CN214486308U

CN214486308U - Desorption SO for improving desulfurization absorbent2Efficient device

Info

Publication number: CN214486308U
Application number: CN202023297155.6U
Authority: CN
Inventors: 宋小良; 徐光泽
Original assignee: Shuangdun Environment Technology Co ltd
Current assignee: Shuangdun Environment Technology Co ltd
Priority date: 2020-12-31
Filing date: 2020-12-31
Publication date: 2021-10-26
Anticipated expiration: 2030-12-31

Abstract

The utility model discloses a desorption SO for improving desulfurization absorbent₂An efficient apparatus comprising a high-pressure desorption column (1) and a low-pressure desorption column (3) for absorbing SO₂Heating the rich amine liquid of the gas and then sending the heated rich amine liquid into a low-pressure desorption tower (3) for pre-desorption; the bottom outlet of the low-pressure desorption tower (3) is connected with the high-pressure desorption tower (1) through a secondary lean amine liquid output pipe (19) to output secondary lean amine liquid; high-pressure desorption steam generated by the output of lean amine liquid generated by the desorption of the high-pressure desorption tower (1) is connected with a variable-frequency booster fan (5) through a high-pressure desorption steam pipe (2) to be used as low-pressure desorption after being boostedThe absorption tower (3) pre-desorbs the heat source of the required steam. The device of the utility model adopts double-tower double-effect and low-pressure-boosting twice deep desorption to make the lean amine liquid absorbed SO₂To below 5g/L or rich amine liquid SO₂The total desorption efficiency is more than 90 percent, the raw steam consumption is saved by 30 to 50 percent, and the comprehensive cost is reduced by 20 to 40 percent; and can realize ultra-low emission of desulfurization.

Description

Desorption SO for improving desulfurization absorbent2Efficient device

Technical Field

The utility model relates to the technical field of environmental protection, especially, relate to all kinds of kilns, reactor produce and contain SO₂Energy-saving ultra-low emission technical field for flue gas desulfurizationIn particular to a method for improving SO desorption of a desulfurization absorbent₂An efficient device.

Background

The flue gas discharged by various kilns or reactors contains SO₂Direct discharge of SO which pollutes the environment or causes resource loss, organic amine desulfurization₂The resources are recycled, and the process is environment-friendly, efficient, energy-saving, safe and high in automation degree, almost free of secondary pollution and the like, so that the process is rapidly popularized and applied in nearly ten years. The flue gas treatment of the organic amine method (also called as 'ionic liquid method') desulfurization device is remarkably increased (more than or equal to 2.0 x 10)⁵m³H), the treated flue gas contains SO₂The concentration is increased (more than or equal to 6000 mg/m)³) And the ultra-low emission (less than or equal to 35 mg/m) is required to be achieved³) The organic amine method desulfurization device adopts a conventional single tower to desorb SO₂The process configuration, the steam consumption greatly increases and even exceeds the supply capacity of a factory; the key point is that the consumption of the raw steam of a large organic amine desulphurization device is reduced, the process of a single tower, a mechanical vapor compression heat pump (MVR) and a double reboiler is commonly adopted in the current market to reduce the consumption of the raw steam, the heat pump is pressurized by about 200KPa, but the desorption steam contains a certain amount of non-condensable gas (SO)₂Etc.) and the wet state corrosivity is stronger, the MVR model selection has high manufacturing cost and high failure rate and needs to be maintained, the power consumption per ton of steam during the operation reaches about 65KWh, the operation cost is obviously increased, particularly, the stable and continuous reliability of the MVR becomes a bottleneck, even the problem of the standard emission of the smoke is harmed, and the MVR model selection is taken as a necessary and urgent breakthrough of the subject.

SUMMERY OF THE UTILITY MODEL

The utility model aims at solving the problems in the prior art and providing a method for improving the desorption SO of a desulphurization absorbent₂An efficient process.

The utility model aims at solving through the following technical scheme:

desorption SO for improving desulfurization absorbent₂An efficient device characterized by: the device comprises a high-pressure desorption tower and a low-pressure desorption tower for absorbing SO₂Heating the rich amine liquid of the gas, and then sending the heated rich amine liquid into a low-pressure desorption tower for pre-desorption; bottom outlet of low-pressure desorption towerThe sub-lean amine liquid output pipe is connected with the high-pressure desorption tower and feeds the sub-lean amine liquid generated after the pre-desorption of the low-pressure desorption tower into the high-pressure desorption tower for desorption; and the lean amine liquid generated by desorption of the high-pressure desorption tower is sent to the absorption tower after heat exchange and cooling, and the high-pressure desorption steam generated by desorption of the high-pressure desorption tower is connected with the variable-frequency booster fan through the high-pressure desorption steam pipe, so that the high-pressure desorption steam is conveyed to the variable-frequency booster fan for pressurization and then is used as a heat source for pre-desorption of the steam required by the low-pressure desorption tower.

