CN112797396B - High-moisture biomass fuel power generation system and operation method - Google Patents

High-moisture biomass fuel power generation system and operation method Download PDF

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CN112797396B
CN112797396B CN202011630668.6A CN202011630668A CN112797396B CN 112797396 B CN112797396 B CN 112797396B CN 202011630668 A CN202011630668 A CN 202011630668A CN 112797396 B CN112797396 B CN 112797396B
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CN112797396A (en
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刘明
李蒙杰
刘荣堂
严俊杰
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Xian Jiaotong University
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
    • F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
    • F22D1/50—Feed-water heaters, i.e. economisers or like preheaters incorporating thermal de-aeration of feed-water
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
    • F22D5/00—Controlling water feed or water level; Automatic water feeding or water-level regulators
    • F22D5/26—Automatic feed-control systems
    • F22D5/34—Applications of valves
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

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Abstract

The invention discloses a high-moisture biomass fuel power generation system and an operation method thereof, wherein the system comprises a biomass-fired power generation system, a drying system and a waste heat recovery system; a biomass outlet of the steam dryer is connected with a fuel inlet of a boiler, a steam outlet of the boiler is connected with a steam inlet of a steam turbine, a steam exhaust port of the steam turbine is connected with a steam turbine regenerative system, the steam turbine is connected with a generator, and an outlet of the steam turbine regenerative system is connected with a water supply inlet of the boiler; steam is extracted by a steam turbine selected from the steam drier, and condensed water released by the extracted steam returns to a turbine regenerative system; the waste heat recovery system is used for heating air and condensed water after recovering heat of the dry exhaust gas. The high-moisture biomass fuel power generation system of the integrated steam dryer pre-dries fuel by using steam extraction of the steam turbine, reduces the moisture content in biomass, increases the power generation efficiency of the system, reduces the smoke amount generated by fuel combustion, greatly reduces the manufacturing cost of a boiler, and improves the energy utilization efficiency.

Description

High-moisture biomass fuel power generation system and operation method
Technical Field
The invention belongs to the field of thermal power generation, relates to the optimal design of a thermodynamic system, and mainly relates to high-moisture biomass combustion pretreatment drying and waste heat recycling.
Background
The biomass energy is a renewable energy, and the energy composition ratio of the biomass energy is gradually increased due to the characteristics of easy acquisition, renewability and cleanness under the dilemma of exhaustion and exhaustion of fossil energy. The total amount of biomass is huge, 1730 hundred million tons of biological organic matters can be produced globally through photosynthesis at present every year, and the energy contained in the biomass is 10-20 times of the total energy consumption. Biomass energy is derived from organisms in nature and is generally large in moisture content, and many can reach 60%. The energy density is low, which is a disadvantage of biomass combustion power generation, the combustion is insufficient due to high moisture content, the boiler smoke emission heat loss is large, and the thermal efficiency of biomass combustion power generation is generally low.
The biomass energy mainly comprises agricultural wastes, wood firewood, processing industry wastes, household garbage, animal wastes and the like. The domestic garbage is mixed with components with high chlorine content such as polyvinyl chloride plastics, the tail part of the boiler faces the problem of low-temperature corrosion, and the drying equipment can be prevented from being corroded by adopting a steam drying mode. The water content of the high-moisture biomass fuel is reduced by using a pre-drying mode, the energy configuration can be optimized, the combustion process inside the boiler is improved, and the power generation efficiency of the biomass power plant is increased.
Disclosure of Invention
Aiming at the situation that the water content of biomass is large and can reach 50% in many cases, the invention provides a high-moisture biomass power generation thermodynamic system integrated with a steam dryer, which can effectively reduce the moisture content of biomass entering a furnace, improve the combustion efficiency of a boiler and increase the power generation efficiency of the system.
