CN110314527B - Device and method for wet desulphurization of high-temperature flue gas - Google Patents
Device and method for wet desulphurization of high-temperature flue gas Download PDFInfo
- Publication number
- CN110314527B CN110314527B CN201910715749.7A CN201910715749A CN110314527B CN 110314527 B CN110314527 B CN 110314527B CN 201910715749 A CN201910715749 A CN 201910715749A CN 110314527 B CN110314527 B CN 110314527B
- Authority
- CN
- China
- Prior art keywords
- flue gas
- water
- temperature
- heat
- heat exchanger
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention provides a device and a method for wet desulphurization of high-temperature flue gas, which utilize condensed water to cool circulating liquid of a desulphurization tower, utilize a heat pump technology to reduce the temperature of the flue gas, condense more than 90% of water vapor in the flue gas, greatly improve the unsaturation degree of the flue gas, eliminate the phenomenon of white smoke, remove more than 80% of pollutants in purified flue gas when the water vapor is condensed and condensed, realize the clean emission of the flue gas, and recycle the waste heat in the flue gas by utilizing a heat pump to prepare heat supply water with the temperature of more than 60 ℃. Meanwhile, the temperature of the flue gas entering the desulfurizing tower is reduced, so that the size of the used desulfurizing tower can be reduced.
Description
Technical Field
The invention relates to the technical field of flue gas desulfurization, in particular to a device and a method for wet desulfurization of high-temperature flue gas.
Background
In electric power and petrochemical industry, the flue gas that burning production such as boiler, catalytic cracking device generally can discharge the air through wet flue gas desulfurization process's processing, and the flue gas temperature after the desulfurization reduces, and the moisture content is high, and the vapor in the flue gas is in the saturated condition, still carries micro fine particulate matter, and after discharging into the atmosphere, meeting cold can produce a large amount of tiny water drops and form white smoke, and then combines to form the haze with fine particulate matter, brings harm to environment and people's physical and mental health.
At present, the treatment of flue gas after wet desulphurization mainly adopts a method of condensation and reheating. The condensation is to reduce the moisture content of the flue gas and simultaneously reduce the concentration of fine particle pollutants by cooling the flue gas; the reheating is to improve the unsaturation degree of the flue gas by heating the flue gas, and the white smoke phenomenon can be weakened after the flue gas enters a chimney and is discharged into the atmosphere.
The prior art only solves the problem of white smoke of the desulfurized flue gas to a certain extent, the purified flue gas after treatment still contains a certain amount of water vapor, and the white smoke phenomenon still can occur in the purified flue gas after treatment in rainy days or when the environmental temperature is lower. And the condensation method and the reheating method do not fully utilize the waste heat in the flue gas, the condensation method has the problem of discharge of secondary pollutants such as waste water and the like, and the reheating method has the defects of high energy consumption and additional auxiliary heat energy.
In view of the above, the present invention is particularly proposed.
Disclosure of Invention
The first purpose of the invention is to provide a device for wet desulphurization of high-temperature flue gas, which completely or partially solves the problems, the device utilizes condensed water to cool the circulating liquid of a desulphurization tower, utilizes a heat pump technology to reduce the temperature of the flue gas, can condense more than 90% of water vapor in the flue gas, greatly improves the unsaturation degree of the flue gas, eliminates the phenomenon of white smoke, can remove more than 80% of pollutants in the purified flue gas when the water vapor is condensed and condensed, realizes the clean emission of the flue gas, and recovers the waste heat in the flue gas by utilizing a heat pump to prepare the heating water with the temperature of more than 60 ℃. Meanwhile, the temperature of the flue gas entering the desulfurizing tower is reduced, so that the size of the used desulfurizing tower can be reduced.
The second purpose of the invention is to provide a wet desulphurization method for high-temperature flue gas, which adopts the modes of cooling before desulphurization and cooling flue gas after desulphurization, reduces the temperature of the purified flue gas to be below 20 ℃, condenses more than 90% of water vapor in the purified flue gas, greatly improves the unsaturation degree of the flue gas, eliminates the phenomenon of white smoke, and can remove more than 80% of pollutants in the purified flue gas when the water vapor is condensed and condensed, thereby realizing clean emission of the flue gas.
In order to achieve the above purpose of the present invention, the following technical solutions are adopted:
a device for wet desulphurization of high-temperature flue gas comprises a desulphurization tower, a water-flue gas heat exchanger, a generator, a condenser, an evaporator, an absorber, a heat pump heat exchanger and a flue gas discharge device;
the generator comprises a flue gas inlet, a flue gas outlet, a water vapor outlet, a refrigerant outlet and a refrigerant inlet;
a smoke outlet of the generator is connected with a smoke inlet of the water-smoke heat exchanger, a water vapor outlet of the generator is connected with a water vapor inlet of the condenser, and a refrigerant outlet and a refrigerant inlet of the generator are respectively connected with a refrigerant inlet and a refrigerant outlet of the absorber;
a refrigerant is arranged in the generator and circulates between the generator and the absorber;
the water inlet of the water-smoke heat exchanger is connected with a normal-temperature water pipe;
the water outlet of the water-flue gas heat exchanger is connected with the water inlet of the absorber;
the flue gas outlet of the water-flue gas heat exchanger is connected with the desulfurizing tower;
the water outlet of the absorber is connected with the water inlet of the condenser, and the water inlet of the absorber is connected with the water outlet of the heat pump heat exchanger;
the flue gas outlet of the desulfurizing tower is connected with the flue gas inlet of the evaporator;
the flue gas outlet of the evaporator is connected with the flue gas inlet of the condenser;
a water vapor outlet and a water vapor inlet of the evaporator are respectively connected with a water vapor inlet and a water vapor outlet of the heat pump heat exchanger;
the flue gas outlet of the condenser is connected with the flue gas discharge device;
the condenser is provided with a hot water outlet.