A groove type liquid distributor above a stripping packing layer in the low-pressure desorption tower is connected with a heat exchanger through a preheated amine-rich liquid input pipe so as to input the preheated amine-rich liquid; and the heat exchanger is communicated with an amine-rich liquid input pipe for inputting the amine-rich liquid.

The top of the low-pressure desorption tower is connected with a tube pass inlet of the smoke white elimination heater through a low-pressure desorption steam tube so as to input low-pressure desorption steam to the smoke white elimination heater, a tube pass outlet of the smoke white elimination heater is connected with a low-pressure condensate output tube so as to output low-pressure condensate, a shell pass inlet of the smoke white elimination heater is connected with a cold smoke input tube so as to input cold smoke, and a shell pass outlet is connected with a hot smoke discharge tube so as to discharge heated hot smoke, so that the aim of eliminating white is achieved.

The temperature in the low-pressure desorption tower is 103-110 ℃, and the pressure is 110-150 KPa; the volume content of steam in the low-pressure desorption steam discharged from the low-pressure desorption tower is 85 to 95 percent, and SO₂The volume content is 15-5%.

The pre-desorption efficiency of the low-pressure desorption tower is 35-85%.

A liquid collecting tank of a steam-separating liquid collecting tank below a stripping packing layer in the low-pressure desorption tower is connected with a tube pass inlet of a low-pressure tower reboiler through a secondary lean amine liquid input tube to output secondary lean amine liquid, and a tube pass outlet of the low-pressure tower reboiler is communicated with a tower kettle of the low-pressure desorption tower below the steam-separating liquid collecting tank in the low-pressure desorption tower through a secondary lean amine liquid return tube to input the secondary lean amine liquid containing steam into the low-pressure desorption tower; and a shell pass inlet of the low-pressure tower reboiler is connected with a variable-frequency booster fan through a pipeline, pressurized high-pressure desorption steam is input to serve as a heat source of the low-pressure tower reboiler, and a shell pass outlet of the low-pressure tower reboiler is connected with a high-pressure condensate output pipe to output high-pressure condensate.

The inner wall of the tower kettle of the low-pressure desorption tower corresponding to the secondary lean amine liquid vapor return pipe is provided with a blocking piece, the blocking piece can enable the secondary lean amine liquid containing steam to fall to the bottom of the tower kettle of the low-pressure desorption tower and be pumped into the high-pressure desorption tower through a secondary lean amine liquid output pipe, correspondingly separated steam bypasses the blocking piece and upwards passes through a steam distribution and collection tank in the low-pressure desorption tower to be used as SO in the pre-desorption rich amine liquid of the low-pressure desorption tower₂(or sulfurous acid and its hydrolyzate) stripping the required steam.

The output pipe of the inferior lean amine liquid is provided with a high temperature resistant and corrosion resistant delivery pump for delivering the inferior lean amine liquid, and the outlet of the output pipe of the inferior lean amine liquid is connected with a groove type liquid distributor above a stripping packing layer in the high-pressure desorption tower.

The desorption temperature in the high-pressure desorption tower is 110-120 ℃, and the desorption pressure is 130-190 KPa; and the volume content of steam in the high-pressure desorption steam generated after the desorption of the high-pressure desorption tower is 93-98 percent, and SO₂The volume content is 2-7%.

The variable-frequency booster fan can boost the high-pressure desorption steam output by the high-pressure desorption tower by 30-80 KPa.

A liquid collecting tank of a steam separation liquid collecting tank below a stripping packing layer in the high-pressure desorption tower is connected with a tube pass inlet of a reboiler of the high-pressure tower through a lean amine liquid input tube to output lean amine liquid, and a tube pass outlet of the reboiler of the high-pressure tower is communicated with a tower kettle of the high-pressure desorption tower below the steam separation liquid collecting tank in the high-pressure desorption tower through a lean amine liquid steam return tube to input the lean amine liquid containing steam into the high-pressure desorption tower; and a shell pass inlet of the high-pressure tower reboiler is connected through a raw steam input pipe to input raw steam, and a shell pass outlet of the high-pressure tower reboiler is connected with a condensed water output pipe to output condensed water.

The inner wall of the tower kettle of the high-pressure desorption tower corresponding to the lean amine liquid vapor return pipe is provided with a blocking piece, and the blocking piece can enable the lean amine liquid in the lean amine liquid containing steam input by the lean amine liquid vapor return pipe to fall to the bottom of the tower kettle of the high-pressure desorption tower and input into the heat exchangerTo heat the amine-rich liquid, and send the cooled amine-poor liquid to SO₂The absorption tower is used for carrying out heat exchange and heating on the amine-rich liquid after the amine-rich liquid is formed and then conveying the amine-rich liquid to the low-pressure desorption tower so as to complete the cycle of desorption and absorption of the amine liquid; wherein the separated steam ascends as a high-pressure desorption tower to desorb SO in the sub-lean amine liquid₂Stripping the steam required, and steam and desorbed SO₂The high-pressure desorption steam formed by the mixed gas is discharged out of the high-pressure desorption tower.

