and the economic benefit is poor. Aiming at the treatment of sulfur-containing flue gas with high flow and high concentration, the conventional wet flue gas desulfurization technology has the defects of different degrees and is difficult to match with gradually severe emission standards. The renewable amine method desulfurization technology is a new flue gas desulfurization technology, has the characteristics of high desulfurization efficiency, recyclable absorbent, no secondary pollution and the like, regenerates to obtain sulfur dioxide gas with higher purity, can further process series 'sulfur series' products (such as liquid sulfur dioxide), has high production efficiency, is easy to form a certain production scale, and has better economic value.
As a main energy consumption unit of a desulfurization system, the optimal design of a desorption system for desulfurization by a renewable amine method is very important for improving the desorption efficiency and the system economy.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a desorption system for can regenerating amine process desulfurization, its whole operation energy consumption is low, and energy utilization is high, and sulfur dioxide recovery efficiency is high.
In order to achieve the above object, the utility model adopts the following technical scheme:
a desorption system for desulfurization by a renewable amine method comprises a rich liquid storage tank, a desorption tower, a lean liquid storage tank, a steam precooler and a reboiler, wherein the rich liquid storage tank is communicated with a liquid inlet of the steam precooler; an upper exhaust port of the desorption tower is communicated with an air inlet of the steam precooler, and a sulfur-containing gas is exhausted from an air outlet of the steam precooler; and the gas outlet of the reboiler is communicated with the lower feed inlet of the desorption tower.
Wherein, the desorption tower adopts a packed tower, which can promote the full contact of gas and liquid and improve the desorption efficiency.
As a preferable scheme, the device further comprises a partial condenser, wherein the gas inlet of the partial condenser is communicated with the gas outlet of the steam pre-cooler, the liquid outlet of the partial condenser is communicated with the upper material inlet of the desorption tower, and the gas outlet of the partial condenser discharges sulfur-containing gas.
As a preferable scheme, the device further comprises a demister, wherein a gas outlet of the partial condenser is communicated with a gas inlet of the demister, and sulfur-containing gas is discharged from the gas outlet of the demister.
As a preferable scheme, the desorption tower further comprises a buffer tank, a liquid outlet is formed in the dephlegmator, the liquid outlet of the steam precooler and the liquid outlet of the dephlegmator are both communicated with the liquid inlet of the buffer tank, and the liquid outlet of the buffer tank is communicated with the upper feed inlet of the desorption tower.
As a preferable scheme, the liquid inlet of the steam precooler and the liquid outlet of the steam precooler are both communicated with the tube pass of the steam precooler, and the air inlet of the steam precooler and the air outlet of the steam precooler are both communicated with the shell pass of the steam precooler; and a condensate outlet communicated with the shell pass of the steam precooler is also arranged on the steam precooler and is communicated with a liquid inlet of the buffer tank.
As a preferable scheme, the air inlet of the partial condenser, the air outlet of the partial condenser and the liquid outlet of the partial condenser are all communicated with the shell pass of the partial condenser; the tube pass of the partial condenser is connected with a refrigerant in series.
As a preferred scheme, the system also comprises a lean and rich liquid heat exchanger, wherein the rich liquid storage tank is communicated with a low-temperature liquid detection inlet of the lean and rich liquid heat exchanger, and a low-temperature liquid detection outlet of the lean and rich liquid heat exchanger is communicated with a liquid inlet of the steam precooler; the lean solution storage tank is communicated with a high-temperature liquid measuring outlet of the lean and rich solution heat exchanger, and a high-temperature liquid measuring inlet of the lean and rich solution heat exchanger is communicated with a liquid outlet of the reboiler.
As a preferable scheme, a rich liquid delivery pump is arranged at a low-temperature liquid inlet of the lean-rich liquid heat exchanger, and a lean liquid delivery pump is arranged at a high-temperature liquid inlet of the lean-rich liquid heat exchanger.
As a preferable scheme, a high-temperature liquid outlet of the lean-rich liquid heat exchanger is provided with a lean liquid cooler.
