CN221015284U - Energy-conserving receipts water system of flue gas - Google Patents
Energy-conserving receipts water system of flue gas Download PDFInfo
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- CN221015284U CN221015284U CN202322485751.4U CN202322485751U CN221015284U CN 221015284 U CN221015284 U CN 221015284U CN 202322485751 U CN202322485751 U CN 202322485751U CN 221015284 U CN221015284 U CN 221015284U
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 200
- 239000003546 flue gas Substances 0.000 title claims abstract description 200
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 142
- 238000009833 condensation Methods 0.000 claims abstract description 86
- 230000005494 condensation Effects 0.000 claims abstract description 86
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 26
- 230000023556 desulfurization Effects 0.000 claims abstract description 26
- 238000010521 absorption reaction Methods 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims description 28
- 238000005507 spraying Methods 0.000 claims description 22
- 239000003513 alkali Substances 0.000 claims description 13
- 230000001105 regulatory effect Effects 0.000 claims description 10
- 239000007921 spray Substances 0.000 claims description 10
- 230000008676 import Effects 0.000 claims description 2
- 238000005728 strengthening Methods 0.000 claims description 2
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 abstract description 16
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Chemical compound [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 abstract description 14
- 238000010438 heat treatment Methods 0.000 abstract description 12
- 238000011084 recovery Methods 0.000 abstract description 8
- 239000002918 waste heat Substances 0.000 abstract 1
- 230000009286 beneficial effect Effects 0.000 description 18
- 238000000034 method Methods 0.000 description 18
- 230000008569 process Effects 0.000 description 18
- 239000000779 smoke Substances 0.000 description 13
- 238000001816 cooling Methods 0.000 description 10
- 239000007788 liquid Substances 0.000 description 10
- 239000012071 phase Substances 0.000 description 8
- 230000001502 supplementing effect Effects 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- 239000003344 environmental pollutant Substances 0.000 description 7
- 231100000719 pollutant Toxicity 0.000 description 7
- 239000006096 absorbing agent Substances 0.000 description 5
- 239000002253 acid Substances 0.000 description 5
- 230000008859 change Effects 0.000 description 5
- 230000002378 acidificating effect Effects 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000005057 refrigeration Methods 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 3
- 206010015137 Eructation Diseases 0.000 description 2
- 238000012824 chemical production Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 230000008570 general process Effects 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000003014 reinforcing effect Effects 0.000 description 1
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- 238000005406 washing Methods 0.000 description 1
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Abstract
The utility model relates to a flue gas energy-saving water receiving system which comprises a desulfurization absorption tower, a flue gas primary condensation tower, a flue gas secondary condensation tower and an air humidification tower which are sequentially connected, wherein the flue gas primary condensation tower is connected with a circulating water inlet and a circulating water outlet of a heat-taking heat exchanger, the air humidification tower is connected with an inlet of a refrigerating device, an outlet of the refrigerating device is connected with the flue gas secondary condensation tower, a clean flue gas outlet is arranged at the top of the flue gas secondary condensation tower, a dry air inlet is arranged at the bottom of the air humidification tower, and a wet air outlet is arranged at the bottom of the air humidification tower. This practicality adds two-stage flue gas condensing tower on former boiler and desulphurization unit's basis to and one-level air humidification tower, increase lithium bromide or lithium chloride heat pump circulation system, increase and get the heat exchanger, can realize the maximize of flue gas waste heat and utilize, can improve the heating efficiency of boiler simultaneously, the heat of recovery is mainly used heating and heating system, can realize the recovery of water simultaneously.
Description
Technical Field
The utility model relates to the technical field of flue gas treatment, in particular to an energy-saving flue gas water receiving system.
Background
The wet desulfurization technology is the most widely applied flue gas desulfurization technology, has the advantages of low investment, low operation cost, wide application range and the like, but needs to consume a large amount of process water, is difficult to bear such large water consumption in areas with lack of water resources, and does not accord with the development direction of water conservation. And a great part of consumed process water is used for cooling flue gas, and the gasification phase change of water loses a large amount of heat, and does not accord with the development direction of energy conservation.
