CN111151103B - Flue gas dehumidification system of thermal power plant - Google Patents

Flue gas dehumidification system of thermal power plant Download PDF

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CN111151103B
CN111151103B CN201911395271.0A CN201911395271A CN111151103B CN 111151103 B CN111151103 B CN 111151103B CN 201911395271 A CN201911395271 A CN 201911395271A CN 111151103 B CN111151103 B CN 111151103B
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程亮
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Hebei Zhongyuan Environmental Protection Technology Co ltd
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Handan College
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B01D53/265—Drying gases or vapours by refrigeration (condensation)
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K17/00—Using steam or condensate extracted or exhausted from steam engine plant
    • F01K17/02—Using steam or condensate extracted or exhausted from steam engine plant for heating purposes, e.g. industrial, domestic
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/80—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases

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Abstract

The invention is suitable for the technical field of environmental protection, and discloses a flue gas dehumidification system of a thermal power plant, which comprises: the system comprises a flue gas heater, a wet smoke plume turbine and a secondary reheating unit; the secondary reheating unit comprises an ultrahigh pressure cylinder and a heater group; the heater group comprises a ninth heater; the wet smoke plume turbine is respectively connected with the ultrahigh pressure cylinder and the smoke heater, the smoke heater is connected with the outlet of the ninth heater, and the ultrahigh pressure cylinder and the wet smoke plume turbine are both connected with the heater group; the smoke heater heats low-temperature smoke by using high-temperature steam obtained by steam extraction of the wet smoke plume turbine to obtain high-temperature smoke, the high-temperature smoke is transmitted to an external chimney, and meanwhile, the low-temperature steam formed by heat release of the high-temperature steam is transmitted to an outlet of the ninth heater; and the steam source of the wet smoke plume turbine is the steam obtained by extracting steam by the ultrahigh pressure cylinder according to the predetermined steam extraction parameters. The invention does not need to go through the links of temperature and pressure reduction, can greatly reduce the throttling loss and heat exchange loss, and improve the efficiency of the unit.

Description

Flue gas dehumidification system of thermal power plant
Technical Field
The invention belongs to the technical field of environmental protection, and particularly relates to a flue gas dehumidification system of a thermal power plant.
Background
When wet desulphurization is adopted for flue gas desulphurization, the temperature of flue gas at a desulphurization outlet is about 50 ℃, the flue gas is usually in a saturated humidity state at the moment, the saturated humidity flue gas is rapidly cooled by the atmosphere with lower temperature after being discharged from a chimney, water vapor in the flue gas is condensed into a liquid state, the light transmittance is reduced, and thus the phenomenon of white wet smoke plume visible to the naked eye appears; along with the diffusion of the water vapor in the atmosphere, the concentration of the water vapor is reduced, the light transmittance is improved, and the white wet smoke plume is slowly reduced until disappears and cannot be seen.
At present, steam of a communication pipe of an intermediate pressure cylinder and a low pressure cylinder is usually extracted to be used as a steam source for flue gas dehumidification, but the temperature and the pressure of the steam at the position can not meet the parameter requirements required by flue gas dehumidification, and the steam can be used only after temperature and pressure reduction, so that great throttling loss and heat exchange loss are caused, and the unit efficiency is low.
Disclosure of Invention
In view of this, the embodiment of the invention provides a flue gas dehumidification system for a thermal power plant, so as to solve the problem that the unit efficiency is low because the temperature and the pressure of steam in a communication pipe between an intermediate pressure cylinder and a low pressure cylinder cannot meet the parameter requirements for flue gas dehumidification and the steam can be used only after being subjected to temperature and pressure reduction, which causes great throttling loss and heat exchange loss.
The embodiment of the invention provides a flue gas dehumidification system of a thermal power plant, which comprises: the system comprises a flue gas heater, a wet smoke plume turbine and a secondary reheating unit;
the secondary reheating unit comprises an ultrahigh pressure cylinder and a heater group; the heater group comprises a ninth heater;
the wet smoke plume turbine is respectively connected with the ultrahigh pressure cylinder and the smoke heater, the smoke heater is connected with an outlet of the ninth heater, and the ultrahigh pressure cylinder and the wet smoke plume turbine are both connected with the heater group;
the smoke heater heats low-temperature smoke by using high-temperature steam obtained by extracting steam by the wet smoke plume turbine to obtain high-temperature smoke, the high-temperature smoke is transmitted to an external chimney, and meanwhile, low-temperature steam formed by heat release of the high-temperature steam is transmitted to an outlet of the ninth heater;
and the steam source of the wet smoke plume turbine is steam obtained by extracting steam by the ultrahigh pressure cylinder according to predetermined steam extraction parameters.
