CN115234918A - No CO based on fluoroplastics heat exchanger 2 Waste incineration power generation system and operation mode thereof - Google Patents
No CO based on fluoroplastics heat exchanger 2 Waste incineration power generation system and operation mode thereof Download PDFInfo
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- 238000010248 power generation Methods 0.000 title claims abstract description 33
- 238000004056 waste incineration Methods 0.000 title claims abstract description 31
- 229920002313 fluoropolymer Polymers 0.000 title claims description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 77
- 239000003546 flue gas Substances 0.000 claims abstract description 77
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 35
- 238000000926 separation method Methods 0.000 claims abstract description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 9
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 9
- 239000001301 oxygen Substances 0.000 claims abstract description 9
- 238000000034 method Methods 0.000 claims description 32
- 230000008569 process Effects 0.000 claims description 28
- 238000001816 cooling Methods 0.000 claims description 26
- 230000007704 transition Effects 0.000 claims description 21
- 230000006835 compression Effects 0.000 claims description 17
- 238000007906 compression Methods 0.000 claims description 17
- 238000010438 heat treatment Methods 0.000 claims description 16
- 238000005516 engineering process Methods 0.000 claims description 15
- 238000006386 neutralization reaction Methods 0.000 claims description 15
- 239000000428 dust Substances 0.000 claims description 14
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 10
- 238000010521 absorption reaction Methods 0.000 claims description 10
- 238000006477 desulfuration reaction Methods 0.000 claims description 6
- 230000023556 desulfurization Effects 0.000 claims description 6
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 3
- 239000000920 calcium hydroxide Substances 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 239000000498 cooling water Substances 0.000 claims description 3
- 239000007789 gas Substances 0.000 claims description 3
- 238000002309 gasification Methods 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 2
- 239000002912 waste gas Substances 0.000 claims description 2
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 abstract description 9
- 229910052731 fluorine Inorganic materials 0.000 abstract description 9
- 239000011737 fluorine Substances 0.000 abstract description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 6
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000002485 combustion reaction Methods 0.000 abstract description 3
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 3
- 238000000746 purification Methods 0.000 abstract description 3
- 238000011084 recovery Methods 0.000 abstract description 3
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000010531 catalytic reduction reaction Methods 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/006—General arrangement of incineration plant, e.g. flow sheets
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
- F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
- F01D15/10—Adaptations for driving, or combinations with, electric generators
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
- F23J15/025—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using filters
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
- F23L7/007—Supplying oxygen or oxygen-enriched air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/20—Waste heat recuperation using the heat in association with another installation
- F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/10—Nitrogen; Compounds thereof
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/10—Nitrogen; Compounds thereof
- F23J2215/101—Nitrous oxide (N2O)
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/20—Sulfur; Compounds thereof
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2217/00—Intercepting solids
- F23J2217/10—Intercepting solids by filters
- F23J2217/101—Baghouse type
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/12—Heat utilisation in combustion or incineration of waste
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Chimneys And Flues (AREA)
Abstract
The invention discloses a fluorine plastic heat exchanger-based CO-free heat exchanger 2 A waste incineration power generation system and an operation mode thereof belong to the technical field of waste incineration power generation, and the system can be implemented on continentsThe system adopts energy step recovery, respectively recovers sensible heat and latent heat of the flue gas and replaces part of low-pressure heaters, saves water resources, improves the heat efficiency of a garbage power plant and a garbage incineration power plant, and compresses or absorbs CO 2 Avoiding the formation of stable CO 2 In addition, the air separation device provides pure oxygen, the pure oxygen and the backflow flue gas are mixed and then enter the incinerator for combustion, nitrogen doping in the flue gas is avoided, equipment load of all flue gas purification ends is reduced, economic benefits of the whole plant are improved, the flue gas and the oxygen are mixed in proportion and then are distributed in a grading mode, existing equipment such as a fire grate of a project is protected, extra equipment replacement is not needed, tail flue gas is compressed in a grading mode, and industrial products SO are produced without extra equipment replacement 2 And so on.
Description
Technical Field
The invention belongs to the technical field of waste incineration power generation, and particularly relates to a fluorine plastic heat exchanger-based CO-free heat exchanger 2 A waste incineration power generation system and an operation mode thereof.
Background
As shown in FIG. 1, a common waste incineration power generation system only aims at SO x 、NO x Pollutants such as dioxin, particulate matters and the like are purified and controlled, but CO is not carried out 2 Emission reduction, one common 500 t/d incinerator discharges CO more than or equal to 350 t every day 2 And the discharge amount is huge.