The wet desulfurization technology utilizes desulfurization slurry and the like to realize the removal of pollutants such as SO 2、SO3, HCl, particulate matters and the like in flue gas. In the washing process, the high-temperature flue gas is cooled, releases heat and evaporates a large amount of water, the desulfurization product needs to discharge part of water, the wastewater needs to be discharged for controlling the accumulated concentration of pollutants such as chloride ions, and the wet desulfurization necessarily needs to supplement a large amount of process water. After the high-temperature flue gas is cooled, the flue gas is saturated by water, the liquid water changes phase, the flue gas contains a large amount of phase change heat, and how to recycle the low-grade latent heat of the water in the flue gas is a problem to be solved urgently at present. The heat in the high-temperature flue gas is directly utilized, and the implementation is difficult due to the problems of acid dew point and equipment materials. The clean flue gas contains a large amount of heat, but the heat quality is low and is difficult to directly convert into high-quality energy, electric energy and the like, but after the heat quality is improved by equipment such as a heat pump and the like, the clean flue gas can be used for systems requiring heating, heat supply and the like, and can also be used for heating, humidifying and the like of air to improve the heat efficiency of a boiler.
The spraying, absorbing and condensing heat exchange device applied in industry can recycle a large amount of water, is successfully applied to a plurality of power plants in north of China, adopts a plurality of spraying layers, but the current cold source used for cooling is mostly air, heat is wasted actually, and the current technology application can only achieve the purpose of collecting water and can not achieve the purpose of energy saving.
Disclosure of utility model
The utility model aims to provide the flue gas water collecting process which can improve the flue gas heat recovery efficiency, improve the flue gas water collecting effect and improve the efficiency of a boiler.
The technical scheme for solving the technical problems is as follows: the utility model provides an energy-conserving receipts water system of flue gas, includes desulfurization absorption tower, flue gas one-level condensing tower, flue gas second grade condensing tower and the air humidifying tower that connects gradually, flue gas one-level condensing tower with get circulating water import and circulating water exit linkage of heat exchanger, the air humidifying tower with refrigerating plant access connection, refrigerating plant's export with flue gas second grade condensing tower is connected, flue gas second grade condensing tower top is provided with clean flue gas export, air humidifying tower bottom is provided with dry air inlet, air humidifying tower bottom is provided with wet air outlet.
The beneficial effects of the utility model are as follows: the utility model is used for draw the low-grade heat in the flue gas, the clean flue gas after the desulfurization emits partial heat to get in the heat exchanger behind flue gas one-level condensing tower is cold at first, and in getting the heat exchanger heat release to the heat source medium again in, another part releases refrigerating plant in, release to the heat source medium again. The first-stage and second-stage flue gas condensing towers have the function of removing secondary and tertiary pollutants, and the outlet flue gas is cleaner; the two-stage heat extraction system of the first-stage and second-stage flue gas condensing towers has higher efficiency, can deeply utilize the latent heat and sensible heat in the clean flue gas, and greatly improves the heat supply and heating efficiency of the boiler; the cooling effect of direct air heat exchange is better, and the efficiency of flue gas water collection can be improved; the efficiency of the boiler can be improved by humidifying air, and the air humidifying process flow is simple and convenient; the equipment used by the whole set of device is a conventional device, is easy to implement, can realize the utilization of heat energy with large quantity and low grade in clean flue gas, can be used for heating and the like after the heat grade is improved, has good water quality of water, can be directly used for desulfurization and water supplementing, can be applied to other process systems to be used as general process water after simple physical filtration and pH value adjustment, has low soluble salt content, and can be used for boiler water supplementing and the like after treatment.
It should be noted that: the heat-taking heat exchanger can be one or more of a plate heat exchanger, a tube type heat exchanger, a shell-and-tube heat exchanger and the like. The air humidified by the air humidifying tower can be used for boiler air, and the overall heat supply efficiency of the boiler can be improved.
On the basis of the technical scheme, the utility model can be improved as follows.
Further, the top of the desulfurization absorption tower is connected with the bottom of the flue gas primary condensation tower through a gas lifting device, and the top of the flue gas secondary condensation tower is connected with the bottom of the air humidifying tower through the gas lifting device.