Preferably, the evaporator is further provided with a water inlet, the water inlet is connected with the normal-temperature water pipe, and a valve is arranged between the water inlet and the normal-temperature water pipe.
Preferably, the evaporator is provided with a water outlet for refrigerating water.
Preferably, a draught fan is arranged in the smoke discharge device, and more preferably, the smoke discharge device is a chimney.
Preferably, the condensed water outlet of the evaporator is connected with the water inlet of the desulfurizing tower.
Preferably, the desulfurization tower is provided with a sewage outlet.
Preferably, the refrigerant comprises one of ammonia water, lithium bromide and lithium nitrate solution, and is circulated between the generator and the absorber, and lithium bromide is more preferable.
Preferably, the heat pump heat exchanger and the water-flue gas heat exchanger are selected from one of a shell-and-tube type, a heat pipe type and a plate type heat exchanger, and more preferably, a shell-and-tube type heat exchanger.
Preferably, the material of the heat pump heat exchanger is selected from one or a combination of 304L stainless steel and 316L stainless steel, and more preferably 304L stainless steel.
Preferably, the water-gas heat exchanger is selected from one or a combination of several of tetrafluoroplastic, graphite, enamel, silicon carbide and ceramic, and is more preferably an enamel material.
A method for wet desulfurization of high-temperature flue gas is suitable for a device for wet desulfurization of high-temperature flue gas, and comprises the following steps:
(a) the flue gas to be treated enters a generator and emits heat, the temperature of the flue gas is reduced and then enters a water-flue gas heat exchanger to exchange heat with normal temperature water, wet desulphurization treatment is carried out after the temperature is further reduced, the treated purified flue gas enters an evaporator and is cooled to below 20 ℃, water vapor is condensed, then the flue gas enters a condenser again to absorb the heat and is raised to above 70 ℃, and the flue gas is discharged;
(b) in the step (a), the flue gas to be treated enters a generator and releases heat, and then is absorbed by refrigerant solution in the generator, the generated water vapor enters a condenser to release heat, and the heat is taken away by the flue gas and cooling water which are discharged by an evaporator and cooled to below 20 ℃;
(c) after entering a heat pump heat exchanger, water discharged from a water outlet of the condenser exchanges heat with water vapor discharged from the evaporator, after heat exchange, the cooled water vapor continues to enter the evaporator through throttling and pressure reduction to absorb heat of the purified flue gas after desulfurization treatment, the cooled water enters an absorber and is absorbed by refrigerant solution from a generator, the refrigerant solution emitting heat returns to the generator to continue circulation, and the emitted heat is carried away by water from the water-flue gas heat exchanger;
(d) the normal temperature water enters the water-smoke heat exchanger, enters the absorber after absorbing heat, enters the condenser after absorbing heat again, and obtains heat supply water after absorbing heat; preferably, the temperature of the heating water is more than 60 ℃.
Preferably, a valve is opened, the normal-temperature water enters the evaporator and exchanges heat with the purified flue gas after desulfurization treatment, and the refrigeration water with the temperature of less than 10 ℃ is obtained.
Preferably, the temperature of the normal temperature water is 25-30 ℃.
Preferably, the temperature of the flue gas to be treated is more than 160 ℃, and more preferably, the temperature of the flue gas to be treated is 160-190 ℃.
Compared with the prior art, the invention has the beneficial effects that:
(1) the device for wet desulphurization of high-temperature flue gas can completely eliminate the white smoke phenomenon of the flue gas, uses the condensed water from the evaporator to cool the circulating liquid of the desulphurization tower, reduces the temperature of the flue gas by utilizing the heat pump technology, reduces the temperature of the purified flue gas to be below 20 ℃, condenses more than 90 percent of water vapor in the purified flue gas, and then raises the temperature of the purified flue gas to be above 70 ℃, thus completely eliminating the white smoke phenomenon of the desulphurization flue gas. Even if the purified smoke is discharged to the atmosphere in rainy days or when the environmental temperature is low, the white smoke phenomenon can not be generated.
(2) According to the device provided by the invention, after the temperature of the flue gas entering the desulfurizing tower is reduced, the spraying amount of the circulating slurry of the desulfurizing tower is reduced, and the volume of the desulfurizing tower is reduced. According to the embodiment of the application, the temperature of the flue gas entering the desulfurizing tower is reduced to be lower than 70 ℃ from 170 ℃, the volume of the high-temperature flue gas entering the desulfurizing tower is reduced by more than 20%, the volume flow of the circulating slurry of the desulfurizing tower can be correspondingly reduced by more than 20%, and the volume of the desulfurizing tower can be synchronously reduced.