Compared with the prior art, the embodiment of the invention has the following beneficial effects: the smoke heater heats low-temperature smoke by using high-temperature steam obtained by steam extraction of the wet smoke plume turbine to obtain high-temperature smoke, the high-temperature smoke is transmitted to an external chimney, and meanwhile, the low-temperature steam formed by heat release of the high-temperature steam is transmitted to an outlet of the ninth heater; the steam source of the wet smoke plume turbine is steam obtained by steam extraction with the ultrahigh pressure cylinder according to the predetermined steam extraction parameters, the steam obtained by steam extraction with the ultrahigh pressure cylinder according to the predetermined steam extraction parameters is used as steam inlet, the steam extraction parameters can just meet the steam parameters required by the flue gas heater, the steam can directly enter the flue gas heater without temperature and pressure reduction to heat and supply energy to the flue gas, and the steam is supplied to the flue gas heater without the high pressure cylinder and the intermediate pressure cylinder, so that throttling loss and heat exchange loss can be greatly reduced, and the unit efficiency is improved.
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In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings needed to be used in the embodiments or the prior art descriptions will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without inventive exercise.
Fig. 1 is a schematic structural diagram of a flue gas dehumidification system of a thermal power plant according to an embodiment of the present invention;
FIG. 2 is a schematic structural diagram of a flue gas dehumidification system of a thermal power plant according to another embodiment of the present invention;
fig. 3 is a schematic structural diagram of a flue gas heater according to an embodiment of the present invention.
Detailed Description
In the following description, for purposes of explanation and not limitation, specific details are set forth, such as particular system structures, techniques, etc. in order to provide a thorough understanding of the embodiments of the present application. It will be apparent, however, to one skilled in the art that the present application may be practiced in other embodiments that depart from these specific details. In other instances, detailed descriptions of well-known systems, devices, circuits, and methods are omitted so as not to obscure the description of the present application with unnecessary detail.
In order to explain the technical means of the present invention, the following description will be given by way of specific examples.
Fig. 1 is a schematic structural diagram of a flue gas dehumidification system of a thermal power plant according to an embodiment of the present invention, and for convenience of description, only parts related to the embodiment of the present invention are shown. As shown in fig. 1, the flue gas dehumidification system of the thermal power plant comprises: the system comprises a flue gas heater, a wet smoke plume turbine and a secondary reheating unit;
the secondary reheating unit comprises an ultrahigh pressure cylinder VHP and a heater group; the heater group includes the ninth heater (# 9 in the low-pressure heater group);
the wet smoke plume turbine is respectively connected with the ultrahigh pressure cylinder VHP and the smoke heater, the smoke heater is connected with the outlet of the ninth heater, and the ultrahigh pressure cylinder VHP and the wet smoke plume turbine are both connected with the heater group;
the smoke heater heats low-temperature smoke by using high-temperature steam obtained by steam extraction of the wet smoke plume turbine to obtain high-temperature smoke, the high-temperature smoke is transmitted to an external chimney, and meanwhile, the low-temperature steam formed by heat release of the high-temperature steam is transmitted to an outlet of the ninth heater;
and the steam source of the wet smoke plume turbine is the steam obtained by extracting steam by the ultrahigh pressure cylinder VHP according to the predetermined steam extraction parameters.
Optionally, referring to fig. 2, the flue gas dehumidification system of the thermal power plant may further include a desulfurization tower, and the desulfurization tower is connected with the flue gas heater; and the external flue gas is desulfurized by the desulfurizing tower to form the low-temperature flue gas.
Optionally, referring to fig. 1, the flue gas dehumidification system of the thermal power plant may further include a water pump W3, where the water pump W3 is connected to outlets of the flue gas heater and the ninth heater, respectively; the low-temperature steam forms return water through a water pump W3, and the return water is transmitted to an outlet of the ninth heater and mixed with condensed water to enter the eighth heater.