The beneficial effects of adopting the further scheme are as follows: the gas raising device is used for connection, so that space can be saved, and other devices can be reasonably and compactly optimally arranged according to flue gas, air, heat utilization parts and the like.
Further, the flue gas primary condensation tower, the flue gas secondary condensation tower and the air humidifying tower are internally provided with a heat exchange enhancement layer, a spraying layer and a mist removing layer from bottom to top.
The beneficial effects of adopting the further scheme are as follows: the spray layer is used for generating water for heat exchange with the flue gas, the heat exchange enhancement layer is used for enabling the water generated by the spray layer to perform full heat exchange with the flue gas, the demisting layer is used for removing water vapor in the flue gas, and meanwhile saturated water vapor in the flue gas is changed from a gas phase to a liquid phase in a phase change mode, so that the purpose of collecting water is achieved.
It should be noted that: the heat exchange enhancement layer can be one or a combination of a plurality of turbulators, a packing layer, a porous screen disc and a porous gas distribution device. The demisting layer can be one or a combination of a plurality of filter type dust collectors, flat plate type demisters, ridge type demisters, cyclone plate demisters and tube bundle type dust collectors.
Further, a circulating water inlet of the heat-taking heat exchanger is connected with an air lifting device at the bottom of the flue gas primary condensation tower, and a circulating water outlet of the heat-taking heat exchanger is connected with a water inlet of a spraying layer of the flue gas primary condensation tower.
The beneficial effects of adopting the further scheme are as follows: the circulating water after temperature rise in the flue gas primary condensation tower enters a heat-taking heat exchanger, heat is released to a heat-using medium, the temperature is reduced, and the cooled water returns to the flue gas primary condensation tower.
It should be noted that: the gas lifting device is a gas-liquid isolation device, only allows gas to pass through, but liquid cannot fall into the gas, and is a conventional device for chemical production, such as a gas lifting cap and the like.
Further, a circulating pump of the flue gas primary condensation tower is arranged between the circulating water inlet of the heat-taking heat exchanger and the gas lifting device at the bottom of the flue gas primary condensation tower.
The beneficial effects of adopting the further scheme are as follows: the circulating pump of the flue gas primary condensing tower is used for driving circulating water in the flue gas primary condensing tower to enter the heat-taking heat exchanger for heat exchange.
Further, an outlet of the flue gas primary condensing tower circulating pump is connected with a circulating water inlet of the heat-taking heat exchanger and an alkali liquor adjusting device.
The beneficial effects of adopting the further scheme are as follows: and part of water recovered by the flue gas primary condensing tower is used for recovery, and the other part of water is used for internal circulation of the flue gas primary condensing tower. The alkali liquor adjusting device is used for adjusting the pH value of the water, and the pH value is adjusted because the smoke primary condensation tower, the smoke secondary condensation tower and the air humidification tower have the secondary pollution removal effect and the circulating water is acidic or even strong acid after long-time operation.
Further, a flue gas secondary condensation tower circulating pump is connected to the bottom of the flue gas secondary condensation tower, and an outlet of the flue gas secondary condensation tower circulating pump is connected with a water inlet of a spraying layer of the air humidifying tower and the alkali liquor regulating device.
The beneficial effects of adopting the further scheme are as follows: and part of water recovered by the flue gas primary condensation tower is used for recovery, and the other part is used for humidification of the air heating tower. The alkali liquor adjusting device is used for adjusting the pH value of the water, and the pH value is adjusted because the smoke primary condensation tower, the smoke secondary condensation tower and the air humidification tower have the secondary pollution removal effect and the circulating water is acidic or even strong acid after long-time operation.
Further, the refrigerating device is a heat pump, an inlet of an evaporator of the heat pump is connected with the bottom of the air humidifying tower, and an outlet of the evaporator of the heat pump is connected with a water inlet of a spraying layer of the flue gas secondary condensing tower.
The beneficial effects of adopting the further scheme are as follows: the humidified air enters an evaporator system of the heat pump system from the bottom of the air humidifying tower, and returns to a spraying layer of the smoke secondary condensing tower after releasing heat.