In order to increase the thermal efficiency of the high-moisture biomass thermodynamic system, the technical scheme of the invention is as follows:
a high-moisture biomass fuel power generation system comprises a biomass fuel power generation system and a drying system, wherein the biomass fuel power generation system is composed of a boiler 1, a steam turbine 2, a primary air preheater 11, a secondary air preheater 12, a condenser 21, a condensate pump 22, a low-pressure heater 23, a deaerator 24, a water feed pump 25 and a high-pressure heater 26, and the drying system is composed of a steam dryer 3 and a water treatment device 31; the system connection relationship is as follows:
the steam outlet of the boiler 1 is divided into two paths, one path is connected with the steam inlet of the steam turbine 2, the other path is connected with the steam extraction inlet of the second-stage air preheater 12, the steam exhaust port of the steam turbine 2 is connected with the steam exhaust inlet of the condenser 21, the condensed water outlet of the condenser 21 is connected with the condensed water pump 22, the outlet of the condensed water pump 22 is sequentially connected with the water supply inlet and outlet of the low-pressure heater 23, the water supply inlet and outlet of the deaerator 24, the water supply inlet and outlet of the water supply pump 25, the water supply inlet and outlet 26 of the high-pressure heater and the water supply inlet of the boiler 1, the steam extraction inlet of the low-pressure heater 23 and the steam extraction inlet of the deaerator 24 are connected with the steam extraction port of the steam turbine 2, the drainage outlet of the high-pressure heater 26 is connected with the drainage inlet of the deaerator 24, and the drainage outlet of the low-pressure heater 23 is connected with the hot well of the condenser 21; an air inlet of the boiler 1 is communicated with the environment through a secondary air preheater 12 and a primary air preheater 11;
the extraction steam inlet of the first-stage air preheater 11 is connected with the extraction steam port of the deaerator of the steam turbine 2, and the drain outlet is connected with the drain inlet of the deaerator 24; the drainage outlet is connected with the drainage inlet of the high-pressure heater 26;
the steam turbine 2 is connected with the generator through mechanical transmission equipment;
the outlet of the steam drier 3 for dry fuel is connected with the fuel inlet of the boiler 1, the drain outlet is connected with the drain inlet of the high-pressure heater 26, and the outlet of the dry exhaust gas is connected with the inlet of the water treatment device 31.
Steam pressure at an inlet of the steam dryer 3 is 0.2-1.0 Mpa, the temperature is 160-330 ℃, high-moisture biomass enters from a material inlet of the steam dryer 3, and air with the mass proportion of 5-10% is introduced along with the biomass to serve as carrier gas; and the temperature of the exhaust gas at the outlet of the steam dryer 3 is 85-110 ℃.
When the biomass fuel is municipal refuse, the exhaust gas temperature of the boiler 1 is 170-210 ℃.
The air preheater is carried out in two stages by adopting a steam heating mode, and the first stage air preheater 11 heats air to 90-110 ℃; the second stage air preheater 12 heats the air to 210-230 ℃.
The steam drier 3 can recover the waste heat by utilizing a waste heat recovery system to dry the exhaust gas; the waste heat recovery system comprises a heater 41, a low-temperature economizer 42, a waste heat recovery system controller 43, a dryer exhaust gas flowmeter 44, a heater exhaust gas regulating valve 45, a low-temperature economizer exhaust gas regulating valve 46 and a low-temperature economizer feed water regulating valve 47; the connection relationship of the waste heat recovery system is as follows: the drying exhaust gas outlet of the steam dryer 3 is connected with a dryer exhaust gas flowmeter 44, and then divided into two paths, one path is connected with the exhaust gas inlet of the heater 41 through a heater exhaust gas regulating valve 45, the other path is connected with the exhaust gas inlet of the low-temperature economizer 42 through a low-temperature economizer exhaust gas regulating valve 46, and the non-condensing gas outlets of the heater 41 and the low-temperature economizer 42 are connected with the air inlet of the second-stage air preheater 12; a drainage outlet of the air heater 41 is connected with a drainage inlet of the low-temperature economizer 42, and a drainage outlet of the low-temperature economizer 42 is connected with an inlet of the water treatment device 31; the air inlet of the air heater 41 is communicated with the environment, and the air outlet is connected with the air inlet of the first-stage air preheater 11; the feed water inlet of the low-temperature economizer 42 is connected with the outlet of the condensate pump 22 through a feed water regulating valve 47 of the low-temperature economizer, and the feed water outlet is connected with the feed water inlet of the deaerator 24.