The invention patent CN112555834A waste incineration system and method of coupled chemical chain air separation technology discloses a waste incineration system and method based on CO 2 The system mainly comprises a chemical chain air separation oxygen absorption and release device and a carbon capture device besides the traditional process. The difference from the traditional system is that: (1) o provided by chemical-looping air separation plant 2 The return flue gas enters the incinerator to replace the traditional mode that air and return flue gas enter the incinerator; (2) the treated flue gas enters a carbon capture device for CO 2 Separation from water vapor to reduce CO 2 Is discharged.
The above invention can theoretically achieve carbon capture, but the core problem is that: (1) nearly no mature CO suitable for complex smoke components in China 2 The trapping technology is difficult to realize, and the invention avoids the technology to realize the total CO 2 Trapping; (2) CO 2 2 The trapping technology has expensive equipment and high operation cost, and a more reliable and low-cost way for realizing CO is searched 2 And (4) trapping. The invention is different from the invention in principle, starting point, main equipment type selection, energy cascade utilization and other aspects.
The invention patent CN102531318A, a sludge drying and incineration integrated zero-emission treatment system and treatment process, discloses a condenser and compressor-based CO-free treatment system 2 The discharged garbage incineration power generation system is different from the traditional process system in that the system treats sludge and garbage and realizes CO 2 Trapping, but the flue gas treatment system of the invention is not reasonable in design (without flue gas treatment system, default flue gas is only CO 2 And H 2 O), the waste heat recovery system is not designed reasonably (no fractional waste heat recovery, serious waste), the condensation design is not designed reasonably (heat of condensation)Large in amount and the condensate water inevitably corrodes the condenser).
In conclusion, there is no CO-free system that is practical and similar to the present invention 2 And (5) an emission reconstruction process.
Disclosure of Invention
Aiming at the technical problems in the prior art, the invention aims to provide a fluorine plastic heat exchanger-based CO-free heat exchanger 2 The 0 carbon emission of the waste incineration power plant is realized by the waste incineration power generation system.
In order to achieve the above purpose, the invention adopts the following technical scheme:
fluorine plastic heat exchanger-based CO-free heat exchanger 2 Discharge waste incineration power generation system, including air separation plant, air separation plant is connected with storage adjusting device, storage adjusting device is connected with burning furnace, it is connected with transition flue to burn furnace, transition flue is connected with horizontal flue heated surface, horizontal flue heated surface is connected with the sack cleaner, the sack cleaner is connected with burning furnace, SCR denitrification facility respectively, SCR denitrification facility is connected with I level MGWH, I level MGWH is connected with II level MGWH, II level MGWH is connected with condenser, cooling tower, neutralization pond respectively, the condenser is connected with hierarchical compressor arrangement, horizontal flue heated surface still is connected with turbo generator set, turbo generator set is connected with the condenser, the condenser is connected with low pressure heater, low pressure heater is connected with II level MGWH, II level MGWH is connected with I level MGWH, I level MGWH still is connected with the oxygen-eliminating device, the oxygen-eliminating device is connected with horizontal flue heated surface, the heat receiver still is connected with the cooling tower, the cooling tower is connected with condenser, II level MGWH respectively.
Furthermore, the incineration hearth is a circulating fluidized bed furnace or a grate furnace.
Further, the incineration hearth is a circulating fluidized bed furnace.
Furthermore, the incineration hearth is a boiling furnace hearth, a desulfurization and deacidification technology is adopted in the incineration hearth, the transition flue is a side flue gas output port and a separator, the transition flue is connected with the incineration hearth, and materials separated from the transition flue return to the incineration hearth to be continuously incinerated.
Furthermore, the incineration hearth is a grate furnace.
Furthermore, the incineration hearth is a first vertical flue, an SNCR technology is adopted in the incineration hearth, and the transition flue is a second vertical flue and a third vertical flue.
Further, the staged compression device is connected with a neutralization pond.