When the desorption system is used, absorption rich liquor from the absorption system is temporarily stored in a rich liquor storage tank, and is driven by a rich liquor delivery pump to firstly perform heat exchange with high-temperature lean liquor desorbed from a reboiler through a lean rich liquor heat exchanger, then perform heat exchange with steam on the top of a desorption tower through a steam precooler, and further raise the temperature of the rich liquor and then enter a buffer tank. The heat is input into the reboiler, so that the liquid phase at the bottom of the desorption tower is gasified, steam carrying sulfur dioxide flows through the desorption tower from bottom to top and enters the steam precooler after being discharged from the top of the tower, condensate liquid generated after partial steam is condensed is discharged into the buffer tank, and the remaining mixed gas of the steam and the sulfur dioxide enters the dephlegmator again, so that the steam is completely condensed and enters the buffer tank. The condensate has high sulfur content, forms a solution with high sulfur content and temperature close to a boiling point after being mixed with the pregnant solution to be desorbed in the buffer tank, and is in countercurrent contact with the incoming steam from the top of the desorption tower downwards, tetravalent sulfur in the liquid phase gradually enters the gas phase under the drive of concentration gradient, and finally the liquid phase returns to the reboiler. The rich solution becomes barren solution after desorption and regeneration, and is conveyed to a barren solution storage tank by a barren solution conveying pump for temporary storage, and during the period, the barren solution passes through a barren solution and rich solution heat exchanger and a barren solution cooler in sequence, and is cooled to below 40 ℃ (proper absorption temperature) step by step for sulfur dioxide absorption, and if the absorption is circulated, the absorption is performed.
Compared with the prior art, the utility model discloses following beneficial effect has:
(1) the utility model discloses desulfurization desorption system of desulfurization of renewable amine process mainly comprises steam precooler, desorber and reboiler and lean and rich liquid storage tank. On one hand, the heat exchange process is optimized, the heat exchange energy consumption is reduced on the whole, and the energy utilization rate is improved; on the other hand, the saturated reflux of the condensate liquid is in countercurrent contact with the steam, so that the sulfur dioxide is gradually led to enter a gas phase and the like, the mass transfer driving force of the desorption tower is improved, a proper lean and rich liquid concentration interval is regulated and controlled, and the absorption unit at the front end is matched, so that the aims of reducing the overall operation energy consumption and improving the sulfur dioxide recovery efficiency are fulfilled.
(2) The utility model discloses utilize desorber top steam further heating to treat the pregnant solution of desorption to mix with high temperature condensate and heat up, improved the pregnant solution and gone into the tower temperature, reduced the refrigerant consumption of top of the tower partial condenser, increased gas-liquid interface department sulfur dioxide partial pressure, promote follow-up pregnant solution desorption, reduce the energy consumption.
(3) The utility model discloses top of the tower steam condensation reflux liquid principal ingredients is sulfur dioxide saturated aqueous solution, and its quaternary sulfur content is high, and with treat that desorption pregnant solution mixes back solution tetravalent sulfur concentration and rise, help promoting the interior average mass transfer driving force of desorption tower, improve and know and inhale efficiency.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Wherein, the names corresponding to the reference numbers are:
1-rich liquid storage tank, 2-desorption tower, 3-barren liquid storage tank, 4-steam precooler, 5-reboiler, 6-fractional condenser, 7-demister, 8-buffer tank, 9-barren and rich liquid heat exchanger, and 10-barren liquid cooler.
Detailed Description
The present invention will be further described with reference to the following description and examples, which are not intended to limit the scope of the invention.
As shown in fig. 1, the present embodiment provides a desorption system for desulfurization by a renewable amine method, including a rich liquid storage tank 1, a desorption tower 2, a lean liquid storage tank 3, a steam pre-cooler 4, a reboiler 5, a partial condenser 6, a demister 7, a buffer tank 8, a lean liquid heat exchanger 9, a lean liquid cooler 10, a rich liquid transfer pump, a lean liquid transfer pump, and a demister, wherein the rich liquid storage tank 1, the lean liquid heat exchanger 9 (cold liquid tube pass), the steam pre-cooler 4 tube pass, the buffer tank 8, the desorption tower 2, the reboiler 5, the lean liquid heat exchanger 9 (hot shell pass), the lean liquid cooler, and a lean liquid storage tank are connected in series; the reboiler 5, the desorption tower 2, the steam pre-cooler 4, the partial condenser shell pass and the demister 7 are connected in series; wherein, the shell passes of the partial condenser 6 and the steam precooler 4 are both provided with liquid outlets, so that the condensed liquid enters the buffer tank from here and then enters the desorption tower for desorption after being mixed with the rich liquid.
