CN104016564A

CN104016564A - Sludge multi-effect drying incineration treatment system and application method thereof

Info

Publication number: CN104016564A
Application number: CN201410283222.9A
Authority: CN
Inventors: 王子国; 艾伟
Original assignee: Individual
Current assignee: Individual
Priority date: 2014-06-23
Filing date: 2014-06-23
Publication date: 2014-09-03

Abstract

The invention discloses a sludge multi-effect drying incineration treatment system and an application method thereof. The system comprises an incineration system, a combined drying system, a flue gas waste heat recycling system and a flue gas treatment discharging system. According to the system, the heat is transferred into a combined gas bed drying process of a hot carried gas by one step through a dividing wall by virtue of high-temperature flue gas obtained via the incineration of the sludge. Thus, the system has the advantages of high heat-transfer drying efficiency, safety, explosion resistance, large production capacity, low large-scale investment of a sludge treatment device, gradient utilization of heat energy of dry waste steam and good energy conservation effect; a dry smelly non-condensable gas which is sent into a fluidized bed incinerator can be completely deodorized.

Description

System and using method that mud multiple-effect anhydration and incineration is processed

Technical field

The invention belongs to field of Environment Protection, be specifically related to system and using method that a kind of mud multiple-effect anhydration and incineration is processed.

Background technology

In fields such as the energy, chemical industry, textile printing and dyeing, papermaking, municipal administration, environmental protection, conventionally can produce the mud that a large amount of water capacities are higher.It is maximum that municipal administration at present and industrial sewage are processed the sludge quantity producing, along with the acceleration of China's Urbanization Construction, and the continuous construction of sewage work, the industry of China and sanitary sewage disposal amount increase sharply, and will produce more mud.

The composition of mud is very complicated, except containing a large amount of moisture, also contains the compositions such as organism, various trace elements, pathogenic micro-organism and parasitic ovum, heavy metal of a large amount of organic matters, difficult degradation, and with stench.In mud, contain the nutritive substances such as a large amount of organism and abundant nitrogen, phosphorus, cause the eutrophication of water quality, cause water quality deterioration, the heavy metal in mud simultaneously, toxic substance, pathogenic bacterium etc. also will bring very big harm to human health.Mud discharges arbitrarily without dealing carefully with and banks up, and will ambient atmosphere, soil, underground water source be caused to serious pollution, makes built Sewage Plant can not give full play to the effect that it eliminates environmental pollution.Therefore, outlet is disposed in the processing that how to solve mud, become great environmental problem urgently to be resolved hurrily in China's urban development process, how that output is huge, the sewage sludge harmlessness of complicated component, resource utilization, reduce environmental pollution and become one of problem that whole world environment circle attractes attention.

At present the method for disposal of mud has landfill, agricultural, burning etc.Landfill disposal options can take a large amount of land resources, and easily because of seepage, causes the secondary pollution of soil water source atmosphere.Agricultural compost is according to the method for sterilization and slaking, its fertilizer efficiency and security are different, the mud of the objectionable constituent such as the organic chemicals that contains part difficult degradation, the viral germ that is difficult to kill and heavy metal, should not adopt in this way and to dispose, developed country limits the landfill of mud and agricultural gradually.Sludge incineration has the remarkable advantage of minimizing, innoxious, resource utilization.In burning process, all germs are all killed, and heavy metal stabilizing improves, the oxidized decomposition of toxic organic compound, after burning, mud remains the volume that grey volume is far smaller than mud after mechanical dehydration, be about its 1/10th.Worldwide sludge incineration is all widely used at present, and will further improve in the ratio of following sludge disposal.Because the moisture percentage in sewage sludge after mechanical dehydration is still in 78%～82% left and right, its calorific value is low, stable burning separately, directly send in boiler and burn, need to consume a large amount of auxiliary fuels, running cost is too high, and a large amount of burning mixed muds not only can cause detrimentally affect to boiler heating power balance, the rising of flue gas dew point also can cause corrosion to heated surface at the end of boiler, so will be dried it before burning sludge.