SO absorbed by the amine-rich liquid input by the low-pressure desorption tower₂20-75 g/L; SO absorbed by lean amine liquid output after desorption of the high-pressure desorption tower₂(or a hydrolysate thereof) to 5g/L or less.

Compared with the prior art, the utility model has the following advantages:

the utility model discloses a device can adopt the degree of depth desorption technology of two tower economic benefits and social benefits + low pressure boost to rich amine liquid, and rich amine liquid is whole to get into low pressure desorber (gas phase pressure 110 ~ 150KPa in the tower) and carries out desorption SO in advance₂The pre-desorption efficiency is 35-85%, and the SO desorption of a high-pressure desorption tower (the gas phase pressure in the tower is 130-190 KPa) is greatly reduced₂The load can reduce 30 to 50 percent of the consumption of the steam consumed by the desorption and stripping of the high-pressure desorption tower, and the SO of the amine-rich liquid is improved₂The desorption efficiency is 4 to 12 percent, and the method is more beneficial to the lean amine liquid (rich amine liquid desorption SO) in the high-pressure desorption tower₂Post liquid) removal of SO₂The method is more thorough, and the aim of ultralow emission of desulfurization is achieved.

The high-pressure desorption steam generated in the device of the utility model is used as the heat source of the low-pressure tower reboiler after passing through the low-pressure booster of 30-80KPa, so that the steam condensation rate of the high-pressure desorption steam in the low-pressure tower reboiler can be improved, more steam in the high-pressure desorption steam releases latent heat, and the utilization rate of secondary steam is improved by 10-20 percentage points; and the quality of the low-pressure desorption steam is greatly improved, so that the temperature and the pressure of the low-pressure desorption steam are both improved, and the low-pressure desorption steam is suitable for being used as a heat source to heat the flue gas (the temperature is increased to be more than or equal to 20 ℃) so as to play the effect of low-energy consumption temperature increase and white elimination.

The utility model discloses a carry out two tower economic benefits and social benefits and hang down pressure boost variable load operation to the rich amine liquid of organic amine desulfurization and carry out twice degree of depth desorption, separate with conventional single tower desorption technology, single tower + MVR and solveCompared with the absorption process, the absorption process is more efficient and energy-saving, and SO is absorbed by the lean amine liquid output after twice deep desorption₂To below 5g/L or rich amine liquid SO₂The total desorption efficiency is more than 90 percent, the low-supercharging frequency conversion booster fan can save 45 percent of investment, the operation is stable, the power consumption is low (the per ton steam is less than or equal to 30 KWh), the raw steam consumption is saved by 30 to 50 percent, the desorption efficiency is improved by 4 to 12 percent, and the SO removal of the flue gas is realized₂The ultra-low emission is realized, and the comprehensive cost of investment and operation is reduced by 20-40%, so the method is suitable for popularization and application.

Drawings

FIG. 1 shows that the desorption SO of the desulfurization absorbent of the present invention₂The structure of the device for efficiency is shown schematically.

Wherein: 1-high pressure desorption column; 2-high pressure desorption steam pipe; 3-low pressure desorption tower; 4-low pressure desorption steam pipe; 5, a variable-frequency booster fan; 6-hot flue gas discharge pipe; 7-cold flue gas input pipe; 8-a smoke white elimination heater; 9-low pressure column reboiler; 10-high pressure column reboiler; 11-a heat exchanger; 12-lean amine liquid output pipe; 13-a rich amine liquid input pipe; 14-condensed water output pipe; 15-raw steam input pipe; 16-high pressure condensation liquid output pipe; 17-low pressure condensation liquid output pipe; 18-preheating an amine-rich liquid input pipe; 19-a second lean amine liquid output pipe; 20-lean amine liquid input pipe; 21-lean amine liquid vapor return pipe; 22-a secondary lean amine liquid input pipe; 23-a secondary lean amine liquid vapor return pipe.

Detailed Description

The present invention will be further described with reference to the accompanying drawings and examples.

