CN115337771B - Coal-fired coupled sludge incineration power generation method - Google Patents
Coal-fired coupled sludge incineration power generation method Download PDFInfo
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- CN115337771B CN115337771B CN202211037691.3A CN202211037691A CN115337771B CN 115337771 B CN115337771 B CN 115337771B CN 202211037691 A CN202211037691 A CN 202211037691A CN 115337771 B CN115337771 B CN 115337771B
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- 239000010802 sludge Substances 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 38
- 238000010248 power generation Methods 0.000 title claims abstract description 16
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 43
- 239000003245 coal Substances 0.000 claims abstract description 39
- 239000007791 liquid phase Substances 0.000 claims abstract description 31
- 239000007789 gas Substances 0.000 claims abstract description 28
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 17
- 238000010438 heat treatment Methods 0.000 claims abstract description 16
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 13
- 238000001816 cooling Methods 0.000 claims abstract description 9
- 239000011259 mixed solution Substances 0.000 claims abstract description 6
- 238000002156 mixing Methods 0.000 claims abstract description 6
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 claims abstract description 5
- 235000012501 ammonium carbonate Nutrition 0.000 claims abstract description 5
- 239000001099 ammonium carbonate Substances 0.000 claims abstract description 5
- 238000012544 monitoring process Methods 0.000 claims abstract description 5
- 238000005507 spraying Methods 0.000 claims abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 20
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 16
- 239000003546 flue gas Substances 0.000 claims description 16
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 16
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 15
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 15
- 230000008569 process Effects 0.000 claims description 7
- 230000005611 electricity Effects 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 3
- 238000006297 dehydration reaction Methods 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000003054 catalyst Substances 0.000 abstract description 10
- 239000003638 chemical reducing agent Substances 0.000 abstract description 9
- 230000000694 effects Effects 0.000 abstract description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 5
- 239000004202 carbamide Substances 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 231100000331 toxic Toxicity 0.000 description 2
- 230000002588 toxic effect Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 230000003071 parasitic effect Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 244000052769 pathogen Species 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
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
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/001—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for sludges or waste products from water treatment installations
-
- 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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/18—Treatment of sludge; Devices therefor by thermal conditioning
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- 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
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Mechanical Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Physics & Mathematics (AREA)
- Hydrology & Water Resources (AREA)
- Organic Chemistry (AREA)
- Thermal Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Treatment Of Sludge (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to a coal-fired coupled sludge incineration power generation method, which comprises the following steps: adding a baking machine after a desiccator for dehydrating sludge, heating sludge from an outlet of the desiccator to generate baked sludge and baked gas, feeding the baked sludge into a pulverized coal furnace for burning, mixing the baked gas with part of steam from the desiccator, cooling to obtain a liquid phase and non-condensable gas, mixing the liquid phase with a mixed solution of ammonia and ammonium carbonate, monitoring the concentration of ammonia nitrogen in the mixed solution in real time, feeding back to a steam three-way valve at the outlet of the desiccator, adjusting the opening of the valve, pressurizing the liquid phase by an ammonia pump, spraying the liquid phase from the upper part of a hearth of the pulverized coal furnace, and reducing NO generated by burning the baked sludge X Non-condensable gas is sent into a pulverized coal furnace for burning. Compared with the prior art, the invention can lead NO in the furnace to be generated under the condition of NO addition of reducing agent X The concentration is reduced to 50mg/Nm 3 In the following, the denitration effect which can be achieved by adopting the SCR denitration method of the catalyst is achieved, and the running cost is greatly reduced.
Description
Technical Field
The invention relates to the field of sludge treatment, in particular to a coal-fired coupled sludge incineration power generation method.
Background
Municipal sludge is sourced from municipal sewage treatment plants, and the sludge yield rises year after year with the improvement of resident living standard. The sludge contains a large amount of nutrient substances such as nitrogen and phosphorus, and also contains toxic and harmful substances such as heavy metals, pathogens, parasitic ova and toxic organic matters, and if the sludge is not treated effectively, the environment is seriously polluted, and the physical health of people is affected. The municipal sewage and sludge has high ash content ratio and relatively low heat value, and the sludge is mixed into the pulverized coal furnace for coupling incineration in the coal-fired power plant to reduce the cost, so that compared with the independent incineration of the sludge, the method has the advantages of saving investment of drying equipment and flue gas purification equipment, on one hand, the function of the coal-fired power plant for serving cities is expanded, on the other hand, the carbon reduction capacity of the coal-fired power plant is improved, and the method has great significance in realizing low-cost and high-efficiency disposal of the municipal sludge and ensuring the coal-fired power generation capacity.