It should be noted that: the heat pump is a conventional lithium bromide or lithium chloride refrigeration or heat pump process system and mainly comprises four modules, namely an absorber, an evaporator, a generator and a condenser, and a corresponding pump and pipeline system.
Further, an air humidifying tower circulating pump is arranged between the inlet of the refrigerating device and the air humidifying tower.
The beneficial effects of adopting the further scheme are as follows: the air humidifying tower circulating pump is used for conveying wet air at the bottom of the air humidifying tower to the refrigerating device.
Drawings
FIG. 1 is a schematic diagram of the structure of the present utility model;
In the drawings, the list of components represented by the various numbers is as follows:
1. The desulfurization absorption tower, 2, flue gas first-stage condensing tower, 3, flue gas second-stage condensing tower, 4, air humidifying tower, 5, flue gas first-stage condensing tower circulating pump, 6, get heat exchanger, 7, flue gas second-stage condensing tower circulating pump, 8, air humidifying tower circulating pump, 901, absorber. 902. The device comprises an evaporator 903, a generator 904, a condenser 10, an alkali liquor adjusting device 11, a heat exchange reinforcing layer 12, a spraying layer 13 and a mist removing layer.
Detailed Description
The principles and features of the present utility model are described below with reference to the drawings, the examples are illustrated for the purpose of illustrating the utility model and are not to be construed as limiting the scope of the utility model.
Examples
As shown in fig. 1, the utility model provides a flue gas energy-saving water receiving system, which comprises a desulfurization absorption tower 1, a flue gas primary condensation tower 2, a flue gas secondary condensation tower 3 and an air humidification tower 4 which are sequentially connected, wherein the flue gas primary condensation tower 2 is connected with a circulating water inlet and a circulating water outlet of a heat-taking heat exchanger 6, the air humidification tower 4 is connected with a refrigerating device inlet, an outlet of the refrigerating device is connected with the flue gas secondary condensation tower 3, a clean flue gas outlet is arranged at the top of the flue gas secondary condensation tower 3, a dry air inlet is arranged at the bottom of the air humidification tower 4, and a wet air outlet is arranged at the bottom of the air humidification tower 4.
The beneficial effects are that: the utility model is used for draw the low-grade heat in the flue gas, the clean flue gas after the desulfurization emits partial heat to get in the heat exchanger behind flue gas one-level condensing tower is cold at first, and in getting the heat exchanger heat release to the heat source medium again in, another part releases refrigerating plant in, release to the heat source medium again. The first-stage and second-stage flue gas condensing towers have the function of removing secondary and tertiary pollutants, and the outlet flue gas is cleaner; the two-stage heat extraction system of the first-stage and second-stage flue gas condensing towers has higher efficiency, can deeply utilize the latent heat and sensible heat in the clean flue gas, and greatly improves the heat supply and heating efficiency of the boiler; the cooling effect of direct air heat exchange is better, and the efficiency of flue gas water collection can be improved; the efficiency of the boiler can be improved by humidifying air, and the air humidifying process flow is simple and convenient; the equipment used by the whole set of device is a conventional device, is easy to implement, can realize the utilization of heat energy with large quantity and low grade in clean flue gas, can be used for heating and the like after the heat grade is improved, has good water quality of water, can be directly used for desulfurization and water supplementing, can be applied to other process systems to be used as general process water after simple physical filtration and pH value adjustment, has low soluble salt content, and can be used for boiler water supplementing and the like after treatment.
It should be noted that: the heat-taking heat exchanger can be one or more of a plate heat exchanger, a tube type heat exchanger, a shell-and-tube heat exchanger and the like. The air humidified by the air humidifying tower can be used for boiler air, and the overall heat supply efficiency of the boiler can be improved.
As shown in fig. 1, preferably, in an embodiment, the top of the desulfurization absorption tower 1 is connected with the bottom of the flue gas primary condensation tower 2 through a gas lift device, and the top of the flue gas secondary condensation tower 3 and the bottom of the air humidification tower 4 are connected through a gas lift device.