As shown in fig. 1: desorption SO for improving desulfurization absorbent₂The device comprises a high-pressure desorption tower 1, a high-pressure desorption steam pipe 2, a low-pressure desorption tower 3, a low-pressure desorption steam pipe 4, a variable-frequency booster fan 5, a hot flue gas discharge pipe 6, a cold flue gas input pipe 7, a flue gas whitening heater 8, a low-pressure tower reboiler 9, a high-pressure tower reboiler 10, a heat exchanger 11, an amine-poor liquid output pipe 12, an amine-rich liquid input pipe 13, a condensed water output pipe 14, a raw steam input pipe 15, a high-pressure condensed liquid output pipe 16, a low-pressure condensed liquid output pipe 17, a preheated amine-rich liquid input pipe 18, a secondary amine-poor liquid output pipe 19, an amine-poor liquid input pipe 20, and an amine-poor liquid steam return pipe 20A return pipe 21, a secondary lean amine liquid input pipe 22 and a secondary lean amine liquid steam return pipe 23. Wherein the high-pressure desorption tower 1 and the low-pressure desorption tower 3 are both made of stainless steel S31603, S22053, S25073 and 904L, SMO254 materials, the structure in the towers comprises a tower kettle, a steam-separating liquid-collecting box, a stripping packing layer, a groove type liquid distributor, a rectifying packing layer, a disc hole type liquid distributor and a wire mesh defogging layer from bottom to top, and the packing in the packing layer has the characteristics of high flux, high specific surface area and low resistance; the variable frequency booster fan 5 is made of materials such as S31603, S22053, S25073, S2605N, TA2 and the like, the rotating speed is less than or equal to 6000RPM, and the load is adjusted by variable frequency speed regulation; the low-pressure tower reboiler 9 and the high-pressure tower reboiler 10 are plate type heavy type made of SMO254 material or horizontal shell type made of S22053, S25073 and SMO 254; the flue gas whitening elimination heater 8 is in a plate tube type or a shell and tube type and is made of S31603 or S22053.

The device comprises a high-pressure desorption tower 1 and a low-pressure desorption tower 3 for absorbing SO₂Aqueous organic amine solutions of gases (also known as rich amine solutions, SO)₂The concentration is 20-75 g/L), and the mixture is heated and then sent into a low-pressure desorption tower 3 for pre-desorption; the bottom outlet of the low-pressure desorption tower 3 is connected with the high-pressure desorption tower 1 through a secondary lean amine liquid output pipe 19, and the secondary lean amine liquid pre-desorbed by the low-pressure desorption tower 3 is sent to the high-pressure desorption tower 1 for desorption through the secondary lean amine liquid output pipe 19; high-pressure desorption steam generated by desorption of the high-pressure desorption tower 1 is connected with the variable-frequency booster fan 5 through the high-pressure desorption steam pipe 2, so that the high-pressure desorption steam is conveyed to the variable-frequency booster fan 5 to be pressurized by 30-80KPa and is used as a heat source of a low-pressure tower reboiler 9 of the low-pressure desorption tower 3 after being heated; SO absorbed by lean amine liquid output after desorption in the high-pressure desorption tower 1₂(or hydrolysate thereof) to less than 5g/L or SO in the input amine-rich liquid₂The total desorption efficiency is greater than 90%.

For the low-pressure desorption tower 3, the pre-desorption temperature in the low-pressure desorption tower 3 is 103-110 ℃, the pre-desorption pressure is 110-150KPa, the pre-desorption efficiency of the low-pressure desorption tower 3 is 35-85%, and the volume content of steam in the low-pressure desorption steam output by the low-pressure desorption tower 3 is 85-95%, SO and the like₂The volume content is 15-5%. The groove-type liquid distributor above the stripping packing layer in the low-pressure desorption tower 3 is connected with the heat exchanger 11 through a preheated rich amine liquid input pipe 18, and the heat exchanger 11 is provided with a liquid distributorAn amine-rich liquid input pipe 13 is communicated; the top of the low-pressure desorption tower 3 is connected with a tube pass inlet of a flue gas white elimination heater 8 through a low-pressure desorption steam tube 4, a tube pass outlet of the flue gas white elimination heater 8 is connected with a low-pressure condensate output tube 17, a shell pass inlet of the flue gas white elimination heater 8 is connected with a cold flue gas input tube 7, and a shell pass outlet is connected with a hot flue gas discharge tube 6. The liquid collecting box of the steam-separating liquid collecting box below the stripping packing layer in the low-pressure desorption tower 3 is connected with the tube pass inlet of a low-pressure tower reboiler 9 through a secondary lean amine liquid input tube 22, the tube pass outlet of the low-pressure tower reboiler 9 is communicated with the tower kettle in the low-pressure desorption tower 3 below the steam-separating liquid collecting box in the low-pressure desorption tower 3 through a secondary lean amine liquid return tube 23, a blocking piece is arranged on the inner wall of the tower kettle of the low-pressure desorption tower 3 corresponding to the secondary lean amine liquid return tube 23, the blocking piece can enable the secondary lean amine liquid in the secondary lean amine liquid containing steam to fall to the bottom of the tower kettle of the low-pressure desorption tower 3 and be pumped into the high-pressure desorption tower 1 through a secondary lean amine liquid output tube 19, and the corresponding steam bypasses the blocking piece and upwards passes through the steam-separating liquid collecting box, the stripping packing layer, the rectifying packing, the wire mesh defogging layer and the like in the low-pressure desorption tower 3 and the desorbed SO₂The gas is mixed to form low-pressure desorption steam which is discharged out of the low-pressure desorption tower 3; the shell side inlet of the low-pressure tower reboiler 9 is connected with the variable-frequency booster fan 5 through a pipeline, and the shell side outlet of the low-pressure tower reboiler 9 is connected with a high-pressure condensate output pipe 16.

