CN108114583B - Method and system for controlling flue gas-related atmospheric acidic particulate matters and controlling haze with low carbon - Google Patents

Method and system for controlling flue gas-related atmospheric acidic particulate matters and controlling haze with low carbon Download PDF

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CN108114583B
CN108114583B CN201711414490.XA CN201711414490A CN108114583B CN 108114583 B CN108114583 B CN 108114583B CN 201711414490 A CN201711414490 A CN 201711414490A CN 108114583 B CN108114583 B CN 108114583B
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heat exchange
flue gas
water
shell
temperature
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CN108114583A (en
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李树生
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Shandong Tianjing Environmental Protection Technology Co ltd
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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
    • B01D53/265—Drying gases or vapours by refrigeration (condensation)
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
    • B01D5/0006—Coils or serpentines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/0075—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with heat exchanging
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
    • B01D5/009—Collecting, removing and/or treatment of the condensate
    • 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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  • Chemical Kinetics & Catalysis (AREA)
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  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
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Abstract

The invention relates to a method for controlling atmosphere acidic particulate matters related to flue gas, an energy-saving micro-emission low-carbon haze treatment method suitable for flue gas pollution control by adopting the method, and an energy-saving micro-emission low-carbon haze treatment system suitable for flue gas pollution control by adopting the method, wherein the particulate matter control method controls or reduces the water content in the flue gas so as to control or reduce the direct or indirect reaction of acidic gas components in the flue gas and alkaline substances under the participation of water to generate salt, and further reduce the atmosphere particulate matters and/or non-granular atmosphere pollutants derived from the salt; the low-carbon haze control method controls atmospheric particulates related to smoke through the method, so that low-carbon haze control is realized; the low-carbon haze treatment system is provided with heat exchange equipment used for removing water vapor on a flue. The invention can greatly reduce the air discharge of water vapor, reduce the pollution source of atmospheric chemical combination evolution, effectively prevent acid-base gas in the air from being infected, and realize the purpose of treating haze from the source by using an energy-saving low-carbon mode.

Description

Method and system for controlling flue gas-related atmospheric acidic particulate matters and controlling haze with low carbon
Technical Field
The invention relates to a method for controlling generation, combination and evolution of flue gas-related atmospheric acidic particulate matters, in particular to an energy-saving micro-emission low-carbon haze treatment method suitable for flue gas pollution control by adopting the method, and an energy-saving micro-emission low-carbon haze treatment system suitable for flue gas pollution control by adopting the method, belonging to the technical field of atmospheric pollution control and environmental protection.
Background
Based on the research and the disclosure of the applicant on the evolution mechanism of the main cause of atmospheric haze and the chemical combination of related pollutants in the current stage of China, the invention overcomes the misunderstanding of people on the main cause of haze pollution and related natural laws for a long time, corrects the long-term technical bias and forms a brand new technical thought and a brand new technical route.
The outbreak of haze is more than four years, the cause is dispute 32429, and at present, the particulate matters causing haze are generally considered as the result of comprehensive direct discharge of the society such as industry, life and the like, and mainly comprise: (1) the coal-fired boiler is shut down for four years in China, so that the total coal consumption is obviously reduced, and the haze pollution condition is not improved as expected; (2) the domestic loose coal is combusted, so that large-scale control of the domestic coal is performed, coal gas change, coal power change and the like are implemented, the domestic coal is basically stopped in the Beijing urban area at present, the quantity of the domestic coal in the suburb is also controlled, and the domestic coal with low quality is banned; (3) the tail gas emission of the automobile is realized, so that a high-pollution fuel automobile is continuously eliminated, the growth amount of the fuel automobile is strictly controlled, the fuel quality is gradually improved from oil country II to country V, and the dust content of the tail gas of the existing fuel automobile is even lower than the dust content in the air in heavy haze weather from the data of multiple actual measurement of the tail gas emission of the automobile; (4) construction dust raising is required, so that the construction site surface is covered, the construction effect is stopped in heavy polluted weather, and the like, but severe haze usually occurs in windless weather, no wind assistance exists, and the dust raising phenomenon is difficult to occur; (5) straw burning: the short-term straw burning in the rural areas only occurs in summer and autumn and is strictly controlled by governments at all levels, and the large-area field straw burning cannot occur due to the fact that the heavy haze frequently occurs in winter and the ground is iced; (6) ammonia water used by agriculture as a chemical fertilizer can form ammonium salt in haze after volatilization, but investigation results show that the ammonia water is not used by farmers 10 years ago when the compound fertilizer is used by the farmers at present; (7) street barbecuing and the like, whereby street barbecuing is strictly limited, there is essentially no street barbecuing in cities, and in the several nines where heavy haze is frequent, few street barbecuing exists even if not strictly controlled.
The generation sources and the processes of the disease and the disease of the haze acid salt particles are sequenced as follows:
(1) chemical reaction of boiler combustion:
C + O2 = CO2
S + O2 = SO2… … etc. of non-condensable gases
(2) The chemical combination reaction of condensable gas and non-condensable gas in the flue:
CO2 + H2O = H2CO3(unstable Carbonic acid)
SO2 + H2O = H2SO3(sulfurous acid)
(3) The processes of desulfurization reaction by a gypsum method and regeneration, absorption and oxidation are as follows:
NaOH + SO2 → Na2SO3 + H2O
Na2SO + SO2 + H2O → NaHSO3
NaHSO3 + Ca(OH)2 → Na2SO3 + CaSO3 ↓ +H2O
Na2SO3 + Ca(OH)2 → NaOH + CaSO3 ↓
(4) chemical reaction of ammonia desulfurization:
NH3 + H2O + SO2 → NH4OH + SO2 → NH4HSO3
(5) denitration function:
（NH4)2SO3 + NO + NO2 →（NH4)2SO4 +N2 ↑
(6) the chemical composition of the boiler flue gas is very complicated, and the acid gas blown out of the wet-type desulfurization tower by the fan comprises H2SO3Sulfurous acid, H2CO3Gas, HNO3Nitric acid, etc. and the alkaline gas (gas) mixed by the fan and blown out of the wet desulfurizing tower comprises NH3Escape of ammonia gas, NaOH and Na2SO3Vapor, and the like.
(7) The acid-base gases (steam) leaving the wet-type desulfurization tower and entering the chimney have strong electrostatic adsorption after being subjected to combustion, chemical combination and electric precipitation, and are bonded together to continuously perform chemical reactions of various complex acid-base neutralization salt-forming micro particles.
In summary, although various air pollution control measures adopted in China have a great effect on reducing direct emission of pollutants on the ground, heavy haze weather is not effectively or completely controlled, and the reason for the situation is that essential or comprehensive understanding of main causes or important influence factors of heavy haze is lacked, and long-term technical prejudice exists, so that an effective method capable of better solving the problem of heavy haze is found by using the natural laws on the basis of correctly knowing the relevant natural laws.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a method for controlling smoke-related atmospheric acidic particulate matters, an energy-saving micro-emission low-carbon haze treatment method suitable for smoke pollution control by adopting the method and an energy-saving micro-emission low-carbon haze treatment system suitable for smoke pollution control by adopting the method, so as to reduce or eliminate an important condition for forming heavy haze from the source, reduce the atmospheric particulate matters and/or non-granular atmospheric pollutants derived from salt by controlling or reducing the reaction of acidic gas components in smoke with alkaline substances directly or indirectly under the participation of water to generate salt, and control or reduce the atmospheric haze pollution related to smoke.
The technical scheme adopted by the invention is as follows: a method for controlling atmosphere acidic particulate matter related to smoke controls or reduces the water content in the smoke so as to control or reduce the reaction of acidic gas components in the smoke and water with alkaline substances directly or indirectly to generate salt, and further reduce the atmosphere particulate matter and/or non-particulate atmosphere pollutants derived from the salt.
Preferably, the flue gas waste heat including the latent heat of vaporization of steam in the flue gas is recycled, the flue is provided with a heat exchange device capable of realizing indirect heat exchange between the flue gas and a low-temperature heat absorbing medium, the low-temperature heat absorbing medium absorbs the flue gas waste heat, the emission temperature of the flue gas is reduced, the water vapor in the flue gas is condensed into liquid water and discharged, and the water content in the flue gas is reduced.
Preferably, the heat exchange device is arranged in front of the flue gas desulfurization device, and a flue gas dust removal device is usually arranged in front of the heat exchange device, according to the dust removal requirement, the flue gas dust removal device can adopt an electrostatic dust collector or a dust removal device combination containing the electrostatic dust collector, or other suitable prior arts, the flue gas desulfurization device adopts any suitable wet type, dry type or semi-dry type desulfurization device, for example, the flue gas desulfurization device adopts a wet type desulfurization tower, the inlet flue gas temperature of the flue gas desulfurization device (such as the wet type desulfurization tower) can be lower than 100 ℃, the evaporation amount of desulfurization water in the wet type desulfurization tower is controlled by reducing the temperature difference of inlet and outlet flue gas of the wet type desulfurization tower, the moisture content of the flue gas is reduced or avoided to be increased due to the desulfurization process, the wet type desulfurization tower adopts constant temperature desulfurization (basically constant temperature) or controls the temperature difference of the inlet and outlet flue gas of the desulfurization tower to, the flue gas temperature in the desulfurization process can be controlled by controlling desulfurization process conditions such as the temperature of desulfurization water (alkaline circulating water) and the like, so that the flue gas temperature meets the corresponding flue gas inlet and outlet temperature control requirements.