At present the more method for sludge treatment of foreign applications is to burn after first mummification, take and burns the target that can reach minimizing, stabilization, innoxious and resource utilization as the method for sludge treatment of core.Sludge incineration after mummification is relatively ripe, the mud that extensively adopts fluidized-bed to burn after mummification at present.The anhydration system of mud is of a great variety at present, and investment production capacity and running cost, whether to produce the technique difference such as secondary pollution larger, be also cause China's sludge anhydration burning process can not large-scale promotion a major cause.In order to study the relative merits of various sludge drying methods and to find suitable processing method, it is as follows that we carry out exhaustive division to it:

A, from dewatered sludge and/or auxiliary fuel, burn the high-temperature flue gas that produces as thermal source, then conduct heat and directly with hot middle number of times, anhydration system is classified to sludge drying, can divide: once conduct heat, secondary conducts heat, three heat transfers are until N heat transfer.

For example high-temperature flue gas directly belongs to once and conducts heat as thermal source sludge-drying; High-temperature flue gas conducts heat and produces steam to waste heat boiler, and steam belongs to secondary by indirect heat exchange mode sludge-drying and conducts heat.High-temperature flue gas conducts heat and produces thermal conductance deep fat to waste heat boiler, and thermal conductance deep fat belongs to secondary by indirect heat exchange mode sludge-drying and conducts heat.High-temperature flue gas conducts heat and produces thermal conductance deep fat to waste heat boiler, and thermal oil conducts heat to fluidized-bed heat-carrying air-flow by indirect heat exchange mode, and in fluid mapper process, heat-carrying air-flow comes sludge-drying to belong to three heat transfers by transmission of heat by convection; Simultaneously in fluidized-bed, thermal oil conducts heat to a small amount of mud granule that collides heat exchanger surface, to come heat exchange to belong to secondary to conduct heat by indirect heat exchange mode.The fewer Thermal Synthetic utilization ratio of the number of times that conducts heat is comparatively speaking higher, and technique is simpler, and investment reduces.

B, the mode contacting with mud by thermal medium can be divided into: Direct Contact Heating formula, indirect contact heating-type, noncontact heating-type, dual heating type.Heat transfer type from thermal source to mud can divide: conduction, convection current, radiative transfer.From the thermal medium of transmission of heat by convection, divide: the gases such as steam, air, flue gas, nitrogen, carbonic acid gas, or some liquid (for example sewage, water, wet goods) are added in employing in mud, and transmission of heat by convection flows.

1, Direct Contact Heating formula, is that thermal medium is directly contacted to mixing with mud, by convection current or heat transfer by heat conduction, mud is heated, and moisture is evaporated also finally obtains dewatered sludge product.For example with high-temperature flue gas to the direct contact drying of mud, adopt convection type.Also, for example with cycling hot ash and the mud mixing direct contact heat transfer of circulating fluidized bed, belong to heat transfer by conduction mode, low with circulating ash and mud heat transfer mummification after product ash content high heating value, do not utilize the efficient burning of dewatered sludge.

Direct Contact Heating gaseous exchange formula heated drying technology, it is by a kind of method of the moisture removal in mud with gaseous heat-carrier.Dry efficiency depends on following two factors: self structure and the feature of the condition of gaseous heat-carrier (dew point, relative humidity, speed) and mud.In operating process, gaseous heat-carrier (steam, air, flue gas, nitrogen, carbonic acid gas etc.) directly contacts with mud, absorbs the moisture in mud in this process, and the dewatered sludge after processing need carry out separated with gaseous heat-carrier.A waste gas part of discharging is got back in original system use again by heat recovery system, and remaining part is discharged after innoxious.This technology heat transfer efficiency and vaporator rate are higher.Owing to directly contacting with mud, gaseous heat-carrier will be polluted, and the useless water and steam of discharge must could discharge after harmless treatment.For reducing efflux gas treatment capacity, there is gas re-circulation technique both at home and abroad: the gas major part by outer row after dedusting, condensation, washing is returned to moisture eliminator, only that all the other a small amount of gaseous emissions removals are smelly, like this, not only reduce vent gas treatment amount, also reduced the introduction volume of outside carrier gas.The tail of direct heat drying installation is large-minded, and processing cost is high, and indirect heating, the amount of tail gas is much smaller, and the burden of corresponding vent gas treatment is light, makes people forward again interest to indirect heating that heat transfer efficiency is low.

