CN117563379A - CO and NO by heat exchanger with CO adsorption function x System for removal - Google Patents
CO and NO by heat exchanger with CO adsorption function x System for removal Download PDFInfo
- Publication number
- CN117563379A CN117563379A CN202311534037.8A CN202311534037A CN117563379A CN 117563379 A CN117563379 A CN 117563379A CN 202311534037 A CN202311534037 A CN 202311534037A CN 117563379 A CN117563379 A CN 117563379A
- Authority
- CN
- China
- Prior art keywords
- flue gas
- heat exchanger
- distribution assembly
- inlet
- desorption
- 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.)
- Pending
Links
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 44
- 229910002091 carbon monoxide Inorganic materials 0.000 title claims abstract description 30
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 85
- 239000003546 flue gas Substances 0.000 claims abstract description 81
- 239000007789 gas Substances 0.000 claims abstract description 71
- 238000003795 desorption Methods 0.000 claims abstract description 54
- 239000003463 adsorbent Substances 0.000 claims abstract description 25
- 238000000034 method Methods 0.000 claims abstract description 14
- 230000008569 process Effects 0.000 claims abstract description 9
- 230000003647 oxidation Effects 0.000 claims abstract description 4
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 4
- 239000000779 smoke Substances 0.000 claims description 17
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 14
- 229910021529 ammonia Inorganic materials 0.000 claims description 7
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims description 6
- 239000003054 catalyst Substances 0.000 claims description 6
- 238000005192 partition Methods 0.000 claims description 6
- 238000001514 detection method Methods 0.000 claims description 5
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 claims description 3
- 239000005751 Copper oxide Substances 0.000 claims description 3
- 238000007084 catalytic combustion reaction Methods 0.000 claims description 3
- 229910000428 cobalt oxide Inorganic materials 0.000 claims description 3
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical compound [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 claims description 3
- 229910000431 copper oxide Inorganic materials 0.000 claims description 3
- 239000002808 molecular sieve Substances 0.000 claims description 3
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 3
- 230000001172 regenerating effect Effects 0.000 claims description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- 239000011787 zinc oxide Substances 0.000 claims description 3
- 239000003575 carbonaceous material Substances 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 238000005245 sintering Methods 0.000 abstract description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D11/00—Heat-exchange apparatus employing moving conduits
- F28D11/02—Heat-exchange apparatus employing moving conduits the movement being rotary, e.g. performed by a drum or roller
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
-
- 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
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen 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
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/404—Nitrogen oxides other than dinitrogen oxide
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Thermal Sciences (AREA)
- Physics & Mathematics (AREA)
- Treating Waste Gases (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention relates to the technical field of environmental protection, in particular to a heat exchanger with CO adsorption function for CO and NO x The system for removing comprises a heat exchanger and a denitration reactor, wherein the heat exchanger comprises a shell, a rotor, a driving device, a heat exchange element, a CO adsorbent, a bottom gas distribution assembly, a top gas distribution assembly, a raw flue gas inlet, a raw flue gas outlet, a purified flue gas inlet, a purified flue gas outlet, a desorption air inlet and a desorption air outlet. The invention provides a heat exchanger with CO adsorption function for CO and NO x Removal system and process system using sameCan realize CO and NO in sintering flue gas x And the combined removal is carried out, and meanwhile, the heat released in the CO oxidation process is fully utilized, so that the problem of high energy consumption of an external heat source in the existing SCR denitration technology is solved, and the SCR denitration operation cost is reduced.
Description
Technical Field
The invention relates to the technical field of environmental protection, in particular to a heat exchanger with CO adsorption function for CO and NO x And (5) a removing system.
Background
Iron ore, flux and additives during the iron and steel sintering process produce SO2, NO at the high temperatures generated by the combustion of fuel x Contaminants such as particulates, CO, etc. The prior sintering flue gas treatment generally adopts a desulfurization-dust removal-denitration process, wherein NO x The treatment generally adopts SCR denitration technology, the flue gas after desulfurization and dust removal needs to be subjected to heat exchange and temperature rise, then is heated by an external heat source (generally needs to be heated by 30-50 ℃) to the denitration reaction temperature, and then NO is completed under the action of a denitration catalyst x And (3) removing the reaction. The technology needs an external heat source and has the problem of high energy consumption.
With the promotion of ultralow emission work in the steel industry, SO2 and NO x The particulate matters are effectively controlled, but the CO does not pay enough attention before, and along with the increasing severity of environmental protection, the emission reduction of the CO also draws a great deal of attention, so that a heat exchanger with the CO adsorption function needs to be designed for CO and NO x And (5) a removing system.