(3) The device provided by the invention realizes ultra-clean emission of flue gas, more than 90% of water vapor in the flue gas is condensed after the purified flue gas emits heat through the water-flue gas heat exchanger and the evaporator, and NO contained in the purified flue gas is condensed and condensed by virtue of the condensation and condensation of the water vaporx、SO3More than 80% of pollutants such as aerosol, fine dust and the like are removed along with the condensation of water vapor, and the ultra-clean emission of purified flue gas is realized.
(4) According to the device provided by the invention, water vapor in the flue gas is recovered in the evaporator, and condensed water enters the desulfurizing tower, so that the water supplementing amount of a desulfurizing system is reduced. The temperature of the purified flue gas is reduced to be below 20 ℃, more than 90% of water vapor in the purified flue gas is condensed out, and the water saving amount is at least 145g/kg of flue gas.
(5) The device provided by the invention can generate medium-temperature hot water in winter, and can be directly used for heating and domestic water. After heat exchange is carried out on the water at normal temperature of 25-30 ℃ by a heat exchanger and a condenser, the temperature is raised to more than 60 ℃, and the water is directly used for heating and domestic water.
(6) The device provided by the invention can produce refrigeration water in summer, and the temperature of the normal temperature water is reduced to below 10 ℃ after passing through the evaporator, so that the device can be directly used for refrigeration.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a schematic connection diagram of a high-temperature flue gas wet desulfurization device according to the present invention;
FIG. 2 is a process flow diagram of a method for wet desulfurization of high-temperature flue gas provided in example 1 of the present invention;
FIG. 3 is a schematic process flow diagram of a wet desulfurization method for high-temperature flue gas provided in example 2 of the present invention.
Reference numerals:
1-a desulfurizing tower; 2-an evaporator; 3-a condenser; 4-a generator; 5-an absorber; 6-heat pump heat exchanger; 7-a flue gas discharge device; 8-water-flue gas heat exchanger.
Detailed Description
The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings and the detailed description, but those skilled in the art will understand that the following described embodiments are some, not all, of the embodiments of the present invention, and are only used for illustrating the present invention, and should not be construed as limiting the scope of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
The invention provides a device for wet desulphurization of high-temperature flue gas, which comprises a desulphurization tower, a water-flue gas heat exchanger, a generator, a condenser, an evaporator, an absorber, a heat pump heat exchanger and a flue gas discharge device, wherein the desulphurization tower is arranged in the middle of the desulphurization tower; the high-temperature flue gas wet desulphurization device can be connected in a manner as shown in figure 1.
The generator comprises a flue gas inlet, a flue gas outlet, a water vapor outlet, a refrigerant outlet and a refrigerant inlet;
a smoke outlet of the generator is connected with a smoke inlet of the water-smoke heat exchanger, a water vapor outlet of the generator is connected with a water vapor inlet of the condenser, and a refrigerant outlet and a refrigerant inlet of the generator are respectively connected with a refrigerant inlet and a refrigerant outlet of the absorber;
a refrigerant is arranged in the generator and circulates between the generator and the absorber;
the water inlet of the water-smoke heat exchanger is connected with a normal-temperature water pipe;
the water outlet of the water-flue gas heat exchanger is connected with the water inlet of the absorber;
the flue gas outlet of the water-flue gas heat exchanger is connected with the desulfurizing tower;
the water outlet of the absorber is connected with the water inlet of the condenser, and the water inlet of the absorber is connected with the water outlet of the heat pump heat exchanger;
the flue gas outlet of the desulfurizing tower is connected with the flue gas inlet of the evaporator;
the flue gas outlet of the evaporator is connected with the flue gas inlet of the condenser;
a water vapor outlet and a water vapor inlet of the evaporator are respectively connected with a water vapor inlet and a water vapor outlet of the heat pump heat exchanger;
the flue gas outlet of the condenser is connected with the flue gas discharge device;
the condenser is provided with a hot water outlet.
The device for wet desulphurization of high-temperature flue gas can completely eliminate the white smoke phenomenon of the flue gas, uses the condensed water from the evaporator to cool the circulating liquid of the desulphurization tower, reduces the temperature of the flue gas by utilizing the heat pump technology, reduces the temperature of the purified flue gas to be below 20 ℃, condenses more than 90 percent of water vapor in the purified flue gas, and then raises the temperature of the purified flue gas to be above 70 ℃, thus completely eliminating the white smoke phenomenon of the desulphurization flue gas. Meanwhile, NO contained in the flue gas is purified by virtue of condensation and condensation of water vaporx、SO3More than 80% of pollutants such as aerosol, fine dust and the like are removed along with the condensation of water vapor, and the ultra-clean emission of purified flue gas is realized. Even if the purified smoke is discharged to the atmosphere in rainy days or when the environmental temperature is low, the white smoke phenomenon can not be generated. And after the temperature of the flue gas entering the desulfurizing tower is reduced, the spraying amount of the circulating slurry of the desulfurizing tower is reduced, and the volume of the desulfurizing tower is reduced. The hot water with the temperature of over 60 ℃ can be obtained by utilizing the recovered heat in the flue gas and can be directly used for heating and domestic water.