Air, flue gas, nitrogen, carbon dioxide gas are all non-condensable gasess under drying sludge operating conditions, and the relative air of the indifferent gas such as nitrogen, carbon dioxide gas and flue gas are difficult for obtaining.Conventional available direct contact convection type dry heat medium is exactly: air, flue gas, steam.When the thermal medium of transmission of heat by convection is air, can not under too high high temperature, be dried, be mainly that the oxygen in high temperature air is easy to cause firing of dewatered sludge in drying process.

Take air or flue gas during as the mummification of convection heat medium heat-transfer, its advantage is that technical process is simple, unit treatment capacity is larger, weak point is that drying medium is non-condensable gases, owing to being mixed with higher concentration odor causing substance in tail gas, must carrying out a large amount of tail gas deodorizations and process and could discharge; And a large amount of steam dew-point temperatures that dried tail gas contains are lower, and condensation latent heat energy gradient rank is low, the latent heat reclaiming in tail gas is difficult to, and the thermosteresis of discharge is also very large.

The superheated vapour of usining is optimum as convective heat exchange drying medium, main because: dry heat efficiency is higher.With superheat steam drying tail vapour temperature of saturation higher (can be greater than 100 ℃ according to working pressure), vapor condensation latent heat is large, and the exhaust steam after sludge-drying is convenient to the utilization of step condensing heat-exchange, further reduces energy consumption for drying, and thermo-efficiency is improved greatly.Superheated vapour has higher specific heat capacity, transmits the required mass rate of certain heat less, and in the identical situation of operating speed, the heat and mass transfer coefficient of superheated vapour is than conventional drying medium (air, flue gas, nitrogen) height.High heat transfer coefficient reduces interchanger heat interchanging area, and the heat and mass transfer coefficient between high vapour is solid has improved drying sludge speed, has shortened time of drying, has reduced the volume of e-quipment and pipe, has reduced its investment.With superheat steam drying, almost under the condition of anaerobic, carry out, substantially without the possibility that is dried detonation.Even if using superheated vapour mixing air as drying medium, due to the existence of a large amount of steam, also greatly reduce the possibility of drying sludge detonation.Because the non-condensable gas containing in superheat steam drying tail gas is few, after condensation gas-water separation, can all by sending into containing odorous non-condensable gas, burn burner hearth high temperature incineration deodorization processing, deodorization the lowest coursing cost.The high-temperature flue gas that transmission of heat by convection thermal medium steam can be produced by burning produces through residual heat boiler for exchanging heat, also can in dewatered sludge process, by mud evaporation, be produced.The steam cost producing through waste heat boiler and investment are higher, but steam quality is good.In dewatered sludge process, by wet mud, directly evaporate generation superheated vapour cost minimum, but steam quality is bad, need to carry out dedusting.

2, indirect contact heating-type, by thermal medium (as steam, flue gas, heat conduction wet goods) heating wall, thereby the wet mud that makes wall opposite side is heated, moisture evaporation, substantially belongs to heat transfer by conduction mode, if wall temperature is very high, also can have radiative transfer mode.Indirect contact heating-type is dry, advantage is that thermal medium does not directly contact with mud, but by heat exchange partition, heat is transmitted to dewing mud, make the moisture evaporation in mud, without the danger of exploding and catching fire, thermal barrier also can not be subject to the pollution of mud, the dry tail gas amount producing is very little, dry heat efficiency is higher, tail gas deodorization be easy to process and working cost lower, shortcoming part is that drying process and equipment are all more complicated, unit treatment capacity is less, and easily glue wall, inapplicable to the mud that adhesivity is large, heat transfer efficiency and vaporator rate are all not as direct heat dry technology.

3, noncontact heating-type, is to adopt the radiation mode heating mud such as microwave, infrared rays, sun power, makes its moisture evaporation.

4, dual heating type is the combination of above-mentioned several type of heating.For example, with cycling hot ash and the mud mixing direct contact heat transfer of circulating fluidized bed, belong to heat transfer by conduction mode, adopt fluidisation air-flow to carry out transmission of heat by convection to mud simultaneously.Also for example, in fluidized bed dryer, thermal oil is conducted heat and is conducted heat exchange to a small amount of mud granule that collides heat exchanger surface by indirect contact mode, and while heat-carrying air-flow in fluid mapper process obtains heat and passes through convection type direct heat transfer to this part mud granule again from thermal oil.