Disclosure of Invention
The invention aims to solve the defects in the prior art and proposes a method for carrying out CO and NO by using a heat exchanger with CO adsorption function x And (5) a removing system.
In order to achieve the above purpose, the present invention adopts the following technical scheme: exchange with function of adsorbing COThe heater carries out CO and NO x The system comprises a heat exchanger and a denitration reactor, wherein the heat exchanger comprises a shell, a rotor, a driving device, heat exchange elements, CO adsorbents, a bottom gas distribution assembly, a top gas distribution assembly, a raw gas inlet, a raw gas outlet, a clean gas inlet, a clean gas outlet, a desorption wind inlet and a desorption wind outlet, the rotor is rotationally connected in the shell, a plurality of partition plates are arranged in the rotor, the rotor is divided into a plurality of fan-shaped areas by the partition plates, the upper layer in each fan-shaped area is provided with the heat exchange elements, the lower layer in each fan-shaped area is provided with the CO adsorbents, the top gas distribution assembly is arranged at the upper end of the rotor, the desorption wind outlets are arranged at two sides of the top gas distribution assembly, the bottom gas distribution assembly is arranged at the lower end of the rotor, and the desorption wind inlets are arranged at two sides of the bottom gas distribution assembly; the middle position of the upper end of the shell is provided with a driving device, two sides of the upper end of the shell are respectively provided with an original smoke outlet and a clean smoke inlet, two sides of the lower end of the shell are respectively provided with an original smoke inlet and a clean smoke outlet, the original smoke inlet corresponds to the original smoke outlet, and the clean smoke outlet corresponds to the clean smoke inlet;
the raw flue gas outlet is connected with an inlet of the denitration reactor through a first flue gas pipeline, a plurality of layers of denitration catalysts are filled in the denitration reactor, and an outlet of the denitration reactor is connected with a clean flue gas inlet through a second flue gas pipeline.
As a further description of the above technical solution:
the device also comprises a desorption fan and a CO utilization device, wherein the inlet of the desorption fan is connected with a second flue gas pipeline through a pipeline, and the outlet of the desorption fan is connected with a desorption wind inlet through a pipeline; the desorption wind outlet is connected with an inlet of the CO utilization device through a third flue gas pipeline, and an outlet of the CO utilization device is connected with the first flue gas pipeline through a pipeline.
As a further description of the above technical solution:
the device for supplying ammonia and the gas hot blast stove are respectively connected with the first flue gas pipeline through pipelines.
As a further description of the above technical solution:
and a CO concentration detection device is arranged on the third flue gas pipeline.
As a further description of the above technical solution:
the fan-shaped area of the top gas distribution assembly and the fan-shaped area of the bottom gas distribution assembly are larger than or equal to the areas of the three fan-shaped areas, the top gas distribution assembly and the bottom gas distribution assembly correspond to each other, the top gas distribution assembly and the bottom gas distribution assembly divide the heat exchanger into an adsorption heat exchange area and a desorption area, the fan-shaped areas covered by the top gas distribution assembly and the bottom gas distribution assembly are analysis areas, and the remaining fan-shaped areas are adsorption heat exchange areas.
As a further description of the above technical solution:
the CO adsorbent is a molecular sieve or an active carbon material of one or more substances of copper oxide, zinc oxide, aluminum oxide and cobalt oxide, and the CO adsorption temperature of the CO adsorbent is 50-100 ℃ and the CO desorption temperature of the CO adsorbent is 180-300 ℃.
As a further description of the above technical solution:
the CO utilization device can be RCO catalytic combustion equipment or RTO regenerative thermal oxidation equipment. Heat exchanger with CO adsorption function for CO and NO x The method for removing the waste water comprises the following steps,
s1: CO adsorption and NO x Removing;
s2: and (5) comprehensively utilizing CO.
The invention has the following beneficial effects:
1. compared with the prior art, the CO adsorbent which is subjected to carbon monoxide adsorption in the adsorption heat exchange area circularly rotates to enter the desorption area; the desorption fan blows hot flue gas with the temperature of 180-300 ℃ in the second flue gas pipeline into a desorption wind inlet, then enters the heat exchanger, and in the desorption area, the CO adsorbent is heated and regenerated to desorb CO from the CO adsorbent, and enters the CO utilization device along with the desorption wind through a desorption wind outlet and a third flue gas pipeline, and in the CO utilization device, CO and oxygen are combusted to generate CO 2 And a large amount of heat is released, hot air generated by the CO utilization device enters the first flue gas pipeline, the flue gas temperature can be raised by 30-50 ℃, and the load of the gas hot blast stove can be reduced or closed at the moment, so that the gas consumption is reduced, and the energy-saving effect is achieved.