A corrosion-resistant delivery pump is arranged on the secondary lean amine liquid output pipe 19 to pressurize the secondary lean amine liquid, the outlet of the secondary lean amine liquid output pipe 19 is connected with a groove-type liquid distributor above a stripping packing layer in the high-pressure desorption tower 1, the desorption temperature in the high-pressure desorption tower 1 is 110-120 ℃, and the desorption pressure is 130-190 KPa; and the volume content of steam in high-pressure desorption steam generated after the high-pressure desorption tower 1 desorbs the sub-lean amine solution is 93-98 percent, and SO₂The volume content is 2-7%. The liquid collecting tank of the vapor-separating liquid collecting tank below the stripping packing layer in the high-pressure desorption tower 1 is connected with the tube side inlet of the high-pressure tower reboiler 10 through a lean amine liquid input tube 20, the tube side outlet of the high-pressure tower reboiler 10 is communicated with the tower kettle of the high-pressure desorption tower 1 below the vapor-separating liquid collecting tank in the high-pressure desorption tower 1 through a lean amine liquid return tube 21, and the high-pressure desorption tower corresponding to the lean amine liquid return tube 21A blocking piece is arranged on the inner wall of the tower kettle of the tower 1, the blocking piece can enable lean amine liquid in the lean amine liquid containing steam input by the lean amine liquid steam return pipe 21 to fall to the bottom of the tower kettle of the high-pressure desorption tower 1 and be discharged to the heat exchanger 11, and the lean amine liquid after heat exchange and cooling is sent to SO through a lean amine liquid output pipe 12₂The absorption tower is used for carrying out heat exchange and heating on the amine-rich liquid after the amine-rich liquid is formed and then conveying the amine-rich liquid to the low-pressure desorption tower 3 so as to complete the cycle of desorption and absorption of the amine liquid; wherein the separated steam bypasses the blocking piece and ascends as the high-pressure desorption tower to desorb SO in the sub-lean amine liquid₂Steam required by steam stripping flows upwards to pass through a steam-separating and liquid-collecting box, a stripping packing layer, a rectifying packing layer, a wire mesh defogging layer and the like in the high-pressure desorption tower 1 and the desorbed SO₂Discharging high-pressure desorption steam formed by the mixed gas out of the high-pressure desorption tower 1; the shell side inlet of the high pressure tower reboiler 10 is connected through a raw steam input pipe 15, and the shell side outlet of the high pressure tower reboiler 10 is connected with a condensed water output pipe 14.

When in use, SO is absorbed₂The organic amine aqueous solution (rich amine liquid for short) of the gas is sent into a heat exchanger 11 for heating through a rich amine liquid input pipe 13, and a hot side outlet of the heat exchanger 11 is connected with a groove type liquid distributor above a stripping packing layer in the low-pressure desorption tower 3 through a preheated rich amine liquid input pipe 18 so as to input the preheated rich amine liquid. The pre-desorption temperature in the low-pressure desorption tower 3 is 103-110 ℃, the pre-desorption pressure is 110-150KPa, and the preheated amine-rich liquid meets the steam generated by the low-pressure tower reboiler 9 in the low-pressure desorption tower 3 to perform steam stripping and pre-desorption to generate low-pressure desorption steam (the steam volume content is 85-95 percent, and the SO content is 85-95 percent)₂The volume content is 15-5 percent) sequentially passes through a rectification packing layer, a wire mesh defogging layer and the like and then enters a low-pressure desorption steam pipe 4 at the top of a low-pressure desorption tower 3, the low-pressure desorption steam pipe 4 is connected with a heat source inlet (optional as a pipe pass inlet) of a smoke gas whitening heater 8, low-pressure desorption steam is input into the smoke gas whitening heater 8 to be used as a heat source for heating cold smoke gas, low-temperature condensate (LP condensate) generated after the low-pressure desorption steam is cooled is output through a low-pressure condensate output pipe 17 at a cooling outlet (optional as a pipe pass outlet) of the smoke gas whitening heater 8, and a cold source inlet (optional as a shell pass inlet) of the smoke gas whitening heater 8 is connected with a cold smoke gas input pipe 7 to input cold smoke gas and a heating outlet(optionally a shell side outlet) is connected to a hot flue gas outlet pipe 6 to discharge the heated hot flue gas. Meanwhile, the sub-lean amine liquid generated after the preheated amine-rich liquid is desorbed in advance by the low-pressure desorption tower 3 enters a liquid collecting box of a steam-distributing liquid collecting box in the low-pressure desorption tower 3, the liquid collecting box is connected with a cold source inlet (which can be selected as a tube pass inlet) of a low-pressure tower reboiler 9 through a secondary lean amine liquid input pipe 22, a heating outlet (which can be selected as a tube pass outlet) of the low-pressure tower reboiler 9 is communicated with a tower kettle of a low-pressure desorption tower 3 positioned below the vapor-separating liquid collecting box through a secondary lean amine liquid return pipe 23, a blocking piece is arranged on the inner wall of the tower kettle of the low-pressure desorption tower 3 corresponding to the secondary lean amine liquid return pipe 23, SO that the sub-lean amine liquid in the sub-lean amine liquid containing steam falls to the bottom of the tower kettle of the low-pressure desorption tower 3 and is sent into the high-pressure desorption tower 1 by a pump through a sub-lean amine liquid output pipe 19, and the corresponding steam bypasses the blocking piece and goes upwards to pass through the steam separation and collection tank to be used as SO in the pre-desorption stripping rich amine liquid of the low-pressure desorption tower 3.₂The required steam; a heat source inlet (optional shell pass inlet) of the low-pressure tower reboiler 9 is connected with the high-pressure desorption tower 1 through a high-pressure desorption steam pipe 2 with a variable-frequency booster fan 5, and a cooling outlet (optional shell pass outlet) of the low-pressure tower reboiler 9 is connected with a high-pressure condensate output pipe 16 to output high-pressure condensate (HP condensate). It should be pointed out that all be equipped with the valve and the valve outside is equipped with the bypass of taking the valve on the high pressure desorption steam pipe 2 of frequency conversion booster fan 5 both sides to when preventing that frequency conversion booster fan 5 overhauls and maintains that the whole equipment can not shut down the operation.