In some preferred embodiments of the present invention, the evaporator is further provided with a water inlet, the water inlet is connected to the normal temperature water pipe, and a valve is disposed between the water inlet and the normal temperature water pipe.
In some preferred embodiments of the invention, the evaporator is provided with a cooling water outlet.
Opening a normal-temperature water valve a, allowing 1/3-1/2 normal-temperature water to enter an evaporator through the valve a, reducing the temperature to 6 ℃ and using the water as refrigeration water in summer, and allowing 1/2-2/3 normal-temperature water to enter a water-smoke heat exchanger; and (4) closing the normal-temperature water valve a, and enabling the normal-temperature water to completely enter the water-smoke heat exchanger and the heat pump system to prepare hot water for heating. And (3) introducing saturated purified flue gas from the desulfurizing tower into an evaporator, reducing the temperature to be below 20 ℃, introducing the saturated purified flue gas into a condenser to absorb heat, raising the temperature to be above 70 ℃, and then introducing the saturated purified flue gas into a chimney for discharging.
In some preferred embodiments of the present invention, an induced draft fan is disposed in the flue gas discharge device, and since the pressure of the flue gas after passing through the heat exchange device is reduced, the induced draft fan can be added at a suitable position along the flue gas to increase the flue gas pressure, and more preferably, the flue gas discharge device is a chimney.
In some preferred embodiments of the present invention, the condensed water outlet of the evaporator is connected to the water inlet of the desulfurization tower.
Condensed water generated by cooling the purified flue gas in the evaporator enters the desulfurizing tower to be used as spraying liquid of the desulfurizing tower, so that the water supplementing amount in the desulfurizing process is reduced. The temperature of the purified flue gas is reduced to be below 20 ℃, more than 90% of water vapor in the purified flue gas is condensed out, and the water saving amount is at least 145g/kg of flue gas.
In some preferred embodiments of the present invention, the desulfurization tower is provided with a wastewater outlet.
In some preferred embodiments of the present invention, the refrigerant comprises one of ammonia, lithium bromide, and lithium nitrate solution, and the refrigerant is circulated between the generator and the absorber, more preferably lithium bromide.
In some preferred embodiments of the present invention, the heat pump heat exchanger and the water-flue gas heat exchanger are selected from one of a shell-and-tube type, a heat pipe type and a plate type heat exchanger, and more preferably a shell-and-tube type heat exchanger.
In some preferred embodiments of the present invention, the heat pump heat exchanger is made of one or a combination of 304L stainless steel and 316L stainless steel, and more preferably 304L stainless steel, to avoid corrosion of the heat exchanger.
In some preferred embodiments of the present invention, the water-flue gas heat exchanger is used for avoiding low-temperature dew point corrosion of flue gas, and is selected from one or more of tetrafluoroplastic, graphite, enamel, silicon carbide and ceramic, and is more preferably an enamel material.
The invention provides a method for wet desulphurization of high-temperature flue gas, which is suitable for a device for wet desulphurization of high-temperature flue gas and comprises the following steps:
(a) the flue gas to be treated enters a generator and emits heat, the temperature of the flue gas is reduced and then enters a water-flue gas heat exchanger to exchange heat with normal temperature water, wet desulphurization treatment is carried out after the temperature is further reduced, the treated purified flue gas enters an evaporator and is cooled to below 20 ℃, water vapor is condensed, then the flue gas enters a condenser again to absorb the heat and is raised to above 70 ℃, and the flue gas is discharged;
(b) in the step (a), the flue gas to be treated enters a generator and releases heat, and then is absorbed by refrigerant solution in the generator, the generated water vapor enters a condenser to release heat, and the heat is taken away by the flue gas and cooling water which are discharged by an evaporator and cooled to below 20 ℃;
(c) after entering a heat pump heat exchanger, water discharged from a water outlet of the condenser exchanges heat with water vapor discharged from the evaporator, after heat exchange, the cooled water vapor continues to enter the evaporator through throttling and pressure reduction to absorb heat of the purified flue gas after desulfurization treatment, the cooled water enters an absorber and is absorbed by refrigerant solution from a generator, the refrigerant solution emitting heat returns to the generator to continue circulation, and the emitted heat is carried away by water from the water-flue gas heat exchanger;
(d) the normal temperature water enters the water-smoke heat exchanger, enters the absorber after absorbing heat, enters the condenser after absorbing heat again, and obtains heat supply water after absorbing heat; preferably, the temperature of the heating water is more than 60 ℃.
According to the method provided by the invention, high-temperature flue gas enters the generator to emit heat, enters the water-flue gas heat exchanger to transfer the heat to water after the temperature is reduced, and enters the desulfurizing tower to be cooled and desulfurized after the temperature is reduced.
The weak solution of the refrigerant in the generator absorbs the heat of the high-temperature flue gas, the generated refrigerant vapor enters the condenser, and the evaporated strong solution enters the absorber.