2. Compared with the prior art, the invention oxidizes the absorbed CO into CO 2 The heat released in the process can raise the temperature of the flue gas by 30-50 ℃, so that the energy consumption of the SCR denitration system is reduced; in the desorption process of CO, the denitration purified flue gas is blown into the heat exchanger by the desorption fan, so that NO in the heat exchanger can be reduced x Is carried by the chimney NO x And (5) discharging after reaching the standard.
Drawings
FIG. 1 shows a heat exchanger with CO adsorption function for CO and NO according to the present invention x A flow chart of the removal system;
FIG. 2 shows a heat exchanger with CO adsorption function for CO and NO according to the present invention x A heat exchanger structure schematic diagram of the removed system;
FIG. 3 shows a heat exchanger with CO adsorption function for CO and NO according to the present invention x A heat exchanger A-A of the removed system is schematically drawn in section;
FIG. 4 shows a heat exchanger with CO adsorption function for CO and NO according to the present invention x A heat exchanger B-B of the removed system is schematically drawn in section;
FIG. 5 shows the CO and NO adsorption by the heat exchanger with CO adsorption function according to the present invention x A schematic diagram of a gas distribution assembly at the top of a heat exchanger of the removed system;
FIG. 6 shows a heat exchanger with CO adsorption function for CO and NO according to the present invention x The structure of the bottom gas distribution component of the heat exchanger of the removal system is schematically shown.
Legend description:
1. a heat exchanger; 101. a housing; 102. a rotor; 103. a driving device; 104. a heat exchange element; 105. a CO adsorbent; 106. a bottom gas distribution assembly; 107. a top gas distribution assembly; 108. a raw flue gas inlet; 109. a raw flue gas outlet; 110. a clean flue gas inlet; 111. a clean flue gas outlet; 112. a desorption wind inlet; 113. a desorption wind outlet; 2. a denitration reactor; 201. a denitration catalyst; 3. a desorption fan; 4. a CO utilization device; 5. an ammonia supply device; 6. gas hot-blast stove; l101, a first flue gas pipeline; l102, a second flue gas pipeline; l103, a third flue gas pipeline; c1, CO concentration detection device.
Detailed Description
Referring to FIGS. 1-6, the invention provides a heat exchanger with CO adsorption function for CO and NO x The system for removing comprises a heat exchanger 1 and a denitration reactor 2, wherein the heat exchanger 1 comprises a shell 101, a rotor 102, a driving device 103, heat exchange elements 104, a CO adsorbent 105, a bottom gas distribution assembly 106, a top gas distribution assembly 107, a raw gas inlet 108, a raw gas outlet 109, a clean gas inlet 110, a clean gas outlet 111, a desorption wind inlet 112 and a desorption wind outlet 113, the rotor 102 is rotatably connected in the shell 101, a plurality of partition plates are arranged in the rotor 102, the rotor 102 is divided into a plurality of fan-shaped areas by the plurality of partition plates, the heat exchange elements 104 are arranged on the upper layer in each fan-shaped area, the CO adsorbent 105 is arranged on the lower layer in each fan-shaped area, the top gas distribution assembly 107 is arranged at the upper end of the rotor 102, desorption wind outlets 113 are arranged on two sides of the top gas distribution assembly 107, the bottom gas distribution assembly 106 is arranged at the lower end of the rotor 102, and desorption wind inlets 112 are arranged on two sides of the bottom gas distribution assembly 106; the middle position of the upper end of the shell 101 is provided with a driving device 103, two sides of the upper end of the shell 101 are respectively provided with a raw flue gas outlet 109 and a clean flue gas inlet 110, two sides of the lower end of the shell 101 are respectively provided with a raw flue gas inlet 108 and a clean flue gas outlet 111, the raw flue gas inlet 108 corresponds to the raw flue gas outlet 109, and the clean flue gas outlet 111 corresponds to the clean flue gas inlet 110;
the raw flue gas outlet 109 is connected with the inlet of the denitration reactor 2 through a first flue gas pipeline L101, a plurality of layers of denitration catalysts 201 are filled in the denitration reactor 2, and the outlet of the denitration reactor 2 is connected with the clean flue gas inlet 110 through a second flue gas pipeline L102.