C, to be dried the air-flow that contains steam taken out of and the speed of relative movement of mud, or to the carrying capacity of dewatered sludge, can divide mobile bed drying, fluidised bed drying, air flow bed dry to be dried the air-flow that contains steam taken out of.

It is minimum that the air-flow that contains steam that mobile bed drying is taken out of carries dewatered sludge ability, and air-flow and mud speed of relative movement are maximum.

It is maximum that the dry air-flow that contains steam of taking out of of air flow bed carries dewatered sludge ability, and air-flow and mud speed of relative movement minimum (both speed are substantially equal), the particle that contains in a large number sludge-drying is taken moisture eliminator out of with air-flow, is all to carry substantially.

Fluidised bed drying is dried between the two in mobile bed drying, air flow bed, and drying air stream only carries less mud granule.

Mobile bed drying dust is taken out of few, but heat transfer coefficient is low, dry throughput is minimum, and heat-transfer surface need to constantly be cleared up constant the carrying out of guarantee heat transfer, for example take heat transfer by conduction as main partition heat exchange mobile bed drying machine, adopt scraper plate spiral to make thinner and stir mud reinforcement heat exchange.And mobile bed drying can increase fast along with the reduction heat transfer resistance of dewatered sludge water content.So moving bed dryer is inapplicable to extensive drying sludge.

The gentle fluidized bed drying of fluidized-bed all belongs to transmission of heat by convection, because the convection velocity of air-flow is fast, conducts heat rapidly, and dry throughput is large.Fluidized-bed is conventionally slightly slow because of gas velocity, therefore need the good mud of back-mixing part mummification to enter the fluidizing fluid-bed active fluidization that carries out before wet mud enters drying machine.Air flow bed is conducted heat the strongest, and throughput is the highest.The two operation of fluidized-bed and air flow bed all needs drying air stream to carry out good dedusting, for example, adopt cyclone dust removal string bag-type dust.

D, by wet mud, enter and whether carry out pre-treatment before drying equipment and classify, can divide two classes: anticipate technique and do not carry out treatment process.

Anticipating technique comprises: wet mud and the sticky wall of mud through the mud of mummification or when other material first mixes or granulation enters desiccation machine to alleviate; To mud, add part easily to dewater material so that compression dehydration in advance; Add in advance some water or liquid, aqueously carry out slurrying and increase mobility, to pump up, with nozzle, to carry out the atomization air flow bed of spraying dry or pump up and circulate evaporation; Add in advance oil wet mud to be mixed so that the dry vaporize water of pumping grades.Pretreatment technology has increased facility investment and energy consumption.Conventionally moisture percentage in sewage sludge is greater than 85%, and mud is the shape that can flow; Moisture percentage in sewage sludge 65～85%, mud is plastic state; Moisture percentage in sewage sludge is less than 65%, is solid-state.So increase mobility for use in circulating-heating by adding water or aqueous solution, along with the carrying out of evaporation drying also easily stopped up heat-exchange equipment.The moisture adding also needs evaporation, has increased investment and the energy consumption of slurrying, pumping, evaporation.

Another kind of is the wet direct charging of mud, does not carry out treatment process before entering drying machine.It is easier that wet mud directly enters drying machine mode, and investment energy consumption is minimum, but need to solve the problems such as sticky wall.

E, with the odorous gas producing after dewatered sludge, whether process minute: process and do not process.Processing the method for odorous gas can divide: burning method, biochemical deodorization, activated carbon deodorization, strong acid-base deodorization etc.Wherein processing the best mode of odorous gas is burning method, the odorous gas that is about to dewatered sludge generation is sent into the burner hearth of burning and drying mud, at high temperature burn decomposition the most thorough, but burning method is not suitable for the technique of high-temperature flue gas or the direct transmission of heat by convection oven dry of air mud, mainly because of odorous gas, sneak in flue gas, very large containing smelly flue gas tolerance, can only partly return to burner hearth burns, burning disposal foul smell completely, residue also will further be undertaken by biochemistry or chemical absorption absorption way containing smelly flue gas, cause deodorization complex treatment process running cost high, process and thoroughly can not cause secondary pollution to environment.

