CN221172205U - Dry quenching thermal power generation system - Google Patents

Abstract

The embodiment of the utility model provides a dry quenching thermal power generation system, which comprises the following components: the device comprises a dry quenching boiler, a steam turbine generator unit, a first steam extraction pipeline, a second steam extraction pipeline, a condensate pump, a desalting water tank, a deoxidized water feed pipeline, a heater and a deoxidizer. The first heat exchange pipeline of the heater is connected in series with the deoxygenated water supply pipeline. The steam turbine cylinder steam inlet to steam turbine cylinder steam outlet direction of the turbo generator set is provided with a first steam extraction port and a second steam extraction port respectively, two ends of the first steam extraction pipeline are connected with the first steam extraction port and the first steam inlet of the deaerator respectively, and the steam extraction with higher temperature of the first steam extraction port can be used as deaeration steam supply of the deaerator. The two ends of the second steam extraction pipeline are respectively connected with the steam extraction port and the steam inlet port of the second heat exchange pipeline, and the steam extraction with lower temperature of the second steam extraction port can be led to the second heat exchange pipeline, so that the condensate water heat exchange after desalting with the first heat exchange pipeline is realized, and the heat utilization rate of the dry quenching thermal power generation system can be improved.

Description

Dry quenching thermal power generation system

Technical Field

The utility model relates to the technical field of dry quenching, in particular to a dry quenching thermal power generation system.

Background

The dry quenching treatment process is an advanced coke production technology, and the working principle is that cold inert gas (nitrogen or waste gas) is used for exchanging heat with red hot red coke in a dry quenching furnace so as to cool the red coke. The inert gas absorbed with red Jiao Reliang transfers heat to the dry quenching boiler to generate steam, and the generated steam can be supplied to a steam turbine generator unit for power generation.

In the operation of the turbo generator set, part of the high-pressure extraction steam can be supplied to the deaerator to deaerate, and the other part of the low-pressure extraction steam cannot meet the pressure value of steam required by the deaerator, so that the steam can be directly discharged, and the energy waste is caused.

Disclosure of utility model

The embodiment of the utility model aims to provide a dry quenching thermal power generation system so as to improve the heat utilization rate of the dry quenching thermal power generation system. The specific technical scheme is as follows:

A dry quenching thermal power generation system comprising:

The system comprises a dry quenching boiler, a steam turbine generator unit, a first steam extraction pipeline, a second steam extraction pipeline, a condensate pump, a desalting water tank, a deoxidized water feed pipeline, a heater and a deoxidizer;

The dry quenching boiler is used for generating main steam, the steam turbine generator unit is used for receiving the main steam of the dry quenching boiler to generate electricity and generate condensed water, the condensed water pump is used for conveying the condensed water to the desalting water tank to desalt the cooling water by the brine outlet tank, and the deoxidized water supply pipeline is used for conveying the desalted condensed water to a water inlet of the deoxidizer; wherein the method comprises the steps of

The heater includes: the first heat exchange pipeline is connected in series with the deoxidized water supply pipeline and is positioned between the water outlet of the desalting water tank and the water inlet of the deoxidizer;

The method comprises the steps that a first steam extraction port and a second steam extraction port are formed in the direction from a steam turbine cylinder steam inlet to a steam turbine cylinder steam outlet of the steam turbine generator unit respectively, and the temperature of the first steam extraction port is higher than that of the second steam extraction port;

The two ends of the first steam extraction pipeline are respectively connected with the first steam extraction port and the first steam inlet of the deaerator, and the two ends of the second steam extraction pipeline are respectively connected with the second steam extraction port and the steam inlet of the second heat exchange pipeline.

In some embodiments, the water outlet of the second heat exchange pipeline is communicated with the water inlet of the condensate pump.

In some embodiments, a liquid check valve is disposed between the water outlet of the second heat exchange line and the water inlet of the condensate pump to restrict the flow of condensate to the second heat exchange line.

In some embodiments, the first extraction line is provided with a first extraction check valve.

In some embodiments, the second extraction line is provided with a second extraction check valve.

In some embodiments, the first steam extraction port is a steam extraction port of 180-220 ℃ of the steam turbine cylinder, the second steam extraction port is a steam extraction port of 100-150 ℃ of the steam turbine cylinder, the deaerator is a medium-low pressure deaerator, and the working pressure of the medium-low pressure deaerator is 0.1-0.32MPa.