The device also comprises a desorption fan 3 and a CO utilization device 4, wherein an inlet of the desorption fan 3 is connected with a second flue gas pipeline L102 through a pipeline, and an outlet of the desorption fan 3 is connected with a desorption wind inlet 112 through a pipeline; the induced-draft outlet 113 is connected to the inlet of the CO utilization apparatus 4 through a third flue gas duct L103, and the outlet of the CO utilization apparatus 4 is connected to the first flue gas duct L101 through a duct.
The device also comprises an ammonia supply device 5 and a gas hot blast stove 6, and the ammonia supply device 5 and the gas hot blast stove 6 are respectively connected with the first flue gas pipeline L101 through pipelines.
The third flue gas pipeline L103 is provided with a CO concentration detection device C1, and the CO concentration in the flue gas is detected by using the CO concentration detection device C1, so that the CO concentration is conveniently controlled, and the CO concentration is controlled to be less than or equal to 3.125% (less than 25% of the lower limit of CO explosion).
The fan-shaped area of the top gas distribution assembly 107 and the fan-shaped area of the bottom gas distribution assembly 106 are larger than or equal to the areas of the three fan-shaped areas, the top gas distribution assembly 107 and the bottom gas distribution assembly 106 correspond to each other, the top gas distribution assembly 107 and the bottom gas distribution assembly 106 divide the heat exchanger 1 into an adsorption heat exchange area and a desorption area, the fan-shaped areas covered by the top gas distribution assembly 107 and the bottom gas distribution assembly 106 are analysis areas, and the remaining fan-shaped areas are adsorption heat exchange areas.
The CO adsorbent 105 is a molecular sieve or an activated carbon material of one or more of copper oxide, zinc oxide, aluminum oxide and cobalt oxide, the CO adsorption temperature of the CO adsorbent 105 is 50-100 ℃, and the CO desorption temperature is 180-300 ℃.
The CO utilization device 4 may be an RCO catalytic combustion device or an RTO regenerative thermal oxidation device.
Heat exchanger 1 with CO adsorption function for CO and NO x The method for removing the waste water comprises the following steps,
s1: CO adsorption and NO x The water is removed from the water-soluble fiber,
the desulfurized flue gas enters an adsorption heat exchange area with a heat exchanger 1 through a raw flue gas inlet 108, carbon monoxide in the flue gas is adsorbed by a CO adsorbent 105, then the flue gas is heated and warmed through a heat exchange element 104, and enters a first flue gas pipeline L101 through a raw flue gas outlet 109. The hot gas with the temperature of 600-1000 ℃ generated by the combustion of the gas hot blast stove 6 enters a first flue gas pipeline L101, the flue gas is heated to the denitration reaction temperature of 180-300 ℃, and simultaneously, the ammonia supply device 5 adds gaseous NH into the first flue gas pipeline L101 3 Flue gas and NH 3 After being mixed evenly, the mixture enters a denitration reactor 2, and NO in the flue gas is reacted by a denitration catalyst 201 x And NH 3 Reaction to produce N 2 And water to complete the flue gas denitration process.
The flue gas after denitration enters the adsorption heat exchange area again through the second flue gas pipeline L102 and the clean flue gas inlet 110, recovers heat through the heat exchange element 104 for cooling, passes through the CO adsorbent 105 again, completes secondary adsorption of CO, and is discharged through a chimney.
S2: the CO is comprehensively utilized and the method has the advantages of high efficiency,
the CO adsorbent 105 which completes the carbon monoxide adsorption in the adsorption heat exchange area circularly rotates to enter the desorption area under the cooperation of the rotor 102 and the driving device 103; the desorption fan 3 blows hot flue gas with the temperature of 180-300 ℃ in the second flue gas pipeline L102 into the desorption wind inlet 112. In the desorption zone, the CO adsorbent 105 is heated and regenerated, so that CO is desorbed from the CO adsorbent 105 and enters the CO utilization device 4 along with the desorption wind through the desorption wind outlet 113 and the third flue gas pipeline L103, and in the CO utilization device 4, CO and oxygen are combusted to generate CO 2 And a large amount of heat is discharged, hot air generated by the CO utilization device 4 enters the first flue gas pipe, so that the flue gas temperature can be raised by 30-50 ℃, and the load of the gas hot blast stove 6 can be reduced or closed at the moment, so that the gas consumption is reduced, and the energy-saving effect is achieved.