In the embodiment of the invention, the flue gas heater heats low-temperature flue gas by using high-temperature steam obtained by extracting steam by using the wet smoke plume turbine to obtain high-temperature flue gas, the high-temperature flue gas is transmitted to an external chimney, and meanwhile, the low-temperature steam formed by releasing heat of the high-temperature steam is transmitted to an outlet of the ninth heater; the steam source of the wet smoke plume turbine is the steam obtained by steam extraction of the ultrahigh pressure cylinder VHP according to the predetermined steam extraction parameters, the steam obtained by steam extraction of the ultrahigh pressure cylinder VHP according to the predetermined steam extraction parameters is used as steam inlet, the steam extraction parameters of the wet smoke plume turbine in the embodiment of the invention can just meet the steam parameters required by the flue gas heater, the wet smoke plume turbine can directly enter the flue gas heater without temperature and pressure reduction to heat and supply energy to the flue gas, and the high pressure cylinder HP and the intermediate pressure cylinder IP are not required to supply steam to the flue gas heater, so that the throttling loss and the heat exchange loss can be greatly reduced, and the unit efficiency and the unit economy are improved. The flow pressure difference of the wet smoke plume turbine is increased, and the efficiency is higher.
In an embodiment of the present invention, the determining process of the steam extraction parameter includes:
generating an initial population of the steam extraction parameters of the VHP, wherein the initial population comprises a plurality of particles;
calculating the fitness value of each particle, and updating the speed and the position of each particle according to the fitness value of each particle;
if the position of a certain particle is better than the optimal value of the particle, taking the position of the particle as the new optimal value of the particle;
if the position of a certain particle is superior to the global optimum value, taking the position of the particle as a new global optimum value;
if the preset convergence condition is met, the current global optimal value is the finally determined steam extraction parameter of the ultrahigh pressure cylinder VHP;
if the preset convergence condition is not met, the step of calculating the fitness value of each particle is continuously executed.
Wherein the extraction parameter may comprise an extraction pressure.
In the embodiment of the invention, the self-adaptive weight particle swarm algorithm is introduced to optimize the steam extraction parameters in real time according to the water content of the flue gas on site. Specifically, an initial particle population of the steam extraction parameter is generated, and an optimal value and a global optimal value of each particle are randomly generated; generating a fitness function according to the current working condition, calculating the fitness value of each particle according to the fitness function, determining the optimal fitness value (the fitness value of the particle which is most matched with the current working condition) and the average fitness value (the fitness value of all the particles is averaged) in the current iteration according to the calculated fitness value of each particle, and updating the speed and the position of each particle according to the optimal fitness value and the average fitness value in the current iteration; if the updated position of a certain particle is superior to the optimal value of the particle, taking the updated position of the particle as the new optimal value of the particle, otherwise, continuing to execute the next step; if the updated position of a certain particle is superior to the global optimum value, taking the updated position of the particle as a new global optimum value, otherwise, continuing to execute the next step; and judging whether a preset convergence condition is met, if so, taking the current global optimal value as the finally determined steam extraction parameter, and if not, skipping to the step of calculating the fitness value of each particle for cyclic execution.
The preset convergence condition may be set according to actual requirements, for example, may be set to reach a preset number of iterations, and the like.
In one embodiment of the present invention, the formula for updating the velocity and position of each particle based on the fitness value of each particle is:
Figure BDA0002346130450000051
Figure BDA0002346130450000052
Figure BDA0002346130450000053
Figure BDA0002346130450000054
Figure BDA0002346130450000055
wherein the content of the first and second substances,
Figure BDA0002346130450000056
the velocity of the ith particle at the t +1 th iteration;
Figure BDA0002346130450000057
the inertia weight of the ith particle at the t iteration;
Figure BDA0002346130450000058
the speed of the ith particle at the t iteration; c. C1Is a first acceleration factor; c. C2Is a second acceleration factor; r is1Is a first random number, r1Is in the range of [0,1]；r2Is a second random number, r2Is in the range of [0,1]；
Figure BDA0002346130450000059
The optimal value of the ith particle in t iterations;
Figure BDA00023461304500000510
is the position of the ith particle at the time of the t-th iteration;
Figure BDA00023461304500000511
the global optimal value of the population in the t iterations is obtained;
Figure BDA00023461304500000512
is the position of the ith particle at the t +1 th iteration;
Figure BDA00023461304500000513
the position of the ith particle at the t-1 st iteration; alpha is a third random number, alpha ranges from 0,1](ii) a Beta is a fourth random number, beta ranges from 0,1]；
Figure BDA00023461304500000514
The evolution speed factor of the ith particle at the t iteration is taken as the evolution speed factor; s1Is an adaptability value concentration factor;
Figure BDA00023461304500000515
is composed of
Figure BDA00023461304500000516
A fitness value of;
Figure BDA00023461304500000517
is composed of
Figure BDA00023461304500000518
A fitness value of; ftIs the best fitness value in the t-th iteration;
Figure BDA00023461304500000519
for the average fitness value in the t-th iteration, n is the total number of particles.