In some embodiments, the first steam extraction port is a 260-300 ℃ steam extraction port, the second steam extraction port is a 100-150 ℃ steam extraction port and/or a 180-220 ℃ steam extraction port, the deaerator is a medium pressure deaerator, and the working pressure of the medium pressure deaerator is 0.5-0.8MPa.

In some embodiments, further comprising:

The inlet of the continuous blowdown expander is connected with the blowdown outlet of the dry quenching boiler, and the outlet of the continuous blowdown expander is connected with the second steam inlet of the deaerator.

In some embodiments, further comprising:

A deoxidizing water supply pump and a secondary economizer;

In the water supply direction from the desalting water tank to the deaerator, the deaerating water supply pump, the auxiliary economizer and the first heat exchange pipeline of the heater are sequentially connected in series with the deaerating water supply pipeline.

In some embodiments, further comprising:

A boiler feed water pump;

and deoxygenated water of the deoxygenator is conveyed to the dry quenching boiler through the boiler feed water pump.

According to the dry quenching thermal power generation system provided by the embodiment of the utility model, the first heat exchange pipeline of the heater is connected in series with the deoxygenated water feed pipeline. The steam turbine cylinder steam inlet to steam turbine cylinder steam outlet direction of the steam turbine generator unit is provided with a first steam extraction port and a second steam extraction port respectively, the temperature of the first steam extraction port is higher than that of the second steam extraction port, two ends of a first steam extraction pipeline are connected with the first steam extraction port and the first steam inlet of the deaerator respectively, and the steam extraction with higher temperature of the first steam extraction port can be used as deaeration and steam supply of the deaerator. The two ends of the second steam extraction pipeline are respectively connected with the second steam extraction port and the steam inlet of the second heat exchange pipeline, the steam extraction with lower temperature of the second steam extraction port can be led to the second heat exchange pipeline, so that condensed water heat exchange with the first heat exchange pipeline after desalination is realized, and compared with the prior art, the heat energy recycling of the steam extraction with lower temperature of the second steam extraction port can be realized, and the heat utilization rate of the dry quenching thermal power generation system is improved.

Of course, it is not necessary for any one product to practice the utility model to achieve all of the advantages set forth above at the same time.

Drawings

In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings used in the embodiments or the description of the prior art will be briefly described, and it is obvious that the drawings in the following description are only some embodiments of the present utility model, and other drawings may be obtained according to these drawings for a person having ordinary skill in the art.

Fig. 1 is a schematic structural diagram of a dry quenching thermal power generation system provided in an embodiment of the present disclosure;

Fig. 2 is a schematic diagram of a pipeline structure of a deaerator of a coke dry quenching thermal power generation system according to an embodiment of the present disclosure.

The reference numerals are as follows:

The dry quenching boiler 101, the turbo generator set 102, the first steam extraction port 102a, the second steam extraction port 102b, the first steam extraction pipeline 103, the second steam extraction pipeline 104, the condensate pump 105, the demineralized water tank 106, the deoxygenated water feed pipeline 107, the heater 108, the deoxygenator 109, the water inlet 109a, the first steam inlet 109b, the second steam inlet 109c, the continuous blowdown expander 110, the deoxygenated water feed pump 111, the auxiliary economizer 112, the boiler feed pump 113, the liquid check valve 11, the first steam extraction check valve 12 and the second steam extraction check valve 13.

Detailed Description

The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by the person skilled in the art based on the present utility model are included in the scope of protection of the present utility model.

Steam generated by the coke dry quenching boiler is used for generating electricity by a steam turbine generator unit and generating condensed water. However, in the negative pressure system, condensed water generated by power generation may cause air infiltration due to insufficient tightness of the system. Under certain conditions, these gases can cause corrosion to equipment and reduce the heat exchange efficiency of the heater and the boiler, adversely affecting the economics of the overall generator set. To solve this problem, deaerators have been introduced to deaerate the condensate. The deaerator can effectively remove the dissolved oxygen in the condensed water by utilizing the principle of thermal deaeration.

In the power generation process of the turbo generator set, the thermal efficiency of the turbo generator set can be effectively improved by extracting steam (extraction steam) at a proper position. Specifically, the temperature and pressure of the extracted steam gradually decrease between the steam inlet and the steam outlet of the steam turbine cylinder. That is, the extraction temperature and pressure is higher near the steam inlet of the steam turbine cylinder, while the extraction temperature and pressure is lower near the steam outlet of the steam turbine cylinder.