The beneficial effects are that: the gas raising device is used for connection, so that space can be saved, and other devices can be reasonably and compactly optimally arranged according to flue gas, air, heat utilization parts and the like.
It should be noted that: the gas lifting device is a gas-liquid isolation device, only allows gas to pass through, but liquid cannot fall into the gas, and is a conventional device for chemical production, such as a gas lifting cap and the like.
As shown in fig. 1, in the preferred embodiment, a heat exchange enhancement layer 11, a spray layer 12 and a demisting layer 13 are arranged in the flue gas primary condensation tower 2, the flue gas secondary condensation tower 3 and the air humidifying tower 4 from bottom to top.
The beneficial effects are that: the spray layer is used for generating water for heat exchange with the flue gas, the heat exchange enhancement layer is used for enabling the water generated by the spray layer to perform full heat exchange with the flue gas, the demisting layer is used for removing water vapor in the flue gas, and meanwhile saturated water vapor in the flue gas is changed from a gas phase to a liquid phase in a phase change mode, so that the purpose of collecting water is achieved.
It should be noted that: the heat exchange enhancement layer can be one or a combination of a plurality of turbulators, a packing layer, a porous screen disc and a porous gas distribution device. The demisting layer can be one or a combination of a plurality of filter type dust collectors, flat plate type demisters, ridge type demisters, cyclone plate demisters and tube bundle type dust collectors.
As shown in fig. 1, preferably, in an embodiment, a circulating water inlet of the heat-taking heat exchanger 6 is connected with a gas lifting device at the bottom of the flue gas primary condensation tower 2, and a circulating water outlet of the heat-taking heat exchanger 6 is connected with a water inlet of a spraying layer of the flue gas primary condensation tower 2.
The beneficial effects are that: the circulating water after temperature rise in the flue gas primary condensation tower enters a heat-taking heat exchanger, heat is released to a heat-using medium, the temperature is reduced, and the cooled water returns to the flue gas primary condensation tower.
As shown in fig. 1, in an embodiment, preferably, a flue gas primary condensation tower circulating pump 5 is disposed between the circulating water inlet of the heat-collecting heat exchanger 6 and the gas lifting device at the bottom of the flue gas primary condensation tower 2.
The beneficial effects are that: the circulating pump of the flue gas primary condensing tower is used for driving circulating water in the flue gas primary condensing tower to enter the heat-taking heat exchanger for heat exchange.
As shown in fig. 1, preferably, in an embodiment, the outlet of the flue gas primary condensing tower circulating pump 5 is connected with the circulating water inlet of the heat-taking heat exchanger 6 and the lye adjusting device 10.
The beneficial effects are that: and part of water recovered by the flue gas primary condensing tower is used for recovery, and the other part of water is used for internal circulation of the flue gas primary condensing tower. The alkali liquor adjusting device is used for adjusting the pH value of the water, and the pH value is adjusted because the smoke primary condensation tower, the smoke secondary condensation tower and the air humidification tower have the secondary pollution removal effect and the circulating water is acidic or even strong acid after long-time operation.
As shown in fig. 1, preferably, in an embodiment, a flue gas secondary condensation tower circulating pump 7 is connected to the bottom of the flue gas secondary condensation tower 3, and an outlet of the flue gas secondary condensation tower circulating pump 7 is connected to a water inlet of a spraying layer of the air humidifying tower 4 and the alkali liquor regulating device 10.
The beneficial effects are that: and part of water recovered by the flue gas primary condensation tower is used for recovery, and the other part is used for humidification of the air heating tower. The alkali liquor adjusting device is used for adjusting the pH value of the water, and the pH value is adjusted because the smoke primary condensation tower, the smoke secondary condensation tower and the air humidification tower have the secondary pollution removal effect and the circulating water is acidic or even strong acid after long-time operation.
As shown in fig. 1, preferably, in an embodiment, the refrigerating device is a heat pump, an inlet of an evaporator 902 of the heat pump is connected with the bottom of the air humidifying tower 4, and an outlet of the evaporator 902 of the heat pump is connected with a water inlet of a spraying layer of the flue gas secondary condensing tower 3.