The fluorine plastic heat exchanger-based CO-free 2 The operation mode of the waste incineration power generation system comprises a flue gas end process stroke, a working medium water end process stroke and a cooling circulating water end process stroke;
the process stroke of the flue gas end is as follows: the air separation device carries out air separation, oxygen-rich flow is generated and enters the storage adjusting device, the storage adjusting device carries out air quantity distribution according to project load, the air-rich flow and the flue gas in the bag-type dust remover are mixed, the flue gas and the flue gas in the bag-type dust remover enter an incineration hearth to be combusted with garbage and carry out desulfurization and denitration, high-temperature flue gas which is completely combusted in the incineration hearth enters a horizontal flue heating surface through a transition flue to release heat, the temperature of the flue gas after being cooled is not lower than 180 ℃, the flue gas enters the bag-type dust remover to be dedusted, the flue gas after being dedusted is divided into two flows, a flow of the flue gas a returns to the incineration hearth, a flow of the flue gas b enters an SCR (selective catalytic reduction) denitration device to carry out denitration reaction, the flue gas after being denitrified enters a first-level MGWH to release the sensible heat of the flue gas to 70-110 ℃, then enters a second-level MGWH to release gasification latent heat and sensible heat, the flue gas after being heated enters a condenser to be continuously cooled to be below 30 ℃, and then enters a graded compression device to be compressed, wherein low-pressure-stage condensate is industrial product sulfur dioxide and the industrial product sulfur dioxide, and the non-compressible gas is discharged as waste gas;
the process stroke of the working medium water end is as follows: the working medium steam after heat absorption of the heating surface of the horizontal flue enters a turbo generator set for power generation, the exhaust steam after power generation enters a condenser to be condensed into saturated water, then sequentially enters a low-pressure heater, a second-level MGWH and a first-level MGWH for heating, and the working medium water after entering a deaerator for deaerating enters the tail part of the heating surface of the horizontal flue to continuously absorb heat;
the cooling circulating water end process stroke is as follows: the low-temperature cooling water provided by the cooling tower enters the condenser and the II-level MGWH to cool the steam and the flue gas respectively, and the cooling circulating water after absorbing heat returns to the cooling tower to release heat.
Further, the operation mode also comprises other process strokes: and the condensed water at the flue gas end of the second-level MGWH enters a neutralization tank to react with calcium hydroxide.
Further, the operation mode also comprises other process strokes: and introducing the low-pressure section condensate and the high-pressure section condensate in the staged compression device into a neutralization tank for absorption reaction.
Furthermore, the flue gas is divided into two paths, and the flue gas with corresponding amount flows back according to the load and the quantitative design of the backflow flue gas.
Compared with the prior art, the invention has the following beneficial effects:
1) Fluorine plastic heat exchanger-based CO-free heat exchanger 2 The waste incineration power generation system has the feasibility of implementation;
2) The energy is recycled in a gradient way, sensible heat and latent heat of the flue gas are respectively recycled, and part of low-pressure heaters are replaced, so that water resources are saved, the heat efficiency of a waste power plant is improved, and the heat efficiency of a waste incineration power plant is improved;
3) Compressing CO 2 Or absorb CO 2 Avoiding the immature and stable CO 2 Trapping technology, and the expensive investment and operating costs of the device;
4) The air separation device is used for providing pure oxygen, and the pure oxygen and the backflow flue gas are mixed and then enter the incinerator for combustion, so that nitrogen doping in the flue gas is avoided, the equipment load of all flue gas purification ends such as a fan, a deacidification device and a bag dust removal device is reduced, and the economic benefit of the whole plant is improved;
5) The flue gas and the oxygen are mixed in proportion and then are distributed in a grading manner, so that existing equipment such as a fire grate and the like in a project are protected, and extra equipment replacement is not needed;
6) Staged compression of tail flue gas to produce industrial products SO 2 、SO 3 And CO 2 And the like.
Drawings
FIG. 1 is a flow chart of a conventional waste incineration power generation process in the background art;
FIG. 2 shows a fluoroplastic-based heat exchanger without CO in example 1 of the present invention 2 The structure schematic diagram of the waste incineration power generation system is discharged;
in the figure: the method comprises the following steps of 1-air separation device, 2-storage adjusting device, 3-incineration hearth, 4-transition flue, 5-horizontal flue heating surface, 6-bag dust remover, 7-SCR denitration device, 8-I-level MGWH, 9-II-level MGWH, 10-condenser, 11-stage compression device, 12-turbo generator set, 13-condenser, 14-low pressure heater, 15-cooling tower, 16-neutralization pond and 17-deaerator.
Detailed Description
The embodiments of the present invention will be described in conjunction with the accompanying drawings, and it should be understood that the embodiments described herein are only for the purpose of illustrating and explaining the present invention, and are not intended to limit the present invention. In addition, if a detailed description of known technologies is not necessary to illustrate the features of the present invention, it is omitted. In the application, the MGWH is a fluoroplastic heat exchanger, is totally called Mitsubishi Gas-Water Heater, absorbs heat from flue Gas in a Water circulation mode, releases heat to Water supply, and can absorb flue Gas waste heat or recover condensation heat of Water vapor in the flue Gas on the premise of avoiding low-temperature corrosion; SNCR is a non-selective catalytic reduction denitration technology; SCR is a selective catalytic reduction denitration technology.