c1And c2The acceleration coefficients can be determined according to actual requirements. r is1、r2Alpha and beta are in [0,1 ]]Random numbers that vary within a range.
In one embodiment of the present invention, referring to fig. 1, the double reheat unit further includes a boiler B, a high pressure cylinder HP, an intermediate pressure cylinder IP, a low pressure cylinder LP, a condenser C, and a condensate pump W1;
the boiler B is respectively connected with the ultrahigh pressure cylinder VHP, the high pressure cylinder HP, the intermediate pressure cylinder IP and the heater group, and the low pressure cylinder LP is respectively connected with the intermediate pressure cylinder IP and the condenser C; the condensate pump W1 is respectively connected with the condenser C and the heater group, and the high-pressure cylinder HP, the intermediate-pressure cylinder IP, the low-pressure cylinder LP and the condenser C are all connected with the heater group.
In one embodiment of the present invention, referring to fig. 1, the heater group further includes a first heater (# 1 in the high-pressure heater group), #2 in the second heater (# 2 in the high-pressure heater group), #3 in the third heater (# 3 in the high-pressure heater group), #4 in the fourth heater (# 4 in the high-pressure heater group), #5 in the fifth heater, #6 in the low-pressure heater group), #7 in the seventh heater (# 7 in the low-pressure heater group), #8 in the low-pressure heater group), #10 in the tenth heater (# 10 in the low-pressure heater group), and a feed water pump W2;
the ultrahigh pressure cylinder VHP and the boiler B are both connected with the first heater, the high pressure cylinder HP is respectively connected with the second heater and the third heater, the intermediate pressure cylinder IP is respectively connected with the fourth heater, the water feed pump W2, the fifth heater and the sixth heater, the low pressure cylinder LP is respectively connected with the seventh heater, the eighth heater, the ninth heater and the tenth heater, the wet smoke plume turbine is respectively connected with the third heater, the fourth heater, the fifth heater and the sixth heater, and the condenser C and the condensate pump W1 are both connected with the tenth heater;
the second heater is respectively connected with the first heater and the third heater, the fourth heater is respectively connected with the third heater, the water feeding pump W2 and the fifth heater, the fifth heater is respectively connected with the water feeding pump W2 and the sixth heater, the seventh heater is respectively connected with the sixth heater and the eighth heater, and the ninth heater is respectively connected with the eighth heater and the tenth heater.
In one embodiment of the present invention, referring to fig. 1, the first heater, the second heater, the third heater and the fourth heater are all high-pressure heaters, the fifth heater is a deaerator, and the sixth heater, the seventh heater, the eighth heater, the ninth heater and the tenth heater are all low-pressure heaters;
the drainage of the heater group adopts a step-by-step self-flow mode, the drainage of the high-pressure heater flows into the deaerator, and the drainage of the low-pressure heater flows into the condenser C.
In the embodiment of the invention, a heater group adopts 10-grade regenerative heaters, the arrangement mode is 'four high five low one oxygen removal', a high-pressure heater group comprises a first heater, a second heater, a third heater and a fourth heater, a low-pressure heater group comprises a sixth heater, a seventh heater, an eighth heater, a ninth heater and a tenth heater, and a fifth heater is an oxygen remover. Drainage of the high-pressure heater group and drainage of the low-pressure heater group all adopt a mode of flowing automatically step by step, drainage of the high-pressure heater group flows into the deaerator, and drainage of the low-pressure heater group flows into the condenser C.