In the process, the hot flue gas blown into the desorption area by the desorption fan 3 can realize the following functions:
1. realize the heating regeneration of the CO adsorbent 105, and send the desorbed carbon monoxide to the CO utilization device 4 to realize the comprehensive utilization of CO.
2. By bubbling the denitrated clean flue gas into the desorption zone, a positive pressure cavity can be formed, and NO is avoided x High concentration of NO after the original flue gas is denitrated x The low-concentration clean flue gas side leakage is avoided, and meanwhile NO is prevented from being entrained when the heat exchange element 104 and the CO adsorbent 105 circularly rotate x The original smoke with higher concentration can effectively ensure the NO of the chimney x And (5) discharging after reaching the standard.
Finally, it should be noted that: the foregoing description is only illustrative of the preferred embodiments of the present invention, and although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described, or equivalents may be substituted for elements thereof, and any modifications, equivalents, improvements or changes may be made without departing from the spirit and principles of the present invention.
Claims (8)
1. CO and NO by heat exchanger with CO adsorption function x The system of desorption, including heat exchanger (1) and denitration reactor (2), its characterized in that: the heat exchanger (1) comprises a shell (101), a rotor (102), a driving device (103), heat exchange elements (104), CO adsorbents (105), a bottom gas distribution assembly (106), a top gas distribution assembly (107), a raw gas inlet (108), a raw gas outlet (109), a clean gas inlet (110), a clean gas outlet (111), a desorption air inlet (112) and a desorption air outlet (113), wherein the rotor (102) is rotationally connected inside the shell (101), a plurality of partition plates are arranged inside the rotor (102), the rotor (102) is divided into a plurality of fan-shaped areas by the partition plates, the heat exchange elements (104) are arranged on the upper layer inside each fan-shaped area, the CO adsorbents (105) are arranged on the lower layer inside each fan-shaped area, the top gas distribution assembly (107) is arranged at the upper end of the rotor (102), the bottom gas distribution assembly (106) is arranged at the two sides of the top gas distribution assembly (107), and the desorption air inlet (112) is arranged at the lower end of the rotor (102); the device comprises a shell (101), wherein a driving device (103) is arranged in the middle of the upper end of the shell (101), an original smoke outlet (109) and a clean smoke inlet (110) are respectively arranged on two sides of the upper end of the shell (101), an original smoke inlet (108) and a clean smoke outlet (111) are respectively arranged on two sides of the lower end of the shell (101), the original smoke inlet (108) corresponds to the original smoke outlet (109), and the clean smoke outlet (111) corresponds to the clean smoke inlet (110);
the raw flue gas outlet (109) is connected with an inlet of the denitration reactor (2) through a first flue gas pipeline (L101), a plurality of layers of denitration catalysts (201) are filled in the denitration reactor (2), and an outlet of the denitration reactor (2) is connected with a clean flue gas inlet (110) through a second flue gas pipeline (L102).
2. CO and NO by a heat exchanger with CO adsorption function according to claim 1 x The system for removing is characterized in that: the device also comprises a desorption fan (3) and a CO utilization device (4), wherein the inlet of the desorption fan (3) is connected with a second flue gas pipeline (L102) through a pipeline, and the outlet of the desorption fan (3) is connected with a desorption wind inlet (112) through a pipeline; the desorption wind outlet (113) is connected with an inlet of the CO utilization device (4) through a third flue gas pipeline (L103), and an outlet of the CO utilization device (4) is connected with the first flue gas pipeline (L101) through a pipeline.
3. CO and NO by a heat exchanger with CO adsorption function according to claim 1 x The system for removing is characterized in that: the device further comprises an ammonia supply device (5) and a gas hot blast stove (6), wherein the ammonia supply device (5) and the gas hot blast stove (6) are respectively connected with a first flue gas pipeline (L101) through pipelines.
4. CO and NO by a heat exchanger with CO adsorption function according to claim 2 x The system for removing is characterized in that: and a CO concentration detection device (C1) is arranged on the third flue gas pipeline (L103).
5. CO and NO by a heat exchanger with CO adsorption function according to claim 1 x The system for removing is characterized in that: the fan-shaped area of the top gas distribution assembly (107) and the fan-shaped area of the bottom gas distribution assembly (106) are larger than or equal to the areas of three fan-shaped areas, the top gas distribution assembly (107) and the bottom gas distribution assembly (106) are corresponding, the top gas distribution assembly (107) and the bottom gas distribution assembly (106) divide the heat exchanger (1) into an adsorption heat exchange area and a desorption area, the fan-shaped areas covered by the top gas distribution assembly (107) and the bottom gas distribution assembly (106) are analysis areas, and the remaining fan-shaped areas are adsorption heat exchange areas.