Example 1
The invention relates to a fluorine plastic heat exchanger-based CO-free heat exchanger 2 The structural schematic diagram of the waste incineration power generation system is shown in figure 2, and comprises an air separation device 1, wherein the air separation device 1 is connected with a storage adjusting device 2, the storage adjusting device 2 is connected with an incineration hearth 3, the incineration hearth 3 is connected with a transition flue 4, the transition flue 4 is connected with a horizontal flue heating surface 5, the horizontal flue heating surface 5 is connected with a bag-type dust collector 6, the bag-type dust collector 6 is respectively connected with the incineration hearth 3 and an SCR (selective catalytic reduction) denitration device 7, the SCR denitration device 7 is connected with a first-level MGWH 8, the first-level MGWH 8 is connected with a second-level MGWH 9, the second-level MGWH 9 is respectively connected with a condenser 10, a cooling tower 15 and a neutralization pond 16, the condenser 10 is connected with a grading compression device 11, and the horizontal flue heating surface is connected with a grading compression device 11The face 5 still is connected with turbo generator set 12, turbo generator set 12 is connected with condenser 13, condenser 13 is connected with low pressure feed water heater 14, low pressure feed water heater 14 is connected with II grades of MGWH 9, II grades of MGWH 9 are connected with I grades of MGWH 8, I grades of MGWH 8 still is connected with oxygen-eliminating device 17, oxygen-eliminating device 17 is connected with horizontal flue heated surface 5, condenser 13 still is connected with cooling tower 15, cooling tower 15 is connected with condenser 13, II grades of MGWH 9 respectively.
The incinerator furnace 3 is a circulating fluidized bed furnace, the incinerator furnace 3 is a boiling furnace, a desulfurization and deacidification technology is adopted in the incinerator furnace 3, the transition flue 4 is a side flue gas output port and a separator, the transition flue 4 is connected with the incinerator furnace 3, and materials separated from the transition flue 4 return to the incinerator furnace 3 to be continuously incinerated.
The fluorine plastic heat exchanger-based CO-free 2 The operation mode of the waste incineration power generation system comprises a flue gas end process stroke, a working medium water end process stroke and a cooling circulating water end process stroke;
the process stroke of the flue gas end is as follows: the air separation device 1 carries out air separation, oxygen-rich flow is generated and enters a storage adjusting device 2, the storage adjusting device 2 carries out air quantity distribution according to project load, the air-rich flow and the flue gas in a bag-type dust collector 6 are mixed and enter an incineration hearth 3 to be combusted with garbage, desulfurization and denitration are carried out, high-temperature flue gas which is completely combusted in the incineration hearth 3 enters a horizontal flue heating surface 5 after passing through a transition flue 4 to release heat, the temperature of the flue gas after being cooled is not lower than 180 ℃, the flue gas enters the bag-type dust collector 6 to be dedusted, the flue gas after being dedusted is divided into two flows, namely according to the quantitative design of the returned flue gas, the corresponding amount of flue gas a is returned to the incineration hearth 3, the flue gas b enters an SCR denitration device 7 to carry out denitration reaction, the flue gas after being denitrified enters an I-level MGWH 8 to release sensible heat to 70-110 ℃, then enters a II-level MGWH 9 to release gasification latent heat and sensible heat, the flue gas after being heated enters a condenser 10 to be continuously cooled to be below 30 ℃, and then enters a staged compression device 11 to be compressed, wherein low-pressure condensation liquid is industrial products such as sulfur dioxide and is not compressible gas;
the process stroke of the working medium water end is as follows: the working medium steam after heat absorption of the horizontal flue heating surface 5 enters a turbo generator unit 12 for power generation, the exhaust steam after power generation enters a condenser 13 to be condensed into saturated water, then sequentially enters a low-pressure heater 14, a second-level MGWH 9 and a first-level MGWH 8 for heating, and the working medium water after oxygen removal entering a deaerator 17 enters the tail part of the horizontal flue heating surface 5 for continuous heat absorption;
the cooling circulating water end process stroke is as follows: the low-temperature cooling water provided by the cooling tower 15 enters the condenser 13 and the II-level MGWH 9 to respectively cool the steam and the flue gas, and the cooling circulating water after absorbing heat returns to the cooling tower 15 to release heat.