And the main steam at the outlet of the boiler B enters the ultrahigh pressure cylinder VHP to do work and then returns to the boiler B to be reheated for the first time. The steam after the first reheating enters a high-pressure cylinder HP to do work, then returns to a boiler B to be reheated for the second time, the steam after the second reheating sequentially enters an intermediate-pressure cylinder IP and a low-pressure cylinder LP to do work, then enters a condenser C, is condensed into saturated water by wet steam and then is pressurized by a condensate pump W1, and is pumped into a low-pressure heater group, the low-pressure heater group flows into a deaerator after being heated and deaerated in the deaerator, and is pressurized by a water feed pump W2, and is pumped into a high-pressure heater group, the high-pressure heater group heats and then enters the boiler B, the steam is heated in the boiler B to become main steam, and the circulation process is repeated.
The wet smoke plume turbine takes ultrahigh pressure cylinder VHP extraction steam as steam inlet and is provided with a steam extraction port, and the extraction steam can be supplied to partial heaters, for example, a smoke heater, a third heater, a fourth heater, a fifth heater and a sixth heater. The extraction steam of the ultrahigh pressure cylinder VHP may be supplied to a part of the heaters, for example, may be supplied to the first heater. The extraction steam of the high pressure cylinder HP may be supplied to a part of the heaters, for example, may be supplied to the second heater and the third heater. The extraction steam of the intermediate pressure cylinder IP may be supplied to a part of the heaters, for example, may be supplied to the fourth heater, the fifth heater, and the sixth heater. The extraction steam of the low pressure cylinder LP may be supplied to a part of the heaters, for example, the seventh heater, the eighth heater, the ninth heater, and the tenth heater.
Optionally, the ultrahigh pressure cylinder VHP, the high pressure cylinder HP, the intermediate pressure cylinder IP, the low pressure cylinder LP and the wet plume turbine may be connected to each heater through a pressure stabilizing valve.
Low pressure jar LP designs according to the flow, need not to keep apart the cocurrent part selectivity, and intermediate pressure jar IP need not to increase the surge damping valve with low pressure jar LP communicating pipe department.
And according to the selection condition of the backwater position of the extracted steam of the wet smoke plume turbine passing through the smoke heater, the backwater position of the unit is selected at the outlet of the ninth heater, and the backwater and the condensed water are mixed and then enter the eighth heater.
And the drain of the wet smoke plume turbine is respectively connected with a third heater, a fourth heater, a fifth heater and a sixth heater according to the actual situation.
In one embodiment of the present invention, referring to fig. 1, the double reheat unit further comprises a first generator G1 connected to low pressure cylinder LP.
In one embodiment of the present invention, referring to fig. 1, the flue gas dehumidification system of a thermal power plant further comprises a second generator G2 connected to the wet plume turbine.
In the embodiment of the invention, the wet smoke plume turbine independently drives one generator to form a double-shaft power generation system together with the secondary reheating unit, so that the efficiency can be improved.
In one embodiment of the invention, referring to fig. 3, the flue gas heater comprises an upper tank 31, a lower tank 32 and heat pipes 33; the heat pipe 33 penetrates through the upper box body 31 and the lower box body 32, and a heat exchange medium is filled in the heat pipe 33;
the low-temperature flue gas flows in from the inlet of the upper box body 31, and the high-temperature flue gas flows out from the outlet of the upper box body 31;
high-temperature steam flows in from the inlet of the lower box body 32, and low-temperature steam flows out from the outlet of the lower box body 32;
after absorbing the heat of the high-temperature steam, the heat exchange medium is evaporated into a gas medium, the gas medium rises to the upper box body 31 side, and meanwhile, the high-temperature steam releases heat to form low-temperature steam; the low-temperature flue gas absorbs the heat of the gas medium to obtain high-temperature flue gas, and meanwhile, the gas medium releases heat and is condensed to form a heat exchange medium and descends to the lower box body 32 side.
In one embodiment of the invention, referring to fig. 3, the flow direction of the low temperature flue gas is opposite to the flow direction of the high temperature steam.