Wherein, the steam precooler, the desorption tower, the reboiler and the lean-rich liquid storage tank. On one hand, the heat exchange process is optimized, the heat exchange energy consumption is reduced on the whole, and the energy utilization rate is improved; on the other hand, the saturated reflux of the condensate liquid is contacted with the steam in a countercurrent way, so that the sulfur dioxide is promoted to gradually enter a gas phase and the like, the mass transfer driving force of the desorption tower is improved, a proper lean and rich liquid concentration interval is regulated and controlled, and the absorption unit at the front end is matched, so that the aims of reducing the integral operation energy consumption and improving the sulfur dioxide recovery efficiency are fulfilled. The steam at the top of the desorption tower is used for further heating the rich liquid to be desorbed, the temperature of the rich liquid entering the tower is increased, the refrigerant consumption of a partial condenser at the top of the tower is reduced, and the sulfur dioxide partial pressure at a gas-liquid interface is increased. Meanwhile, the main component of the tower top steam condensation reflux liquid is a sulfur dioxide saturated aqueous solution, the content of the tetravalence sulfur is high, the solution tetravalence sulfur concentration is increased after the condensation reflux liquid is mixed with the pregnant solution to be desorbed, and the promotion of the average mass transfer driving force in the desorption tower is facilitated.
The desorption system was assembled as shown in FIG. 1, wherein, as equipment, the desorption column was a packed column having an inner diameter of 26 mm and a packed section height600 mm, and 4 mm specification theta ring packing is adopted; the minimum heat transfer temperature difference of the steam precooler is about 6 ℃. As for the material, the tetravalent sulfur content in the pregnant solution to be desorbed. The flow rates of the rich liquid transfer pump and the lean liquid transfer pump were 25 mL/min under the control conditions -1 。
The specific operation flow is as follows:
firstly, a rich liquid delivery pump is started, liquid enters the top of a desorption tower after sequentially passing through a lean rich liquid heat exchanger, a pre-cooler and a buffer tank, the liquid flows into a reboiler from top to bottom by virtue of gravity, a reboiler heating system (steam heating or electric heating) is started after the liquid level of the reboiler reaches a certain height, liquid in the reboiler is vaporized, formed sulfur dioxide vapor flows through the desorption tower from bottom to top and enters the pre-cooler to heat rich liquid to be desorbed, part of the vapor in the pre-cooler is condensed and enters the buffer tank, the rest vapor continuously enters a dephlegmator, non-condensable sulfur dioxide leaves the dephlegmator from the top after cooling heat exchange, the vapor droplets entrained by a demister are removed and then discharged out of the system (namely sulfur dioxide products obtained after deep processing), condensate generated by the dephlegmator enters the buffer tank, and the temperature and concentration of the rich liquid to be desorbed are increased after being mixed in the buffer tank, then the lean solution enters the top of the desorption tower, is in countercurrent contact with ascending steam and flows into a reboiler, sulfur in a liquid phase gradually enters a gas phase, the concentration of the rich solution is reduced and is converted into a lean solution, the lean solution discharged from the reboiler has higher temperature, and is driven by a lean solution delivery pump to sequentially pass through a lean and rich solution exchanger and a lean solution cooler for gradual temperature reduction, and finally the lean solution with lower temperature is formed and stored in a lean solution storage tank for absorption. The flow of the lean-rich liquid delivery pump is consistent, and the flow is used for maintaining the stable liquid level of the reboiler. When the temperature, flow and concentration of each stream of the system reach stability, the system is considered to reach stable operation, and the sulfur content of the barren solution is measured to be 0.165 mol.L -1 。
Through measurement and calculation, after stable operation, 13 g of saturated low-pressure steam is required to be consumed for desorbing 1 g of sulfur dioxide, and the saturated low-pressure steam is used as a small-volume desorption system, so that the heat loss of the system achieves the expected effect.
To sum up, the utility model provides a desulfurization desorption system for amine desulfurization by renewable method, which optimizes the heat exchange process, reduces the heat exchange energy consumption on the whole and improves the energy utilization rate; on the other hand, the saturated reflux of the condensate liquid is in countercurrent contact with the steam, so that the sulfur dioxide is gradually led to enter a gas phase and the like, the mass transfer driving force of the desorption tower is improved, a proper lean and rich liquid concentration interval is regulated and controlled, and the absorption unit at the front end is matched, so that the aims of reducing the overall operation energy consumption and improving the recovery efficiency of the sulfur dioxide are fulfilled; the steam at the top of the desorption tower is used for further heating the rich liquid to be desorbed and is mixed with the high-temperature condensate for heating, so that the temperature of the rich liquid entering the tower is increased, the refrigerant consumption of a partial condenser at the top of the tower is reduced, the sulfur dioxide partial pressure at a gas-liquid interface is increased, the follow-up rich liquid desorption is promoted, and the energy consumption is reduced; the main component of the tower top steam condensation reflux liquid is sulfur dioxide saturated aqueous solution, the tetravalence sulfur content of the solution is high, the solution tetravalence sulfur concentration is increased after the solution is mixed with the pregnant solution to be desorbed, the promotion of the average mass transfer driving force in the desorption tower is facilitated, and the desorption efficiency is improved.