After the exhaust gas is subjected to heat release through the air heater 41 and the low-temperature economizer 42, the temperature of the residual non-condensable gas after moisture condensation is 85-95 ℃, and the residual non-condensable gas is sent to the secondary air preheater 12; if a waste heat recovery system is not arranged, after the exhaust gas directly releases heat with the environment, the non-condensed gas is sent to the second-stage air preheater 12, and the condensed water is sent to the water treatment device 31.
The water supply inlet temperature of the low-temperature economizer 42 is the same as that of the low-pressure heater 23, and the outlet water temperature error is controlled within 10 ℃; the air heater 41 preheats the air to 60-70 ℃; the low-temperature economizer 42 consists of a steam condensation section and a drainage heat release section, and the drainage water contained in the exhaust gas in the air heater 41 after condensation and the drainage water of the low-temperature economizer 42 are collected in the drainage heat release section and then cooled to 60-70 ℃, and then the collected water is sent to the water treatment device 31.
The enthalpy value of a condensed water outlet of the steam dryer 3 is lower than 500-600 kJ-kg-1And is then connected to the deaerator 24.
The waste heat recovery system may be provided with only the low-temperature economizer 42 or the air heater 41, or may be provided with no waste heat recovery device.
The operation method of the high-moisture biomass fuel power generation system is characterized by comprising the following steps of: the high-moisture biomass fuel enters from the inlet of the steam dryer 3 along with the carrier gas, absorbs the heat of steam extraction in the steam dryer, part of free water is changed into gas state, and leaves the steam dryer 3 from the exhaust gas outlet of the steam dryer under the carrying of the carrier gas, and the high-moisture biomass fuel enters the boiler 1 to be combusted to release heat after the moisture content is reduced;
the method comprises the following steps that water in a boiler 1 absorbs heat to become high-temperature steam, the high-temperature steam enters a steam turbine 2 to do work, steam discharged by the steam turbine 2 enters a condenser 21 to be condensed, then sequentially passes through a condensate pump 22, a low-pressure heater 23, a low-temperature economizer 42 and a deaerator 24, enters a high-pressure heater 26 after being pressurized by a water supply pump 25, and finally enters the boiler to complete the circulation of working media; wherein the low-pressure heater 23 extracts steam to release heat and then gathers condensed water from a hot well, the deaerator 24 extracts steam to directly mix with feed water to release heat, and the second-stage air preheater 12 drains water and gathers the water to the deaerator 24 after releasing heat in the high-pressure heater 26;
the air heater 41, the first-stage air preheater 11 and the second-stage air preheater 12 sequentially heat air;
after measuring the exhaust gas flow, the dryer exhaust gas flow meter 44 sends the parameters to the waste heat recovery system controller 43, and after the waste heat recovery system controller 43 calculates, the valve opening is adjusted according to the drying number to control the working state of the waste heat recovery system; when the drying number is less than or equal to 0.08, the waste heat recovery system controller 43 opens the exhaust gas regulating valve 45 of the heater, closes the exhaust gas regulating valve 46 of the low-temperature economizer, and all the exhaust gas of the dryer enters the heater 41; when the drying number is more than 0.08, the waste heat recovery system controller 43 opens the low-temperature economizer exhaust gas regulating valve 46 and the low-temperature economizer water supply regulating valve 47 and regulates the opening size of the valves, the drying exhaust gas is divided into two paths, one path of flow is kept unchanged and enters the air heater 41 to preheat air, the other path of flow enters the low-temperature economizer 42 to heat condensed water, the condensed water of steam in the exhaust gas in the air heater 41 and the water of the low-temperature economizer 42 are collected in a water drainage section and then are further cooled, and then the condensed water and the condensed water are sent to the water treatment device 31; after the exhaust gas is subjected to heat release through the air heater 41 and the low-temperature economizer 42, the residual uncondensed gas after moisture condensation is sent back to the second-stage air preheater 12 for heating and then sent to the boiler 1 for treatment;
the dry number is calculated as follows:
Figure GDA0003334353420000051
Figure GDA0003334353420000052
in the formula: m isH2O_r-the amount of the base water/kg.kg-1；mH2O_d-moisture content of dried biomass/kg-kg-1(ii) a Lambda-degree of dryness/kg-1(ii) a LHV-fuel low calorific value/kJ.kg-1(ii) a Mu-dryingNumber/kg. kJ-1。
Compared with the prior art, the invention has the following advantages:
1. the invention utilizes the low-pressure steam extraction of the steam turbine to pre-dry the high-moisture biomass, thereby reducing the moisture content, increasing the power generation efficiency, reducing the smoke quantity of biomass combustion and greatly reducing the manufacturing cost of a biomass-fired boiler;
2. the invention increases the waste heat recovery system to utilize the waste heat generated in the drying process, thereby further improving the heat efficiency of the biomass power plant;
3. according to the invention, the waste heat recovery system is used for treating the dry waste gas, the non-condensable gas in the waste gas is recovered and then sent to the boiler for treatment, and the water vapor in the waste gas is subjected to heat release by the waste heat recovery system, and then the condensed water enters the water treatment device for treatment and then is discharged, so that pollutants generated in the drying process are effectively treated.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention.
In the figure: 1 is a boiler; 2 is a steam turbine; 3 is a steam drier; 11 is a primary air preheater; 12 is a secondary air preheater; 21 is a condenser; 22 is a condensate pump; 23 is a low pressure heater; 24 is a deaerator; 25 is a water supply pump; 26 is a high pressure heater; 31 is a water treatment device; 41 is a warm air blower; 42 is a low-temperature economizer; 43 is a waste heat recovery system controller; 44 is a drier exhaust gas flowmeter; 45 is a ventilation regulating valve of the air heater; 46 is a low-temperature economizer exhaust gas regulating valve; and 47 is a feed water regulating valve of the low-temperature economizer.
Detailed Description
The invention will be described in further detail with reference to the drawings and the working principle.
As shown in fig. 1, the high-moisture biomass fuel power generation system of the present invention comprises a biomass-fired power generation system and a drying system, wherein the biomass-fired power generation system comprises a boiler 1, a steam turbine 2, a primary air preheater 11, a secondary air preheater 12, a condenser 21, a condensate pump 22, a low-pressure heater 23, a deaerator 24, a water feed pump 25, and a high-pressure heater 26, and the drying system comprises a steam dryer 3 and a water treatment device 31. The system connection relationship is as follows:
the steam outlet of the boiler 1 is divided into two paths, one path is connected with the steam inlet of the steam turbine 2, the other path is connected with the steam extraction inlet of the second-stage air preheater 12, the steam outlet of the steam turbine 2 is connected with the steam exhaust inlet of the condenser 21, the condensed water outlet of the condenser 21 is connected with the condensed water pump 22, the outlet of the condensed water pump 22 is sequentially connected with the water supply inlet and outlet of the low-pressure heater 23, the water supply inlet and outlet of the deaerator 24, the water supply pump 25, the water supply inlet and outlet of the high-pressure heater 26 and the water supply inlet of the boiler 1, the steam extraction inlet of the low-pressure heater 23 and the steam extraction inlet of the deaerator 24 are connected with the steam extraction inlet of the steam turbine 2, the drainage outlet of the high-pressure heater 26 is connected with the drainage inlet of the deaerator 24, and the drainage outlet of the low-pressure heater 23 is connected with the hot well of the condenser 21; an air inlet of the boiler 1 is communicated with the environment through a secondary air preheater 12 and a primary air preheater 11;
the extraction steam inlet of the first-stage air preheater 11 is connected with the extraction steam port of the deaerator of the steam turbine 2, and the drain outlet is connected with the drain inlet of the deaerator 24; the water drainage outlet of the second-stage air preheater 12 is connected with the water drainage inlet of the high-pressure heater 26;
the steam turbine 2 is connected with the generator through mechanical transmission equipment;
the outlet of the steam drier 3 for dry fuel is connected with the fuel inlet of the boiler 1, the drain outlet is connected with the drain inlet of the high-pressure heater 26, and the outlet of the dry exhaust gas is connected with the inlet of the water treatment device 31.