The outlet of the secondary lean amine liquid output pipe 19 is connected with a groove type liquid distributor above a stripping packing layer in the high-pressure desorption tower 1 so as to input the secondary lean amine liquid. The desorption temperature in the high-pressure desorption tower 1 is 110-120 ℃, the desorption pressure is 130-190KPa, and the sub-lean amine liquid is desorbed by the high-pressure desorption tower 1 to generate high-pressure desorption steam (the volume content of steam is 93-98 percent, SO)₂The volume content is 2-7 percent) sequentially passes through a rectification packing layer and a silk screen demisting layer and then enters a high-pressure desorption steam pipe 2 at the top of a high-pressure desorption tower 1, the high-pressure desorption steam pipe 2 is connected with a heat source inlet (which can be selected as a shell side inlet) of a low-pressure tower reboiler 9, and the high-pressure desorption steam pipe 2 with a variable-frequency booster fan 5 can output the high-pressure desorption tower 1After the high-pressure desorption steam is pressurized to 30-80KPa, the high-pressure desorption steam is input into a low-pressure tower reboiler 9 as a heat source. Meanwhile, the lean amine liquid generated after the sub-lean amine liquid is desorbed by the high-pressure desorption tower 1 enters a liquid collecting tank of a steam-distributing liquid collecting tank in the high-pressure desorption tower 1, the liquid collecting tank is connected with a cold source inlet (optionally a tube pass inlet) of a high-pressure tower reboiler 10 through a lean amine liquid input tube 20, a heating outlet (optionally a tube pass outlet) of the high-pressure tower reboiler 10 is communicated with a tower kettle of the high-pressure desorption tower 1 positioned below the steam-distributing liquid collecting tank through a lean amine liquid return tube 21, a blocking piece is arranged on the inner wall of the tower kettle of the high-pressure desorption tower 1 corresponding to the lean amine liquid return tube 21, SO that the lean amine liquid in the lean amine liquid containing steam falls to the bottom of the tower kettle of the high-pressure desorption tower 1 and is input into a heat source inlet of the heat exchanger 11 for heat exchange and cooling, and the lean amine liquid (containing SO) is output tube 12 to output the lean amine liquid₂To below 5 g/L), the corresponding steam bypasses the blocking piece and goes upwards to pass through the steam-separating and collecting tank to be used as SO in the sub-lean amine liquid input by the output pipe 19 for desorbing the sub-lean amine liquid by the high-pressure desorption tower 1₂Stripping the required steam; a heat source inlet (optionally a shell-side inlet) of the high-pressure tower reboiler 10 is connected with a raw steam input pipe 15 to input raw steam, and a cooling outlet (optionally a shell-side outlet) of the high-pressure tower reboiler 10 is connected with a condensed water output pipe 14 to output condensed water. Two times of deep desorption are carried out to ensure that SO in the amine-rich liquid₂The total desorption efficiency is more than 90 percent or SO absorbed by lean amine liquid₂(or hydrolysate thereof) is less than or equal to 5 g/L.

Example one

The smoke gas amount of a certain multi-metal resource recovery factory is 600000Nm³/h、SO₂The concentration of the active ingredient is 12-30 g/Nm³The flue gas temperature ~ 80 ℃, flue gas pressure ~ 8.5KPa, adopt organic amine method desulfurization to combine the utility model provides a two tower economic benefits and social benefits + desorption low pressure boost variable load degree of depth desorption technology, desorption temperature in the high pressure desorber 1 is 110 ~ 120 ℃, desorption pressure is 130 ~ 190KPa, frequency conversion booster fan 5 pressure boost 45 ~ 65KPa, the temperature of desorption in advance in the low pressure desorber 3 is 105 ~ 110 ℃, desorption pressure is 135 ~ 150KPa in advance, the live steam consumption 32t/h, the tail SO of flue gas row₂The concentration is 20 mg/m³The concentration of the particles is less than or equal to 5mg/m³Power consumption load of system 2230KW, direct consumption cost about 635 yuan/ton SO₂The device is simple in arrangement, occupies less land, is simple to operate, and achieves the purposes of saving investment and reducing production and operation costs.