6. Root of Chinese characterA CO and NO process using a heat exchanger with CO adsorption function as claimed in claim 1 x The system for removing is characterized in that: the CO adsorbent (105) is a molecular sieve or an active carbon material of one or more of copper oxide, zinc oxide, aluminum oxide and cobalt oxide, the CO adsorption temperature of the CO adsorbent (105) is 50-100 ℃, and the CO desorption temperature is 180-300 ℃.
7. CO and NO by a heat exchanger with CO adsorption function according to claim 2 x The system for removing is characterized in that: the CO utilization device (4) can be RCO catalytic combustion equipment or RTO regenerative thermal oxidation equipment.
8. Heat exchanger with CO adsorption function for CO and NO x The removing method is characterized in that: comprises the steps of,
s1: CO adsorption and NO x Removing;
s2: and (5) comprehensively utilizing CO.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311534037.8A CN117563379A (en) | 2023-11-17 | 2023-11-17 | CO and NO by heat exchanger with CO adsorption function x System for removal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311534037.8A CN117563379A (en) | 2023-11-17 | 2023-11-17 | CO and NO by heat exchanger with CO adsorption function x System for removal |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN117563379A true CN117563379A (en) | 2024-02-20 |
Family
ID=89861962
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202311534037.8A Pending CN117563379A (en) | 2023-11-17 | 2023-11-17 | CO and NO by heat exchanger with CO adsorption function x System for removal |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN117563379A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN118079598A (en) * | 2024-04-28 | 2024-05-28 | 四川发展环境科学技术研究院有限公司 | Carbon dioxide mineralization capturing reactor |
-
2023
- 2023-11-17 CN CN202311534037.8A patent/CN117563379A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN118079598A (en) * | 2024-04-28 | 2024-05-28 | 四川发展环境科学技术研究院有限公司 | Carbon dioxide mineralization capturing reactor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN208824192U (en) | A kind of VOCs exhaust-gas efficient adsorption/desorption catalyzing burning processing system | |
| CN203437014U (en) | Movable integrated organic waste gas treatment device | |
| CN109794146B (en) | Grate-rotary kiln SNCR/SCR denitration and active coke desulfurization combined system and process | |
| CN106524771B (en) | Process method for denitration of sintering flue gas | |
| CN108579369B (en) | Coke oven flue gas multi-pollutant cooperative treatment system and method | |
| WO2018000857A1 (en) | Flue gas desulfurization and denitrification method and device | |
| CN103331086A (en) | Movable integrated device for treating organic waste gas | |
| CN107694282A (en) | Utilize the technique and device of activated carbon processing organic exhaust gas | |
| CN105771946A (en) | Regeneration system and method for activated coke | |
| CN111482052A (en) | Module combined type VOC waste gas purification equipment and waste gas purification method | |
| CN210699424U (en) | Organic waste gas adsorbs desorption catalytic combustion system | |
| CN203437035U (en) | Movable enrichment-fixed catalytic oxidation type organic waste gas treatment device | |
| CN113975938B (en) | Rotary device and method for adsorbing and capturing carbon dioxide in flue gas at low temperature | |
| CN106984169A (en) | The denitrating system and method for a kind of direct utilization sintering deposit heat | |
| CN201295583Y (en) | Adsorption and catalysis integration device | |
| CN114984721B (en) | System and method for recycling carbon dioxide in flue gas | |
| CN106621702A (en) | Organic exhaust gas concentration treatment device | |
| CN210186776U (en) | Waste gas treatment system for semiconductor industry | |
| CN110917813A (en) | Integrated treatment process and device for harmful gas in production of new composite material | |
| CN213824071U (en) | Active carbon adsorption and desorption catalytic combustion equipment | |
| CN112322363A (en) | Nano composite zeolite adsorption blast furnace gas fine desulfurization process and device | |
| CN211328798U (en) | Movable catalytic combustion active carbon regenerating unit | |
| CN117563379A (en) | CO and NO by heat exchanger with CO adsorption function x System for removal | |
| CN112076586A (en) | Catalytic combustion device and waste gas treatment method thereof | |
| CN208583143U (en) | Afterheat utilizing system |
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 |