The operation mode also comprises other process strokes: condensed water at the flue gas end of the second-level MGWH 9 enters a neutralization tank 16 to react with calcium hydroxide.
Example 2
The difference from embodiment 1 is that the incineration furnace 3 is a grate furnace, the incineration furnace 3 is a first vertical flue, the SNCR technology is adopted in the incineration furnace 3, and the transition flue 4 is a second vertical flue and a third vertical flue, as in embodiment 1.
Example 3
Unlike example 1, the staged compression device 11 is connected to the neutralization tank 16, and the low-pressure-stage condensate and the high-pressure-stage condensate in the staged compression device 11 are introduced into the neutralization tank 16 to perform an absorption reaction, unlike example 1.
Example 4
Unlike example 2, the difference from example 2 is that the staged compression device 11 is connected to the neutralization tank 16, and the low-pressure-stage condensate and the high-pressure-stage condensate in the staged compression device 11 are introduced into the neutralization tank 16 for absorption reaction.
The invention relates to a fluorine plastic heat exchanger-based CO-free 2 The waste incineration power generation system has the feasibility of implementation; the energy is recycled in a gradient way, sensible heat and latent heat of the flue gas are respectively recycled, and part of low-pressure heaters are replaced, so that water resources are saved, the thermal efficiency of a waste power plant is improved, and the thermal efficiency of a waste incineration power plant is improved; compressing CO 2 Or absorb CO 2 Avoiding the immature and stable CO 2 Trapping technology, and the expensive investment and operating costs of the device; the air separation device is used for providing pure oxygen, and the pure oxygen and the backflow flue gas are mixed and then enter the incinerator for combustion, so that nitrogen doping in the flue gas is avoided, the equipment load of all flue gas purification ends such as a fan, a deacidification device and a bag dust removal device is reduced, and the economic benefit of the whole plant is improved; the flue gas and the oxygen are mixed in proportion and then are distributed in a grading manner, so that existing equipment such as a fire grate and the like in a project are protected, and extra equipment replacement is not needed; staged compression of tail flue gas to produce industrial products SO 2 、SO 3 And CO 2 And the like.
Finally, it should be noted that the above-mentioned embodiments are only preferred embodiments of the present invention, and not intended to limit 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 and equivalents can be made in the technical solutions described in the foregoing embodiments, or some technical features thereof can be replaced. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. No CO based on fluoroplastics heat exchanger 2 The waste incineration power generation system is characterized in that: including air separation plant (1), air separation plant (1) is connected with storage adjusting device (2), it is connected with incineration furnace (3) to store adjusting device (2), incineration furnace (3) are connected with transition flue (4), transition flue (4) are connected with horizontal flue heated surface (5), horizontal flue heated surface (5) are connected with sack cleaner (6), sack cleaner (6) are connected with incineration furnace (3), SCR denitrification facility (7) respectively, SCR denitrification facility (7) are connected with I level MGWH (8), I level MGWH (8) are connected with II level MGWH (9), II level MGWH (9) are connected with condenser (10), cooling tower (15), neutralization pond (16) respectively, condenser (10) are connected with hierarchical compression device (11), horizontal flue heated surface (5) still with the turbine of launchingMotor group (12) are connected, turbo generator group (12) are connected with condenser (13), condenser (13) are connected with low pressure heater (14), low pressure heater (14) are connected with II grades of MGWH (9), II grades of MGWH (9) are connected with I grades of MGWH (8), I grades of MGWH (8) still are connected with oxygen-eliminating device (17), oxygen-eliminating device (17) are connected with horizontal flue heated surface (5), condenser (13) still are connected with cooling tower (15), cooling tower (15) are connected with condenser (13), II grades of MGWH (9) respectively.
2. The fluoroplastic heat exchanger-based CO-free device according to claim 1 2 The waste incineration power generation system is characterized in that: the incineration hearth (3) is a circulating fluidized bed furnace or a grate furnace.
3. The CO-free fluoroplastic heat exchanger based on claim 2 2 The waste incineration power generation system is characterized in that: the incineration hearth (3) is a circulating fluidized bed furnace.
4. CO-free heat exchanger based on fluoroplastic according to claim 3 2 The waste incineration power generation system is characterized in that: the incinerator hearth (3) is a fluidized bed furnace hearth, a desulfurization and deacidification technology is adopted in the incinerator hearth (3), the transition flue (4) is a side flue gas output port and a separator, the transition flue (4) is connected with the incinerator hearth (3), and materials separated in the transition flue (4) return to the incinerator hearth (3) to be continuously incinerated.
