A steam jet energy-saving device for ion liquid desulfurization

Abstract

The utility model relates to the field of environmental protection technology discloses a kind of steam injection energy-saving devices for ionic liquid desulfurization, including regenerator, regenerator side is connected with steam injection energy-saving assembly by pipeline, injection energy-saving assembly includes steam ejector, the outlet of steam ejector is connected with the middle part of regenerator side, the two steam inlets of steam ejector are connected with the steam outlet of evaporator and the steam outlet of flash tank top respectively, the lean liquid outlet of regenerator bottom is connected with the upper end side of flash tank, the other end of flash tank opposite regenerator is connected with evaporator, the two outlets of the lower part and bottom of flash tank are connected with the side inlet of lean-liquid heat exchanger and lean-liquid reheater respectively, the outlet of lean-liquid regeneration gas other side is connected with evaporator, lean-liquid heat exchanger is connected with rich-liquid reheater between regenerator, by adding a set of steam injection energy-saving device, to reduce the steam consumption of existing regenerative system, thereby greatly reduce the effect of sulfur system operating cost.

Description

Technical Field

[0001] This utility model relates to the field of environmental protection technology, and in particular to a steam jet energy-saving device for ion liquid desulfurization. Background Technology

[0002] With increasingly stringent environmental protection requirements, the state has also put forward energy-saving and consumption-reducing requirements for newly built desulfurization environmental protection facilities, such as saving electricity, water, and steam. For ion-liquid desulfurization units, their high steam consumption and high operating costs have increased the burden on many enterprises and limited the promotion and development of ion-liquid desulfurization technology. Utility Model Content

[0003] The purpose of this invention is to provide a steam injection energy-saving device for ion liquid desulfurization, which can reduce the steam consumption of the existing regeneration system by adding a steam injection energy-saving device, thereby greatly reducing the operating cost of the sulfur system.

[0004] The above-mentioned technical objective of this utility model is achieved through the following technical solution: A regeneration tower is included, one side of which is connected to a steam jet energy-saving component via a pipeline. The steam jet energy-saving component includes a steam ejector, the outlet of which is connected to the middle of one side of the regeneration tower. Two steam inlets of the steam ejector are respectively connected to the steam outlet of the evaporator and the steam outlet at the top of the flash tank. One side of the upper end of the flash tank is connected to the lean liquid outlet at the bottom of the regeneration tower. The other end of the flash tank opposite the regeneration tower is connected to the evaporator. Two outlets at the lower and bottom of the flash tank are respectively connected to one side inlets of a lean-rich liquid heat exchanger and a lean liquid reheater. The outlet on the other side of the lean liquid regeneration gas is connected to the evaporator. A rich liquid reheater is connected between the lean-rich liquid heat exchanger and the regeneration tower, and the rich liquid reheater is connected to the upper part of one side of the regeneration tower.

[0005] A further feature of this invention is that the steam ejector includes an intake chamber, a mixing chamber, and a diffusion chamber. The inlets on opposite sides of the intake chamber are connected to the evaporator and the flash tank, respectively, and the outlet of the diffusion chamber is connected to the regeneration tower via a pipeline.

[0006] A further feature of this invention is that the gas outlet at the top of the regeneration tower is connected to a rich liquid reheater and a lean liquid reheater, respectively. The outlets of the rich liquid reheater and the lean liquid reheater are both connected to the same pipe and then connected to a regeneration gas condenser. The other end of the regeneration gas condenser is connected to a gas-liquid separator.

[0007] A further feature of this invention is that the outlet at the bottom of the gas-liquid separator is connected to the reflux liquid heat exchanger, the outlet of the reflux liquid heat exchanger is connected to the upper end of the regeneration tower, and the inlet on one side of the reflux unit is connected to the outlet of the reboiler.

[0008] A further feature of this invention is that an outlet connected to a reboiler is provided on one side of the regeneration tower relative to the steam ejector, and the outlet of the reboiler is connected to the regeneration tower via a pipe.

[0009] A further feature of this invention is that the vertical position of the inlet of the reflux heat exchanger connected to the regeneration tower via a pipe is higher than the inlet of the rich liquid reheater connected to the regeneration tower via a pipe.

[0010] A further feature of this invention is that the gas outlet at the top of the regeneration tower is directly connected to the regeneration gas condenser via a pipeline.

[0011] A further feature of this invention is that a reflux pump is provided between the gas-liquid separator and the reflux heat exchanger.

[0012] A further feature of this invention is that a flash pump is provided between the flash tank and the lean reheater.