The refrigerant vapor enters a condenser, is condensed to release heat and then is liquefied, and the heat is taken away by purified flue gas and cooling water.
The refrigerant solution enters a heat pump heat exchanger to exchange heat with refrigerant vapor generated by an evaporator, and then enters the evaporator to absorb and purify smoke heat (absorb and purify smoke and normal temperature water heat in summer) for evaporation after throttling and pressure reduction. The purified flue gas generates heat in the evaporator, the temperature is reduced to below 20 ℃, and more than 90% of water vapor in the flue gas is condensed.
Refrigerant vapor generated by the evaporator enters the heat pump heat exchanger for heat exchange and temperature rise and then enters the absorber, the refrigerant vapor is absorbed by the concentrated solution from the generator to release heat, the heat is changed into dilute solution and returns to the generator for continuous circulation, and the heat released by the absorber is taken away by cooling water.
The normal temperature water enters the water-smoke heat exchanger, enters the absorber after absorbing the heat of the smoke, absorbs the heat emitted by the absorber, enters the condenser after the temperature is further raised, absorbs partial heat emitted by the liquefaction of the solvent vapor in the condenser, and is used for heating and domestic water when the temperature is raised to more than 60 ℃.
In some preferred embodiments of the present invention, a valve is opened, and the normal temperature water enters the evaporator to perform heat exchange with the purified flue gas after desulfurization treatment, so as to obtain refrigeration water with a temperature of less than 10 ℃.
In some preferred embodiments of the present invention, the temperature of the normal temperature water is 25 to 30 ℃.
In some preferred embodiments of the present invention, the temperature of the flue gas to be treated is greater than 160 ℃, and more preferably, the temperature of the flue gas to be treated is 160-190 ℃.
Example 1: winter heat supply
As shown in fig. 2, 200000kg/h of high temperature flue gas of 170 ℃ enters the generator 4 to release heat, the temperature is reduced to 100 ℃ and then enters the water-flue gas heat exchanger 8 to exchange heat with water of 30 ℃, and the temperature is reduced to 60 ℃ and then enters the desulfurizing tower 1 to be cooled and desulfurized.
The flue gas with the temperature of 60 ℃ enters the desulfurizing tower 1 and is washed by the circulating slurry to remove substances such as sulfide, particulate matters and the like, and the temperature is reduced to 48 ℃ and is discharged from the top of the desulfurizing tower 1.
The saturated purified flue gas from the desulfurizing tower 1 enters the evaporator 2 to emit heat, the temperature is reduced to 13 ℃, the saturated purified flue gas enters the condenser 3 to absorb the heat, the temperature is raised to 75 ℃, and then the saturated purified flue gas enters the flue gas discharge device 7 to be discharged.
The lithium bromide solution in the generator 4 absorbs the heat of the high-temperature flue gas at 170 ℃, the generated water vapor at 90 ℃ enters the condenser 3, and the lithium bromide concentrated solution at 85 ℃ enters the absorber 5. The 90 ℃ water vapor enters the condenser 3 to be condensed and release heat, and the heat is taken away by the 13 ℃ purified flue gas and the 55 ℃ cooling water. The liquid water with the temperature of 80 ℃ enters the heat pump heat exchanger 6 to exchange heat with the water vapor with the temperature of 2 ℃ generated by the evaporator 2, the temperature is reduced, the liquid water is throttled and reduced, the liquid water with the temperature of 80 ℃ enters the evaporator 2 to absorb the heat of purified flue gas with the temperature of 48 ℃ to evaporate after the temperature is reduced to 1 ℃, the purified flue gas with the temperature of 48 ℃ emits heat in the evaporator 2 to be reduced to 13 ℃, and 94 percent of the water vapor in the flue gas is condensed out. The 2 ℃ water vapor generated by the evaporator 2 enters the heat pump heat exchanger 6 for heat exchange, the temperature rises to 75 ℃ and then enters the absorber 5, the 85 ℃ lithium bromide concentrated solution from the generator 4 absorbs the released heat and changes the released heat into the lithium bromide dilute solution, the lithium bromide dilute solution returns to the generator 4 for continuous circulation, and the heat released by the absorber 5 is taken away by 35 ℃ cooling water.
In winter, the normal temperature water valve a is closed, and the normal temperature water completely enters the water-smoke heat exchanger and the heat pump system. The water with the normal temperature of 30 ℃ enters the water-smoke heat exchanger 8 to exchange heat with the smoke with the temperature of 100 ℃, the temperature rises to 35 ℃ and enters the absorber 5 to absorb the heat emitted by the absorber 5, the temperature further rises to 55 ℃ and then enters the condenser 3 to absorb part of the heat emitted by the liquefaction of the water vapor in the condenser 3, and the temperature rises to 68 ℃ and is used for heating in winter and using as domestic water.
13 ℃ condensed water generated by cooling the purified flue gas in the evaporator 2 enters the desulfurizing tower 1 to be used as spraying liquid of the desulfurizing tower, so that the water supplementing amount in the desulfurizing process is reduced, and the water supplementing amount in the desulfurizing tower in the whole process can be reduced by 29.9 t/h.