As a preferred embodiment of the invention, the steam pressure at the inlet of the steam dryer 3 is 0.2-1.0 Mpa, the temperature is 160-330 ℃, the high-moisture biomass enters from the material inlet of the steam dryer 3, and air with the mass proportion of 5-10% is introduced along with the biomass to serve as carrier gas; and the temperature of the exhaust gas at the outlet of the steam dryer 3 is 85-110 ℃.
In a preferred embodiment of the present invention, when the biomass fuel is municipal waste, the exhaust gas temperature of the boiler 1 is 170 to 210 ℃.
As a preferred embodiment of the invention, the air preheater adopts a steam heating mode and is divided into two stages, and the first stage air preheater 11 heats the air to 90-110 ℃; the second stage air preheater 12 heats the air to 210-230 ℃.
As a preferred embodiment of the present invention, the steam dryer 3 recovers the waste heat by using a waste heat recovery system, where the waste heat recovery system includes a heater 41, a low-temperature economizer 42, a waste heat recovery system controller 43, a dryer waste gas flowmeter 44, a heater waste gas regulating valve 45, a low-temperature economizer waste gas regulating valve 46, and a low-temperature economizer feed water regulating valve 47; the system connection relationship is as follows: a drying exhaust gas outlet of the steam dryer 3 is connected with a dryer exhaust gas flowmeter 44, and then divided into two paths, wherein one path is connected with an exhaust gas inlet of the heater 41 through a heater exhaust gas regulating valve 45 and is connected with an exhaust gas inlet of the low-temperature economizer 42 through a low-temperature economizer exhaust gas regulating valve 46, and non-condensing gas outlets of the heater 41 and the low-temperature economizer 42 are connected with an air inlet of the second-stage air preheater 12; a drain outlet of the air heater 41 is connected with a drain inlet of the low-temperature coal economizer 42, and a drain outlet of the low-temperature coal economizer 42 is connected with an inlet of the water treatment device 31; the air inlet of the air heater 41 is communicated with the environment, and the air outlet is connected with the air inlet of the first-stage air preheater 11; the feed water inlet of the low-temperature economizer 42 is connected with the outlet of the condensate pump 22 through a feed water regulating valve 47 of the low-temperature economizer, and the feed water outlet is connected with the feed water inlet of the deaerator 24.
In a preferred embodiment of the invention, after the exhaust gas is subjected to heat release through the air heater 41 and the low-temperature economizer 42, the temperature of the residual uncondensed gas after moisture condensation is 85-95 ℃, and the exhaust gas is sent to the secondary air preheater 12; if a waste heat recovery system is not arranged, after the exhaust gas directly releases heat with the environment, the non-condensed gas is sent to the second-stage air preheater 12, and the condensed water is sent to the water treatment device 31.
As the preferred embodiment of the invention, the temperature of the water supply inlet of the low-temperature economizer 42 is the same as the temperature of the water supply inlet and outlet of the low-pressure heater 23, and the error of the water temperature of the outlet is controlled within 10 ℃; the air heater 41 preheats the air to 60-70 ℃; the low-temperature economizer 42 consists of a steam condensation section and a drainage heat release section, and the drainage water contained in the exhaust gas in the air heater 41 after condensation and the drainage water of the low-temperature economizer 42 are collected in the drainage heat release section and then cooled to 60-70 ℃, and then the collected water is sent to the water treatment device 31.
Is an advantage of the present inventionAccording to an embodiment, the enthalpy value of the condensed water outlet of the steam dryer 3 is lower than 500-600 kJ-kg-1And is then connected to the deaerator 24.