[0013] A further feature of this invention is that a lean liquid pump is provided between the flash tank and the lean / rich liquid reheater.

[0014] The beneficial effects of this utility model are:

[0015] 1. Based on the characteristics of steam jet pumps and desulfurization regeneration processes, this technology employs a steam jet regeneration process. High-temperature, high-pressure working steam undergoes adiabatic expansion inside the nozzle of the steam ejector, with its velocity continuously increasing and pressure continuously decreasing, reaching supersonic speeds at the nozzle outlet, forming a relatively low-pressure / negative-pressure zone. Due to the shearing effect of this low-pressure zone at the nozzle outlet, ejected steam enters the suction chamber. Specifically, flash steam generated from the flash evaporation of lean liquid in the flash tank and regeneration steam from the evaporator outlet enter the suction chamber from opposite sides of the steam ejector. After complex mixing in isobaric and isoarea mixing chambers, the velocity of the mixed steam continuously decreases while its pressure continuously increases in the diffusion chamber, pressurizing the ejected steam at the steam ejector outlet. The pressurized steam is then injected into the ion-liquid desulfurization regeneration tower, thus achieving secondary utilization of the regeneration gas. By incorporating energy-saving steam jet components, the reuse of secondary steam is achieved, correspondingly reducing the amount of live steam required by the original desulfurization regeneration system, resulting in overall steam savings.

[0016] 2. The lean liquor at the bottom of the regeneration tower is sent to the flash tank. After flash evaporation in the flash tank, the lean liquor exits from the bottom and is pressurized by the lean liquor pump and sent to the lean-rich liquor heat exchanger to exchange heat with the rich liquor from the adsorption tank. The temperature of the rich liquor from the adsorption tank is still low. If it enters the regeneration tower directly, a large amount of steam heat from the reboiler is required to reach the desorption temperature, resulting in high energy consumption. The regeneration gas discharged from the top of the regeneration tower is at a high temperature and carries a large amount of waste heat. The high-temperature gas passes through the lean liquor reheater and the rich liquor reheater to heat the liquid to be treated and the rich liquor entering the lean liquor reheater and the rich liquor reheater. "Waste heat reuse" is achieved through heat exchange.

[0017] 3. After the regenerated gas at the top of the tower is cooled by the lean liquid reheater and the rich liquid reheater, although the temperature decreases, it still contains a large amount of water vapor. Cooling medium needs to be introduced into the condenser to further reduce the temperature of the regenerated gas. After being separated by the gas-liquid separator, the purified SO2 can be sent to the acid production process for recycling, realizing resource reuse, reducing waste emissions, and avoiding pollution caused by direct discharge. The condensate enters the reflux liquid heat exchanger through the reflux pump and exchanges heat with the steam condensate from the reboiler. In this process, the reflux liquid absorbs heat and its temperature rises, while the steam condensate is cooled and its temperature decreases. For the reflux liquid, the heated reflux liquid is more adaptable to the temperature environment inside the tower when it enters the regeneration tower, which is conducive to the mass and heat transfer process inside the tower and improves the operating efficiency of the regeneration tower.

[0018] 4. In the regeneration tower, the rich liquid descends and the gas phase rises, making countercurrent contact. Although partial desorption can be achieved, the temperature gradient within the tower limits the temperature in the upper part of the tower to a lower level. The heat from the rising gas phase alone is insufficient to completely evaporate the rich liquid. Therefore, a significant amount of the target component remains in the rich liquid in the lower part of the tower. After the rich liquid at the bottom of the tower is sent to the reboiler, it can be directly heated by external low-pressure saturated steam to raise the temperature of the rich liquid to a level close to the boiling point. At this point, the component can completely evaporate from the liquid phase to the gas phase, ultimately generating a qualified lean liquid. Attached Figure Description

[0019] To more clearly illustrate the technical solutions in the embodiments of this utility model, the drawings used in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0020] Figure 1 This is a schematic diagram of the structure of this utility model.

[0021] Figure 2 This is a cross-sectional structural diagram of the steam ejector in this utility model.

[0022] In the diagram, 1 is the regeneration tower; 2 is the steam ejector; 21 is the suction chamber; 22 is the mixing chamber; 23 is the diffusion chamber; 3 is the evaporator; 4 is the flash tank; 5 is the lean and rich liquid heat exchanger; 6 is the lean liquid reheater; 7 is the rich liquid reheater; 8 is the regeneration gas condenser; 9 is the gas-liquid separator; 10 is the reflux liquid heat exchanger; 11 is the reboiler; 12 is the reflux pump; 13 is the flash pump; and 14 is the lean liquid pump. Detailed Implementation

[0023] The technical solution of this utility model will now be clearly and completely described with reference to specific embodiments. Obviously, the described embodiments are only a part of the embodiments of this utility model, and not all of them. All other embodiments obtained by those skilled in the art based on the embodiments of this utility model without creative effort are within the scope of protection of this utility model.