The removal rate of the water vapor in the flue gas is preferably not less than 80% by condensation of the heat exchange equipment.
The inlet flue gas temperature of the wet desulfurization tower is preferably about 60-80 ℃.
The temperature of the flue gas at the outlet of the wet desulfurization tower is preferably about 55-80 ℃.
The heat exchange apparatus is preferably adapted to an upper inlet flue gas temperature limit of not less than 140 ℃.
Because the steam in the flue gas entering the wet-type desulfurization tower is in a saturated or nearly saturated state and the temperature of the flue gas is lower than 100 ℃, the steam can react with alkaline substances in the desulfurization water to eliminate acid components such as sulfur dioxide and the like in the process of contacting with the desulfurization water, the temperature and the volume of the flue gas are approximately stable or reduced, the moisture content of the flue gas is also approximately unchanged or even reduced to some extent, and the great increase of the total moisture content of the flue gas caused by wet-method desulfurization is avoided.
Preferably, the flue gas desulfurization equipment adopts a wet desulfurization tower, all or part of condensed water discharged by the heat exchange equipment is treated and then is used as make-up water of the wet desulfurization tower, the treatment of the condensed water comprises removing solid particles or removing solid particles and acidity in the condensed water, can be determined according to the requirements of a water using device of the wet-type desulfurizing tower, can eliminate the acidity of condensed water through the process of adding alkali into the desulfurized water of the wet-type desulfurizing tower, can also eliminate the acidity in the process of treating the condensed water, also reduces the burden of alkali adding equipment of the wet-type desulfurizing tower, according to the requirement of the desulfurization equipment on the temperature of the desulfurization water, when the supplementary water needs to be heated, the supplementary water needing to be heated is used as a heat absorbing medium of the heat exchange equipment to carry out heat exchange through the heat exchange equipment, and is connected to the water using device of the wet desulfurization tower after being heated through the heat exchange equipment.
The invention discloses an energy-saving micro-emission low-carbon haze treatment method suitable for controlling smoke pollution.
The utility model provides a be suitable for energy-conserving low carbon of arranging a little of flue gas pollution control and treat haze system, its sets up the indirect heat exchange equipment that can realize flue gas and low temperature heat-absorbing medium and carry out indirect heat exchange on the flue to low temperature heat-absorbing medium absorbs flue gas heat energy, reduces the exhaust temperature of flue gas, makes the vapor condensation in the flue gas be liquid water and discharge, reduces the water content in the flue gas, with control or reduce in the flue gas acid gas composition directly or indirectly react with alkaline substance under the participation of water and produce the salt.
The outlet flue gas of the heat exchange equipment can be connected into the desulfurization equipment through the flue to be desulfurized, the desulfurization equipment preferably adopts a wet desulfurization tower, the inlet flue gas temperature of the wet desulfurization tower is lower than 100 ℃, and the temperature difference between the inlet flue gas and the outlet flue gas is not more than 5 ℃ or 10 ℃.
Preferably, the heat exchange device adopts multi-stage heat exchange, condensed water generated by the multi-stage heat exchange is led out in a segmented manner, the heat exchange device comprises a shell suitable for being connected with a flue, an air inlet side port of the shell is a shell side medium inlet used for being connected with the air inlet side flue, an air outlet side port is a shell side medium outlet used for being connected with the air outlet side flue, a plurality of heat exchange units which are mutually spaced are distributed in the shell along the axial direction in a segmented manner, a closed tube side medium channel is arranged in a heat exchange part of each heat exchange unit, shell cavities on the front side and the rear side of each heat exchange unit are communicated through the shell side medium channel of the heat exchange unit, the heat exchange device is also provided with a plurality of segmented condensed water discharge pipes, at least one condensed water drainage port (or called as a, the number of the water inlets arranged on the same sectional type condensed water discharge pipe can be one or more), at least one condensed water drainage outlet communicated with the sectional type condensed water discharge pipe is arranged at the back of a heat exchange unit closest to the air outlet side port, any one or more of a hollow pore plate, an annular heat exchange pipe and a plane spiral pipe is adopted as a heat exchange part of the heat exchange unit, four-phase flow distribution including water vapor condensation, dust sedimentation, condensed water leading-out and smoke gas discharge is realized in the heat exchange process, smoke gas containing steam and dust in an air inlet side flue enters the heat exchange equipment from a shell side medium inlet of the heat exchange equipment, and indirectly exchanges heat with a heat absorbing medium in the heat exchange part when passing through the heat exchange unit, and an inertia separation effect and a gravity separation effect are formed in the smoke gas flowing process by means of blocking and area change formed in an inner cavity of the heat exchange, suspended particles including smoke dust are separated from the smoke and settled, steam in the smoke is converted into condensed water due to heat release and is condensed on and/or flows through a deposition area of the suspended particles, dust is mixed with the condensed water and is discharged from a condensed water outlet of the heat exchange equipment, and the condensed and separated smoke is discharged from a shell-side medium outlet of the heat exchange equipment.
Preferably, the condensed water mixed with dust discharged by the heat exchange equipment enters corresponding water treatment equipment to separate the dust in the condensed water, and according to actual needs, the water treatment equipment can adopt the prior art such as an inclined plate sedimentation tank and the like, and can also adopt a combined treatment device with multiple processes such as neutralization, biochemical treatment, flocculation precipitation and the like.
Preferably, the number of the heat exchange elements of the heat exchange unit is one or more, and the shell-side medium channel of the heat exchange unit comprises any one or more of the following components:
1) gaps between the heat exchange pieces and the inner wall of the shell comprise edge notches of the heat exchange pieces in various shapes;
2) the axial through hole arranged on the heat exchange piece comprises various shaped spaces formed by the shape of the heat exchange piece and communicated with the shell cavities on the front side and the rear side of the heat exchange unit;
3) gaps among all parts of the heat exchange piece;
4) when the number of the heat exchanging elements is plural, a gap between the heat exchanging elements, and the like.
Preferably, the heat exchange equipment is vertical or horizontal, a shell of the vertical heat exchange equipment is vertically arranged, a port at the lower end of the shell is an air inlet side port, a port at the upper end of the shell is an air outlet side port, opposite end surfaces of adjacent heat exchange units are mutually parallel inclined planes, and an included angle which is not 90 degrees is formed between the opposite end surfaces and an axis of the shell of the heat exchange equipment, so that inclined equal-thickness gaps among the heat exchange units are formed; the horizontal heat exchange equipment is characterized in that a shell of the horizontal heat exchange equipment is horizontally arranged, a front end port of the shell is an air inlet side port, a rear end port of the shell is an air outlet side port, opposite end faces of adjacent heat exchange units are inclined planes with opposite inclination directions, included angles of 90 degrees are formed between the opposite end faces and the axis of the shell of the heat exchange equipment, the distance between the upper ends of the two end faces is large, the distance between the lower ends of the two end faces is small, a V-shaped gap which is wide at the upper part and narrow at the lower part is formed between the heat exchange units, and the bottom width of.