Working steam required by the deaerator can come from extraction steam of a steam turbine generator unit, but the deaerator has certain requirements on the temperature of the working steam. If the temperature of the extracted steam is too low, the requirement of the deaerator cannot be met, so that part of the extracted steam with lower temperature and low pressure cannot be effectively utilized, and direct discharge causes waste.

Fig. 1 is a schematic structural diagram of a dry quenching thermal power generation system provided by an embodiment of the present disclosure, fig. 2 is a schematic structural diagram of a pipeline of a deaerator of a dry quenching thermal power generation system provided by an embodiment of the present disclosure, and as shown in fig. 1 and fig. 2, the dry quenching thermal power generation system provided by an embodiment of the present disclosure includes: the coke dry quenching boiler 101, the steam turbine generator unit 102, the first steam extraction pipeline 103, the second steam extraction pipeline 104, the condensate pump 105, the desalted water tank 106, the deoxygenated water feed pipeline 107, the heater 108 and the deaerator 109.

The dry quenching boiler 101 is used for generating main steam, the steam turbine generator unit 102 is used for receiving the main steam of the dry quenching boiler 101 for generating electricity and generating condensed water, the condensed water pump 105 is used for conveying the condensed water to the desalting water tank 106 so that the desalting water tank can desalt cooling water, and the deoxidized water feed pipeline 107 is used for conveying the desalted condensed water to the water inlet 109a of the deoxidizer 109.

As shown in fig. 1 and 2, the heater 108 includes: the first heat exchange pipeline and the second heat exchange pipeline realize heat exchange, the first heat exchange pipeline is connected in series with the deoxygenated water feed pipeline 107 and is positioned between the water outlet of the demineralized water tank 106 and the water inlet 109a of the deaerator 109. The steam turbine generator set 102 has a first steam extraction port 102a and a second steam extraction port 102b in the direction from the steam turbine cylinder steam inlet to the steam turbine cylinder steam outlet, and the temperature of the first steam extraction port 102a is greater than the temperature of the second steam extraction port 102 b. The two ends of the first steam extraction pipeline 103 are respectively connected with the first steam extraction port 102a and the first steam inlet 109b of the deaerator 109, and the two ends of the second steam extraction pipeline 104 are respectively connected with the second steam extraction port 102b and the steam inlet of the second heat exchange pipeline.

In the dry quenching thermal power generation system provided by the embodiment of the utility model, the first heat exchange pipeline of the heater 108 is connected in series with the deoxygenated water feed pipeline 107. The direction from the steam inlet of the steam turbine cylinder to the steam outlet of the steam turbine cylinder of the steam turbine generator unit 102 is provided with a first steam extraction port 102a and a second steam extraction port 102b respectively, the temperature of the first steam extraction port 102a is higher than that of the second steam extraction port 102b, two ends of a first steam extraction pipeline 103 are connected with the first steam extraction port 102a and the first steam inlet 109b of the deaerator 109 respectively, and the steam extracted by the first steam extraction port 102a with higher temperature can be used as deoxidization and steam supply of the deaerator 109. The two ends of the second steam extraction pipeline 104 are respectively connected with the second steam extraction port 102b and the steam inlet of the second heat exchange pipeline, and the steam extracted at the lower temperature of the second steam extraction port 102b can be led to the second heat exchange pipeline to realize the heat exchange with the condensate water after the desalination of the first heat exchange pipeline, so that compared with the prior art, the heat energy of the steam extracted at the lower temperature of the second steam extraction port 102b can be recycled, and the heat utilization rate of the dry quenching thermal power generation system is improved.

As shown in fig. 1, in this scheme, before the condensate water after desalination enters the deaerator 109, a heater 108 is set, and steam extracted with a low temperature of the turbo generator set 102 is used to enter the heater 108 and exchange heat with the condensate water (deoxidized backwater) after desalination, and the condensate water after desalination after temperature rise enters the deaerator 109 again, so that steam extracted with a low temperature can be recycled.

The dry quenching boiler 101 described in the present embodiment is not limited to a specific model. For example, the parameters of the water supply system of the dry quenching boiler 101 may be a high temperature and high pressure parameter, a high temperature and ultrahigh pressure parameter, or a ultrahigh temperature and ultrahigh pressure parameter, and have a reheat function, etc., and in this embodiment, the model of the dry quenching boiler 101 is not particularly limited.