EXAMPLE 2 Cooling in summer with simultaneous production of cold and hot water
As shown in fig. 3, 200000kg/h of high temperature flue gas of 170 ℃ enters the generator 4 to release heat, and enters the water-flue gas heat exchanger 8 after the temperature is reduced to 120 ℃, and exchanges heat with water of 30 ℃, and enters the desulfurizing tower 1 to be cooled and desulfurized after the temperature is reduced to 70 ℃.
The flue gas with the temperature of 70 ℃ enters the desulfurizing tower 1 and is washed by the circulating slurry to remove substances such as sulfide, particulate matters and the like, and the temperature is reduced to 50 ℃ and is discharged from the top of the desulfurizing tower 1.
The lithium bromide solution in the generator 4 absorbs the heat of the high-temperature flue gas at 170 ℃, the generated water vapor at 90 ℃ enters the condenser 3, and the lithium bromide concentrated solution at 85 ℃ enters the absorber 5. The 90 ℃ water vapor enters the condenser 3 to be condensed and release heat, and the heat is taken away by the 20 ℃ purified flue gas and the 55 ℃ cooling water. The liquid water with the temperature of 80 ℃ enters the heat pump heat exchanger 6 to exchange heat with the water vapor with the temperature of 2 ℃ generated by the evaporator 2, the temperature is reduced, the liquid water is throttled and depressurized, the liquid water with the temperature of 1 ℃ enters the evaporator 2 to absorb and absorb the heat of the purified flue gas with the temperature of 50 ℃ and the normal temperature water with the temperature of 30 ℃ to evaporate, the purified flue gas with the temperature of 50 ℃ emits heat in the evaporator 2, the temperature is reduced to 20 ℃, and 90% of the water vapor in the flue gas is condensed out. The 2 ℃ water vapor generated by the evaporator 2 enters the heat pump heat exchanger 6 for heat exchange, the temperature rises to 75 ℃ and then enters the absorber 5, the 85 ℃ lithium bromide concentrated solution from the generator 4 absorbs the released heat and changes the released heat into the lithium bromide dilute solution, the lithium bromide dilute solution returns to the generator 4 for continuous circulation, and the heat released by the absorber 5 is taken away by 35 ℃ cooling water.
In summer, the normal temperature water valve a is opened. 1/3 normal temperature water enters the evaporator 2 through the valve a, the temperature is reduced to 6 ℃ and can be used as cooling water in summer, 2/3 normal temperature water enters the water-smoke heat exchanger and the heat pump system. 2/3, the water at normal temperature of 30 ℃ enters a water-smoke heat exchanger 8 to exchange heat with the smoke at 120 ℃, the temperature rises to 35 ℃ and enters an absorber 5 to absorb the heat emitted by the absorber 5, the temperature further rises to 55 ℃ and then enters a condenser 3 to absorb part of the heat emitted by the liquefaction of the water vapor in the condenser 3, and the temperature rises to 68 ℃ and is used for heating in winter and using as domestic water.
The 20 ℃ condensed water generated by cooling the purified flue gas in the evaporator 2 enters the desulfurizing tower 1 to be used as the spray liquid of the desulfurizing tower, so that the water supplementing amount in the desulfurizing process is reduced, and the water supplementing amount of the desulfurizing tower in the whole process can be reduced by 28.1 t/h.
While particular embodiments of the present invention have been illustrated and described, it will be appreciated that the above embodiments are merely illustrative of the technical solution of the present invention and are not restrictive; those of ordinary skill in the art will understand that: modifications may be made to the above-described embodiments, or equivalents may be substituted for some or all of the features thereof without departing from the spirit and scope of the present invention; the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention; it is therefore intended to cover in the appended claims all such alternatives and modifications that are within the scope of the invention.