Claims (9)
1. A desorption system for desulfurization by a renewable amine method comprises a rich liquid storage tank (1), a desorption tower (2) and a lean liquid storage tank (3), and is characterized by further comprising a steam precooler (4) and a reboiler (5), wherein the rich liquid storage tank (1) is communicated with a liquid inlet of the steam precooler (4), a liquid outlet of the steam precooler is communicated with an upper feeding port of the desorption tower (2), a lower discharging port of the desorption tower is communicated with a liquid inlet of the reboiler (5), and a liquid outlet of the reboiler is communicated with the lean liquid storage tank (3); an upper exhaust port of the desorption tower (2) is communicated with an air inlet of the steam precooler (4), and a sulfur-containing gas is discharged from an air outlet of the steam precooler; and the gas outlet of the reboiler (5) is communicated with the lower feed inlet of the desorption tower (2).
2. The desorption system for desulfurization by renewable amine method as set forth in claim 1, further comprising a partial condenser (6), wherein the gas inlet of the partial condenser is communicated with the gas outlet of the steam pre-cooler (4), the liquid outlet of the partial condenser is communicated with the upper material inlet of the desorption tower (2), and the gas outlet of the partial condenser discharges sulfur-containing gas.
3. A desorption system for desulfurization by renewable amine method according to claim 2, which further comprises a demister (7), wherein the gas outlet of the partial condenser (6) is communicated with the gas inlet of the demister, and the gas outlet of the demister discharges sulfur-containing gas.
4. The desorption system for desulfurization by renewable amine method as set forth in claim 2 or 3, further comprising a buffer tank (8), wherein the partial condenser (6) is provided with a liquid outlet, the liquid outlet of the steam pre-cooler (4) and the liquid outlet of the partial condenser are both communicated with a liquid inlet of the buffer tank, and the liquid outlet of the buffer tank is communicated with an upper feed inlet of the desorption tower (2).
5. The desorption system for desulfurization by renewable amine method according to claim 4, wherein the liquid inlet of the steam precooler (4) and the liquid outlet of the steam precooler are both communicated with the tube side of the steam precooler, and the gas inlet of the steam precooler and the gas outlet of the steam precooler are both communicated with the shell side of the steam precooler; and a condensate outlet communicated with the shell pass of the steam precooler is also arranged on the steam precooler (4), and the condensate outlet is communicated with a liquid inlet of the buffer tank (8).
6. The desorption system for desulfurization by renewable amine method as set forth in claim 5, wherein the gas inlet of the partial condenser (6), the gas outlet of the partial condenser and the liquid outlet of the partial condenser are all communicated with the shell side of the partial condenser; the tube pass of the partial condenser (6) is connected with a refrigerant in series.
7. The desorption system for desulfurization by the renewable amine method according to claim 1, further comprising a lean-rich liquid heat exchanger (9), wherein the rich liquid storage tank (1) is communicated with a low-temperature liquid inlet of the lean-rich liquid heat exchanger (9), and a low-temperature liquid outlet of the lean-rich liquid heat exchanger is communicated with a liquid inlet of the steam precooler (4); the barren liquor storage tank (3) is communicated with a high-temperature liquid outlet of the barren and rich liquor heat exchanger (9), and a high-temperature liquid inlet of the barren and rich liquor heat exchanger is communicated with a liquid outlet of the reboiler (5).
8. The desorption system for desulfurization by renewable amine method according to claim 7, wherein the low-temperature liquid inlet of the lean-rich liquid heat exchanger (9) is provided with a rich liquid delivery pump, and the high-temperature liquid inlet of the lean-rich liquid heat exchanger is provided with a lean liquid delivery pump.
9. A desorption system for desulfurization by renewable amine according to claim 7 or 8, characterized in that the outlet of high temperature liquid of the lean-rich liquid heat exchanger (9) is provided with a lean liquid cooler (10).
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| CN202221458495.9U CN217367848U (en) | 2022-06-13 | 2022-06-13 | Desorption system for regenerable amine process desulfurization |
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| CN202221458495.9U CN217367848U (en) | 2022-06-13 | 2022-06-13 | Desorption system for regenerable amine process desulfurization |
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