5. The fluoroplastic heat exchanger-based CO-free device according to claim 2 2 The waste incineration power generation system is characterized in that: the incineration hearth (3) is a grate furnace.
6. CO-free heat exchanger based on fluoroplastic according to claim 5 2 The waste incineration power generation system is characterized in that: what is neededThe incineration hearth (3) is a first vertical flue, an SNCR technology is adopted in the incineration hearth (3), and the transition flue (4) is a second vertical flue and a third vertical flue.
7. The fluoroplastic heat exchanger-based CO-free device according to claim 1 2 The waste incineration power generation system is characterized in that: the staged compression device (11) is connected with a neutralization tank (16).
8. A fluoroplastic heat exchanger based CO-free set forth in any one of claims 1~7 2 The operation mode of the waste incineration power generation system is characterized in that: the method comprises a flue gas end process stroke, a working medium water end process stroke and a cooling circulating water end process stroke;
the process stroke of the flue gas end is as follows: the air separation device (1) carries out air separation, oxygen-enriched flow is generated and enters the storage adjusting device (2), the storage adjusting device (2) carries out air quantity distribution according to project load, the air-enriched flow and the flue gas in the bag-type dust collector (6) are mixed and enter the incineration hearth (3) to be combusted with garbage, desulfurization and denitrification are carried out, high-temperature flue gas which is completely combusted in the incineration hearth (3) enters a horizontal flue heating surface (5) through a transition flue (4) to release heat, the temperature of the flue gas after cooling is not lower than 180 ℃, the flue gas enters the bag-type dust collector (6) to remove dust, the flue gas after dust removal is divided into two paths, flue gas a flows back to the incineration hearth (3), flue gas b enters the SCR denitrification device (7) to carry out denitrification reaction, the flue gas after denitrification enters the I-stage MGWH (8) to release flue gas sensible heat to 70 to 110 ℃, then enters the II-stage MGWH (9) to release gasification latent heat and sensible heat, the flue gas after heat and the heat release enter the condenser (10) to be cooled to be below 30 ℃, and then enter the graded compression device (11) to be compressed, wherein low-pressure sulfur dioxide and sulfur dioxide condensate industrial products are industrial products which are uncondensed and non-condensable liquid, and are non-condensable gas which are used as waste gas which can not be compressed;
the process stroke of the working medium water end is as follows: working medium steam after heat absorption of the horizontal flue heating surface (5) enters a turbo generator set (12) for power generation, exhaust steam after power generation enters a condenser (13) to be condensed into saturated water, then sequentially enters a low-pressure heater (14), a second-level MGWH (9) and a first-level MGWH (8) for heating, and working medium water after oxygen removal entering a deaerator (17) enters the tail part of the horizontal flue heating surface (5) for continuous heat absorption;
the cooling circulating water end process stroke is as follows: the low-temperature cooling water provided by the cooling tower (15) enters the condenser (13) and the second-level MGWH (9) to respectively cool the steam and the flue gas, and the cooling circulating water after absorbing heat returns to the cooling tower (15) to release heat.
9. CO-free heat exchanger based on fluoroplastics according to claim 8 2 The operation mode of the waste incineration power generation system is characterized in that: the operation mode also comprises other process strokes: condensed water at the flue gas end of the second-level MGWH (9) enters a neutralization tank (16) to react with calcium hydroxide.
10. CO-free heat exchanger based on fluoroplastic according to claim 8 2 The operation mode of the waste incineration power generation system is characterized in that: the operation mode also comprises other process strokes: the low-pressure section condensate and the high-pressure section condensate in the staged compression device (11) are introduced into a neutralization tank (16) for absorption reaction.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104501176A (en) * | 2014-11-15 | 2015-04-08 | 北京交通大学 | Harmless disposal system for refuse and method for refuse disposal by harmless disposal system |
| CN114623447A (en) * | 2022-03-25 | 2022-06-14 | 光大环境科技（中国）有限公司 | Waste incineration system and method without carbon dioxide emission |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104501176A (en) * | 2014-11-15 | 2015-04-08 | 北京交通大学 | Harmless disposal system for refuse and method for refuse disposal by harmless disposal system |
| CN114623447A (en) * | 2022-03-25 | 2022-06-14 | 光大环境科技（中国）有限公司 | Waste incineration system and method without carbon dioxide emission |
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