In addition, when the condition of the invention is insufficient, the waste heat recovery system can be provided with only the low-temperature economizer 42 or the air heater 41, or can be not provided with a waste heat recovery device.
The operation method of the high-moisture biomass fuel power generation system comprises the following steps: the high-moisture biomass fuel enters from the inlet of the steam dryer 3 along with the carrier gas, absorbs the heat of steam extraction in the dryer, part of free water is changed into gas state, and leaves the steam dryer 3 from the exhaust gas outlet of the steam dryer under the carrying of the carrier gas, and the high-moisture biomass fuel enters the boiler 1 to be combusted to release heat after the moisture content is reduced;
the method comprises the following steps that water in a boiler 1 absorbs heat to become high-temperature steam, the high-temperature steam enters a steam turbine 2 to do work, steam discharged by the steam turbine 2 enters a condenser 21 to be condensed, then sequentially passes through a condensate pump 22, a low-pressure heater 23, a low-temperature economizer 42 and a deaerator 24, enters a high-pressure heater 26 after being pressurized by a water supply pump 25, and finally enters the boiler to complete the circulation of working media; wherein the low-pressure heater 23 extracts steam to release heat and then gathers condensed water from a hot well, the deaerator 24 extracts steam to directly mix with feed water to release heat, and the second-stage air preheater 12 drains water and gathers the water to the deaerator 24 after releasing heat in the high-pressure heater 26;
the air heater 41, the first-stage air preheater 11 and the second-stage air preheater 12 sequentially heat air;
after measuring the exhaust gas flow, the dryer exhaust gas flow meter 44 sends the parameters to the waste heat recovery system controller 43, and after the waste heat recovery system controller 43 calculates, the valve opening is adjusted according to the drying number to control the working state of the waste heat recovery system; when the drying number is less than or equal to 0.08, the waste heat recovery system controller 43 opens the exhaust gas regulating valve 45 of the heater, closes the exhaust gas regulating valve 46 of the low-temperature economizer, and all the exhaust gas of the dryer enters the heater 41; when the drying number is more than 0.08, the waste heat recovery system controller 43 opens the low-temperature economizer exhaust gas regulating valve 46 and the low-temperature economizer water supply regulating valve 47 and regulates the opening size of the valves, the drying exhaust gas is divided into two paths, one path of flow is kept unchanged and enters the air heater 41 to preheat air, the other path of flow enters the low-temperature economizer 42 to heat condensed water, the condensed water of steam in the exhaust gas in the air heater 41 and the water of the low-temperature economizer 42 are collected in a water drainage section and then are further cooled, and then the condensed water and the condensed water are sent to the water treatment device 31; after the exhaust gas is subjected to heat release through the air heater 41 and the low-temperature economizer 42, the residual non-condensable gas after moisture condensation is sent back to the second-stage air preheater 12 for heating and then sent to the boiler 1 for treatment.