[0024] Example: A steam injection energy-saving device for ion liquid desulfurization, such as... Figure 1-2As shown, the system includes a regeneration tower 1. One side of the regeneration tower 1 is connected to a steam jet energy-saving component via a pipe. The steam jet energy-saving component includes a steam ejector 2. The outlet of the steam ejector 2 is connected to the middle of one side of the regeneration tower 1. The two steam inlets of the steam ejector 2 are respectively connected to the steam outlet of the evaporator 3 and the steam outlet at the top of the flash tank 4. One side of the upper end of the flash tank 4 is connected to the lean liquid outlet at the bottom of the regeneration tower 1. The other end of the flash tank 4 opposite to the regeneration tower 1 is connected to the evaporator 3. The two outlets at the bottom and lower part of the flash tank 4 are respectively connected to one side inlet of the lean-rich liquid heat exchanger 5 and the lean liquid reheater 6. The outlet of the lean liquid regeneration gas on the other side is connected to the evaporator 3. The lean-rich liquid heat exchanger 5 is connected to the regeneration tower. A rich liquid reheater 7 is connected between the two parts. The rich liquid reheater 7 is connected to the upper part of one side of the regeneration tower 1. The steam ejector 2 includes an intake chamber 21, a mixing chamber 22 and a diffusion chamber 23. The inlets on opposite sides of the intake chamber 21 are connected to the evaporator 3 and the flash tank 4, respectively. The outlet of the diffusion chamber 23 is connected to the regeneration tower 1 through a pipe. The flash steam generated by the flash evaporation of the lean liquid in the flash tank 4 and the regeneration steam from the outlet of the evaporator 3 enter the intake chamber 21 from both sides of the steam ejector 2. After complex mixing in the isobaric and isoarea mixing chamber 22, the velocity of the mixed steam continuously decreases and the pressure continuously increases in the diffusion chamber 23. The pressurization of the ejector steam is completed at the outlet of the steam ejector 2. The pressurized steam is injected into the ion liquid desulfurization regeneration tower 1, thereby realizing the secondary utilization of regeneration gas. By setting up a steam injection energy-saving component, the secondary steam is reused, and the amount of live steam required by the original desulfurization regeneration system is reduced accordingly, thus saving steam overall. At the same time, the lean liquid at the bottom of the regeneration tower 1 is sent to the flash tank 4. The lean liquid after flashing in the flash tank 4 exits from the bottom and is pressurized by the lean liquid pump 14 and sent to the lean-rich liquid heat exchanger 5 to exchange heat with the rich liquid from the adsorption tank. The temperature of the rich liquid from the adsorption tank at the front end is still low. If it directly enters the regeneration tower 1, a large amount of steam heat from the reboiler 11 is required to reach the desorption temperature, resulting in high energy consumption. The regeneration gas discharged from the top of the regeneration tower 1 is at a high temperature and carries a large amount of waste heat. The high-temperature gas passes through the lean liquid reheater 6 and the rich liquid reheater 7 to heat the liquid to be treated and the rich liquid entering the lean liquid reheater 6 and the rich liquid reheater 7, thus realizing "waste heat reuse" through heat exchange.

[0025] like Figure 1As shown, the gas outlet at the top of regeneration tower 1 is connected to both the rich liquid reheater 7 and the lean liquid reheater 6. The outlets of both reheaters 7 and 6 are connected to the same pipe and then to the regeneration gas condenser. The other end of the regeneration gas condenser is connected to the gas-liquid separator 9. The outlet at the bottom of the gas-liquid separator 9 is connected to the reflux heat exchanger 10. The outlet of the reflux heat exchanger 10 is connected to the upper end of regeneration tower 1. The vertical position of the inlet of the reflux heat exchanger 10, which is connected to regeneration tower 1 via a pipe, is higher than the inlet of the rich liquid reheater 7. The inlet on one side of the reflux heat exchanger is connected to the outlet of reboiler 11. After being cooled by the lean liquid reheater 6 and the rich liquid reheater 7, the temperature of the regeneration gas at the top of the tower... The temperature of the regenerated gas is reduced, but it still contains a large amount of water vapor. Cooling medium needs to be introduced into the condenser to further reduce the temperature of the regenerated gas. After being separated by the gas-liquid separator 9, the purified SO2 can be sent to the acid production process for recycling, realizing resource reuse, reducing waste emissions, and avoiding pollution caused by direct discharge. The condensate enters the reflux liquid heat exchanger 10 through the reflux pump 12 and exchanges heat with the steam condensate from the reboiler 11. In this process, the reflux liquid absorbs heat and its temperature rises, while the steam condensate is cooled and its temperature decreases. For the reflux liquid, the heated reflux liquid can better adapt to the temperature environment inside the regeneration tower 1, which is conducive to the mass and heat transfer process inside the tower and improves the operating efficiency of the regeneration tower 1.