The nitrogen content of the power coal in China is about 1%, the nitrogen content of the sludge is generally between 3 and 9%, and the hearth temperature of a coal powder furnace commonly used for coal-fired power generation is higher, so that a large amount of NO is generated X Is formed and discharged. Therefore, methods such as SNCR and SCR are commonly used for denitration after combustion of flue gas generated by coal. The SCR reaction temperature is low, the purification rate is high and can reach more than 85%, but due to the fact that the catalyst is needed to be used, certain pollutants in the flue gas can poison the catalyst, dust particles with high dispersity can cover the surface of the catalyst, and the activity of the catalyst is reduced; in addition, some unreacted NH is present in the system 3 And SO in flue gas 2 Acting to produce (NH) which is prone to corrosion and plugging equipment 4 ) 2 SO 4 And NH 4 HSO 4 Meanwhile, the utilization rate of ammonia is reduced, and the investment and the operation cost are high. While SNCR needs to spray reducing agents such as ammonia, urea and the like into the flue gas in a specific temperature window (850-1050 ℃) to achieve higher denitration efficiency and even ultra-low emission of NOx, but has NO catalyst, strict requirements on temperature, low temperature and NO X The conversion rate is low; in addition, in the SNCR process, the main operation cost is the investment cost of the reducing agent, for a 660MW pulverized coal furnace, the consumption of liquid ammonia of SNCR is about 3t/d each day, the current liquid ammonia cost is about 5000 yuan/t, the SNCR method is adopted to treat the flue gas generated by sludge combined fire coal burning, the cost of liquid ammonia only reaches more than 500 ten thousand yuan each year, and the cost of urea serving as the reducing agent is higher. Therefore, for the coal-fired power plant of the sludge, a coal-fired power generation method with low cost and good denitration effect is needed.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide the coal-fired coupled sludge incineration power generation method, which can achieve good denitration effect without adding a reducing agent and greatly reduce the operation cost.
The aim of the invention can be achieved by the following technical scheme:
the invention aims to provide a coal-fired coupled sludge incineration power generation method, which comprises the following steps of:
s1, dehydrating sludge in a desiccator to obtain dehydrated sludge and water vapor;
s21, sending the dehydrated sludge obtained in the S1 into a baking machine for heating to obtain baked sludge and baked gas production;
s22, sending the water vapor obtained in the S1 into a three-way valve, dividing the water vapor into two parts, mixing the first part of water vapor with the baked gas obtained in the S21 to prepare ammonia water, and carrying out aftertreatment on the second part of water vapor;
s31, sending the baked sludge obtained in the S21 into a pulverized coal furnace for incineration;
s32, mixing the baked gas obtained in the S21 with the first steam obtained in the S22, and then sending the mixture into a condenser for cooling to obtain a liquid phase and non-condensable gas;
s4, monitoring ammonia nitrogen concentration of a liquid phase in the condenser, feeding back to the three-way valve, adjusting the opening of the three-way valve, and controlling the amount of the first stream of water vapor in S22;
s5, feeding the liquid phase obtained in the S32 into an ammonia water pump for pressurization, spraying into the pulverized coal furnace, and reducing NOx generated by incineration of baked sludge;
and S6, feeding the non-condensable gas obtained in the S32 into the pulverized coal furnace for incineration.
Preferably, the temperature of the dewatered sludge in S1 at the outlet of the drier is 75-110 ℃.
Preferably, the temperature of heating of the baking machine in the step S21 is 200-300 ℃ and the speed is 10-100 ℃/min.
Further preferably, the temperature at which the baking machine heats in S21 is 300 ℃.
Preferably, the heat source used for heating the baking machine in S21 is high-temperature flue gas generated by burning in the pulverized coal furnace or steam generated by heating the high-temperature flue gas.
Further, the liquid phase is a mixed solution of ammonia and ammonium carbonate.
Preferably, in S4, the opening degree of the three-way valve is adjusted, and the ammonia concentration in the liquid phase is controlled to be 20-25wt%.
Preferably, the ammonia nitrogen concentration of the liquid phase in the condenser is obtained through an ammonia nitrogen sensor in the step S4.
Preferably, in the step S4, the three-way valve is an electromagnetic three-way valve, a singlechip is further arranged on the three-way valve, and the singlechip is respectively and electrically connected with the ammonia nitrogen sensor and the three-way valve through an I/O interface.
Further, the baking gas production comprises ammonia gas and CO 2 Water vapor, methane and CO, wherein the concentration of ammonia is 40-70wt%.
Further, the non-condensable gas comprises methane and CO.
Preferably, the cooling temperature in S32 is 0-40 ℃.
Preferably, after said pressurizing in S5, the pressure of the liquid phase is greater than 0.3MPa.
Preferably, the heat released in the cooling process in S32 is used to preheat air supplied to the pulverized coal furnace.
Preferably, a storage tank is additionally arranged between the condenser and the ammonia water pump.
Further preferably, the liquid phase obtained in S32 is split into two streams, the first stream is directly fed to the ammonia pump for pressurization, and the second stream is fed to the storage tank for pressurization.
Compared with the prior art, the invention has the following beneficial effects:
1) The method provided by the invention can be used for preparing the catalyst without adding a reducing agent NH 3 In the case of urea or the like, NO in the furnace X The concentration is reduced to 50mg/Nm 3 In the following, the denitration effect is superior to that of the SNCR method, and the denitration effect which can be achieved by adopting the SCR denitration method of the catalyst is achieved, so that the running cost is greatly reduced.
2) On the basis of coupling the traditional pulverized coal furnace with sludge incineration, baking equipment is additionally arranged, a catalyst is not needed, and the cost is far lower than that of SCR facilities.
Drawings
FIG. 1 is a flow chart of a method for generating electricity by coal-fired coupled sludge incineration.
The reference numerals in the figures illustrate:
1. the device comprises a three-way valve, 2, a desiccator, 3, a baking machine, 4, a condenser, 5, a storage tank, 6, a coal dust furnace, 7 and an ammonia water pump.
Detailed Description
The invention will now be described in detail with reference to the drawings and specific examples. The following examples will assist those skilled in the art in further understanding the present invention, but are not intended to limit the invention in any way. It should be noted that variations and modifications could be made by those skilled in the art without departing from the inventive concept. These are all within the scope of the present invention.
In the technical scheme, the characteristics of preparation means, materials, structures or composition ratios and the like which are not explicitly described are regarded as common technical characteristics disclosed in the prior art.
The technical proposal fully realizes the reducing agent NH in the prior art in the conception process 3 The problems caused by urea are innovatively solved without adding reducing agent NH 3 In the case of urea or the like, NO in the furnace X The concentration is reduced to 50mg/Nm 3 In the following, the denitration effect is superior to that of the SNCR method, and the denitration effect which can be achieved by adopting the SCR denitration method of the catalyst is achieved, so that the running cost is greatly reduced.
Example 1
The coal-fired coupled sludge incineration power generation method in the embodiment comprises the following steps:
as shown in fig. 1, surplus sludge with a water content of 80% from municipal sewage treatment plants is sent into a desiccator 2 for dehydration, and dehydrated sludge and water vapor are obtained. The steam is sent to the pulverized coal furnace 6 after passing through the three-way valve 1 or is discharged after condensation treatment, and is sent to the condenser 4 for preparing ammonia water. The dehydrated sludge at the outlet of the desiccator 2 is heated to 300 ℃ at a heating rate of 100 ℃ per minute by feeding the dehydrated sludge into a baker 3, so as to obtain baked sludge and baked gas. The heating source of the baking machine 3 is high-temperature flue gas generated by burning in the pulverized coal furnace 6, and the heated flue gas is sent back to the tail flue to be mixed with main flue gas and is discharged after being purified. The baked sludge is sent into a pulverized coal furnace 6 for incineration. The baking gas comprises ammonia gas and CO 2 Methane,CO, water vapor, wherein the ammonia concentration is 65%. The baked gas is mixed with part of the water vapor from the dryer 2 and then cooled in the condenser 4 to 20 ℃ to obtain liquid phase and non-condensable gas. And the heat released in the cooling process is used for preheating the air fed into the pulverized coal furnace. The non-condensable gas comprises methane and CO, and is sent into the pulverized coal furnace 6 for incineration. The liquid phase is a mixed solution of ammonia and ammonium carbonate.
Monitoring ammonia nitrogen concentration in the liquid phase in real time, feeding back to the three-way valve 1, adjusting the opening of the three-way valve 1, and ensuring NH in the liquid phase 3 The concentration is between 20 and 25wt%. The liquid phase is directly sent to the ammonia water pump 7 for pressurization, or is stored in the storage tank 5 and then sent to the ammonia water pump 7 for pressurization. The liquid phase is pressurized to 0.4MPa by an ammonia water pump 7, sprayed from the upper part of a hearth of a pulverized coal furnace 6, and reduced and baked to NO generated by sludge incineration X NO measured at chimney X The concentration is reduced to 45mg/Nm 3 。
In the specific implementation, the ammonia nitrogen concentration of the liquid phase in the condenser is obtained through an ammonia nitrogen sensor. The three-way valve 1 is an electromagnetic three-way valve, a singlechip is further arranged on the three-way valve 1, and the singlechip is respectively and electrically connected with the ammonia nitrogen sensor and the three-way valve 1 through an I/O interface. The singlechip sends an instruction to the three-way valve 1 based on the ammonia nitrogen concentration, so that the opening control of the three-way valve 1 is realized, and a logic association algorithm between the ammonia nitrogen concentration and the opening of the three-way valve 1 is preset and is not described in detail.
The pressure steam obtained by heating the pulverized coal furnace 6 is input into a steam generator to realize power output.
In specific implementation, the power of the pulverized coal furnace 6 is 660MW. A single 660MW coal powder furnace is coupled with sludge incineration, and the dry sludge treatment capacity is 150 t/day. If the method is adopted for denitration, two baking devices of 75 t/day are additionally arranged in the system, the cost is about 1000 ten thousand yuan, and the baking process before incineration generates ammonia of 150 x 5% (nitrogen content) 35% (ammonia precipitation before 300 degrees) 17/14=3.18 t/day, so that the denitration requirement can be met. If the SCR method is adopted for denitration, the cost of the SCR facility is about 6000 ten thousand yuan. If the SNCR method is adopted for denitration, the consumption of liquid ammonia is 3t per day, the price of the liquid ammonia is 5000 yuan/t, the cost of a denitration reducing agent per day is 1.5 ten thousand yuan, and the cost of ammonia water is about 500 ten thousand yuan per year.
Example 2
The coal-fired coupled sludge incineration power generation method in the embodiment comprises the following steps:
as shown in fig. 1, surplus sludge with a water content of 82% from municipal sewage treatment plants is sent into a desiccator 2 for dehydration, and dehydrated sludge and water vapor are obtained. The steam is sent to the pulverized coal furnace 6 after passing through the three-way valve 1 or is discharged after condensation treatment, and is sent to the condenser 4 for preparing ammonia water. The dehydrated sludge at the outlet of the desiccator 2 is heated to 300 ℃ at a heating rate of 10 ℃/min by feeding the dehydrated sludge into a baker 3, so as to obtain baked sludge and baked gas. The heating source of the baking machine 3 is high-temperature flue gas generated by burning in the pulverized coal furnace 6, and the heated flue gas is sent back to the tail flue to be mixed with main flue gas and is discharged after being purified. The baked sludge is sent into a pulverized coal furnace 6 for incineration. The baking gas comprises ammonia gas and CO 2 Methane, CO, water vapor, wherein the ammonia concentration is 55%. The baked gas is mixed with part of the water vapor from the dryer 2 and then cooled in the condenser 4 to 40 ℃ to obtain liquid phase and non-condensable gas. And the heat released in the cooling process is used for preheating the air fed into the pulverized coal furnace. The non-condensable gas comprises methane and CO, and is sent into the pulverized coal furnace 6 for incineration. The liquid phase is a mixed solution of ammonia and ammonium carbonate.
Monitoring ammonia nitrogen concentration in the liquid phase in real time, feeding back to the three-way valve 1, adjusting the opening of the three-way valve 1, and ensuring NH in the liquid phase 3 The concentration is between 20 and 25wt%. The liquid phase is directly sent to the ammonia water pump 7 for pressurization, or is stored in the storage tank 5 and then sent to the ammonia water pump 7 for pressurization. The liquid phase is pressurized to 0.35MPa by an ammonia water pump 7, sprayed from the upper part of a hearth of a pulverized coal furnace 6, and reduced and baked to NO generated by sludge incineration X NO measured at chimney X The concentration was reduced to 43mg/Nm 3 。
The pressure steam obtained by heating the pulverized coal furnace 6 is input into a steam generator to realize power output.
In this example the power of the pulverized coal furnace 6 is 1000MW.
The previous description of the embodiments is provided to facilitate a person of ordinary skill in the art in order to make and use the present invention. It will be apparent to those skilled in the art that various modifications can be readily made to these embodiments and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above-described embodiments, and those skilled in the art, based on the present disclosure, should make improvements and modifications without departing from the scope of the present invention.
Claims (8)
1. The coal-fired coupled sludge incineration power generation method is characterized by comprising the following steps of:
s1, placing sludge into a desiccator (2) for dehydration to obtain dehydrated sludge and steam, wherein the temperature of the dehydrated sludge at an outlet of the desiccator (2) is 75-110 ℃;
s21, sending the dehydrated sludge obtained in the S1 into a baking machine (3) to heat to obtain baked sludge and baking gas production, wherein the heating temperature of the baking machine (3) is 200-300 ℃ and the heating speed is 10-100 ℃/min;
s22, feeding the water vapor obtained in the S1 into a three-way valve (1) and dividing the water vapor into two streams, mixing the first stream of water vapor with the baked gas obtained in the S21 to prepare ammonia water, and carrying out aftertreatment on the second stream of water vapor;
s31, sending the baked sludge obtained in S21 into a pulverized coal furnace (6) for burning to generate NO X ；
S32, mixing the baking gas obtained in the S21 with the first steam obtained in the S22, and then sending the mixture into a condenser (4) for cooling to obtain a liquid phase and non-condensable gas, wherein the liquid phase is a mixed solution of ammonia and ammonium carbonate;
s4, monitoring ammonia nitrogen concentration of a liquid phase in the condenser (4), feeding back to the three-way valve (1), adjusting the opening of the three-way valve (1), and controlling the amount of the first stream of water vapor in S22;
s5, feeding the liquid phase obtained in the S32 into an ammonia water pump (7) for pressurizing, spraying into the pulverized coal furnace (6), and reducing NO generated by incineration of baked sludge X ；
S6, feeding the non-condensable gas obtained in the S32 into the pulverized coal furnace (6) for incineration, and inputting pressure steam obtained by heating the pulverized coal furnace (6) into a steam generator to realize power output.
2. The coal-fired coupled sludge incineration power generation method according to claim 1, wherein the heat source used for heating the roasting machine (3) in S21 is high-temperature flue gas generated by incineration in the pulverized coal furnace (6) or steam generated by heating the high-temperature flue gas.
3. The coal-fired coupled sludge incineration power generation method according to claim 1, wherein the ammonia concentration in the liquid phase is controlled to be 20-25wt% by adjusting the opening of the three-way valve (1) in S4.
4. The method for generating electricity by coal-fired coupled sludge incineration according to claim 1, wherein the baking gas comprises ammonia gas and CO 2 Steam, methane and CO, wherein the concentration of ammonia is 40-70wt%;
the non-condensable gas comprises methane and CO.
5. The method for power generation by coal-fired coupled sludge incineration according to claim 1, wherein the cooling temperature in S32 is 0-40 ℃.
6. The method for generating electricity by coal-fired coupled sludge incineration according to claim 1, wherein the pressure of the liquid phase is greater than 0.3MPa after the pressurization in S5.
7. The coal-fired coupled sludge incineration power generation method according to claim 1, characterized in that the heat released by the cooling process in S32 is used for preheating the air fed into the pulverized coal furnace (6).
8. The method for generating electricity by coal-fired coupled sludge incineration according to claim 1, wherein the post-treatment in S22 is carried out in the pulverized coal furnace (6) or discharged after condensation treatment.
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