In the embodiment of the invention, the flue gas heater is a heat pipe 33 flue gas heater, and is heat exchange equipment designed by utilizing the heat pipe 33 technology. After the heat pipe 33 is evacuated, a heat exchange medium is filled therein. The heat pipe 33 communicates the upper case 31 and the lower case 32. The flue gas flows in the upper box 31, and the high-temperature steam flows in the lower box 32 in a reverse direction, that is, the inlet of the lower box 32 is arranged at the outlet side of the upper box 31, and the outlet of the lower box 32 is arranged at the inlet side of the upper box 31.
The heat of the high-temperature steam is transferred to the heat exchange medium in the heat pipe 33 through the pipe wall, and the heat exchange medium boils to evaporate the displacement gas medium after absorbing heat. The gas medium rises to the low temperature side (i.e. the upper box body 31 side) under the action of the pressure difference, transfers latent heat of vaporization to the low temperature flue gas outside the heat pipe 33, condenses to form a heat exchange medium, and then returns to the high temperature side (i.e. the lower box body 32 side) under the action of gravity. The heat transfer is realized by the heat exchange medium in such a cycle. Wherein, the heat exchange medium can be a liquid medium.
According to the embodiment of the invention, the aim of dehumidifying the smoke is achieved by heating the low-temperature smoke, so that the aim of eliminating white smoke plume is achieved. Eliminating white plume can eliminate visual pollution: eliminate wet smoke plume at the outlet of the chimney, eliminate visual pollution which is disliked by the public, and establish active enterprisesAn industrial and social image; can save water: taking a 300MW unit as an example, the clean flue gas is condensed at 5 ℃, and the condensed water can be recovered for about 30-40 t, so that the desulfurized water can be reduced, and the process water consumption can be reduced; advanced treatment of the contaminants can be carried out: condensing saturated wet flue gas to separate out fine liquid drops to dust and SO3Partial soluble salt, mercury and other pollutants have the function of further removing synergistically; acid corrosion can be avoided: the corrosion of the flue and the chimney at the downstream of the desulfurizing tower due to the coagulation of acidic liquid drops is reduced.
It should be noted that, all the examples in the above embodiments are only for explaining the technical solutions of the present invention, and are not used to limit the present invention.
It will be apparent to those skilled in the art that, for convenience and brevity of description, only the above-mentioned division of the functional units and modules is illustrated, and in practical applications, the above-mentioned function distribution may be performed by different functional units and modules according to needs, that is, the internal structure of the system is divided into different functional units or modules to perform all or part of the above-mentioned functions. Each functional unit and module in the embodiments may be integrated in one processing unit, or each unit may exist alone physically, or two or more units are integrated in one unit, and the integrated unit may be implemented in a form of hardware, or in a form of software functional unit. In addition, specific names of the functional units and modules are only for convenience of distinguishing from each other, and are not used for limiting the protection scope of the present application. The specific working processes of the units and modules in the above-mentioned apparatus may refer to the corresponding processes in the foregoing method embodiments, and are not described herein again.
Those of ordinary skill in the art will appreciate that the various illustrative elements and algorithm steps described in connection with the embodiments disclosed herein may be implemented as electronic hardware or combinations of computer software and electronic hardware. Whether such functionality is implemented as hardware or software depends upon the particular application and design constraints imposed on the implementation. Skilled artisans may implement the described functionality in varying ways for each particular application, but such implementation decisions should not be interpreted as causing a departure from the scope of the present application.
In the embodiments provided in the present application, it should be understood that the disclosed terminal device and method may be implemented in other ways. For example, the above-described terminal device embodiments are merely illustrative, and for example, the division of the modules or units is only one logical function division, and there may be other divisions when actually implemented, for example, a plurality of units or components may be combined or may be integrated into another system, or some features may be omitted or not executed. In addition, the shown or discussed mutual coupling or direct coupling or communication connection may be an indirect coupling or communication connection through some interfaces, devices or units, and may be in an electrical, mechanical or other form.
The units described as separate parts may or may not be physically separate, and parts displayed as units may or may not be physical units, may be located in one place, or may be distributed on a plurality of network units. Some or all of the units can be selected according to actual needs to achieve the purpose of the solution of the embodiment.
In addition, functional units in the embodiments of the present application may be integrated into one processing unit, or each unit may exist alone physically, or two or more units are integrated into one unit. The integrated unit can be realized in a form of hardware, and can also be realized in a form of a software functional unit.