Example two

The smoke gas amount of a certain lead waste battery resource recovery factory is 100000+200000Nm³/h、SO₂The concentration of the active ingredient is 12-30 g/Nm³The flue gas temperature ~ 80 ℃, flue gas pressure ~ 8.0KPa, adopt organic amine method desulfurization to combine the utility model provides a two tower economic benefits and social benefits + desorption low pressure boost variable load degree of depth desorption technology, desorption temperature in the high pressure desorber 1 is 108 ~ 118 ℃, desorption pressure is 130 ~ 175KPa, frequency conversion booster fan 5 pressure boost 35 ~ 70KPa, the temperature of desorption in advance in the low pressure desorber 3 is 103 ~ 109 ℃, desorption pressure is 120 ~ 145KPa in advance, the live steam consumption 11.8t/h, the flue gas tail SO of arranging combines₂The concentration is 20 mg/m³The concentration of the particles is less than or equal to 5mg/m³The power consumption load of the system is 1130KW, and the direct consumption cost is about 680 yuan/ton SO_2，The device is simple in arrangement, small in occupied area, high in operation efficiency and simple in management and operation, and achieves the purposes of saving investment and reducing production cost.

The device of the utility model can adopt double-tower double-effect and low-supercharging twice deep desorption process for the rich amine liquid, and the rich amine liquid is totally introduced into the low-pressure desorption tower 3 (the gas phase pressure in the tower is 110 and 150 KPa) to carry out pre-desorption SO₂The pre-desorption efficiency is 35 to 85 percent, SO that the SO desorption of the high-pressure desorption tower 1 (the gas phase pressure in the tower is 130-190 KPa) is greatly reduced₂The load is reduced by 30 to 50 percent of the consumption of the steam consumed by the desorption and stripping of the high-pressure desorption tower 1, and the rich amine liquid SO is improved₂The desorption efficiency is 4 to 12 percent, and the method is more beneficial to the lean amine liquid (rich amine liquid desorption SO) in the high-pressure desorption tower 1₂Post liquid) removal of SO₂The method is more thorough, and the aim of ultralow emission of desulfurization is fulfilled; SO contained in output lean amine liquid₂To below 5g/L or rich amine liquid SO₂The total desorption efficiency is more than 90 percent, the low-supercharging frequency conversion booster fan 5 can save 45 percent of investment, the operation is stable, the power consumption is low (the per ton steam is less than or equal to 30 KWh), the raw steam consumption is saved by 30 to 50 percent, the desorption efficiency is improved by 4 to 12 percent, and the SO removal of the flue gas is realized₂The ultra-low emission is realized, and the comprehensive cost of investment and operation is reduced by 20-40%, so the method is suitable for popularization and application.

The above embodiments are only for explaining the technical idea of the present invention, and the protection scope of the present invention cannot be limited thereby, and any modification made on the basis of the technical scheme according to the technical idea provided by the present invention all fall within the protection scope of the present invention; the technology not related to the utility model can be realized by the prior art.

Claims

1. Desorption SO for improving desulfurization absorbent₂An efficient device characterized by: the device comprises a high-pressure desorption tower (1) and a low-pressure desorption tower (3) for absorbing SO₂Heating the rich amine liquid of the gas and then sending the heated rich amine liquid into a low-pressure desorption tower (3) for pre-desorption; the bottom outlet of the low-pressure desorption tower (3) is connected with the high-pressure desorption tower (1) through a secondary lean amine liquid output pipe (19), and the secondary lean amine liquid output pipe (19) feeds the secondary lean amine liquid generated after the low-pressure desorption tower (3) is pre-desorbed into the high-pressure desorption tower (1) for desorption; lean amine liquid generated by desorption of the high-pressure desorption tower (1) enters the absorption tower after heat exchange and cooling, and high-pressure desorption steam generated by desorption of the high-pressure desorption tower (1) is connected with a variable-frequency booster fan (5) through a high-pressure desorption steam pipe (2) to be used as a heat source for pre-desorption of steam required by the low-pressure desorption tower (3) after being boosted.

2. The SO desorption improving absorbent for desulfurization according to claim 1₂An efficient device characterized by: a groove type liquid distributor above a stripping packing layer in the low-pressure desorption tower (3) is connected with a heat exchanger (11) through a preheated rich amine liquid input pipe (18) so as to input preheated rich amine liquid; and the heat exchanger (11) is communicated with an amine-rich liquid input pipe (13) for inputting the amine-rich liquid.

3. The SO desorption improving absorbent for desulfurization according to claim 1₂An efficient device characterized by: the top of the low-pressure desorption tower (3) is connected with a tube pass inlet of a flue gas whitening heater (8) through a low-pressure desorption steam tube (4) so as to input low-pressure desorption steam and the flue gas whitening heater (8) ((8) The tube side outlet of the heater is connected with a low-pressure condensate outlet pipe (17) for outputting low-pressure condensate, the shell side inlet of the smoke white elimination heater (8) is connected with a cold smoke gas input pipe (7) for inputting cold smoke gas, and the shell side outlet is connected with a hot smoke gas discharge pipe (6) for discharging heated hot smoke gas.

4. The SO desorption improving absorbent for desulfurization according to claim 1₂An efficient device characterized by: a liquid collecting tank of a steam-separating liquid collecting tank below a stripping packing layer in the low-pressure desorption tower (3) is connected with a tube pass inlet of a low-pressure tower reboiler (9) through a secondary lean amine liquid input tube (22) to output secondary lean amine liquid, and a tube pass outlet of the low-pressure tower reboiler (9) is communicated with a tower kettle of the low-pressure desorption tower (3) below the steam-separating liquid collecting tank in the low-pressure desorption tower (3) through a secondary lean amine liquid steam return tube (23) to input secondary lean amine liquid containing steam into the low-pressure desorption tower (3); the shell side inlet of the low-pressure tower reboiler (9) is connected with a variable-frequency booster fan (5) through a pipeline, pressurized high-pressure desorption steam is input to serve as a heat source of the low-pressure tower reboiler (9), and the shell side outlet of the low-pressure tower reboiler (9) is connected with a high-pressure condensate output pipe (16) to output high-pressure condensate.

5. The SO desorption improvement method for the desulfurization absorbent according to claim 4₂An efficient device characterized by: a blocking piece is arranged on the inner wall of the tower kettle of the low-pressure desorption tower (3) corresponding to the secondary lean amine liquid return pipe (23), the blocking piece can enable the secondary lean amine liquid in the secondary lean amine liquid containing steam to fall to the bottom of the tower kettle of the low-pressure desorption tower (3) and be pumped into the high-pressure desorption tower (1) through a secondary lean amine liquid output pipe (19), and the corresponding steam bypasses the blocking piece and upwards passes through a steam separation and collection tank in the low-pressure desorption tower (3) to be used as the low-pressure desorption tower (3) to pre-desorb SO in the rich amine liquid₂Stripping the steam required.

6. SO desorption improvement of desulfurization absorbent according to claim 1 or 5₂An efficient device characterized by: the hypo-anemiaAn anti-corrosion delivery pump is arranged on the amine liquid output pipe (19) to deliver the sub-lean amine liquid, and the outlet of the sub-lean amine liquid output pipe (19) is connected with a groove type liquid distributor above a stripping packing layer in the high-pressure desorption tower (1).

7. The SO desorption improving absorbent for desulfurization according to claim 1₂An efficient device characterized by: a liquid collecting tank of a steam-separating liquid collecting tank below a stripping packing layer in the high-pressure desorption tower (1) is connected with a tube pass inlet of a high-pressure tower reboiler (10) through a lean amine liquid input tube (20) to output lean amine liquid, and a tube pass outlet of the high-pressure tower reboiler (10) is communicated with a tower kettle of the high-pressure desorption tower (1) below the steam-separating liquid collecting tank in the high-pressure desorption tower (1) through a lean amine liquid return tube (21) to input the lean amine liquid containing steam into the high-pressure desorption tower (1); the shell side inlet of the high-pressure tower reboiler (10) is connected through a raw steam input pipe (15) to input raw steam, and the shell side outlet of the high-pressure tower reboiler (10) is connected with a condensed water output pipe (14) to output condensed water.

8. The SO desorption improvement method for absorbent for sulfur removal according to claim 7₂An efficient device characterized by: a blocking piece is arranged on the inner wall of the tower kettle of the high-pressure desorption tower (1) corresponding to the lean amine liquid vapor return pipe (21), the blocking piece can enable the lean amine liquid in the lean amine liquid containing steam input by the lean amine liquid vapor return pipe (21) to fall to the bottom of the tower kettle of the high-pressure desorption tower (1) and input into a heat exchanger (11) for heating the lean amine liquid, and the cooled lean amine liquid is sent to SO₂The absorption tower is used for carrying out heat exchange and heating on the amine-rich liquid after the amine-rich liquid is formed and then conveying the amine-rich liquid to the low-pressure desorption tower (3), so that the circulation of amine liquid desorption and absorption is completed; wherein the separated steam ascends as a high-pressure desorption tower (1) to desorb SO in the sub-lean amine liquid₂Stripping the steam required, and steam and desorbed SO₂High-pressure desorption steam formed by the mixed gas is discharged out of the high-pressure desorption tower (1).