Whether F, the exhaust steam producing by drying process obtain utilizing can be divided: utilize and do not utilize.The form of utilizing of exhaust steam can be divided into: heat of condensation adds warm air and enters burning burner hearth, and heat of condensation is used for dry wet mud again, and heat of condensation adopts the approach such as heat pump or unit cooler heat production water or cold water.The utilization optimum of tail gas vapor condensation heat is from a high position to low level cascade utilization, first for sludge-drying heat supply, secondly by air flue gas heat exchange, obtain high as far as possible temperature and return to burner hearth utilization, treat that dew point is reduced to try one's best low time to adopt water quench to discharge to reduce cooling water consumption.The water of condensation of lesser temps can only adopt heat pump or unit cooler to produce the hot water of cold water or higher temperature substantially, so cold water hot water is limited because the lower drying and incineration system of energy rank utilizes it, mainly can provide regional air conditioner to use.

G, by the appearance forrns of drying equipment, have: the various ways such as rotary drum, rotating disc type, belt, spiral, rake, centrifugal, multiple coil tube type, film type, hollow paddle type, fluidized-bed, air flow bed.

Chinese invention patent application prospectus CN200710060213.3 innocent incineration integrated processing technique for wet sludge circulating fluid bed, by circulating fluidized bed high temperature ash and the granulation in moisture eliminator of wet mud, send in circulation bed and burn again, have that complex structure facility investment is high, mummification after product ash content high heating value is low, be unfavorable for the problems such as efficient burning of dewatered sludge.

Chinese invention patent application prospectus CN201310670098.7 bis-effect evaporation sludge drying system and drying methods, is characterized in that: comprise the following steps: the first, and mud oil mixing step, mud mixes in mud mixing bunker with oil; The second, multiple-effect evaporation step, mud oil mixt is transpiring moisture in 1st effective evaporator and 2nd effect evaporator; The 3rd, the solid separating step of oil, the mud oil mixt after evaporation is product separation dewatered sludge in separating centrifuge and de-oiling device; The 4th, water of condensation and separating of oil step are carried out water of condensation and separating of oil operation in water-and-oil separator.Visible the method is sneaked in order to increase the mobility of wet mud and is spontaneously adopted afterwards evaporation, and evaporation separation process is very complicated, and profit is easy to emulsification and is difficult to separation.The steam that the method adopts steam boiler to produce is that thermal source evaporates greasy filth mixture by indirect heating, and the high-temperature flue gas after burning conducts heat and conducts heat to greasy filth mixture to steam, steam again, belongs to twice heat transfer, and heat transfer efficiency is lower.

Chinese invention patent ZL200710070060.0 sludge drying, incineration treatment method and integrating device, the method is: pretreated wet mud enters the shower nozzle on spray-drying tower top together with pressurized air, with droplet form, contact with tower top high-temperature gas stream, spray and be dried to obtain mummification particle, tail gas is discharged pending from the tail gas outlet of spray-drying tower bottom; Described wet sludge pretreatment, is by mechanical disintegration, and the increase mobility of sizing mixing, sieves, and removes 10 orders and above granule and impurity.Although visible the method adopts the wet mud slurrying spraying air flow bed drying machine that heat exchange efficiency is high, but owing to adopting high-temperature flue gas convection drying mud, the low-temperature flue gas that contains a large amount of water vapors producing after mummification is unfavorable for recycling water vapor condensation heat, and the dry rear mixed gas that contains foul smell, low temperature non-condensable gas is difficult to process; And the method will be carried out pre-treatment to wet mud, sieves with broken the sizing mixing of pigment, the high operation of investment is very complicated, wearing and tearing spraying nozzle and increased and additionally add evaporation of water energy consumption.

Specification sheets CN200910015341.5 sludge superheated vapor drying system of two-stage paddle dryer and drying process thereof are authorized in Chinese invention patent authorization, the superheated vapour that this invention adopts sludge incineration to produce by boiler heat exchange is transported in secondary blade dryer and uses as thermal source, and semi-dry sludge is dried.Be that the method adopts the high-temperature flue gas after burning to conduct heat to boiler generation steam, steam conducts heat to mud in secondary blade dryer again, belongs to twice heat transfer, and heat transfer efficiency is lower, and comes dewatered sludge steam cost with high investment large with boiler producing steam.The blade dryer that the method adopts in addition belongs to mobile bed drying machine, it is few that the advantage of mobile bed drying machine is that the thermal medium superheated vapour of drying sludge direct heat transfer carries dust, so only have secondary drying machine to adopt cyclone dust removal from the method, one-level drying machine does not carry out dedusting; But it is low that the shortcoming of mobile bed drying machine is heat transfer efficiency, and throughput is little, along with the increase of sludge treatment ability can cause the significantly increase of investment and floor space, be unsuitable for the maximization of sludge treatment.