Claims (8)

1. A high-moisture biomass fuel power generation system comprises a biomass fuel power generation system and a drying system, wherein the biomass fuel power generation system is composed of a boiler (1), a steam turbine (2), a primary air preheater (11), a secondary air preheater (12), a condenser (21), a condensate pump (22), a low-pressure heater (23), a deaerator (24), a water feed pump (25) and a high-pressure heater (26), and the drying system is composed of a steam dryer (3) and a water treatment device (31); the system connection relationship is as follows:
the steam outlet of the boiler (1) is divided into two paths, one path is connected with the steam inlet of the steam turbine (2), the other path is connected with the steam extraction inlet of the second-stage air preheater (12), the steam exhaust port of the steam turbine (2) is connected with the steam exhaust inlet of the condenser (21), the condensed water outlet of the condenser (21) is connected with the condensed water pump (22), the outlet of the condensed water pump (22) is sequentially connected with the water supply inlet and outlet of the low-pressure heater (23), the water supply inlet and outlet of the deaerator (24), the water supply pump (25), the water supply inlet and outlet of the high-pressure heater (26) and the water supply inlet and outlet of the boiler (1), the steam extraction inlet of the low-pressure heater (23) and the steam extraction inlet of the deaerator (24) are connected with the steam extraction port of the steam turbine (2), the drainage outlet of the high-pressure heater (26) is connected with the drainage inlet of the deaerator (24), and the drainage outlet of the low-pressure heater (23) is connected with the hot well of the condenser (21); an air inlet of the boiler (1) is communicated with the environment through a secondary air preheater (12) and a primary air preheater (11);
the extraction steam inlet of the first-stage air preheater (11) is connected with the extraction steam port of the deaerator of the steam turbine (2), and the drain outlet is connected with the drain inlet of the deaerator (24); the water drainage outlet of the second-stage air preheater (12) is connected with the water drainage inlet of the high-pressure heater (26);
the steam turbine (2) is connected with the generator through mechanical transmission equipment;
a dry fuel outlet of the steam dryer (3) is connected with a fuel inlet of the boiler (1), a hydrophobic outlet is connected with a hydrophobic inlet of the high-pressure heater (26), and a dry exhaust gas outlet is connected with an inlet of the water treatment device (31);
the steam dryer (3) is characterized in that waste heat is recovered by a waste heat recovery system for drying exhaust gas, wherein the waste heat recovery system comprises a heater (41), a low-temperature economizer (42), a waste heat recovery system controller (43), a dryer exhaust gas flowmeter (44), a heater exhaust gas regulating valve (45), a low-temperature economizer exhaust gas regulating valve (46) and a low-temperature economizer water supply regulating valve (47); the connection relationship of the waste heat recovery system is as follows: a drying exhaust gas outlet of the steam dryer (3) is connected with a dryer exhaust gas flowmeter (44), and then the drying exhaust gas outlet is divided into two paths, one path is connected with an exhaust gas inlet of the heater (41) through a heater exhaust gas regulating valve (45), the other path is connected with an exhaust gas inlet of the low-temperature economizer (42) through a low-temperature economizer exhaust gas regulating valve (46), and non-condensable gas outlets of the heater (41) and the low-temperature economizer (42) are connected with an air inlet of the second-stage air preheater (12); a drainage outlet of the air heater (41) is connected with a drainage inlet of the low-temperature economizer (42), and a drainage outlet of the low-temperature economizer (42) is connected with an inlet of the water treatment device (31); an air inlet of the air heater (41) is communicated with the environment, and an air outlet is connected with an air inlet of the first-stage air preheater (11); the water supply inlet of the low-temperature economizer (42) is connected with the outlet of the condensate pump (22) through a water supply regulating valve (47) of the low-temperature economizer, and the water supply outlet is connected with the water supply inlet of the deaerator (24).
2. The high moisture biomass fuel power generation system according to claim 1, wherein: steam pressure at an inlet of the steam dryer (3) is 0.2-1.0 Mpa, the temperature is 160-330 ℃, high-moisture biomass enters from a material inlet of the steam dryer (3), and air with the mass proportion of 5-10% is introduced into the biomass to serve as carrier gas; the temperature of the exhaust gas at the outlet of the steam dryer (3) is 85-110 ℃.
3. The high moisture biomass fuel power generation system according to claim 1, wherein: when the biomass fuel is municipal refuse, the exhaust gas temperature of the boiler (1) is 170-210 ℃.
4. The high moisture biomass fuel power generation system according to claim 1, wherein: the air preheater is carried out in two stages by adopting a steam heating mode, and the first stage air preheater (11) heats air to 90-110 ℃; the second stage air preheater (12) heats the air to 210-230 ℃.
5. The high moisture biomass fuel power generation system according to claim 1, wherein: after the exhaust gas is subjected to heat release through the air heater (41) and the low-temperature economizer (42), the temperature of the residual non-condensable gas after moisture condensation is 85-95 ℃, and the residual non-condensable gas is sent to the secondary air preheater (12); if a waste heat recovery system is not arranged, after the exhaust gas directly releases heat with the environment, the non-condensed gas is sent to a second-stage air preheater (12), and the condensed water is sent to a water treatment device (31).