The integrated modules/units, if implemented in the form of software functional units and sold or used as separate products, may be stored in a computer readable storage medium. Based on such understanding, all or part of the flow in the method of the embodiments described above can be realized by a computer program, which can be stored in a computer-readable storage medium and can realize the steps of the embodiments of the methods described above when the computer program is executed by a processor. Wherein the computer program comprises computer program code, which may be in the form of source code, object code, an executable file or some intermediate form, etc. The computer-readable medium may include: any entity or device capable of carrying the computer program code, recording medium, usb disk, removable hard disk, magnetic disk, optical disk, computer Memory, Read-Only Memory (ROM), Random Access Memory (RAM), electrical carrier wave signals, telecommunications signals, software distribution medium, and the like. It should be noted that the computer readable medium may contain other components which may be suitably increased or decreased as required by legislation and patent practice in jurisdictions, for example, in some jurisdictions, computer readable media which may not include electrical carrier signals and telecommunications signals in accordance with legislation and patent practice.
The above-mentioned embodiments are only used for illustrating the technical solutions of the present application, and not for limiting the same; although the present application has been described in detail with reference to the foregoing embodiments, it should be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; such modifications and substitutions do not substantially depart from the spirit and scope of the embodiments of the present application and are intended to be included within the scope of the present application.

Claims (8)

1. The utility model provides a flue gas dehumidification system of thermal power plant which characterized in that includes: the system comprises a flue gas heater, a wet smoke plume turbine and a secondary reheating unit;
the secondary reheating unit comprises an ultrahigh pressure cylinder and a heater group; the heater group comprises a ninth heater;
the wet smoke plume turbine is respectively connected with the ultrahigh pressure cylinder and the smoke heater, the smoke heater is connected with an outlet of the ninth heater, and the ultrahigh pressure cylinder and the wet smoke plume turbine are both connected with the heater group;
the smoke heater heats low-temperature smoke by using high-temperature steam obtained by extracting steam by the wet smoke plume turbine to obtain high-temperature smoke, the high-temperature smoke is transmitted to an external chimney, and meanwhile, low-temperature steam formed by heat release of the high-temperature steam is transmitted to an outlet of the ninth heater;
the steam source of the wet smoke plume turbine is steam obtained by extracting steam by the ultrahigh pressure cylinder according to predetermined steam extraction parameters;
the steam extraction parameter determination process comprises the following steps:
generating an initial population of steam extraction parameters of the ultra-high pressure cylinder, wherein the initial population comprises a plurality of particles;
calculating the fitness value of each particle, and updating the speed and the position of each particle according to the fitness value of each particle;
if the position of a certain particle is better than the optimal value of the particle, taking the position of the particle as the new optimal value of the particle;
if the position of a certain particle is superior to the global optimum value, taking the position of the particle as a new global optimum value;
if the preset convergence condition is met, the current global optimal value is the finally determined steam extraction parameter of the ultrahigh pressure cylinder;
if the preset convergence condition is not met, continuing to execute the step of calculating the fitness value of each particle;
and updating the formula of the speed and the position of each particle according to the fitness value of each particle as follows:
Figure FDA0003319209190000021
Figure FDA0003319209190000022
Figure FDA0003319209190000023
Figure FDA0003319209190000024
Figure FDA0003319209190000025
wherein the content of the first and second substances,
Figure FDA0003319209190000026
the velocity of the ith particle at the t +1 th iteration;
Figure FDA0003319209190000027
the inertia weight of the ith particle at the t iteration;
Figure FDA0003319209190000028
the speed of the ith particle at the t iteration; c. C1Is a first acceleration factor; c. C2Is a second acceleration factor; r is1Is a first random number, r1Is in the range of [0,1]；r2Is a second random number, r2Is in the range of [0,1]；
Figure FDA0003319209190000029
The optimal value of the ith particle in t iterations;
Figure FDA00033192091900000210
is the position of the ith particle at the time of the t-th iteration;
Figure FDA00033192091900000211
the global optimal value of the population in the t iterations is obtained;
Figure FDA00033192091900000212
is the position of the ith particle at the t +1 th iteration;
Figure FDA00033192091900000213
the position of the ith particle at the t-1 st iteration; alpha is a third random number, alpha ranges from 0,1](ii) a Beta is a fourth random number, beta ranges from 0,1]；
Figure FDA00033192091900000214
The evolution speed factor of the ith particle at the t iteration is taken as the evolution speed factor; s1Is an adaptability value concentration factor;
Figure FDA00033192091900000215
is composed of
Figure FDA00033192091900000216
A fitness value of;
Figure FDA00033192091900000217
is composed of
Figure FDA00033192091900000218
A fitness value of; ftIs the best fitness value in the t-th iteration;
Figure FDA00033192091900000219
for the average fitness value in the t-th iteration, n is the total number of particles.