The beneficial effects are that: the humidified air enters an evaporator system of the heat pump system from the bottom of the air humidifying tower, and returns to a spraying layer of the smoke secondary condensing tower after releasing heat.
It should be noted that: the heat pump is a conventional lithium bromide or lithium chloride refrigeration or heat pump process system and mainly comprises four modules, namely an absorber 901, an evaporator 902, a generator 903 and a condenser 904, and a corresponding pump and pipeline system.
As shown in fig. 1, preferably, in an embodiment, an air humidifying tower circulation pump 8 is disposed between the inlet of the refrigerating device and the air humidifying tower 4.
The beneficial effects are that: the air humidifying tower circulating pump is used for conveying wet air at the bottom of the air humidifying tower to the refrigerating device.
As shown in fig. 1, the flue gas energy-saving water receiving system comprises a desulfurization absorption tower 1, a flue gas primary condensation tower 2, a flue gas secondary condensation tower 3 and an air humidifying tower 4 which are sequentially connected. The top of the desulfurization absorption tower 1 is connected with the bottom of the flue gas primary condensation tower 2 through a gas lifting device, and the top of the flue gas secondary condensation tower 3 is connected with the bottom of the air humidifying tower 4 through a gas lifting device. The flue gas primary condensation tower 2, the flue gas secondary condensation tower 3 and the air humidification tower 4 are internally provided with a heat exchange enhancement layer 11, a spray layer 12 and a demisting layer 13 from bottom to top. The top of the flue gas secondary condensation tower 3 is provided with a clean flue gas outlet, the bottom of the air humidification tower 4 is provided with a dry air inlet, and the bottom of the air humidification tower 4 is provided with a wet air outlet.
The circulating water inlet of the heat-taking heat exchanger 6 is connected with the gas lifting device at the bottom of the flue gas primary condensation tower 2, and the circulating water outlet of the heat-taking heat exchanger 6 is connected with the water inlet of the spraying layer of the flue gas primary condensation tower 2. A flue gas primary condensation tower circulating pump 5 is arranged between the circulating water inlet of the heat-taking heat exchanger 6 and the gas lifting device at the bottom of the flue gas primary condensation tower 2.
The refrigeration device is a conventional lithium bromide heat pump system, and comprises four modules, namely an absorber 901, an evaporator 902, a generator 903 and a condenser 904, and a corresponding pump and a pipeline system, and the specific structure of the refrigeration device is the prior art and is not described herein. An inlet of the evaporator 902 of the heat pump is connected with the bottom of the air humidifying tower 4, and an outlet of the evaporator 902 of the heat pump is connected with a water inlet of the spraying layer of the flue gas secondary condensing tower 3. An air humidifying tower circulation pump 8 is provided between the inlet of the evaporator 902 and the air humidifying tower 4.
The outlet of the circulating pump 5 of the flue gas primary condensing tower is connected with the circulating water inlet of the heat-taking heat exchanger 6 and the alkali liquor regulating device 10. The bottom of the flue gas secondary condensation tower 3 is connected with a flue gas secondary condensation tower circulating pump 7, and the outlet of the flue gas secondary condensation tower circulating pump 7 is connected with a water inlet of a spraying layer of the air humidifying tower 4 and an alkali liquor regulating device 10.
When in use, the raw flue gas temperature is about 110-160 ℃, the raw flue gas enters the desulfurization absorption tower 1 for desulfurization, and the clean flue gas temperature after desulfurization is about 55-72 ℃. The desulfurized flue gas enters the bottom of the flue gas primary condensation tower 2, exchanges heat with cooled water sprayed by the spraying layer 12 at the upper part of the tower, the heat exchange happens in the space of the heat exchange strengthening layer 11 and the spraying layer 12, the heat in the flue gas comprises the sensible heat of the flue gas and the latent heat of the water, the heat is transferred to the circulating water after the heat exchange, and the temperature of the circulating water is increased. In the flue gas cooling process, the water vapor is condensed to form tiny fog drops or is adhered to liquid drops sprayed out of the spraying layer 12, part of SO 2 in the flue gas can be absorbed, and meanwhile, particles in the flue gas can be trapped for the second time. The flue gas enters the next stage after being defogged by the defogging layer 12 after heat exchange, most tiny liquid drops in the process are captured and then fall down together with the spray liquid, and a very small part of the liquid drops circulate or are discharged along with cooling flue gas, so that the purpose of collecting water is achieved, and pollutants in the flue gas are secondarily removed at the moment. The heated circulating water is subjected to heat exchange by the heat-taking heat exchanger 6, heat is released to a heat-using medium, the temperature is reduced, and the cooled water returns to the flue gas primary condensation tower 2.