Specification sheets CN200910089940.1 sludge drying-incineration integrated system and using method are authorized in the Chinese invention patent authorization of Tsing-Hua University's application, this invention be take steam that heat heating water that sludge incineration produces generates as thermal source indirect heating is to hot sludge dryer, steam becomes water of condensation after mud is cooling, then with pump circulation and incineration flue gas heat exchange, produce again steam, be that incineration flue gas heat exchange is to water generates steam, steam heat-exchanging is to mud, belong to twice heat transfer, cause complex process, increase of investment, heat transfer efficiency low.This invention has also adopted dry mud back-mixing device, in order to by the dewatered sludge mixing granulation of the wet mud of water ratio 75%～80% and water ratio 30%, although avoided mud to occur bonding phenomenon in moisture eliminator, reduced sludge treatment ability, and equipment and complicated operation.The inerting carrier gas (flue gas) that this invention also utilizes sludge incinerator to produce, enter sludge dryer and take the water vapor of its generation out of, waste gas after moisture absorption is discharged after moisture eliminator for heating after the low-temp low-pressure heat pump fluid that heat pump cycle produces, a part is discharged cooling, and a part of and a certain amount of fresh air mixes and after boosting, passes into incinerator and burn.Because adopting flue gas to enter drying machine as carrier gas direct heating, this invention dries, have and take flue gas and directly contact the merits and demerits of convection type heat dry technology as thermal medium, be that convection drying efficiency is improved, but can only partial fume recirculation return to incinerator burning deodorizing, major part also will further be processed containing smelly flue gas, a deodorization is not thorough, and deodorization cost significantly increases.In addition, owing to being mixed with a large amount of flue gases and wetting vapour in dry gas, so wetting vapour dew point in dry gas is low, be difficult to carry out condensation cascade utilization, can only adopt heat pump to improve heat supply temperature, caused increase of investment.

Specification sheets CN201010149945.1 municipal sludge drying and incineration system and treatment process thereof are authorized in Chinese invention patent authorization, the mud that this technique is 70%-90% by water ratio enters in sludge drier by worm conveyor or sludge pump, in sludge drier, after dispersing device is broken up and from the flue gas direct contact heat transfer of incinerator, is realizing drying-granulating; Lead up to worm conveyor or scraper conveyor in sludge drier gained dewatered sludge are sent into incinerator and are burned, and after the high-temperature flue gas after burning and air mixed temperature adjustment, send into sludge drier, directly contact and are dried with mud.Visible because this invention employing flue gas enters drying machine oven dry as carrier gas direct heating, have and take flue gas and directly contact the merits and demerits of convection type heat dry technology as thermal medium, be that drying efficiency is higher, but major part is difficult to thoroughly process containing smelly flue gas or processing cost is high, wetting vapour dew point in dry gas is low is difficult to carry out condensation cascade utilization, and whole system energy consumption is high and easily environment is caused to secondary pollution.

Generally speaking, current sludge anhydration burning processing system, mainly there are the following problems: the heat transfer efficiency of sludge dry system is low, and energy consumption is large, and throughput is low, and investment running cost is high, and in anhydration and incineration process, the pollutent such as foul smell is wayward, is difficult to maximize etc.

Summary of the invention

The shortcoming existing in order to overcome current technology, the object of this invention is to provide a kind ofly can make sludge reduction, innoxious, energy consumption significantly reduces, invest and economize mud multiple-effect anhydration burning processing system and the using method that is suitable for maximization.