6. The high moisture biomass fuel power generation system according to claim 1, wherein: the water supply inlet temperature of the low-temperature economizer (42) is the same as that of the low-pressure heater (23), and the outlet water temperature error is controlled within 10 ℃; the air heater (41) preheats the air to 60-70 ℃; the low-temperature economizer (42) consists of a steam condensation section and a drainage heat release section, and the drainage water of the condensed steam contained in the exhaust gas in the air heater (41) and the drainage water of the low-temperature economizer (42) are collected in the drainage heat release section and then cooled to 60-70 ℃ and then sent into the water treatment device (31).
7. The high moisture biomass fuel power generation system according to claim 1, wherein: the enthalpy value of a condensed water outlet of the steam dryer (3) is lower than 500-600 kJ-kg-1When the water is used, the water is connected with a deaerator (24).
8. The method of operating a high moisture biomass fuel power generation system according to any one of claims 1 to 7, wherein: the high-moisture biomass fuel enters from the inlet of the steam dryer (3) along with the carrier gas, absorbs the heat of steam extraction in the steam dryer, part of free water is changed into gas state, the gas leaves the steam dryer (3) from the exhaust gas outlet of the steam dryer under the carrying of the carrier gas, and the high-moisture biomass fuel enters the boiler (1) to be combusted and release the heat after the moisture content is reduced;
the method comprises the following steps that water in a boiler (1) absorbs heat to become high-temperature steam, the high-temperature steam enters a steam turbine (2) to do work, exhaust steam of the steam turbine (2) enters a condenser (21) to be condensed, then sequentially passes through a condensate pump (22), a low-pressure heater (23), a low-temperature economizer (42) and a deaerator (24), enters a high-pressure heater (26) after being pressurized by a water feed pump (25), and finally enters the boiler to finish circulation of working media; wherein the low-pressure heater (23) extracts steam to release heat and then converges the steam into condensed water through a hot well, the deaerator (24) extracts steam and directly mixes with feed water to release heat, and the second-stage air preheater (12) drains water, releases heat in the high-pressure heater (26) and converges the heat to the deaerator (24);
the air heater (41), the first-stage air preheater (11) and the second-stage air preheater (12) sequentially heat air;
after measuring the exhaust gas flow, the dryer exhaust gas flow meter (44) sends the parameters to the waste heat recovery system controller (43), and the waste heat recovery system controller (43) adjusts the opening of the valve according to the drying number after operation to control the working state of the waste heat recovery system; when the drying number is less than or equal to 0.08, the waste heat recovery system controller (43) opens the exhaust gas regulating valve (45) of the heater, closes the exhaust gas regulating valve (46) of the low-temperature economizer, and all the exhaust gas of the dryer enters the heater (41); when the drying number is larger than 0.08, the waste heat recovery system controller (43) opens the low-temperature economizer exhaust gas regulating valve (46) and the low-temperature economizer water supply regulating valve (47) and regulates the opening size of the valve, the drying exhaust gas is divided into two paths, one path of flow is kept unchanged and enters the air heater (41) to preheat air, the other path of flow enters the low-temperature economizer (42) to heat condensed water, and the condensed water of steam in the exhaust gas in the air heater (41) and the condensed water of the low-temperature economizer (42) are collected in a water drainage section and then are further cooled, and then the condensed water and the condensed water are sent to the water treatment device (31); after the exhaust gas is subjected to heat release through the air heater (41) and the low-temperature economizer (42), the residual non-condensable gas after moisture condensation is sent back to the second-stage air preheater (12) for heating and then sent to the boiler (1) for treatment;
the dry number is calculated as follows:
Figure FDA0003334353410000051
Figure FDA0003334353410000052
in the formula: m isH2O_r-the amount of the base water/kg.kg-1；mH2O_d-moisture content of dried biomass/kg-kg-1(ii) a Lambda-degree of dryness/kg-1(ii) a LHV-fuel low calorific value/kJ.kg-1(ii) a Mu-number of dried/kg. kJ-1。
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