The condensate water generated by the turbo generator set 102 can be realized by adopting an air cooling technology or a water cooling technology.

As shown in fig. 1, the water outlet of the second heat exchange pipeline is communicated with the water inlet 109a of the condensate pump 105, so as to realize the steam extraction with lower temperature, and after the steam extraction is converted into condensate water, the steam is recycled.

A liquid check valve 11 may be provided between the water outlet of the second heat exchange line and the water inlet 109a of the condensate pump 105 to restrict the flow of condensate to the second heat exchange line. Therefore, the operation reliability of the dry quenching thermal power generation system can be further improved, and condensate water generated by the steam turbine generator unit 102 is prevented from flowing backwards to the second heat exchange pipeline.

As shown in fig. 1 and 2, the first steam extraction pipe 103 may be provided with a first steam extraction check valve 12 to prevent the steam extraction in the first steam extraction pipe 103 from flowing back to the first steam extraction port 102a after the pressure of the first steam extraction port 102a is reduced. Specifically, the first steam extraction pipeline 103 may further be provided with a safety valve, a quick-closing valve, and a pressure regulating valve, where the first steam extraction check valve 12, the safety valve, the quick-closing valve, and the pressure regulating valve are sequentially disposed in the steam flow direction of the first steam extraction pipeline 103.

As shown in fig. 1, the second steam extraction pipeline 104 may be provided with a second steam extraction check valve 13 to prevent the steam extraction in the second steam extraction pipeline 104 from flowing back to the second steam extraction port 102b after the pressure of the second steam extraction port 102b is reduced. Thereby improving the operation reliability of the dry quenching thermal power generation system and preventing the backflow of the extraction steam in the first extraction steam pipeline 103 and the second extraction steam pipeline 104.

In a specific implementation, as shown in fig. 2, the water outlet of the second heat exchange pipeline may be communicated with the water inlet 109a of the condensate pump 105, so that the condensate converted by the heat exchange and cooling of the second heat exchange pipeline is conveyed to the demineralized water tank 106 through the condensate pump 105 to remove salt, thereby realizing recycling of the steam extracted by the second steam extraction port 102 b.

At present, the dry quenching boiler 101 used in the dry quenching thermal power generation system is mainly of medium temperature and medium pressure type, the oxygen content of the water discharged from the deaerator 109 is less than or equal to 15 mug/L, and the deaeration effect of the low-pressure deaerator 109 adopting the water supply temperature of 104 ℃ can reach the requirement of less than or equal to 15 mug/L. With the rapid development of the dry quenching technology, the high-temperature and high-pressure dry quenching boiler 101 is gradually replacing the medium-temperature and medium-pressure dry quenching boiler 101. The oxygen content of the water discharged from the deaerator 109 is required to be less than or equal to 7 mug/L by the high-temperature high-pressure dry quenching boiler 101, so that the low-pressure deaerator 109 adopted in the market at present can not meet the deoxidization effect requirement of the high-temperature high-pressure dry quenching boiler 101 and above, and the deoxidization effect is mainly compensated by auxiliary dosing.

In some embodiments of the present disclosure, the deaerator 109 may select a medium-low pressure deaerator 109, where the working pressure of the medium-low pressure deaerator 109 is 0.1-0.32Mpa, and the deaerator 109 has a better deaeration effect compared with the low pressure deaerator 109. But at the same time, the required temperature and pressure of the extracted steam are also improved. For example, the medium-low pressure deaerator 109 of 0.2MPa requires a temperature of about 200℃and a pressure of about 0.2 MPa. Therefore, the steam requirement of the 0.2MPa medium-low pressure deaerator 109 cannot be satisfied for steam extraction at 150 ℃. In some embodiments of the present disclosure, as shown in fig. 1, the first steam extraction port 102a is a steam extraction port of 180-220 ℃ of a steam turbine cylinder, the second steam extraction port 102b is a steam extraction port of 100-150 ℃ of the steam turbine cylinder, the deaerator 109 is a medium-low pressure deaerator 109, and the working pressure of the medium-low pressure deaerator 109 is 0.1-0.32MPa. The 180-220 ℃ higher pressure steam extraction of the first steam extraction port 102a supplies steam for the middle-low pressure deaerator 109, the 100-150 ℃ lower pressure steam extraction of the second steam extraction port 102b enters the heater 108 and exchanges heat with desalted condensate water (deoxidized backwater), and the desalted condensate water after temperature rise enters the deaerator 109 again, so that the recovery and reutilization of the 100-150 ℃ steam extraction with lower temperature can be realized.