The purified flue gas cooled by the flue gas primary condensation tower 2 enters the flue gas secondary condensation tower 3 for continuous condensation, a cold source is from circulating water cooled by an evaporator 902 of a lithium bromide or lithium chloride heat pump system, the purified flue gas enters the bottom of the flue gas secondary condensation tower 3 and exchanges heat with the cooled water sprayed by the spray layer 12 at the upper part of the tower, the heat exchange occurs in the space of the heat exchange enhancement layer 11 and the spray layer 12, heat in the flue gas is transferred to the circulating water after heat exchange, and the temperature of the circulating water is increased. In the flue gas cooling process, the water vapor is condensed to form tiny fog drops or is adhered to liquid drops sprayed out of the spraying layer 12, part of SO 2 in the flue gas can be absorbed, and meanwhile, the particulate matters in the flue gas can be trapped for three times. The smoke is discharged after being defogged by the defogging layer 13 after heat exchange, saturated vapor in the smoke is changed from gas phase to liquid phase in the process, the purpose of collecting water is achieved at the same time, and pollutants in the smoke are removed for three times at the moment. The circulating water in the flue gas secondary condensation tower 3 is powered by the flue gas secondary condensation tower circulating pump 7, and is firstly sent to the air humidification tower 4 for air humidification and then sent to the evaporator 902 of the lithium bromide or lithium chloride refrigerating device for cooling by the air humidification tower circulating pump 8, heat recovered from the flue gas is transferred to a heat utilization medium, and the cooled circulating water is returned to the flue gas secondary condensation tower 3.
The circulating process of the circulating water is powered by a flue gas primary condensing tower circulating pump 5, a flue gas secondary condensing tower circulating pump 7 and an air humidifying tower circulating pump 8. The cooling circulating water is heated in the flue gas primary condensing tower 2, and meanwhile, the water in the flue gas is cooled and recycled. The cooling circulating water is heated in the flue gas secondary condensing tower 3, and meanwhile, the water in the flue gas is further cooled and recycled. The cooled and recovered water is pumped to a desulfurization device for water supplementing or is sent to a water-collecting buffer tank for water supplementing and water supplementing of the process by an external drainage pump.
A part of the heat medium of the heat utilization system is used for removing heat from the heat-removing heat exchanger 6, the heat discharged by the flue gas primary condensation tower 2 is removed, and the other part of the heat medium of the heat utilization system is used for removing heat from the absorber 901 and the condenser 903 of the lithium bromide or lithium chloride heat pump system and then is mixed with the heat medium of the heat utilization system 6, and then the mixed heat is returned to the heat utilization system, wherein the generator of the lithium bromide or lithium chloride heat pump system can adopt steam or high-temperature flue gas. The air humidified by the air humidifying tower 4 is taken to a boiler for boiler air supply. The air heater 6 can be reasonably adjusted according to the process requirement and the change of the local temperature, the heating dosage is controlled, the temperature and the humidity of the air are regulated, the heat efficiency of the whole system is highest, and the purposes of energy saving and water collection are achieved.
The flue gas primary condensation tower 2 is connected with the top end outlet of the desulfurization absorption tower 1 through a flue, water is received by the flue gas primary condensation tower 2 and enters the flue gas secondary condensation tower 2, and meanwhile, secondary and tertiary trapping of pollutants and particulate matters is realized; the flue gas primary condensation tower 1 and the flue gas secondary condensation tower 2 are provided with flue gas condensate water at the bottom of the tower, are regulated by pipelines and are used for supplementing water for a desulfurization device, and can be discharged to a water receiving buffer tank to supply process water by an external drainage pump, and an alkali liquor regulating system is arranged at the same time and is used for regulating the pH value of recovery.