The heat exchange part of the heat exchange unit can adopt one or a combination of a plurality of forms of any forms suitable for transverse arrangement, such as a hollow pore plate, an annular heat exchange tube, a planar spiral heat exchange tube and the like:
1) the hollow pore plates are transversely arranged (in a direction perpendicular to the axis of the shell or with an included angle larger than 45 degrees), the number of the hollow pore plates in the same heat exchange unit can be generally one, each hollow pore plate is provided with a windward side panel and a leeward side panel, the outer side surfaces of the windward side panel and the leeward side panel respectively form a windward side end surface and a leeward side end surface of the heat exchange unit, through holes which correspond to each other and are connected in a sealing way through a pore plate connecting pipe are arranged on the windward side panel and the leeward side panel, the pore plate connecting pipe is an axial (in a direction parallel to the axis of the shell or with an included angle not larger than 45 degrees) straight pipe and penetrates through the space between the two panels, pore plates of the pore plate connecting pipe form a shell pass medium channel of the hollow pore plates, the inner cavity of the hollow pore plates is used for forming a tube pass medium channel of the hollow pore plates, and the, a partition plate and/or a guide plate can be arranged in the cavity to form a required medium flow channel, so that a medium flows through each part of the cavity, dead angles and short circuits are avoided as much as possible, and the flow velocity of each part meets the requirement as much as possible, and the specific separation or flow guide mode can be according to the prior art;
2) when the number of the annular heat exchange tubes in the same heat exchange unit is one, the outer surfaces of the windward side and the leeward side of the annular heat exchange tubes are both flat surfaces and respectively form the end surface of the windward side and the end surface of the leeward side of the heat exchange unit; when the number of the annular heat exchange tubes in the same heat exchange unit is multiple, the annular heat exchange tubes are concentric and have different sizes and are sequentially distributed at intervals from inside to outside, the windward outer surfaces of the annular heat exchange tubes are positioned on the same plane to jointly form a windward side end face of the heat exchange unit, and the leeward outer surfaces of the annular heat exchange tubes are positioned on the same plane to jointly form a leeward side end face of the heat exchange unit; for example, the heat exchange unit can be a plurality of adjacent annular heat exchange tubes connected in pairs or a plurality of adjacent annular heat exchange tubes connected in pairs which are mutually nested but have intervals between each other, any independent tube side medium channel consisting of a plurality of mutually communicated annular heat exchange tubes is provided with an inlet and an outlet of a heat absorbing medium for connecting and leading out the heat absorbing medium, or each annular heat exchange tube is respectively provided with an independent inlet and an outlet of the heat absorbing medium for directly connecting and leading out the heat absorbing medium without being connected with each other;
3) the spiral heat exchange tubes are transversely arranged and are plane spiral heat exchange tubes or vertical surface spiral heat exchange tubes, the central lines of tube holes of the plane spiral heat exchange tubes are positioned in a plane, the central lines of the tube holes of the vertical surface spiral heat exchange tubes are not positioned in a plane, the tube holes of the spiral heat exchange tubes form tube pass medium channels, the number of the spiral heat exchange tubes in the same heat exchange unit is one or more, when the plane spiral heat exchange tubes are adopted, when the number of the plane spiral heat exchange tubes in the same heat exchange unit is one, the outer surfaces of the windward side and the leeward side of the plane spiral heat exchange tubes are both flat, and the windward side end face and the leeward side end face of the heat exchange unit are respectively formed; when the number of the plane spiral heat exchange tubes in the same heat exchange unit is one, the windward side outer surface and the leeward side outer surface of each vertical face spiral heat exchange tube respectively form the windward side end surface and the leeward side end surface of the heat exchange unit; when the number of the vertical surface spiral heat exchange tubes in the same heat exchange unit is multiple, a space is reserved between partial areas of at least part of the vertical surface spiral heat exchange tubes, the windward side outer surfaces of the vertical surface spiral heat exchange tubes jointly form the windward side end face of the heat exchange unit, and the leeward side outer surfaces of the vertical surface spiral heat exchange tubes jointly form the leeward side end face of the heat exchange unit.
Preferably, the edges of the windward end face and the leeward end face of the heat exchange element are respectively provided with a water retaining weir extending axially, so that a diversion trench with an axial opening is formed on the corresponding end face of the heat exchange element for water collection and diversion of condensed water, the water retaining weir forms the wall of the corresponding diversion trench, the condensed water outlet is arranged at the lowest position of the corresponding diversion trench and is used for accessing the condensed water in the diversion trench, the condensed water outlet is preferably funnel-shaped, the outlet of the sectional condensed water discharge pipe is connected with the conveying inlet of the liquid conveying power device, the liquid conveying power device preferably adopts a multi-stage multi-pipe high-efficiency jet pump, the multi-stage multi-pipe high-efficiency jet pump is used for connecting the pumped medium inlet of the pumped medium channel, and the pumped medium inlet forms the conveying inlet of the liquid conveying power device.
Preferably, the sectional condensed water discharge pipe and the washing water discharge pipe of the heat exchange device are connected to a water treatment device capable of performing solid-liquid separation or solid-liquid separation and acid-base neutralization, a water outlet of the water treatment device is connected to a water using device of the wet desulfurization tower through a condensed water recycling pipeline, the condensed water recycling pipeline can be a main pipe, or a plurality of branch pipes which are parallel to each other are arranged on a partial section of the main pipe, and a pipe pass of the heat exchange device is connected in series on the main pipe or one of the branch pipes of the condensed water recycling pipeline to serve as a heat absorbing medium of the heat exchange device, and is connected to the water using device of the wet desulfurization tower after.
The mechanism and the beneficial effects of the invention are as follows:
firstly, the origin of haze is made a prescription and is prescribed a medicine to the disease, at least, seized an important factor that causes heavy haze weather, the technological measure with low carbon energy-conserving row a little to this kind of factor realizes the haze purpose from the source, chimney steam emission through the steam after the boiler combustion of significantly reducing and the desulfurization denitration a large amount of water spray formation, thereby reduce the chemical reaction volume of the acid gas (vapour) body in the chimney that bonds together, extend and reduce these acid gas again with the alkaline material of desulfurization usefulness and the alkaline material's in the air emergence chemical combination reaction and replacement reaction generate acid salt particulate matter, reduce the formation volume of haze particulate matter in the atmosphere promptly from the source, open up the new road for the haze is controlled.
The low-carbon haze treatment greatly recycles the waste heat of the boiler flue gas, improves the energy saving and emission reduction proposed by the state into energy saving and micro emission, not only reduces the temperature of the flue gas and saves energy, but also more importantly, the energy saving benefit of a large amount of latent heat of vaporization released by water vapor is obvious, belongs to the low-carbon field, recycles the waste heat of the waste gas discharged by the industry in a large amount of air in a contract energy management mode with little or no investment of users, saves energy and improves the efficiency of hot users, reduces the fuel consumption and the production cost, reduces the emission of harmful gases such as carbon dioxide and the like by the boiler, and realizes the.
And thirdly, the problems of acidic corrosion of steam and water in the flue and flue blockage are solved, acidic water generated by cooling the boiler flue cannot be directly discharged out under the negative pressure of the flue device, and the acidic water is discharged out to be environment-friendly and not up to standard, and the zero-emission recycling of sewage is realized through a recycling system with automatic control, condensed water suction pressurization and conveying and up to standard acidic water treatment.
FIG. 7 shows the visual effect of smoke treatment by the present invention and the comparison with the visual effect of smoke treatment by the present invention, wherein the left side shows the chimney emitting steam before the chimney is modified by the present invention to form haze, and the right side shows the chimney micro-exhausting steam after the chimney is modified by the present invention to greatly reduce the emission of haze components.
The heat exchange equipment adopted by the invention is established as special equipment for sectionally separating and flowing out four-phase liquid phase of water vapor, air, condensed water and dust in the device on the basis of a four-phase flow-splitting theory developed successfully by the inventor, and is mainly used for solving the problems of acidic water corrosion and flue blockage under the condition that the temperature of boiler smoke is reduced to below a dew point and steam-liquid phase change is inevitably generated.
Drawings
FIG. 1 is a general flow chart of a boiler smoke energy-saving low-carbon haze treatment system of the invention;
FIG. 2 is a schematic view of the construction of a vertical heat exchange apparatus according to the present invention;
FIG. 3 is a schematic view showing the construction of a horizontal heat exchange apparatus according to the present invention;
FIG. 4 is a schematic diagram of a heat exchange apparatus, a desulfurization tower, and a water treatment apparatus configuration in accordance with the present invention;
FIG. 5 is a schematic diagram of a multi-stage multi-tube jet pump according to the present invention;
FIG. 6 is a graph showing the relationship between desulfurization commissioning rate and haze concentration in the past year in China;
FIG. 7 is a photograph showing a comparison of the flue gas emission according to the treatment effect of the present invention.
Detailed Description
Referring to fig. 1-5, the basic technical route of the present invention is to eliminate the conditions for forming heavy haze from the source, and control or reduce the water content in the flue gas, so as to control or reduce the reaction of the acidic gas components in the flue gas with the alkaline substances directly or indirectly in the presence of water to generate salts, and further reduce the atmospheric particulate matters and/or non-particulate atmospheric pollutants derived from the salts.
Referring to fig. 1, the flow is the general description of the core technology of the invention, and is a general figure of the invention patent application of the mechanism and treatment of the formation of the chemical combination evolution of atmospheric acidic particulate matters, and illustrates that a boiler flue gas energy-saving micro-discharge device (heat exchange equipment) is installed on a flue between a boiler flue gas economizer and a wet desulfurization tower, and a low-temperature heat-absorbing medium required to be heated is used for entering the boiler flue gas energy-saving micro-discharge device to absorb heat to form high-temperature water or heated to form steam and then is sent to heat-using equipment to release heat; the water vapor in the flue gas is cooled into acid water due to heat release and then discharged out of the flue, and then the acid water is recycled after qualified pollution treatment; the smoke energy-saving micro-exhaust device cools smoke from high temperature to low temperature and then enters a wet-type desulfurizing tower, water vapor is cooled by most of the water vapor and discharged out of a flue, the water content entering the wet-type desulfurizing tower can be greatly reduced, the temperature of the smoke is reduced as the temperature of the original smoke entering the wet-type desulfurizing tower is reduced from more than 130 ℃ to less than 80 ℃, the desulfurizing water supplement amount can be greatly reduced to form water-saving resources, the temperature reduction of the wet-type desulfurizing tower is favorable for improving the desulfurizing crystallization effect, the desulfurizing circulating water amount is reduced due to the reduction of the water supplement amount, the resistance of rising emission of the smoke is reduced due to the reduction of the circulating water amount, and the electricity consumption; the water vapor and the desulfurization water supplement amount of the flue are greatly reduced twice, so that the water vapor discharged by the flue gas is reduced by more than 80%, and the large white dragon discharged by the chimney is changed into the small white dragon; because the steam reduces and leads to the chemical combination evolution volume of "acid-base neutralization salifying" in the chimney to reduce more than 70%, the chemical combination evolution volume of "tailing" flue gas at the flue gas discharge chimney reduces more than 70% simultaneously, the most crucial is that the low temperature wet flue gas that is reduced 70% steam under the contrary warm condition of windless atmosphere equals the haze granule physical and chemical combination evolution variable that the atmosphere reduces 70%, detain subaerial direct vent less than 10% particulate matter, it is in fact reducing 60% generation of atmosphere haze particulate matter, it can weaken into light haze with the improvement of low carbon haze technology to reduce heavy haze, light haze becomes blue sky white cloud, reach the purpose that the atmospheric pollution was administered.
The invention discloses a low-carbon haze-treating overall measure which comprises the following steps: the waste steam (flue gas) waste heat of the power plant is recycled in a closed way by arranging heat exchange equipment in a flue, and the waste steam (flue gas) waste heat can also be conveyed to a nearby city by matching with a heat pump technology and temperature raising and pressure increasing, so that 'zero urban energy consumption' is realized; after steam power plant's waste steam heat source and city cold source match, replace the original boiler in urban area and the heat supply mode of steam heat transfer with a large amount of power plant's used heat, not only do not increase the energy consumption, stop urban area heating boiler moreover and reduce the boiler combustion of steam power plant and discharge and pollute, hold many, with the haze square of treating of low carbon measure, can drive national low carbon city and to haze propaganda and fight, the haze is treated to the low carbon and is realized the five antithetical couplets of steam power plant and supply the increment: firstly, the boiler supplies more steam or generates more power, secondly, the steam turbine extracts more steam to expand the demand of industrial production, thirdly, the heat consumption in winter in urban areas is reduced or zero energy consumption is realized, fourthly, the lithium bromide refrigeration in summer is reduced or zero energy consumption is realized, and fifthly, the energy consumption in four seasons for bathing in hotel hospitals and residents in urban areas is reduced or zero energy consumption is realized.
The scientific research conclusion of the invention is as follows: the low-carbon haze treatment technology is a new low-carbon haze treatment way which is characterized by exploring a 'waste steam and waste steam of a power plant' for a low-carbon city, realizing 'zero energy consumption of the city' and having Chinese characteristics.
Referring to fig. 2 and 3, the present invention provides a more efficient heat exchange apparatus, preferably a boiler flue gas energy-saving micro-exhaust device, comprising a housing 1, the housing is provided with an inlet side port 10 and an outlet side port 2, the inlet side port 10 of the housing is used for connecting an inlet side flue, the outlet side port 2 is used for connecting an outlet side flue, a plurality of sets of heat exchange units 4 are arranged in the housing in a segmented manner, the space (including the gaps and through holes on the heat exchange members or between the heat exchange members) not occupied by the hollow pore plates or the heat exchange tubes 4 in the housing forms a shell side medium channel 3 of the heat exchange unit, the medium channels or the tube holes of the heat exchange tubes in the hollow pore plates form a heat absorbing medium channel 5, a heat absorbing medium (generally water) input pipeline 6 and a heat absorbing medium output pipeline 9 are respectively connected with a heat absorbing medium inlet and a heat absorbing medium outlet of the heat exchange unit 4, the bottom of casing is provided with acid comdenstion water discharge pipe 7, sets up water collection funnel 8 at the import department of comdenstion water discharge pipe, water collection funnel can be for comdenstion water discharge pipe import department to be the structure of leaking hopper-shaped, lays the water distribution pipeline 15 that is used for the inside washing/washing of heat exchanger, sets up regularly to wash on water distribution pipeline 15 and rotates control flap 14 and rotatory nozzle 12 by turns, and is adjacent interval 16 between the heat exchange unit 4 is the slant form or "V" shape, constitutes to wash and overhauls the space (the vertical slant interval that adopts the uniform thickness, horizontal adoption "V" shape interval).
After the heat exchange units are arranged in the cavity of the shell, various sizes or size proportion designs can be carried out according to factors which need to be considered in an important way, such as resistance, heat exchange capacity, condensed water collecting effect and the like, for example, when enough gravity sedimentation needs to be formed in the cavity between the heat exchange units, the smoke speed is reduced to a required degree, the proportion between the shell side medium channel area and the total cross-sectional area of the inner cavity of the shell in the heat exchange unit is mainly determined by the proportion of the cross-sectional area of the cavity of the shell occupied by the heat exchange piece contained in the heat exchange unit, and the proportion can be set to be 5050-70% and other appropriate ranges, such as 50%, 60% and 70%, so as to comprehensively balance the volume of equipment, the resistance, the gravity sedimentation effect and.
High-temperature flue gas (gas) of the boiler dispersedly enters two or a plurality of sections of flue gas channels 3 through an air inlet side port 10, the flue gas channels 3 in adjacent sections are arranged in a positive or staggered way, the flue gas (gas) after heat release is collected and discharged through an air outlet side port 2, and then enters desulfurization equipment, a flue gas heat exchanger (GGH) or a chimney and the like according to system design.
When the boiler smoke energy-saving micro-exhaust device is arranged on the vertical flue, the vertical boiler smoke energy-saving micro-exhaust device is adopted, because of the sectional heat exchange, the entering cold water is ensured not to directly fall to the bottom due to heavier specific gravity, the sectional heat exchange process of the cold and heat corresponding exchange is gradually completed in sequence instead of single mixed exchange, the lower part of the vertical shell is provided with a water receiving plate 11, the water receiving plate 11 is provided with a through hole 18 for forming a flue gas channel and a water receiving plate water retaining weir for receiving water, a water collecting funnel is arranged at the water outlet side of the water receiving plate water retaining weir, the water receiving plate 11 is set aiming at the falling position of the condensed water of the upper heat exchange tube, the through holes are preferably staggered with the shell pass channel left in the heat exchange unit as much as possible, so that the primary deflection and reversing of the smoke are increased, and particularly, the acidic water can be prevented from falling into the flue 10.
When the boiler flue gas energy-saving micro-exhaust device is installed on a horizontal flue, the horizontal boiler flue gas energy-saving micro-exhaust device is adopted, a communicating pipeline between two adjacent groups of heat exchange tube passes is formed between two adjacent groups of hollow pore plates or heat exchange tubes and comprises an upper communicating pipeline 13 and a lower communicating pipeline 17, namely, an upper communicating pipeline 13 which is positioned above the heat exchange units and is communicated with the tops of the two heat exchange units and a lower communicating pipeline 17 which is positioned below the heat exchange units and is communicated with the bottoms of the two heat exchange units are arranged between the adjacent heat exchange units, the upper communicating pipeline 13 can be used for liquid phase flow of heat absorption media, more importantly, steam (gas) phase flow to eliminate steam resistance, the lower communicating pipeline 17 can be used for liquid phase flow of the heat absorption media, and the sectional heating mode is favorable for eliminating steam resistance and water resistance in heat exchange.
In the process of heat release of the waste heat of the boiler flue gas, water vapor contained in the flue gas is cooled into liquid water through multi-section heat exchange of a heat exchange tube pass formed by each heat exchange unit, so that the acidic water mixed with smoke dust is prevented from blocking and corroding and damaging a flue or a chimney, the acidic water in the flue or the chimney needs to be discharged outside the device as soon as possible, because the flue or the chimney of the boiler is influenced by the suction force of an induced draft fan and the ascending air flow attraction of a high chimney, negative pressure is generally generated in heat exchange equipment, the flue and the chimney and is lower than the atmospheric pressure, and acidic condensed water in the flue or the chimney is not discharged due to the gravity alone, the front end surface and/or the rear end surface of each hollow pore plate or heat exchange tube 4 are obliquely arranged and provided with a water retaining weir 19 higher than the end surface, the water retaining weir 19 is arranged around the flue gas channel 3 to collect and guide the condensed water, so as, the guiding gutter that makes the comdenstion water can enclose along the manger plate weir flows downwards under self action of gravity, collects and through the discharge tube drainage through corresponding water-collecting funnel, when the negative pressure is great in the flue, can be equipped with the pump on the comdenstion water discharge tube to overcome the negative pressure effect in the flue.
The water retaining weirs 19 at the same end face position can be mutually communicated or separated, according to the structure of a specific heat exchange member, the water retaining weirs are used as side walls to form a diversion trench together with the end faces of the hollow pore plates or the heat exchange tubes 4, the lowest part of the diversion trench is a water outlet side and is provided with a water collecting funnel 8, each water collecting funnel 8 is communicated with a condensed water drainage branch pipe, each condensed water drainage branch pipe is communicated with a condensed water discharge pipeline 7, acid condensed water centrally flows to the water collecting funnel 8 through the end faces of the hollow pore plates or the heat exchange tubes 4 and passes through the condensed water discharge pipeline 7, the acid water is timely discharged from the device and is subjected to necessary acid water treatment, and water vapor condensation and condensed water leading-out.
The rotary spray head is additionally arranged at a relatively high point of a sectional inclined or V-shaped structural area (inclined equal-thickness interval or V-shaped interval between adjacent heat exchange units) 16 of the boiler flue gas energy-saving micro-exhaust device, dust deposition and discharge in flue gas are realized by periodically rotating and automatically washing dust and haze scaling in a V-shaped space, and due to the fact that the rotary spray head is resistant to acid corrosion, uniform dirt cleaning can be performed on each hollow pore plate and each heat exchange pipe by using a specific dilute sulfuric acid solution periodically as required, and safe and reliable operation of the rotary spray head is guaranteed.
Referring to fig. 4, the boiler flue gas energy-saving micro-discharge device is provided with a condensate water recovery device and a condensate water treatment device (water treatment device). The condensate water recovery device comprises a multi-stage multi-pipe jet pump 35 and a condensate water recovery tank 36, circulating water of the condensate water recovery tank is used as power jet, a motor-driven water pump (generally, a high-pressure pump) 38 is arranged on a circulating water jet pipeline 37, acid condensate water of the boiler smoke energy-saving micro-discharging device is sucked out under the action of the multi-stage multi-pipe jet pump 35 and flows into the condensate water recovery tank 36 along with jet, the water pump 38 can be arranged on a water outlet pipe of the condensate water recovery tank, the water outlet pipeline of the water pump 38 is divided into two paths, one path of the acid condensate water enters the multi-stage multi-pipe jet pump 35 through the circulating water jet pipeline 37 to serve as jet media, the acid condensate water in the boiler smoke energy-saving micro-discharging device is sucked out under negative pressure, and the other path of the acid.
Referring to fig. 5, the multi-stage multi-tube jet pump may include a first taper section 358, a second taper section 359, and a third taper section 355, the axes of which are located on the same straight line, and the smaller ends of which are located backward, the larger ends of which are located forward, the first taper section is located behind the second taper section, the front end of which extends into the second taper section with an annular gap therebetween, the second taper section is located behind the third taper section, the front end of which extends into the third taper section with an annular gap therebetween, the inner hole of the first taper section forms a primary jet medium passage, the annular gap between the second taper section and the first taper section forms a pumped medium passage, and the annular gap between the third taper section and the second taper section forms a secondary jet medium passage, the front end of the third conical pipe section is connected with a gradually expanding pipe section 356, the front port of the gradually expanding pipe section forms the outlet of the jet pump and is provided with a corresponding connecting flange, the rear part of the pump body is provided with a jet inlet pipe section 351, the side surface of the pump body is provided with a suction inlet pipe section 353, the inlet sides of the primary jet medium channel and the secondary jet medium channel are both connected with the jet inlet pipe section, the rear port of the jet inlet pipe section forms the jet inlet of the jet pump, the jet inlet is the inlet of the primary jet medium channel and the inlet of the secondary jet medium channel and is provided with a corresponding connecting flange, the inlet side of the sucked medium channel is connected with the suction inlet pipe section, the outer port of the suction inlet pipe section forms the sucked medium inlet and is provided with a corresponding connecting flange.
The rear end of the first conical pipe section can be connected with a primary jet medium conveying pipe section 352 which is integrally connected with the primary jet medium conveying pipe section, and the jet inlet pipe section is positioned behind the primary jet medium conveying pipe section and integrally connected with the primary jet input pipe section, so that the connection between the inlet side of the primary jet medium channel and the jet inlet pipe section is realized.
The rear end of the second conical section can be connected with a pumped medium conveying pipe section 354 which is connected with the pumped medium conveying pipe section into a whole, the pumped medium conveying pipe section is sleeved outside the primary jet medium conveying pipe section, an annular gap is reserved between the pumped medium conveying pipe section and the primary jet medium conveying pipe section, the rear end of the pumped medium conveying pipe section is provided with a sealing connection end plate used for sealing the primary jet medium conveying pipe section, and the inner end of the pumping inlet pipe section is connected to the pumped medium conveying pipe section, so that the connection between the inlet side of the pumped medium receiving channel and the pumping inlet pipe section is realized.
A jet flow connecting pipe 7 can be arranged between the third conical pipe section and the jet flow inlet pipe section, the rear end of the third conical pipe section is provided with a sealing connecting pipe section which is used for being connected with the second conical pipe section and the pumped medium conveying pipe section into an integrated structure for sealing, the jet flow connecting pipe is positioned outside the pumped medium conveying pipe section, and the outlet end of the jet flow connecting pipe is connected to the sealing connecting pipe section, so that the connection between the inlet side of the secondary jet flow medium channel and the jet flow inlet pipe section is realized, and the jet flow medium of the inlet pipe section is introduced into the secondary jet flow medium inlet to form secondary jet flow.
Generally, the same jet flow equipment is not suitable for selecting multiple pressure media on the whole, and the high-pressure medium selects one pressure more simply and conveniently, so a jet flow communicating pipe is additionally arranged between the primary jet flow body and the secondary jet flow body, the integral structure is simplified on the premise of ensuring the functions, a shutdown or regulating valve can be additionally arranged on the pipeline, and the multi-requirements of the change of the pressure at the tail end of the outlet of the multi-stage multi-pipe jet flow pump under various conditions are met.
The sealing connection pipe section may be a circular pipe having the same diameter as the pumped medium conveying pipe section, and may be a circular pipe integrally connected to the pumped medium conveying pipe section, and thus, the sealing connection pipe section may also be regarded as a forward extending portion of the pumped medium conveying pipe section beyond the second taper section.
Preferably, the orifice of the second cone section is located behind the orifice of the third cone section, and the diameter of the orifice of the second cone section is preferably smaller than that of the orifice of the third cone section, so that the flow of each part of the medium is better organized, and the suction and mixing effect is improved.
Preferably, the jet flow inlet pipe section is coaxial with the primary jet flow medium conveying pipe section, the diameter of the jet flow inlet pipe section is larger than that of the primary jet flow medium conveying pipe section, and the inlet end of the jet flow connecting pipe is connected to the side wall of the jet flow inlet pipe section, so that the structure is optimized, and the resistance is reduced.
The first conical pipe section, the second conical pipe section and the third conical pipe section can be in a regular cone shape with pipe orifices at the front ends, and the main body part of the primary jet flow conveying pipe section and the main body part of the pumped medium conveying pipe section are in a circular pipe shape.
Preferably, the mouth of the first cone segment and/or the mouth of the second cone segment may adopt a toothed structure, such as a slotted toothed structure, a toothed structure, and the like, and the mouth of the toothed structure of the first cone segment and/or the second cone segment is preferably provided with partially inwardly inclined inner teeth and/or partially outwardly inclined outer teeth, the inner inclined teeth are preferably distributed at intervals with other teeth (such as the outer inclined teeth and/or the teeth which are not inwardly and outwardly inclined), the outer inclined teeth are preferably distributed at intervals with other teeth (such as the inner inclined teeth and/or the teeth which are not inwardly and outwardly inclined), and the toothed structure may also adopt a crossed inclined toothed structure.
The nozzle of the first cone segment and/or the nozzle of the second cone segment may be provided with partially inwardly inclined teeth and/or partially outwardly inclined teeth, the inwardly inclined teeth being preferably spaced apart from other teeth (e.g., outwardly inclined teeth and/or teeth that are not inwardly and outwardly inclined), and the outwardly inclined teeth being preferably spaced apart from other teeth (e.g., inwardly inclined teeth and/or teeth that are not inwardly and outwardly inclined).
Preferably, the tooth structure can also adopt a crossed oblique tooth structure.
Through the design of the pipe orifice tooth form, the internal and external contact area of a jet cone formed by jet flow is increased, the mixed friction thrust is improved, the kinetic energy self consumption of high-pressure jet flow is reduced, the suction force and the pressurization efficiency of a jet pump can be improved, and the contact area and the friction thrust between a jet flow medium and a suction medium are enlarged.
The mouth of the third conic section may be provided with a diversion mixing weir, the diversion mixing weir may be an inward annular protrusion with a convex-concave structure at the inner edge, may be an annular protrusion with saw teeth or groove teeth protruding radially inwards or an annular protrusion with a wavy edge, or other similar structures with convex-concave edges, and the number of teeth (or protrusions with other shapes) on the diversion weir preferably corresponds to the position of the teeth on the mouth of the second conic section.
Because the setting of water conservancy diversion mixes the weir, this medium "picks up" under the inertia effect and is directly or indirectly sneaked into in the pumped medium cone, the fluidic medium of whole circumference body mixes with pumped medium "dog tooth form", cross area of contact and frictional thrust have obtained promoting greatly, have played the cross mixed suction effect to pumped medium, make its suction force big, it is effectual to suck, set up the orderly cross water conservancy diversion of range and mix the weir in the front and back, cooperate with the mouth of pipe tooth form of first, second taper pipe section, form the cascaded pressure raising effect again, can further satisfy the requirement that more efficient medium was carried.
The multi-stage multi-pipe jet pump pumps sectional condensate water formed by heat exchange in a high-pressure jet and internal and external cross mixed suction mode, the internal and external contact area of the condensate water of a pumped medium is increased in a stepped manner, and the complex mixed jet obviously improves the pressure of the medium at the outlet of the jet device. Meanwhile, as the outlet of the jet flow pipeline is additionally provided with the crossed oblique tooth-shaped structure, the contact area of the jet flow medium and the pumped medium is enlarged, and the working efficiency of the jet flow pump is improved; because the outlet of the pumped pipeline is additionally provided with the crossed oblique tooth-shaped structure, the contact area between the pumped medium and the jet medium is increased, and the jet efficiency is improved again; and because the crossed oblique tooth-shaped structure additionally arranged at the outlet of the jet flow pipeline is matched with the tooth-shaped structure additionally arranged at the outlet of the suction pipeline, the curved surface area contact of the jet flow medium and the sucked medium is increased in an occlusion mode by the wavy circumferential curve, and the jet flow efficiency is further improved or the jet flow energy consumption is reduced. Cascaded multistage multitube efflux, compensate by the velocity of flow loss in pipeline or the pump body of the mixture of suction medium or by suction medium and efflux medium, inside and outside alternately slant mixed efflux improves the suction capacity of jet pump and by the suction volume of suction medium by a wide margin, satisfy the medium transport requirement of higher efficiency, and the utility model discloses can form high enough output pressure, especially when the suction medium is exhaust steam, because convert into liquid after mixing the pressurization with the efflux medium, the volume obviously reduces, the volume and the velocity of flow of mixed medium have been reduced from this, adopt the mode of the multistage multitube high-efficient efflux of this application, mend efflux medium constantly, be favorable to reducing the velocity of flow that reduces to bring because of the exhaust steam condenses, cascaded multistage alternately slant mended efflux more makes the medium momentum in the jet pump increase step by step, be favorable to improving the medium flow state in the jet pump, the utilization effect of power is improved, so that the suction capacity is improved, and the output pressure is ensured. In addition, the stepped crossed oblique mixed jet flow is subjected to internal and external layering of a sucked medium and multistage complementary jet flow for increasing the area of a contact curve, so that the momentum of the medium in the jet pump is further increased, the medium flowing state in the jet pump is improved again, and the utilization effect of power is improved, so that the suction capacity of the stepped crossed oblique mixed jet flow is improved, and the output pressure is ensured and increased. Applicant's repeated experiments, adopt the utility model discloses a high-efficient jet pump of multistage multitube, require under the same condition at output pressure and suction volume isoparametric, can reduce the pressure head of jet pump by a wide margin, reduce power consumption about more than 50%, the cascaded alternately slant mixed jet of high-efficient jet pump of multistage multitube, the lifting surface area of contact friction thrust is enlarged to the interior outer floor of pumped medium abundant contact and nozzle dentate structure, make full use of jet medium's pressure and velocity of flow, be favorable to reducing mixed torrent and smooth power, improve suction force and suction effect, require the large tracts of land to reduce industry waste steam waste heat discharge by a wide margin to environmental protection and have the efficiency of subducing energy waste and environmental pollution.
The water pump 38 of the condensed water recovery tank 36 pressurizes and conveys the condensed water, the automatic control system of the condensed water recovery tank 36 automatically adjusts the control valve 39 on the conveying pipeline according to the water volume, the stable pressure and the specific liquid level in the condensed water recovery tank 36 are maintained, the jet flow function is ensured, and the condensed water is conveyed into the condensed water treatment equipment by the water pump under the constant pressure.
Preferably, water treatment facilities is including catchment regulating box 40, neutralization box 41, biochemical reaction case 42, flocculation reaction case 43, settling tank 47, water quality testing case 48 and the play water regulating box 49 that establish ties in proper order, catchment regulating box 49 is equipped with water control door 51, neutralization box 41 is equipped with lime breast and puts in pipeline 45, flocculation reaction case 43 is equipped with flocculating agent and puts in pipeline 46, organic flocculating agent PAM and inorganic flocculating agent PAC are chooseed for use to the flocculating agent, play water regulating box 49 is equipped with outlet conduit 44.
Through the water yield control valve regulation gets into catchment regulating box 40's water yield and gets into neutralization box 41, throw in pipeline 45 through the lime breast and throw in the lime breast and carry out acid-base neutralization treatment back into neutralization box 41, send into biochemical reaction case 42 that is equipped with special environmental detection instrument, then choose for use organic flocculant PAM to clear away aquatic suspended particles and inorganic flocculant PAC and carry out the stable sediment with the particulate matter, the flocculating agent is thrown in pipeline 46 through the flocculating agent and is got into flocculating agent reaction case 43 to get into settling tank 47, water quality testing case 48 and play water regulating box 49 in proper order, handle qualified neutral water and send the cyclic utilization outward through outlet conduit 44.
Preferably, the automatic control system comprises a plurality of automatic control valves and pipelines, at least comprising an equalizing regulating valve 32, a heat absorbing medium outlet regulating valve 33, an acid condensate conveying control valve 39, a self-cleaning circulation control valve 50 and a water treatment pipeline control valve 14.
The regulating valve 32 of the heat absorbing medium inlet pipeline 31 of the boiler flue gas energy-saving micro-exhaust device controls the opening degree of the valve 32 according to the set temperature of the flue gas emission outlet 2, so as to ensure the specific temperature and heat of the flue gas entering the desulfurizing tower; the temperature or pressure of the water or steam required by the heat consumer is adjusted by the control valve 33 on the heat absorbing medium outlet pipeline 34 to meet the requirement of the production heating system; the automatic cleaning function of the dust haze scaling inside the boiler smoke energy-saving micro-exhaust device is that a control valve 50 on a circulating flushing pipeline is automatically opened and a water quantity control valve 51 on a water treatment pipeline is automatically closed according to a cleaning instruction which is observed by a detection hole on the device or is sent by a detection instrument to the detection data of the dust haze, and the automatic cleaning function is automatically switched back to an original system after being cleaned regularly.
The flue gas (steam) heat energy of the boiler flue gas energy-saving micro-discharge device is gradually discharged by a sectional type sequence, the flue gas (steam) originally is water vapor of high-temperature three-phase flow, air and dust, the water vapor of the four-phase flow is changed into through heat exchange, cooling, air, dust and condensate water, wherein the condensate water is discharged out of the flue gas energy-saving micro-discharge device by sectional diversion, the water vapor of the four-phase flow in the device, air, dust and condensate water are changed into a small amount of water vapor of the low-temperature three-phase flow at an outlet, air and a small amount of dust, because the water vapor can bring out a flue together with the dust in a certain proportion when condensing, under the air suction effect of an induced draft fan and a chimney, the low-temperature three-phase flow passes through a flue gas pipeline and enters a.
Because the water quality after the boiler flue gas cooling belongs to acidity and has extremely strong corrosiveness, acid-resistant corrosive materials are needed to be selected as structural materials which are directly contacted with the flue gas and the acidic condensate water in the boiler flue gas energy-saving micro-emission device, and most of the materials are corrosion-resistant materials such as titanium alloy, titanium alloy lining, stainless steel such as 316 or 304 and special acid-resistant stainless steel such as 445J2, and comprise acidic water discharge pipelines 7, 8, 12 and the like.
The invention researches a chemical combination evolution process after boiler flue gas desulfurization, wherein the origin of haze is caused by chemical reaction caused by a large amount of water spraying and cooling of boiler flue gas with negative charges and adsorption force in a wet desulfurization tower, and the chemical combination evolution process of haze is divided into three stages:
1. amount of evolution of acid-base combination in chimney
The first stage is generated in the chimney after desulfurization, the PM2.5 is increased by more than about 100% through a chemical combination reaction and a replacement reaction of acid-base neutralization and salt formation, and chimney condensate water observed by eyes is in a black state. In addition, according to experimental research on the influence of wet desulphurization on PM2.5 emission of a 660MW coal powder furnace, which is performed by scientific researchers such as Hua-Electricity academy of sciences and Ha-Gong university in 2015, the discovery shows that ultrafine particles discharged into the atmosphere are 2 times of that discharged from a boiler outlet without dust removal equipment and 458 times of that discharged from a dust removal equipment, and the strange phenomenon that the dust content of desulfurized gas in many power plants is larger than that before desulphurization after being diluted by a large amount of water is solved.
2. The acid-base combination of the flue gas is changed into 'Dabailong'
The second stage is a chemical combination reaction and a displacement reaction which are generated in a large bailong or a double bailong at the outlet of the chimney, on one hand, the chemical combination evolution of the original acid-base gas is generated, on the other hand, the acid-base gas is discharged to form two rotating airflow which generates adsorption chemical combination and displacement reaction with the acid-base gas in the air, and more than 500% of PM2.5 particulate matters are increased, and the research result finds out the reason of the tail of the flue gas after desulfurization.
3. Acid-base combination evolution into heavy haze in calm weather
In the third stage, acid-base gas combination and replacement reaction can be rapidly carried out on various acidic gases such as sulfate radicals and chloride ions in calm weather and various alkaline gases such as calcium ions or ammonium ions generated by desulfurization in the air, and PM2.5 particles which are about 500 times more than the acidic gases are increased.
According to the existing ground emission condition, the generation amount of the first and second-stage particulate matters is far less than the dust haze emission amount in 2012, and the key of heavy haze outbreak is that the third-stage chemical combination evolution is a static and stable day and becomes a geometric growth pollution source.
The specific test results of the invention are as follows:
1) three factors of heavy haze outbreak are provided: firstly, a low-temperature wet flue gas is required to have a discharge pollution source with a catalytic effect, secondly, breeze meteorological conditions below third-level wind are adopted, thirdly, the atmospheric inverse temperature, namely the high-altitude temperature is higher than or close to the ground temperature, the convection expansion condition of the high-altitude ground temperature to the atmospheric low temperature is eliminated, and the capability of dust haze to diffuse to the high altitude is lost;
2) only the low-temperature wet flue gas stuck together is discharged into the atmosphere, and the low-temperature wet flue gas quickly infects H which is discharged into the atmosphere at high temperature, such as automobile exhaust and the like, under the condition of windless atmosphere inverse temperature2O、CO2When the gas is cleaned, the gas is rapidly changed into complex acid salt particles, and heavy haze can be generated from the day to the day;
3) the heavy haze is difficult to remove after explosion, the air specific gravity is increased when the heavy haze is exploded for a long time and floats in the atmosphere, the larger the air specific gravity in the area is, the more external wind power can be reduced or blocked, and the national wind power is weakened in recent years;
4) the ultra-clean emission and the smoke tower integration have no effect on haze treatment, the source of heavy haze particles is not particles directly emitted, the coal-fired boiler emits water and gas in a ratio of 1:8, which shows that only 1/8 non-condensable gas can participate in chemical reaction, the smoke tower integration structure integrates and evolves lacking water vapor in a cooling tower, the complete complement is realized in the cooling tower, the pollution source of the haze is increased, and the haze treatment effect of the smoke tower integration environment-friendly power plant is just opposite to the haze treatment effect;
5) the haze is mostly generated from 10 months to 3 months in the coming year because the air temperature after 10 months is continuously reduced and the air temperature is extremely low in winter, so that the phenomenon of atmospheric temperature inversion is easily caused, and in addition, the emission of low-temperature wet flue gas in winter heating is increased, and in addition, the wet flue gas at low temperature is more favorable for the condensation and gathering of acid and alkali gases, and the chemical combination evolution condition is more sufficient.
The invention can change waste steam of the power plant boiler into valuable, and has the following specific effects:
1. energy conservation:
the low-carbon haze treatment project is put into operation, so that the energy-saving benefit or the power generation benefit is remarkably increased;
2. the desulfurization comprehensive benefits of the boiler flue gas system optimization are as follows:
saving water: the wet-type desulfurizing tower greatly reduces the water consumption,
secondly, power saving: reduces the power consumption of the induced draft fan and the circulating pump,
saving resources: the low-carbon haze treatment technology is applied, so that the investment of a wet desulfurization tower and the environment-friendly operation cost can be greatly reduced;
3. the low-carbon haze-controlling environmental protection value of enterprises is as follows:
firstly, the discharge capacity of the dust haze of the flue gas of the boiler is reduced by 40-60%,
reducing the low-temperature wet flue gas discharge of the boiler by 40-60%,
and reducing the acid salt particles in the atmosphere caused by low-temperature wet flue gas emission by 30-50%.
The above embodiments only express a certain specific embodiment of the present invention, and the description is specific and detailed, but it should not be understood that the invention is limited to the claims, and all equivalent structures made by the content of the present specification, or other related technical fields, which are directly or indirectly applied, are included in the scope of the present invention.
The technical means disclosed by the invention can be combined arbitrarily to form a plurality of different technical schemes except for special description and the further limitation that one technical means is another technical means.

Claims (7)

1. A method for controlling the atmosphere acidic particulate matter related to flue gas is characterized in that the water content in the flue gas is controlled or reduced, so that the acidic gas component in the flue gas is controlled or reduced to directly or indirectly react with alkaline substances to generate salt under the participation of water, further, the atmosphere particulate matter and/or non-particulate atmosphere pollutants derived from the salt are reduced, the flue gas waste heat including steam vaporization latent heat in the flue gas is recycled, heat exchange equipment capable of realizing indirect heat exchange between the flue gas and a low-temperature heat absorption medium is arranged on a flue, the low-temperature heat absorption medium absorbs the flue gas waste heat, the emission temperature of the flue gas is reduced, the water vapor in the flue gas is condensed into liquid water and is discharged, the water content in the flue gas is reduced, the heat exchange equipment is arranged behind a flue gas dust collector and in front of a flue gas desulfurization equipment, the flue gas dust collection equipment adopts an electrostatic dust collector or a dust collection, the flue gas desulfurization equipment adopts a wet desulfurization tower, the condensed water discharged by the heat exchange equipment is completely or partially used as make-up water of the wet desulfurization tower after being treated, the control flue gas temperature in the desulfurization process is controlled by controlling desulfurization process conditions, so that the control flue gas temperature meets the control requirement of the temperature of a corresponding flue gas inlet and outlet, the control desulfurization process conditions comprise the control of the temperature of the desulfurization water, the evaporation capacity of the desulfurization water in the wet desulfurization tower is controlled by reducing the temperature difference of the flue gas at the inlet and outlet of the wet desulfurization tower, the moisture content of the flue gas increased by the desulfurization process is reduced or avoided, the steam in the flue gas entering the wet desulfurization tower is in a saturated or near saturated state, the flue gas temperature is lower than 100 ℃, and in the process of contacting with the desulfurization water, the steam can react with alkaline substances in the desulfurization water to eliminate acidic components of sulfur dioxide, and the, the moisture content of the flue gas is also approximately unchanged and even reduced to some extent, thereby avoiding the great increase of the total moisture content of the flue gas caused by wet desulphurization,
the heat exchange equipment adopts multi-section heat exchange, condensed water generated by the multi-section heat exchange is led out in a sectional manner, the heat exchange equipment comprises a shell suitable for being connected into a flue, an air inlet side port of the shell is a shell side medium inlet and is used for being connected with the air inlet side flue, an air outlet side port is a shell side medium outlet and is used for being connected with the air outlet side flue, a plurality of heat exchange units which are mutually spaced are distributed in the shell along the axial direction in a sectional manner, a closed tube side medium channel is arranged in a heat exchange part of each heat exchange unit, shell cavities on the front side and the rear side of each heat exchange unit are communicated through the shell side medium channels of the heat exchange units, the heat exchange equipment is also provided with a plurality of sectional condensed water discharge pipes, at least one condensed water drainage port communicated with the sectional condensed water discharge pipes is arranged between any two, the heat exchange part of the heat exchange unit adopts any one or more of a hollow pore plate, an annular heat exchange tube and a plane spiral tube, four-phase flow distribution including water vapor condensation, dust sedimentation, condensed water leading-out and smoke discharge is realized in the heat exchange process, smoke containing steam and dust in a smoke channel at the air inlet side enters the heat exchange equipment from a shell side medium inlet of the heat exchange equipment, indirectly exchanges heat with a heat absorbing medium in the heat exchange part when passing through the heat exchange unit, an inertia separation and gravity separation effect is formed in the smoke flowing process by means of blocking and area change formed in an inner cavity of a shell of the heat exchange unit, suspended particulate matters including smoke and dust are separated and settled from the smoke, the steam in the smoke is converted into condensed water due to heat release and is condensed in a deposition area of the suspended particulate matters, and the dust is mixed with the condensed water and discharged from a condensed water outlet of the, the condensed and separated flue gas is discharged from a shell side medium outlet of the heat exchange equipment,
the heat exchange equipment is vertical or horizontal, a shell of the vertical heat exchange equipment is vertically arranged, a port at the lower end of the shell is an air inlet side port, a port at the upper end of the shell is an air outlet side port, opposite end surfaces of adjacent heat exchange units are mutually parallel inclined planes, and an included angle which is not 90 degrees is formed between the opposite end surfaces and the axis of the shell of the heat exchange equipment, so that inclined equal-thickness gaps among the heat exchange units are formed; the horizontal heat exchange equipment is characterized in that a shell of the horizontal heat exchange equipment is horizontally arranged, a front end port of the shell is an air inlet side port, a rear end port of the shell is an air outlet side port, opposite end faces of adjacent heat exchange units are inclined planes with opposite inclination directions, an included angle of not 90 degrees is formed between the front end port and the axis of the shell of the heat exchange equipment, the distance between the upper ends of the two end faces is large, the distance between the lower ends of the two end faces is small, so that a V-shaped gap with a wide upper part and a narrow lower part is formed between the heat exchange units, the width of the bottom end of the V-shaped gap is not zero, water retaining weirs axially extending out are arranged on the edges of the windward side end face and the leeward side end face of the heat exchange piece, so that a diversion groove with an axial opening is formed on the end face of the heat exchange piece and is used for collecting and diverting condensed water, the water is, the outlet of the sectional condensate water discharge pipe is connected with the conveying inlet of a liquid conveying power device, the liquid conveying power device adopts a multi-stage multi-pipe high-efficiency jet pump, and the multi-stage multi-pipe high-efficiency jet pump is connected with a pumped medium inlet of a pumped medium channel to form the conveying inlet of the multi-stage multi-pipe high-efficiency jet pump.
2. The method of claim 1, wherein the wet desulfurization tower adopts constant temperature desulfurization or controls the temperature difference of the flue gas at the inlet and outlet of the desulfurization tower to be not higher than 5 ℃, the removal rate of the water vapor in the flue gas is not less than 80% by condensation of the heat exchange equipment, the inlet flue gas temperature of the wet desulfurization tower is 60-80 ℃, the outlet flue gas temperature of the wet desulfurization tower is 55-80 ℃, and the upper limit of the inlet flue gas temperature adapted by the heat exchange equipment is not lower than 140 ℃.
3. The method as set forth in claim 1 or 2, wherein the treatment of the condensed water comprises removing solid particles from the condensed water, and when the supplementary water needs to be warmed according to the temperature requirement of the desulfurization water by the desulfurization equipment, the supplementary water needing to be warmed is used as a heat absorption medium of the heat exchange equipment to be subjected to heat exchange through the heat exchange equipment, and the supplementary water is heated by the heat exchange equipment and then is connected to the water using device of the wet desulfurization tower.
4. An energy-saving micro-emission low-carbon haze treatment method suitable for controlling smoke pollution is characterized in that the generation and evolution of atmosphere acidic particulate matters related to smoke are controlled by adopting any one of the methods in claims 1 to 3, and chemical combination and displacement reaction after smoke emission is eliminated or reduced, so that the atmosphere haze pollution related to the smoke is controlled or reduced.
5. A low-carbon haze treatment system suitable for energy-saving micro-emission of flue gas pollution control is characterized in that a heat exchange device capable of realizing indirect heat exchange between flue gas and a low-temperature heat absorbing medium is arranged on a flue, the low-temperature heat absorbing medium absorbs heat energy of the flue gas, the emission temperature of the flue gas is reduced, water vapor in the flue gas is condensed into liquid water and discharged, the water content in the flue gas is reduced, acidic gas components in the flue gas are controlled or reduced to directly or indirectly react with alkaline substances under the participation of water to generate salt, the flue gas at the outlet of the heat exchange device is connected into a desulfurization device through the flue to be desulfurized, a plurality of heat exchange units which are mutually spaced are distributed in a shell of the heat exchange device in a segmented mode along the axial direction, a closed tube pass medium channel is arranged in a heat exchange piece of each heat exchange unit, shell cavities on the front side and the rear side of each heat exchange, the heat exchange equipment is also provided with a plurality of sectional condensed water discharge pipes, at least one condensed water drainage port communicated with the sectional condensed water discharge pipes is arranged between any two adjacent heat exchange units, the condensed water drainage port communicated with the sectional condensed water discharge pipes is arranged behind the heat exchange unit closest to the air outlet side port of the shell, four-phase flow division including water vapor condensation, dust sedimentation, condensed water leading-out and smoke discharge is realized in the process of heat exchange, smoke containing steam and dust in an air inlet side flue enters the heat exchange equipment from a shell side medium inlet of the heat exchange equipment, the smoke indirectly exchanges heat with a heat absorbing medium in a heat exchange piece when passing through the heat exchange unit, an inertia separation effect and a gravity separation effect are formed in the process of smoke flowing by means of blocking and area change formed in an inner cavity of the shell by the heat exchange unit, and suspended particles including the smoke and dust are separated from the, steam in flue gas is converted into condensed water due to heat release and is condensed in a deposition area of suspended particles, dust is mixed into the condensed water and is discharged from a condensed water outlet of heat exchange equipment, the condensed and separated flue gas is discharged from a shell-side medium outlet of the heat exchange equipment, the heat exchange equipment is arranged behind a flue gas dust remover and in front of flue gas desulfurization equipment, a flue gas outlet of the heat exchange equipment is connected with a flue gas inlet of separation equipment through a flue, the flue gas dust removal equipment adopts an electrostatic dust remover or a dust removal equipment combination containing the electrostatic dust remover, the flue gas desulfurization equipment adopts a wet desulfurization tower, all or part of the condensed water discharged by the heat exchange equipment is used as make-up water of the wet desulfurization tower after being treated, the temperature of the flue gas in the desulfurization process is controlled by controlling desulfurization process conditions, so that the temperature of the flue gas meets the temperature control requirements of corresponding flue gas inlet and, the steam in the flue gas entering the wet-type desulfurizing tower is in a saturated or nearly saturated state, the temperature of the flue gas is lower than 100 ℃, and the steam can react with alkaline substances in the desulfurizing water to eliminate acidic components of sulfur dioxide in the process of contacting with the desulfurizing water, the temperature and the volume of the flue gas are approximately stable or reduced, the moisture content of the flue gas is also approximately unchanged or even reduced, so that the great increase of the total moisture content of the flue gas caused by wet-type desulfurization is avoided,
the heat exchange equipment is vertical or horizontal, a shell of the vertical heat exchange equipment is vertically arranged, a port at the lower end of the shell is an air inlet side port, a port at the upper end of the shell is an air outlet side port, opposite end surfaces of adjacent heat exchange units are mutually parallel inclined planes, and an included angle which is not 90 degrees is formed between the opposite end surfaces and the axis of the shell of the heat exchange equipment, so that inclined equal-thickness gaps among the heat exchange units are formed; the horizontal heat exchange equipment is characterized in that a shell of the horizontal heat exchange equipment is horizontally arranged, a front end port of the shell is an air inlet side port, a rear end port of the shell is an air outlet side port, opposite end faces of adjacent heat exchange units are inclined planes with opposite inclination directions, an included angle of not 90 degrees is formed between the front end port and the axis of the shell of the heat exchange equipment, the distance between the upper ends of the two end faces is large, the distance between the lower ends of the two end faces is small, so that a V-shaped gap with a wide upper part and a narrow lower part is formed between the heat exchange units, the width of the bottom end of the V-shaped gap is not zero, water retaining weirs axially extending out are arranged on the edges of the windward side end face and the leeward side end face of the heat exchange piece, so that a diversion groove with an axial opening is formed on the end face of the heat exchange piece and is used for collecting and diverting condensed water, the water is, the outlet of the sectional condensate water discharge pipe is connected with the conveying inlet of a liquid conveying power device, the liquid conveying power device adopts a multi-stage multi-pipe high-efficiency jet pump, and the multi-stage multi-pipe high-efficiency jet pump is connected with a pumped medium inlet of a pumped medium channel to form the conveying inlet of the multi-stage multi-pipe high-efficiency jet pump.
6. The system of claim 5, wherein the evaporation capacity of the desulfurization water in the wet desulfurization tower is controlled by reducing the temperature difference of the flue gas at the inlet and outlet of the wet desulfurization tower, so as to reduce or avoid the increase of the moisture content of the flue gas due to the desulfurization process, the wet desulfurization tower adopts constant temperature desulfurization or controls the temperature difference of the flue gas at the inlet and outlet of the desulfurization tower to be not higher than 5 ℃, the proportion of water vapor removed by condensation of the heat exchange equipment in the flue gas is not less than 80%, the inlet flue gas temperature of the wet desulfurization tower is 60-80 ℃, the outlet flue gas temperature of the wet desulfurization tower is 55-80 ℃, and the upper limit of the inlet flue gas temperature adapted by the heat exchange.
7. The system of claim 5 or 6, wherein the segmented condensed water discharge pipe and the washing water discharge pipe of the heat exchange device are connected to a water treatment device capable of performing solid-liquid separation or solid-liquid separation and acid-base neutralization, a water outlet of the water treatment device is connected to a water using device of a wet desulfurization tower through a condensed water recycling pipeline, a pipe pass of the heat exchange device is connected in series to a main pipe or one branch pipe of the condensed water recycling pipeline, the main pipe or the branch pipe is used as a heat absorbing medium of the heat exchange device, and the heat absorbing medium and the water using device are connected to the wet desulfurization tower after heat absorption and temperature rise.
CN201711414490.XA 2017-08-16 2017-12-22 Method and system for controlling flue gas-related atmospheric acidic particulate matters and controlling haze with low carbon Active CN108114583B (en)

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