Claims (15)
1. The method for wet desulfurization of high-temperature flue gas is characterized by being carried out by adopting a device for wet desulfurization of high-temperature flue gas;
the method for wet desulfurization of the high-temperature flue gas comprises the following steps:
(a) the flue gas to be treated enters a generator and emits heat, the temperature of the flue gas is reduced and then enters a water-flue gas heat exchanger to exchange heat with normal temperature water, wet desulphurization treatment is carried out after the temperature is further reduced, the treated purified flue gas enters an evaporator and is cooled to below 20 ℃, water vapor is condensed, then the flue gas enters a condenser again to absorb the heat and is raised to above 70 ℃, and the flue gas is discharged;
(b) in the step (a), the flue gas to be treated enters a generator, the heat emitted by the flue gas to be treated is absorbed by a refrigerant solution in the generator, the generated water vapor enters the condenser to release heat, and the heat is taken away by the flue gas and cooling water which are discharged by the evaporator and cooled to the temperature below 20 ℃;
(c) after entering a heat pump heat exchanger, the water discharged from the water outlet of the condenser exchanges heat with the water vapor discharged from the evaporator, after heat exchange, the cooled water enters the evaporator after throttling and pressure reduction, the heat of the purified flue gas after desulfurization treatment is absorbed, the heated water vapor enters an absorber and is absorbed by the refrigerant solution of a self-generator, the refrigerant solution which emits heat returns to the generator for continuous circulation, and the emitted heat is carried away by the water from the water-flue gas heat exchanger;
(d) the normal temperature water enters the water-smoke heat exchanger, enters the absorber after absorbing heat, enters the condenser after absorbing heat again, and obtains heat supply water after absorbing heat; the temperature of the hot water is more than 60 ℃; opening a valve, allowing the normal-temperature water to enter the evaporator, and performing heat exchange with the purified flue gas subjected to desulfurization treatment to obtain refrigeration water with the temperature of less than 10 ℃;
the device for wet desulphurization of the high-temperature flue gas comprises a desulphurization tower, a water-flue gas heat exchanger, a generator, a condenser, an evaporator, an absorber, a heat pump heat exchanger and a flue gas discharge device;
the generator comprises a flue gas inlet, a flue gas outlet, a water vapor outlet, a refrigerant outlet and a refrigerant inlet;
a smoke outlet of the generator is connected with a smoke inlet of the water-smoke heat exchanger, a water vapor outlet of the generator is connected with a water vapor inlet of the condenser, and a refrigerant outlet and a refrigerant inlet of the generator are respectively connected with a refrigerant inlet and a refrigerant outlet of the absorber;
a refrigerant is arranged in the generator and circulates between the generator and the absorber;
the water inlet of the water-smoke heat exchanger is connected with a normal-temperature water pipe;
the water outlet of the water-flue gas heat exchanger is connected with the water inlet of the absorber;
the flue gas outlet of the water-flue gas heat exchanger is connected with the desulfurizing tower;
the water outlet of the absorber is connected with the water inlet of the condenser, and the water inlet of the absorber is connected with the water outlet of the heat pump heat exchanger;
the water outlet of the condenser is connected with the water inlet of the heat pump heat exchanger;
the flue gas outlet of the desulfurizing tower is connected with the flue gas inlet of the evaporator;
the flue gas outlet of the evaporator is connected with the flue gas inlet of the condenser;
a water vapor outlet and a water vapor inlet of the evaporator are respectively connected with a water vapor inlet and a water vapor outlet of the heat pump heat exchanger;
the flue gas outlet of the condenser is connected with the flue gas discharge device;
the condenser is provided with a heat supply water outlet;
the evaporator is also provided with a water inlet, the water inlet is connected with the normal-temperature water pipe, and a valve is arranged between the water inlet and the normal-temperature water pipe;
the evaporator is provided with a refrigeration water outlet;
and a condensed water outlet of the evaporator is connected with a water inlet of the desulfurizing tower.
2. The method for wet desulfurization of high temperature flue gas according to claim 1, wherein an induced draft fan is arranged in the flue gas discharge device.
3. The method for wet desulfurization of high temperature flue gas according to claim 1, wherein the flue gas discharge device is a chimney.
4. The method for wet desulfurization of high temperature flue gas according to claim 1, wherein the desulfurization tower is provided with a sewage outlet.
5. The method for wet desulfurization of high temperature flue gas according to claim 1, wherein the refrigerant comprises one of ammonia, lithium bromide and lithium nitrate solution.
6. The method for wet desulfurization of high temperature flue gas according to claim 1, wherein the refrigerant is lithium bromide.
7. The method for wet desulfurization of high-temperature flue gas according to claim 1, wherein the heat pump heat exchanger and the water-flue gas heat exchanger are selected from one of shell-and-tube type, heat pipe type and plate type heat exchangers.
8. The method for wet desulfurization of high-temperature flue gas according to claim 1, wherein the heat pump heat exchanger and the water-flue gas heat exchanger are shell-and-tube heat exchangers.
9. The method for wet desulfurization of high-temperature flue gas according to claim 1, wherein the material of the heat pump heat exchanger is selected from one or a combination of 304L stainless steel and 316L stainless steel.
10. The method for wet desulfurization of high-temperature flue gas according to claim 1, wherein the heat pump heat exchanger is made of 304L stainless steel.
11. The method for wet desulfurization of high-temperature flue gas according to claim 1, wherein the water-flue gas heat exchanger is selected from one or more of tetrafluoroplastic, graphite, enamel, silicon carbide and ceramic.
12. The method for wet desulfurization of high temperature flue gas according to claim 1, wherein the water-flue gas heat exchanger is an enamel material.
13. The method for wet desulfurization of high temperature flue gas according to claim 1, wherein the temperature of the normal temperature water is 25-30 ℃.
14. The method for wet desulfurization of high-temperature flue gas according to claim 1, wherein the temperature of the flue gas to be treated is greater than 160 ℃.