[0026] like Figure 1 As shown, the regeneration tower 1, relative to the steam ejector 2, has an outlet connected to the reboiler 11. The outlet of the reboiler 11 is connected to the regeneration tower 1 through a pipe. In the regeneration tower 1, the rich liquid descends and the gas phase rises, making countercurrent contact. Although partial desorption can be achieved, the temperature in the upper part of the tower is relatively low due to the temperature gradient in the tower. The heat from the rising gas phase alone is insufficient to completely evaporate the rich liquid. Therefore, a large amount of target components remain in the rich liquid in the lower part of the tower. After the rich liquid at the bottom of the tower is sent to the reboiler 11, it can be directly heated by the external low-pressure saturated steam to raise the temperature of the rich liquid to a level close to the boiling point. At this time, the target liquid can be completely evaporated from the liquid phase to the gas phase, and finally a qualified lean liquid is generated.

[0027] like Figure 1 As shown, the gas outlet at the top of regeneration tower 1 is also directly connected to the regeneration gas condenser via a pipe.

[0028] like Figure 1 As shown, a reflux pump 12 is installed between the gas-liquid separator 9 and the reflux heat exchanger, a flash pump 13 is installed between the flash tank 4 and the lean liquor reheater 6, and a lean liquor pump 14 is installed between the flash tank 4 and the lean and rich liquor reheater 7. The use of various pump bodies is beneficial to improving the material conveying efficiency.

[0029] Working principle of a steam jet energy-saving device for ion liquid desulfurization:

[0030] The lean liquor at the bottom of regeneration tower 1 is sent to flash tank 4. After flash evaporation in flash tank 4, the lean liquor exits from the bottom and is pressurized by lean liquor pump 14 and sent to lean-rich liquor heat exchanger 5 to exchange heat with the rich liquor from adsorption tank. The temperature of the rich liquor from the adsorption tank is still low. If it enters regeneration tower 1 directly, a large amount of steam heat from reboiler 11 is required to reach the desorption temperature, resulting in high energy consumption. The regeneration gas discharged from the top of regeneration tower 1 is at a high temperature and carries a large amount of waste heat. The high-temperature gas passes through lean liquor reheater 6 and rich liquor reheater 7 to heat the liquid to be treated and the rich liquor entering lean liquor reheater 6 and rich liquor reheater 7, thus realizing "waste heat reuse" through heat exchange.

[0031] After the regenerated gas at the top of the tower is cooled by the lean liquid reheater 6 and the rich liquid reheater 7, although the temperature decreases, it still contains a large amount of water vapor. Cooling medium needs to be introduced into the condenser to further reduce the temperature of the regenerated gas. After being separated by the gas-liquid separator 9, the purified SO2 can be sent to the acid production process for recycling, realizing resource reuse, reducing waste emissions, and avoiding pollution caused by direct discharge. The condensate enters the reflux liquid heat exchanger 10 through the reflux pump 12 and exchanges heat with the steam condensate from the reboiler 11. In this process, the reflux liquid absorbs heat and its temperature rises, while the steam condensate is cooled and its temperature decreases. For the reflux liquid, the heated reflux liquid entering the regeneration tower 1 is more adapted to the temperature environment inside the tower, which is conducive to the mass and heat transfer process inside the tower and improves the operating efficiency of the regeneration tower 1.

[0032] In regeneration tower 1, the rich liquid descends while the gas phase rises, forming a countercurrent contact. Although this allows for partial desorption, the temperature gradient within the tower limits the temperature in the upper part, making it difficult for the rich liquid to completely evaporate using only the heat from the rising gas phase. As a result, a significant amount of the target components remain in the rich liquid in the lower part of the tower. After the rich liquid at the bottom of the tower is fed into reboiler 11, it can be directly heated by external low-pressure saturated steam, raising its temperature to near the boiling point. At this point, the components can completely evaporate from the liquid phase to the gas phase, ultimately generating a qualified lean liquid.

[0033] The flash steam generated by the flash evaporation of lean liquid in flash tank 4 and the regenerated steam from the outlet of evaporator 3 enter the suction chamber 21 from both sides of steam ejector 2. After complex mixing in isobaric and isoarea mixing chambers 22, the velocity of the mixed steam continuously decreases and the pressure continuously increases in diffusion chamber 23, thus pressurizing the ejected steam at the outlet of steam ejector 2. The pressurized steam is then injected into the ion liquid desulfurization regeneration tower 1, thereby realizing the secondary utilization of regenerated gas. By setting up steam injection energy-saving components, the secondary steam is reused, and the amount of live steam required by the original desulfurization regeneration system is correspondingly reduced, resulting in overall steam saving.

Claims

1. A steam injection energy-saving device for ion liquid desulfurization, comprising a regeneration tower (1), characterized in that: One side of the regeneration tower (1) is connected to the steam jet energy-saving component via a pipe. The steam jet energy-saving component includes a steam ejector (2). The outlet of the steam ejector (2) is connected to the middle of one side of the regeneration tower (1). The two steam inlets of the steam ejector (2) are respectively connected to the steam outlet of the evaporator (3) and the steam outlet at the top of the flash tank (4). One side of the upper end of the flash tank (4) is connected to the lean liquid outlet at the bottom of the regeneration tower (1). The other end of the flash tank (4) opposite to the regeneration tower (1) is connected to the evaporator (3). The two outlets at the bottom of the flash tank (4) are respectively connected to one side inlet of the lean and rich liquid heat exchanger (5) and the lean liquid reheater (6). The outlet on the other side of the lean liquid regeneration gas is connected to the evaporator (3). A rich liquid reheater (7) is connected between the lean and rich liquid heat exchanger (5) and the regeneration tower (1). The rich liquid reheater (7) is connected to the upper part of one side of the regeneration tower (1).

2. The steam injection energy-saving device for ion liquid desulfurization according to claim 1, characterized in that: The steam ejector (2) includes an intake chamber (21), a mixing chamber (22) and a diffusion chamber (23). The inlets on opposite sides of the intake chamber (21) are connected to the evaporator (3) and the flash tank (4) respectively. The outlet of the diffusion chamber (23) is connected to the regeneration tower (1) through a pipeline.

3. The steam injection energy-saving device for ion liquid desulfurization according to claim 2, characterized in that: The gas outlet at the top of the regeneration tower (1) is connected to the rich liquid reheater (7) and the lean liquid reheater (6) respectively. The outlets of the rich liquid reheater (7) and the lean liquid reheater (6) are connected to the same pipeline and then connected to the regeneration gas condenser. The other end of the regeneration gas condenser is connected to the gas-liquid separator (9).

4. The steam injection energy-saving device for ion liquid desulfurization according to claim 3, characterized in that: The outlet at the bottom of the gas-liquid separator (9) is connected to the reflux heat exchanger (10), the outlet of the reflux heat exchanger (10) is connected to the upper end of the regeneration tower (1), and the inlet on one side of the regeneration tower (1) is connected to the outlet of the reboiler (11).

5. A steam injection energy-saving device for ion liquid desulfurization according to claim 4, characterized in that: An outlet connected to a reboiler (11) is provided on the side of the regeneration tower (1) opposite to the steam ejector (2), and the outlet of the reboiler (11) is connected to the regeneration tower (1) via a pipe.

6. A steam injection energy-saving device for ion liquid desulfurization according to claim 5, characterized in that: The vertical position of the inlet of the reflux heat exchanger (10) connected to the regeneration tower (1) via a pipe is higher than the inlet of the rich liquid reheater (7) connected to the regeneration tower (1) via a pipe.

7. A steam injection energy-saving device for ion liquid desulfurization according to claim 6, characterized in that: The gas outlet at the top of the regeneration tower (1) is also directly connected to the regeneration gas condenser via a pipeline.

8. A steam injection energy-saving device for ion liquid desulfurization according to claim 7, characterized in that: A reflux pump (12) is provided between the gas-liquid separator (9) and the reflux heat exchanger.

9. A steam injection energy-saving device for ion liquid desulfurization according to claim 8, characterized in that: A flash pump (13) is provided between the flash tank (4) and the lean liquor reheater (6).

10. A steam injection energy-saving device for ion liquid desulfurization according to claim 9, characterized in that: A lean liquid pump (14) is provided between the flash tank (4) and the lean and rich liquid reheater (7).

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