In the description of the present utility model, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present utility model and simplifying the description, and do not indicate or imply that the device or element being referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present utility model.
In the present utility model, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; either directly or indirectly, through intermediaries, or both, may be in communication with each other or in interaction with each other, unless expressly defined otherwise. The specific meaning of the above terms in the present utility model can be understood by those of ordinary skill in the art according to the specific circumstances.
While embodiments of the present utility model have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the utility model, and that variations, modifications, alternatives and variations may be made to the above embodiments by one of ordinary skill in the art within the scope of the utility model.
Claims (9)
1. The utility model provides an energy-conserving water system of receiving of flue gas, its characterized in that, including desulfurization absorption tower (1), flue gas one-level condensing tower (2), flue gas second grade condensing tower (3) and air humidifying tower (4) that connect gradually, flue gas one-level condensing tower (2) are with the circulating water import and the circulating water exit linkage who gets heat exchanger (6), air humidifying tower (4) and refrigerating plant access connection, refrigerating plant's export with flue gas second grade condensing tower (3) are connected, flue gas second grade condensing tower (3) top is provided with clean flue gas export, air humidifying tower (4) bottom is provided with dry air inlet, air humidifying tower (4) bottom is provided with wet air outlet.
2. The flue gas energy-saving water receiving system according to claim 1, wherein the top of the desulfurization absorption tower (1) is connected with the bottom of the flue gas primary condensation tower (2) through a gas lifting device, and the top of the flue gas secondary condensation tower (3) is connected with the bottom of the air humidification tower (4) through a gas lifting device.
3. The flue gas energy-saving water receiving system according to claim 2, wherein the flue gas primary condensation tower (2), the flue gas secondary condensation tower (3) and the air humidification tower (4) are internally provided with a heat exchange strengthening layer (11), a spraying layer (12) and a demisting layer (13) from bottom to top.
4. A flue gas energy-saving water receiving system according to claim 3, wherein the circulating water inlet of the heat-taking heat exchanger (6) is connected with a gas lifting device at the bottom of the flue gas primary condensation tower (2), and the circulating water outlet of the heat-taking heat exchanger (6) is connected with the water inlet of the spraying layer of the flue gas primary condensation tower (2).
5. The flue gas energy-saving water receiving system according to claim 4, wherein a flue gas primary condensation tower circulating pump (5) is arranged between the circulating water inlet of the heat-taking heat exchanger (6) and the gas lifting device at the bottom of the flue gas primary condensation tower (2).
6. The flue gas energy-saving water receiving system according to claim 5, wherein the outlet of the flue gas primary condensing tower circulating pump (5) is connected with the circulating water inlet of the heat-taking heat exchanger (6) and the alkali liquor regulating device (10).
7. The flue gas energy-saving water receiving system according to claim 6, wherein the bottom of the flue gas secondary condensation tower (3) is connected with a flue gas secondary condensation tower circulating pump (7), and the outlet of the flue gas secondary condensation tower circulating pump (7) is connected with the water inlet of the spraying layer of the air humidifying tower (4) and the alkali liquor regulating device (10).
8. A flue gas energy saving water receiving system according to claim 3, wherein the refrigerating device is a heat pump, an inlet of an evaporator (902) of the heat pump is connected with the bottom of the air humidifying tower (4), and an outlet of the evaporator (902) of the heat pump is connected with a water inlet of a spray layer of the flue gas secondary condensing tower (3).
9. The flue gas energy-saving water receiving system according to claim 1, wherein an air humidifying tower circulating pump (8) is arranged between the inlet of the refrigerating device and the air humidifying tower (4).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN118598252A (en) * | 2024-06-18 | 2024-09-06 | 昊姆（上海）节能科技有限公司 | A high-salt sewage purification double-stage tower system and high-salt sewage purification method |
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2023
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN118598252A (en) * | 2024-06-18 | 2024-09-06 | 昊姆（上海）节能科技有限公司 | A high-salt sewage purification double-stage tower system and high-salt sewage purification method |
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