15. The method for wet desulfurization of high temperature flue gas as recited in claim 1, wherein the temperature of the flue gas to be treated is 160-190 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910715749.7A CN110314527B (en) | 2019-08-05 | 2019-08-05 | Device and method for wet desulphurization of high-temperature flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910715749.7A CN110314527B (en) | 2019-08-05 | 2019-08-05 | Device and method for wet desulphurization of high-temperature flue gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110314527A CN110314527A (en) | 2019-10-11 |
| CN110314527B true CN110314527B (en) | 2021-12-17 |
Family
ID=68125460
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910715749.7A Active CN110314527B (en) | 2019-08-05 | 2019-08-05 | Device and method for wet desulphurization of high-temperature flue gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110314527B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111336580A (en) * | 2020-03-19 | 2020-06-26 | 宁波市成大机械研究所 | Internal combustion heating and ground source heat pump coupling heating system |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101949609A (en) * | 2010-10-18 | 2011-01-19 | 河南科技大学 | Low-temperature heat source-driven air-cooling ammonia water absorption refrigerating machine |
| CN104235864A (en) * | 2013-06-13 | 2014-12-24 | 烟台龙源电力技术股份有限公司 | Flue gas moisture recovery system and method |
| JP2015137797A (en) * | 2014-01-22 | 2015-07-30 | 株式会社大川原製作所 | Gas treatment system |
| CN107676805A (en) * | 2017-09-22 | 2018-02-09 | 华电电力科学研究院 | A kind of efficiently water intaking eliminating white smoke cooperation-removal pollutant device and its method of work |
| CN207379110U (en) * | 2017-11-15 | 2018-05-18 | 中国大唐集团科学技术研究院有限公司西北分公司 | A kind of energy-saving and water-saving type coal-burning boiler wet flue gas depth total system |
| CN109316907A (en) * | 2018-08-20 | 2019-02-12 | 李俊峰 | A kind of system and method for the white tail that removes smoke |
| CN109631390A (en) * | 2019-01-15 | 2019-04-16 | 西安交通大学 | A kind of absorption heat pump fume waste heat depth recovery system for realizing the full return water heating of boiler |
-
2019
- 2019-08-05 CN CN201910715749.7A patent/CN110314527B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101949609A (en) * | 2010-10-18 | 2011-01-19 | 河南科技大学 | Low-temperature heat source-driven air-cooling ammonia water absorption refrigerating machine |
| CN104235864A (en) * | 2013-06-13 | 2014-12-24 | 烟台龙源电力技术股份有限公司 | Flue gas moisture recovery system and method |
| JP2015137797A (en) * | 2014-01-22 | 2015-07-30 | 株式会社大川原製作所 | Gas treatment system |
| CN107676805A (en) * | 2017-09-22 | 2018-02-09 | 华电电力科学研究院 | A kind of efficiently water intaking eliminating white smoke cooperation-removal pollutant device and its method of work |
| CN207379110U (en) * | 2017-11-15 | 2018-05-18 | 中国大唐集团科学技术研究院有限公司西北分公司 | A kind of energy-saving and water-saving type coal-burning boiler wet flue gas depth total system |
| CN109316907A (en) * | 2018-08-20 | 2019-02-12 | 李俊峰 | A kind of system and method for the white tail that removes smoke |
| CN109631390A (en) * | 2019-01-15 | 2019-04-16 | 西安交通大学 | A kind of absorption heat pump fume waste heat depth recovery system for realizing the full return water heating of boiler |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110314527A (en) | 2019-10-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP5913369B2 (en) | Non-contact exhaust residual heat sludge drying system | |
| CN102734787B (en) | Concurrent recycling system for boiler smoke afterheat | |
| US20110073669A1 (en) | Apparatus and method for energy recovery | |
| CN106914124A (en) | The heat pipe heat exchanging water saving anti-gypsum rain device of demisting in wet desulfuration tower | |
| CN103486603A (en) | Flue gas treatment device and treatment method | |
| CN110314527B (en) | Device and method for wet desulphurization of high-temperature flue gas | |
| CN109432935B (en) | System for deeply eliminating white smoke of wet desulphurization flue gas | |
| WO2023050702A1 (en) | Low-temperature desulfurization and denitrification method and system for flue gas from rotary kiln combustion furnace of refuse incineration power plant | |
| CN109163477A (en) | A kind of absorption type heat pump system of gas fired-boiler fume afterheat and condensate-water polishing | |
| CN111569630B (en) | Wet desulfurization system and wet desulfurization method | |
| CN203215653U (en) | Vapor-recovery unit | |
| CN109990305B (en) | White smoke plume eliminating device for coal-fired power plant and working method | |
| CN207214097U (en) | A kind of coal-burning boiler based on smoke evacuation vapor internal-circulation type condensing units | |
| CN216273195U (en) | System for noncondensable gas is got rid of in desulfurization thick liquid flash distillation | |
| CN202692016U (en) | Flue gas waste heat recovery system for concurrent boiler | |
| CN110102143B (en) | Method and system for eliminating white smoke from desulfurized flue gas | |
| CN211677009U (en) | Smoke whitening system | |
| CN109966887B (en) | Energy quality allocation-based flue gas treatment method and device | |
| CN108105795B (en) | Compression type and absorption type heat pump coupling flue gas treatment equipment | |
| CN102338371A (en) | Flue gas waste heat utilization system | |
| CN205957357U (en) | Heat -pump type solution dehumidification equipment | |
| CN217423663U (en) | Smoke type lithium bromide absorption type second-class heat pump unit | |
| CN216367378U (en) | Desulfurization system for eliminating colored smoke plume | |
| CN109794144A (en) | A kind of flue gas takes off white device | |
| CN203595136U (en) | Flue gas treating device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |