An ammonia production system and method for use in denitrification systems of thermal power plants

Abstract

This invention discloses an ammonia production system and method for a denitrification system in a thermal power plant, comprising a unit extraction steam system, a rotary pyrolysis reactor system, an ammonia condensation and mixing system, an ammonia injection and control system, and a subcooled water recovery system. The outlet of the unit extraction steam system is connected to the exothermic inlet of the rotary pyrolysis reactor system. The exothermic outlet of the rotary pyrolysis reactor system is connected to the return water low-pressure heat exchanger in the thermal power plant's denitrification system via the subcooled water recovery system. The pyrolysis gas outlet of the rotary pyrolysis reactor system is connected to the inlet of the ammonia condensation and mixing system. The outlet of the ammonia condensation and mixing system is connected to the inlet of the ammonia injection and control system. This system and method can achieve efficient coupling between ammonium bicarbonate pyrolysis and steam extraction from the thermal power unit's steam turbine, improving ammonia production efficiency and achieving efficient energy utilization.

Description

Technical Field

[0001] This invention belongs to the field of flue gas denitrification technology in thermal power plants, and relates to an ammonia production system and method for denitrification systems in thermal power plants. Background Technology

[0002] With increasingly stringent environmental policies, the efficiency and safety requirements for denitrification systems in thermal power plants are constantly rising. Selective catalytic reduction (SCR) denitrification technology is widely used due to its high efficiency, but the selection and use of its reducing agent still faces many challenges.

[0003] Currently, the commonly used reducing agents in SCR denitrification systems of thermal power plants mainly include liquid ammonia, ammonia water, and urea. However, these traditional reducing agents each have their limitations: 1) Liquid ammonia has low preparation costs, but as a Class B hazardous material stipulated by the state, it poses significant safety hazards and has strict requirements for transportation and storage. 2) Ammonia water is relatively safer than liquid ammonia, but it is still a hazardous chemical, corrosive, and has high transportation costs, requiring large-scale storage equipment. 3) Urea has relatively good safety, but its system investment and operating costs are high, energy consumption is large, and it is prone to crystallization at low temperatures.

[0004] Therefore, developing new, safe, efficient, and low-cost methods for preparing reducing agents has become an urgent need in the industry. In recent years, ammonium bicarbonate has attracted widespread attention as a potential alternative raw material. Ammonium bicarbonate is the second largest nitrogen fertilizer after urea, with abundant sources and relatively low prices. More importantly, ammonium bicarbonate begins to decompose to produce ammonia gas at around 100℃, a characteristic that makes its application in the preparation of denitrification reducing agents possible.

[0005] However, how to efficiently convert ammonium bicarbonate into ammonia and integrate it organically with existing thermal power plant systems remains a pressing technical challenge. In particular, how to fully utilize the heat sources within the power plant to achieve efficient energy use is one of the key research directions at present. Summary of the Invention

[0006] The purpose of this invention is to overcome the shortcomings of the prior art and provide an ammonia production system and method for denitrification systems in thermal power plants. This system and method can achieve efficient coupling of ammonium bicarbonate pyrolysis and steam extraction from the steam turbine of thermal power units, thereby improving ammonia production efficiency and realizing efficient energy utilization.

[0007] To achieve the above objectives, this invention discloses an ammonia production system for a denitrification system in a thermal power plant, comprising a unit extraction steam system, a rotary pyrolysis reactor system, an ammonia condensation and mixing system, an ammonia injection and control system, and a subcooled water recovery system. The outlet of the unit extraction steam system is connected to the exothermic inlet of the rotary pyrolysis reactor system. The exothermic outlet of the rotary pyrolysis reactor system is connected to the return water low-pressure heat exchanger in the thermal power plant's denitrification system via the subcooled water recovery system. The pyrolysis gas outlet of the rotary pyrolysis reactor system is connected to the inlet of the ammonia condensation and mixing system. The outlet of the ammonia condensation and mixing system is connected to the inlet of the ammonia injection and control system.

[0008] Furthermore, the unit's steam extraction system includes a steam extraction port, a steam extraction pipeline, a multi-stage pressure regulating device, a flow regulating valve, and a pipeline insulation layer. The steam extraction port is connected to the exothermic inlet of the rotary pyrolysis reactor system via the steam extraction pipeline. The multi-stage pressure regulating device, the flow regulating valve, and the pipeline insulation layer are all installed on the steam extraction pipeline.

[0009] Furthermore, the rotary pyrolysis reactor system is either an externally heated rotary pyrolysis reactor or an internally heated rotary pyrolysis reactor.

[0010] Furthermore, the ammonia condensation and mixing system includes a condenser, a fan, and a mixer. The pyrolysis gas outlet of the rotary pyrolysis reactor system is connected to the inlet of the mixer via the condenser and the fan. The outlet of the mixer is connected to the inlet of the ammonia injection and control system.

[0011] Furthermore, the subcooled water recovery system includes a condensate collection device and a subcooled water pump. The condensate output from the heat release outlet of the rotary pyrolysis reactor system and the condensate generated by the pyrolysis reaction enter the return water low-pressure heat exchanger via the condensate collection device and the subcooled water pump.

[0012] This invention discloses a method for ammonia production in a denitrification system of a thermal power plant, comprising the following steps:

[0013] Steam extracted by the unit's extraction steam system enters the rotary pyrolysis reactor system to release heat, thereby heating the ammonium bicarbonate particles in the rotary pyrolysis reactor system. This causes the ammonium bicarbonate particles to pyrolyze and produce pyrolysis gas. The pyrolysis gas is condensed by an ammonia condensation and mixing system, then mixed with preheated air, and then injected into the flue through an ammonia injection and control system. At the same time, the condensate output from the rotary pyrolysis reactor system is sent to the return water low-pressure heat exchanger through a cold water recovery system.

[0014] Furthermore, the rotary pyrolysis reactor system is either an externally heated rotary pyrolysis reactor or an internally heated rotary pyrolysis reactor.

[0015] Furthermore, it also includes:

[0016] Calculate the logarithmic mean temperature difference between the two ends of the rotary pyrolysis reactor system, calculate the heat exchange area of ​​the rotary pyrolysis reactor system based on the logarithmic mean temperature difference, and determine the number and size of the heat exchange tubes in the rotary pyrolysis reactor system based on the heat exchange area of ​​the rotary pyrolysis reactor system.

[0017] Furthermore, the logarithmic mean temperature difference is:

[0018]

[0019] A = Q / (K * ΔT)

[0020]

[0021] Where K is the overall heat transfer coefficient, h o h is the heat transfer coefficient on the shell side of the heat exchanger. i R is the heat transfer coefficient inside the heat transfer tube, b is the thickness of the heat transfer tube in meters, A is the total heat transfer area of ​​the heat transfer tube, ΔT is the average heat transfer temperature difference based on the heat exchanger, and R is the heat transfer coefficient inside the heat transfer tube. i and R o For the fouling thermal resistance inside and outside the heat transfer tube, λ w is the thermal conductivity of the pipe wall.

[0022] Furthermore, the subcooled water recovery system includes a condensate collection device and a subcooled water pump. The condensate output from the heat release outlet of the rotary pyrolysis reactor system and the condensate generated by the pyrolysis reaction enter the return water low-pressure heat exchanger via the condensate collection device and the subcooled water pump.

[0023] The present invention has the following beneficial effects:

[0024] In the specific operation of the ammonia production system and method for denitrification systems in thermal power plants described in this invention, a large amount of extracted steam resources exist in the turbine system of thermal power units. This extracted steam is typically used for feedwater heating, deaerator heating, etc., but some waste heat remains unutilized. This invention innovatively utilizes extracted steam (typically superheated steam with a pressure range of 0.4–0.8 MPa and a temperature range of 230–300°C) from the low-pressure cylinder connecting pipe of the unit as a heat source, deeply integrating it with the ammonium bicarbonate pyrolysis process. This high-quality heat source provides sufficient thermal energy for the system, achieving cascaded energy utilization. Utilizing this extracted steam waste heat for ammonium bicarbonate pyrolysis to produce ammonia not only improves the overall energy efficiency of the unit but also significantly reduces ammonia production costs, possessing significant theoretical and practical application value. This not only solves the problems associated with traditional reducing agents but also improves the overall energy efficiency of thermal power plants, providing a new technological path for the clean and efficient development of the thermal power industry. Attached Figure Description

[0025] The accompanying drawings, which form part of this specification, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an undue limitation of the invention. In the drawings:

[0026] Figure 1 This is a structural diagram of the present invention;

[0027] Figure 2 This is a structural diagram of an externally heated rotary pyrolysis reactor;

[0028] Figure 3 This is a structural diagram of an internally heated rotary pyrolysis reactor.

[0029] Among them, 1 is the rotary pyrolysis reactor system, 2 is the blower, 3 is the condenser, 4 is the mixer, and 5 is the subcooling water pump. Detailed Implementation

[0030] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0031] In the description of this invention, it should be understood that the terms "comprising" and "including" indicate the presence of the described features, integrals, steps, operations, elements and / or components, but do not exclude the presence or addition of one or more other features, integrals, steps, operations, elements, components and / or collections thereof.

[0032] It should also be understood that the terminology used in this specification is for the purpose of describing particular embodiments only and is not intended to limit the invention. As used in this specification and the appended claims, the singular forms “a,” “an,” and “the” are intended to include the plural forms unless the context clearly indicates otherwise.

[0033] It should also be further understood that the term "and / or" as used in this specification and the appended claims refers to any combination and all possible combinations of one or more of the associated listed items, and includes such combinations. For example, A and / or B can represent three cases: A alone, A and B simultaneously, and B alone. Additionally, the character " / " in this invention generally indicates that the preceding and following objects have an "or" relationship.

[0034] It should be understood that although terms such as first, second, third, etc., may be used in the embodiments of the present invention to describe the preset range, these preset ranges should not be limited to these terms. These terms are only used to distinguish the preset ranges from one another. For example, without departing from the scope of the embodiments of the present invention, the first preset range may also be referred to as the second preset range, and similarly, the second preset range may also be referred to as the first preset range.

[0035] Depending on the context, the word "if" as used here can be interpreted as "when," "when," "in response to determination," or "in response to detection." Similarly, depending on the context, the phrase "if determination" or "if detection (of the stated condition or event)" can be interpreted as "when determination," "in response to determination," "when detection (of the stated condition or event)," or "in response to detection (of the stated condition or event)."

[0036] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of the present invention. The components of the embodiments of the present invention described and shown in the accompanying drawings can generally be arranged and designed in various different configurations. Therefore, the following detailed description of the embodiments of the present invention provided in the accompanying drawings is not intended to limit the scope of the claimed invention, but merely to illustrate selected embodiments of the invention. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without inventive effort are within the scope of protection of the present invention.

[0037] The accompanying drawings illustrate various structural schematic diagrams according to embodiments disclosed in this invention. These drawings are not to scale, and some details have been enlarged for clarity, and some details may have been omitted. The shapes of the various regions and layers shown in the drawings, as well as their relative sizes and positional relationships, are merely exemplary and may deviate from reality due to manufacturing tolerances or technical limitations. Furthermore, those skilled in the art can design regions / layers with different shapes, sizes, and relative positions as needed.

[0038] Example 1

[0039] refer to Figure 1The ammonia production system for denitrification systems in thermal power plants according to the present invention includes a unit extraction steam system, a rotary pyrolysis reactor system 1, an ammonia condensation and mixing system, an ammonia injection and control system, and a subcooled water recovery system. The outlet of the unit extraction steam system is connected to the heat release side inlet of the rotary pyrolysis reactor system 1. The heat release side outlet of the rotary pyrolysis reactor system 1 is connected to the return water low-pressure heat exchanger in the denitrification system of the thermal power plant via the subcooled water recovery system. The pyrolysis gas outlet of the rotary pyrolysis reactor system 1 is connected to the inlet of the ammonia condensation and mixing system. The outlet of the ammonia condensation and mixing system is connected to the inlet of the ammonia injection and control system.

[0040] Specifically, the unit's steam extraction system:

[0041] This invention closely integrates the ammonium bicarbonate pyrolysis device with the steam extraction system of a thermal power unit, making full use of the high-grade thermal energy in the unit. Specifically, steam is extracted from the intermediate-pressure cylinder of the turbine through the unit's steam extraction system. Preferably, intermediate-pressure steam at about 260°C and a pressure of about 0.5 MPa is extracted from the thermal power unit's turbine.

[0042] The unit's steam extraction system includes a steam extraction port, a steam extraction pipeline, a multi-stage pressure regulating device, a flow regulating valve, and a pipeline insulation layer. The steam extraction port is connected to the exothermic inlet of the rotary pyrolysis reactor system 1 via the steam extraction pipeline. The multi-stage pressure regulating device, the flow regulating valve, and the pipeline insulation layer are all installed on the steam extraction pipeline. During operation, the steam parameters are precisely adjusted according to the ammonia production requirements by the multi-stage pressure regulating device. By cooperating with the flow regulating valve, the ammonia production system can be quickly started and stopped without affecting the normal operation of the unit.

[0043] Rotary pyrolysis reactor system 1:

[0044] Based on thermodynamic calculations, taking an ammonia mass flow rate of approximately 170 kg / h required by the ammonia production system of a single 300MW unit as an example. With an ammonia production rate of 170 kg / h and a target conversion rate of 95%, 832 kg / h of ammonium bicarbonate feedstock is needed, fed at ambient temperature and pressure. In rotary pyrolysis reactor system 1, the inlet feed rate is 0.832 t / h and the outlet feed rate is 0.17 t / h, yielding an average value of G. m =0.5t / h. The material filling rate is set at 15%, and the material residence time is 20 minutes. The cylinder inclination angle is set at 3°, and the cylinder rotation speed is 1 r / min. Based on the rotary kiln heating device size design formula, the length L of the rotary pyrolysis device is 6m, and the diameter D is 0.75m.

[0045] For details, please refer to Figure 2 and Figure 3 The rotary pyrolysis reactor system 1 is an externally heated rotary pyrolysis reactor or an internally heated rotary pyrolysis reactor.

[0046] Externally heated rotary pyrolysis reactor:

[0047] Ammonium bicarbonate solid particles are stored in a silo and fed directly into the kiln via a conveyor during ammonia production. The extraction unit provides the heat required for the decomposition of ammonium bicarbonate solids through medium-pressure steam extraction. This heat is transferred to the ammonium bicarbonate solid particles near the kiln wall via heat transfer, and then to most of the particles inside the kiln through heat conduction. The resulting ammonia is extracted from the pyrolysis furnace under negative pressure, diluted, and then sent to the SCR reactor. This implementation requires additional heat exchange surfaces and steam flow space outside the rotating kiln.

[0048] Internally heated rotary pyrolysis reactor:

[0049] The internally heated rotary pyrolysis reactor is equipped with multiple parallel heat transfer tubes. The tubes are filled with ammonium bicarbonate particles, and the tubes contain high-temperature flue gas. The rotation of the cylinder ensures that the particles are in full contact with the heat transfer tubes, thereby improving the heat transfer efficiency.

[0050] The enthalpy change of the decomposition reaction required for ammonium bicarbonate pyrolysis is 167.92 kJ / mol. Considering the heat of reaction and air temperature rise, the system requires an external heating power of about 900 kW. The inlet steam pressure is 5 bar, the inlet temperature is 260 °C, the outlet pressure is 2 bar, and the steam outlet temperature is 120 °C. After heating, the steam condenses into saturated water, making full use of the latent heat of condensation of the steam. According to the calculation, the required steam volume is about 0.96 t / h.

[0051] First, based on the physical properties of the steam and the required total heating power, estimate the total heat transfer area and the number of heat transfer tubes.

[0052] The formula for the heat transfer coefficient of condensation phase change in a horizontal tube is:

[0053]

[0054] The thermal resistance R of fouling inside and outside the heat transfer tube i and R o All are 0.00017179m 2 ·K / W; thermal conductivity λ of the pipe wall w It is 45 W / (m·K).

[0055] The overall heat transfer coefficient is:

[0056]

[0057] Among them, h o The heat transfer coefficient on the shell side of the heat exchanger is given by the formula, and the heat transfer coefficient between the ammonium bicarbonate particles and the heat transfer tubes is 500 W / (m²). 2 ·K);h i denoted as , where is the heat transfer coefficient inside the heat transfer tube; b is the thickness of the heat transfer tube in meters (m).

[0058] The total heat transfer area of ​​the heat transfer tube is A = Q / (K*ΔT); this yields the average heat transfer temperature difference ΔT based on the heat exchanger. The average temperature difference is the logarithmic mean of the temperature differences at both ends of the heat exchanger, also known as the logarithmic mean temperature difference. The formula for calculating the countercurrent average temperature difference is the same, but the calculation methods for the temperature difference at both ends are different. The following formula can be used to calculate it:

[0059]

[0060]

[0061] Based on the calculated temperature difference, the required heat exchange area for steam heating is approximately 25 m². 2 The selected heat transfer tubes have a diameter of Φ25×2.5mm, a length of 5m, and a spacing of 32mm. Based on the heat exchange area, 64 tubes are required for steam heating. Using a 4-pass design with tubes arranged at angular intervals circumferentially within the rotating device, a maximum of 38 rows of 4-pass tubes can be arranged circumferentially. For the steam heating scheme, only 16 rows are needed to meet the heat exchange area requirements. The heat exchange tubes are mainly concentrated in the lower half of the cylinder, ensuring full contact with the ammonium bicarbonate particles.

[0062] Ammonia condensation and mixing system:

[0063] The ammonia condensation and mixing system includes a condenser 3, a blower 2, and a mixer 4. The condenser 3 is designed to reduce the moisture content in the product ammonia and improve ammonia separation efficiency. After leaving the rotary pyrolysis reactor system 1, the product gas is sent to the mixer 4 through the condenser 3 and the blower 2 to be diluted with hot dilution air, and then sent to the denitrification flue to participate in the denitrification reaction.

[0064] Ammonia injection and control system:

[0065] Ammonia injection grids are installed in accordance with the requirements for precision ammonia injection retrofitting, and ammonia flow precision control device is equipped to achieve on-demand ammonia injection. Intelligent PID control algorithm is also used to optimize system operating parameters and achieve automatic control of the ammonia injection process.

[0066] Subcooled water recovery system:

[0067] The subcooled water recovery system includes a condensate collection device and a subcooled water pump 5. The condensate output from the heat release outlet of the rotary pyrolysis reactor system 1, as well as the condensate generated by the pyrolysis reaction, enters the return water low-pressure heat exchanger through the condensate collection device and the subcooled water pump 5 to improve the overall thermal efficiency, realize the recycling of water resources, and further optimize the economy and environmental protection of the ammonia production system.

[0068] Example 2

[0069] The ammonia production method for a denitrification system in a thermal power plant according to the present invention includes the following steps:

[0070] Steam extracted by the unit's extraction steam system enters the rotary pyrolysis reactor system 1 to release heat, thereby heating the ammonium bicarbonate particles in the rotary pyrolysis reactor system 1. This causes the ammonium bicarbonate particles to pyrolyze and produce pyrolysis gas. The pyrolysis gas is condensed by an ammonia condensation and mixing system, then mixed with preheated air, and then injected into the flue through an ammonia injection and control system. At the same time, the condensate output from the rotary pyrolysis reactor system 1 is sent to the return water low-pressure heat exchanger through a cold water recovery system.

[0071] Compared with the prior art, the present invention has the following characteristics:

[0072] 1. This invention makes full use of the waste heat extracted from the steam turbine of a thermal power unit, significantly reducing the energy consumption for ammonia production and improving the overall thermal efficiency of the unit by about 2-3%.

[0073] 2. This invention uses solid pyrolysis, which avoids the heat absorption of solution evaporation, further reducing energy consumption and achieving high thermal efficiency.

[0074] 3. The system of the present invention is simple in equipment, occupies only 1 / 3 of the area of ​​the traditional ammonia water preparation system, and reduces investment costs by about 40%.

[0075] 4. The raw material cost of this invention is low, and the operating cost is reduced by about 30% compared with the traditional ammonia production method.

[0076] 5. This invention improves the safety of the denitrification system and completely eliminates the risks associated with the use of hazardous chemicals such as liquid ammonia.

[0077] 6. The pyrolysis reaction temperature of the present invention is low (110-150℃), resulting in less equipment corrosion and extending the service life of the equipment.

[0078] 7. The system of the present invention has a fast response speed and can adjust the ammonia production in real time within 15 minutes according to the unit load and denitrification requirements.

[0079] 8. This invention uses medium-pressure steam extraction as a heat source, which makes the temperature easier to control and improves the stability and controllability of the ammonia production process.

[0080] 9. The system of the present invention can achieve rapid start-up and shutdown (start-up time <30min), without affecting the normal operation of the unit, and enhances the peak-shaving capacity of the unit.

[0081] 10. The pyrolysis device and automatic control system in this invention realize a high degree of automation in the ammonia production process, reducing the number of operators from 3 per shift to 1 per shift, thus reducing the difficulty of operation and labor costs.

[0082] 11. The system of the present invention operates stably, with an annual operating time of over 8,000 hours, which greatly improves the reliability of the denitrification system.

[0083] Other embodiments of the invention will readily occur to those skilled in the art upon consideration of the specification and disclosure of the invention. This application is intended to cover any variations, uses, or adaptations of the invention that follow the general principles of the invention and include common knowledge or customary techniques in the art not disclosed herein. The specification and examples are to be considered exemplary only, and the true scope and spirit of the invention are indicated by the following claims.

[0084] It should be understood that the present invention is not limited to the precise structure described above and shown in the accompanying drawings, and various modifications and changes can be made without departing from its scope. The scope of the invention is limited only by the appended claims.

[0085] The above description is merely a preferred embodiment of the present invention and does not constitute any limitation on the present invention. Any simple modifications, alterations, or equivalent structural changes made to the above embodiments based on the technical essence of the present invention shall still fall within the protection scope of the present invention.

Claims

1. An ammonia production system for a denitrification system of a thermal power plant, characterized in that, The system comprises a unit steam extraction system, a rotary pyrolysis reactor system (1), an ammonia gas condensation and mixing system, an ammonia injection and control system, and a supercooled water recovery system. The unit steam extraction system comprises a steam extraction port, a steam extraction pipeline, a multi-stage pressure regulating device, a flow regulating valve, and a pipeline insulation layer.

2. The ammonia production system for a denitration system of a thermal power plant according to claim 1, characterized in that, The rotary pyrolysis reactor system (1) is an external heating rotary pyrolysis reactor or an internal heating rotary pyrolysis reactor.

3. The ammonia production system for a denitration system of a thermal power plant according to claim 1, characterized in that, The ammonia gas condensation and mixing system comprises a condenser (3), a fan (2), and a mixer (4).

4. The ammonia production system for a denitration system of a thermal power plant according to claim 1, characterized in that, The supercooled water recovery system comprises a condensate water collecting device and a supercooled water pump (5).

5. A method for ammonia production for a denitrification system of a thermal power plant, characterized in that, The system for an ammonia production system for a denitration system of a thermal power plant according to claim 1 comprises the following steps: The steam extracted by the unit steam extraction system is introduced into the rotary pyrolysis reactor system (1) to release heat, so as to heat the ammonium bicarbonate particles in the rotary pyrolysis reactor system (1), so that the ammonium bicarbonate particles are pyrolyzed to generate pyrolysis gas.

6. The method for ammonia production for a denitration system of a thermal power plant according to claim 5, characterized in that, The rotary pyrolysis reactor system (1) is an external heating rotary pyrolysis reactor or an internal heating rotary pyrolysis reactor.

7. The method for ammonia production for a denitration system of a thermal power plant according to claim 5, characterized in that, Further comprising: The logarithmic mean temperature difference of the temperature difference between the two ends of the rotary pyrolysis reactor system (1) is calculated, the heat exchange area of the rotary pyrolysis reactor system (1) is calculated according to the logarithmic mean temperature difference, and the number and size of the heat exchange pipes in the rotary pyrolysis reactor system (1) are determined according to the heat exchange area of the rotary pyrolysis reactor system (1).

8. The method for ammonia production for a denitrification system of a thermal power plant according to claim 7, characterized in that, The supercooled water recovery system comprises a condensate water collecting device and a supercooled water pump (5).

9. The method for ammonia production for a denitrification system of a thermal power plant according to claim 7, characterized in that, The ammonia condensation mixing system comprises a condenser (3), a fan (2) and a mixer (4), the pyrolysis gas outlet of the rotary pyrolysis reactor system (1) is connected with the inlet of the mixer (4) through the condenser (3) and the fan (2), and the outlet of the mixer (4) is connected with the inlet of the ammonia injection and control system.

Images