2. The flue gas dehumidification system of a thermal power plant as recited in claim 1, wherein said secondary reheating unit further comprises a boiler, a high pressure cylinder, a medium pressure cylinder, a low pressure cylinder, a condenser and a condensate pump;
the boiler is respectively connected with the ultrahigh pressure cylinder, the high pressure cylinder, the intermediate pressure cylinder and the heater group, and the low pressure cylinder is respectively connected with the intermediate pressure cylinder and the condenser; the condensate pump respectively with the condenser with the heater group link, the high pressure jar, the intermediate pressure jar, the low pressure jar with the condenser all with the heater group link.
3. The flue gas dehumidification system of a thermal power plant of claim 2, wherein the heater group further comprises a first heater, a second heater, a third heater, a fourth heater, a fifth heater, a sixth heater, a seventh heater, an eighth heater, a tenth heater, and a feedwater pump;
the ultrahigh pressure cylinder and the boiler are both connected with the first heater, the high pressure cylinder is respectively connected with the second heater and the third heater, the intermediate pressure cylinder is respectively connected with the fourth heater, the water feed pump, the fifth heater and the sixth heater, the low pressure cylinder is respectively connected with the seventh heater, the eighth heater, the ninth heater and the tenth heater, the wet smoke plume turbine is respectively connected with the third heater, the fourth heater, the fifth heater and the sixth heater, and the condenser and the condensate pump are both connected with the tenth heater;
the second heater is respectively connected with the first heater and the third heater, the fourth heater is respectively connected with the third heater, the water feeding pump and the fifth heater, the fifth heater is respectively connected with the water feeding pump and the sixth heater, the seventh heater is respectively connected with the sixth heater and the eighth heater, and the ninth heater is respectively connected with the eighth heater and the tenth heater.
4. The flue gas dehumidification system of a thermal power plant of claim 3, wherein the first heater, the second heater, the third heater and the fourth heater are all high pressure heaters, the fifth heater is a deaerator, and the sixth heater, the seventh heater, the eighth heater, the ninth heater and the tenth heater are all low pressure heaters;
the drainage of the heater group adopts a step-by-step self-flow mode, the drainage of the high-pressure heater flows into the deaerator, and the drainage of the low-pressure heater flows into the condenser.
5. The flue gas dehumidification system of a thermal power plant of claim 2, wherein the secondary reheat train further comprises a first generator coupled to the low pressure cylinder.
6. The thermal power plant flue gas dehumidification system of any one of claims 1 to 5, further comprising a second generator coupled to the wet plume turbine.
7. The flue gas dehumidification system of a thermal power plant according to any one of claims 1 to 5, wherein the flue gas heater comprises an upper tank, a lower tank and a heat pipe; the heat pipe penetrates through the upper box body and the lower box body, and a heat exchange medium is filled in the heat pipe;
the low-temperature flue gas flows in from the inlet of the upper box body, and the high-temperature flue gas flows out from the outlet of the upper box body;
the high-temperature steam flows in from an inlet of the lower box body, and the low-temperature steam flows out from an outlet of the lower box body;
after absorbing the heat of the high-temperature steam, the heat exchange medium is evaporated into a gas medium, the gas medium rises to the upper box side, and meanwhile, the high-temperature steam releases heat to form the low-temperature steam; the low-temperature flue gas absorbs the heat of the gas medium to obtain the high-temperature flue gas, and meanwhile, the gas medium releases heat and is condensed to form the heat exchange medium and descends to the lower box body side.
8. The thermal power plant flue gas dehumidification system of claim 7, wherein a flow direction of the low temperature flue gas is opposite to a flow direction of the high temperature steam.
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