It is readily appreciated that for a higher oxygen scavenging effect dry quenching thermal power generation system, the pressure of the deaerator 109 may be selected to be of a higher model. For example, when the deaerator 109 is a medium pressure deaerator 109, the working pressure of the medium pressure deaerator 109 is 0.5-0.8Mpa, the temperature of the extraction gas required by the medium pressure deaerator 109 is about 280 ℃, and the pressure of the extraction gas is about 0.6 Mpa. The first steam extraction 102a may be 260-300 c steam extraction. The second steam extraction port 102b may be a steam extraction port at 100-150 ℃, the steam extraction at 100-150 ℃ of the second steam extraction port 102b passes through the heater 108, exchanges heat with the condensate water (deoxidized backwater) after desalting, and the condensate water after desalting after heating enters the deaerator 109 again, so that the recovery and reutilization of the steam extraction at 100-150 ℃ with lower temperature can be realized. Of course, in practice, the second steam extraction 102b may be a 180-220 ℃ steam extraction. For the extraction of low pressure at 180-220 ℃, the steam requirement of the medium-pressure deaerator 109 cannot be met, and the steam can also pass through the heater 108 and exchange heat with condensate water (deoxidized backwater) after desalination. It is easy to understand that the second steam extraction port 102b may also be a steam extraction port at 100-150 ℃ and a steam extraction port at 180-220 ℃, the steam extraction port at 100-150 ℃ and the steam extraction port at 180-220 ℃ are respectively connected to the second steam extraction pipeline 104, and a steam extraction check valve is provided in each pipeline.

As shown in fig. 2, a check valve may be disposed on the deoxygenated water supply line 107 between the water outlet of the demineralized water tank 106 and the water inlet 109a of the deoxygenated water supply line 109 to prevent backflow of deoxygenated water due to an excessive pressure of the deoxygenated water supply line 109.

As shown in fig. 2, one pipeline at the bottom of the deaerator 109 is used as a water supply pipeline of the dry quenching boiler 101, and the other pipeline is used as a water drain pipe and can be connected to a trench.

The first steam extraction port 102a may be a non-adjustable steam extraction port, so as to prevent the steam turbine generator unit 102 from malfunctioning and affecting the steam consumption of the deaerator 109, and may provide a standby steam source to supply steam to the deaerator 109 under the condition that the steam turbine generator unit 102 is malfunctioning and cannot supply steam. In addition, a safety valve, etc. may be further disposed in the first steam extraction pipeline 103, so as to ensure the steam supply safety of the first steam extraction pipeline 103.

As shown in fig. 1, in particular, the dry quenching thermal power generation system further includes: boiler feed water pump 113. The deoxygenated water of the deoxygenator 109 is delivered to the dry quenching boiler 101 by the boiler feed water pump 113. In a specific implementation, the deaerator 109 takes the medium-pressure deaerator 109 as an example, in the arrangement of the medium-pressure deaerator 109 and the boiler feed pump 113, the arrangement height of the medium-pressure deaerator 109 and the height of the water inlet 109a of the boiler feed pump 113 can have a height difference of 7-12 meters, the deaerating head and the deaerating water tank of the medium-pressure deaerator 109 are respectively provided with 1 fully-opened spring safety valve, the total discharge steam quantity of the 2 fully-opened spring safety valves is more than or equal to 2.5 times the rated steam inlet quantity of the medium-pressure deaerator 109, and the nominal diameter of the safety valve of the medium-pressure deaerator 109 is more than or equal to DN150mm.

The temperature of the flue gas discharged from the coke dry quenching boiler 101 after heat exchange needs to be maintained within the range of 160-180 ℃ to ensure the proper working temperature of the internal components of the coke dry quenching boiler 101. If the flue gas temperature is too high, the problem of burning the belt is caused by high coke dry quenching temperature. In the control scheme of the temperature of the flue gas discharged by the dry quenching boiler 101, the heat exchange area of the economizer at the tail part of the dry quenching boiler 101 can be increased.

In the embodiment of the scheme, the deaerator 109 can adopt a medium-low pressure deaerator 109 or a medium-pressure deaerator 109, and a good deaeration effect can be achieved. In a dry quenching thermal power generation system, the realization of a good deoxidization effect is important to the economic benefit of a dry quenching treatment process.

Taking a common dry quenching treatment capacity of 190t/h as an example, the calculation can be seen in the following economic benefit analysis table of the 190t/h dry quenching water-cooled power generation system:

Specifically, as shown in fig. 1 and fig. 2, the above-mentioned dry quenching thermal power generation system further includes: a continuous blowdown expander 110. An inlet of the continuous blowdown expander 110 is connected to a blowdown outlet of the dry quenching boiler 101, and an outlet of the continuous blowdown expander 110 is connected to a second steam inlet 109c of the deaerator 109. On the connection line between the outlet of the continuous blowdown expander 110 and the second steam inlet 109c of the deaerator 109, a check valve may be provided to prevent the deaerator 109 from being pressurized too high to cause backflow of the second steam inlet 109c of the deaerator 109.

In a specific implementation, as shown in fig. 1, the dry quenching thermal power generation system further includes: a deoxygenated feedwater pump 111 and a secondary economizer 112. In the water supply direction from the desalting water tank 106 to the deaerator 109, the deaerating water supply pump 111, the auxiliary economizer 112, and the first heat exchange pipeline of the heater 108 are sequentially connected in series to the deaerating water supply pipeline 107.

The dry quenching thermal power generation system provided by the embodiment of the scheme can have one of the following advantages:

1. The medium-low pressure deaerator 109 or the medium-pressure deaerator 109 is adopted in the dry quenching thermal power generation system, and the oxygen content of the effluent of the deaerator 109 can be lower than 7 mug/L by improving the deaerating effect of the deaerator 109, so that the effect of not using a dry quenching agent, namely acetone oxime, is realized. The service life of the dry quenching boiler 101 can be prolonged, and the running cost of the dry quenching thermal power generation system can be effectively reduced.

2. In the prior art, if the steam supplied from the factory is used as the steam for the deaerator 109, because the low-pressure steam generated from the factory is supplied as the steam source, softened water or primary desalted water is generally used, the water quality does not meet the water supply requirement of the dry quenching boiler 101, and the water quality of the water supplied by the dry quenching boiler 101 is deteriorated after long-term running. In the scheme, the deaerator 109 of the dry quenching thermal power generation system can completely adopt the steam extraction of the steam turbine generator unit 102, and the water quality of the water fed by the dry quenching boiler 101 can be prevented from being poor.

3. According to the embodiment of the scheme, the steam turbine generator unit 102 is adopted for extracting steam for the deaerator 109 system, so that the safe operation of the steam extraction system of the steam turbine generator unit 102 and the deaerator 109 can be ensured, and the danger caused by the overpressure operation of the steam extraction system and the deaerator 109 system is avoided.

4. Compared with a dry quenching thermal power generation system adopting a low-pressure deaerator 109 with the water supply temperature of 104 ℃, in the scheme, the medium-low pressure deaerator 109 with the pressure of 0.2Mpa is adopted, only 30-70 ten thousand yuan is needed to be added in one-time investment of engineering, and the subsequent operation can save the cost of energy and medium consumption for the dry quenching thermal power generation system every year. Taking a common dry quenching water-cooled power generation system with the dry quenching treatment capacity of 190t/h as an example, the embodiment of the scheme can improve the power by about 400 ten thousand degrees per year. Generating benefits of over 200 ten thousand yuan per year can be generated according to electricity price 0.5 yuan/degree calculation. Meanwhile, the dry quenching thermal power generation system can save the consumption of circulating cooling water and deoxidizing agents, and has a value of more than 40 ten thousand yuan. The dry quenching thermal power generation system adopts the medium-pressure deaerator 109 or the medium-low pressure deaerator 109 to replace the atmospheric deaerator 109, and simultaneously uses the steam extracted by the steam turbine generator unit 102 as the deaeration steam for the medium-pressure deaerator 109 or the medium-low pressure deaerator 109, thereby improving the water supply deaeration effect of the dry quenching boiler 101 and creating great economic benefit.

The foregoing description is only of the preferred embodiments of the present utility model and is not intended to limit the scope of the present utility model. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model are included in the protection scope of the present utility model.

Claims (10)

1. A dry quenching thermal power generation system, comprising:

The coke dry quenching device comprises a dry quenching boiler (101), a steam turbine generator unit (102), a first steam extraction pipeline (103), a second steam extraction pipeline (104), a condensate pump (105), a demineralized water tank (106), a deoxidized water feed pipeline (107), a heater (108) and a deaerator (109);

The dry quenching boiler (101) is used for generating main steam, the steam turbine generator unit (102) is used for receiving the main steam of the dry quenching boiler (101) to generate electricity and generate condensed water, the condensed water pump (105) is used for conveying the condensed water to the desalting water tank (106) to enable the desalting water outlet tank to desalt the cooling water, and the deoxidized water feed pipeline (107) is used for conveying the desalted condensed water to a water inlet (109 a) of the deoxidizer (109); wherein the method comprises the steps of

The heater (108) includes: the first heat exchange pipeline and the second heat exchange pipeline realize heat exchange, the first heat exchange pipeline is connected in series with the deoxygenated water feed pipeline (107) and is positioned between the water outlet of the demineralized water tank (106) and the water inlet (109 a) of the deaerator (109);

The method comprises the steps that a first steam extraction port (102 a) and a second steam extraction port (102 b) are respectively arranged in the direction from a steam turbine cylinder steam inlet to a steam turbine cylinder steam outlet of the steam turbine generator unit (102), and the temperature of the first steam extraction port (102 a) is higher than that of the second steam extraction port (102 b);

the two ends of the first steam extraction pipeline (103) are respectively connected with the first steam extraction port (102 a) and the first steam inlet (109 b) of the deaerator (109), and the two ends of the second steam extraction pipeline (104) are respectively connected with the second steam extraction port (102 b) and the steam inlet of the second heat exchange pipeline.

2. A dry quenching thermal power generation system as claimed in claim 1, wherein,

The water outlet of the second heat exchange pipeline is communicated with the water inlet (109 a) of the condensate pump (105).

3. A dry quenching thermal power generation system as claimed in claim 2, wherein,

A liquid check valve (11) is arranged between the water outlet of the second heat exchange pipeline and the water inlet (109 a) of the condensate pump (105) so as to limit the condensate to flow to the second heat exchange pipeline.

4. A dry quenching thermal power generation system as claimed in claim 1, wherein,

The first steam extraction pipeline (103) is provided with a first steam extraction check valve (12).

5. A dry quenching thermal power generation system as claimed in claim 1, wherein,

The second steam extraction pipeline (104) is provided with a second steam extraction check valve (13).

6. A dry quenching thermal power generation system as claimed in claim 1, wherein,

The first steam extraction port (102 a) is a steam extraction port of 180-220 ℃ of the steam turbine cylinder, the second steam extraction port (102 b) is a steam extraction port of 100-150 ℃ of the steam turbine cylinder, the deaerator (109) is a medium-low pressure deaerator (109), and the working pressure of the medium-low pressure deaerator (109) is 0.1-0.32MPa.

7. A dry quenching thermal power generation system as claimed in claim 1, wherein,

The first steam extraction port (102 a) is a steam extraction port at 260-300 ℃, the second steam extraction port (102 b) is a steam extraction port at 100-150 ℃ and/or a steam extraction port at 180-220 ℃, the deaerator (109) is a medium-pressure deaerator (109), and the working pressure of the medium-pressure deaerator (109) is 0.5-0.8MPa.

8. The dry quenching thermal power generation system as recited in claim 7, further comprising:

The continuous blowdown expander (110), the inlet of continuous blowdown expander (110) is connected to the drain of dry quenching boiler (101), the outlet of continuous blowdown expander (110) is connected second steam inlet (109 c) of deaerator (109).

9. The dry quenching thermal power generation system as recited in claim 1, further comprising:

an oxygen-scavenging water feed pump (111) and a secondary economizer (112);

the deaeration water supply pump (111), the auxiliary economizer (112) and the first heat exchange pipeline of the heater (108) are sequentially connected in series to the deaeration water supply pipeline (107) in the water supply direction from the deaeration water tank (106) to the deaerator (109).

10. The dry quenching thermal power generation system as recited in claim 1, further comprising:

A boiler feed water pump (113);

The deoxygenated water of the deoxygenator (109) is delivered to the dry quenching boiler (101) by the boiler feed water pump (113).