For achieving the above object, the present invention takes following technical scheme:

A mud multiple-effect anhydration burning processing system, is characterized in that: comprise an incineration system, a combination drying system, a flue gas waste heat recovery system, a flue gas processing blowdown system;

Described incineration system comprises fluidized bed incinerator, hot precipitator;

Described flue gas waste heat recovery system comprises steam boiler, air preheater or only comprises air preheater;

Described combination drying system comprises the dry subsystem of N level air flow bed;

The dry subsystem of described N level air flow bed, N=1～5, preferred N=2;

The dry subsystem of every grade of air flow bed of described combination drying system is comprised of carrier gas interchanger, air flow bed moisture eliminator, drying, dedusting device, drying air fan, dry gas condenser, air water separator; In the dry subsystem of adjacent two-stage air flow bed, upper level dry gas condenser is simultaneously as next stage carrier gas interchanger;

In described air flow bed moisture eliminator, be provided with mud diverting device;

Described drying, dedusting device is composed in series by tornado dust collector and sack cleaner;

Described fluidized bed incinerator is provided with wind interface, secondary air interface, non-condensable gas interface, exhanst gas outlet, dewatered sludge interface, auxiliary fuel interface, a slag and exports, and described hot precipitator is provided with gas approach, exhanst gas outlet, ash outlet;

Described wind interface of fluidized bed incinerator connects the wind outlet that in flue gas waste heat recovery system, air preheater comes, the boiling section dewatered sludge interface of fluidized bed incinerator connects the dewatered sludge outlet that combination drying system is come, fluidized bed incinerator non-condensable gas interface connects air water separator non-condensable gas outlet in combination drying system, fluidized bed incinerator exhanst gas outlet connects hot precipitator gas approach, hot precipitator exhanst gas outlet connects the dry subsystem carrier gas interchanger gas approach of first step air flow bed in combination drying system, the dry subsystem carrier gas interchanger exhanst gas outlet of first step air flow bed connects the gas approach of steam boiler in flue gas waste heat recovery system, the exhanst gas outlet of steam boiler connects air preheater gas approach, an air preheater exhanst gas outlet road in parallel is connected to each drying air fan import in combination drying system, an air preheater exhanst gas outlet road simultaneously in parallel connects flue gas and processes blowdown system import, flue gas is processed blowdown system outlet and is entered atmosphere,

A wind entrance of the air preheater of described flue gas waste heat recovery system connects primary air fan air vout, a wind outlet of air preheater connects a wind interface of fluidized bed incinerator, the secondary air entrance connecting secondary blower air outlet of air preheater, the secondary air outlet of air preheater connects the secondary air interface of fluidized bed incinerator;

In the dry subsystem of each air flow bed of described combination drying system, drying air fan exports carrier gas interchanger carrier gas inlet in parallel and dry gas condenser is arranged carrier gas inlet outward, carrier gas interchanger carrier gas outlet connects air flow bed moisture eliminator carrier gas inlet, air flow bed dryer export connects drying, dedusting device, drying, dedusting device carrier gas outlet is connected to drying air fan import, dry gas condensator outlet connects air water separator, and the outlet of air water separator non-condensable gas connects the import of fluidized bed incinerator non-condensable gas; In the dry subsystem of adjacent two-stage air flow bed, upper level dry gas condenser is simultaneously as next stage carrier gas interchanger;

The using method of described mud multiple-effect anhydration burning processing system, is characterized in that:

1) comprise an incineration system, a combination drying system, a flue gas waste heat recovery system, a flue gas processing blowdown system;

The dry subsystem of described N level air flow bed, N=1～5, preferred N=2;

2) incineration system: jointly burn in fluidized bed incinerator with the mud after auxiliary fuel and mummification; In the air compartment of fluidized bed incinerator, pass into the heat primary air of flue gas waste heat recovery system, auxiliary fuel and dewatered sludge fluidized bed combustion in fluidized bed incinerator; Freeboard of fluidized bed at fluidized bed incinerator, the hot secondary air that adds heat recovery system, carry out flue gas disturbance oxygenating and strengthen burning, what pass into the generation of combination drying system carries out high temperature incineration deodorizing containing smelly non-condensable gas simultaneously, and the high-temperature flue gas that fluidized bed incinerator produces enters hot precipitator and carries out dedusting;

Described auxiliary fuel comprises coal water slurry that coal, coal gangue, high-concentration waste water make, oil fuel, combustible gas, biomass fuel one of them or its mixture; The coal water slurry that the high-concentration waste water of usining is made during as auxiliary fuel fluidized bed incinerator processed high-concentration waste water simultaneously;

Described mud comprises domestic sludge, oil, chemical industry, printing and dyeing, papermaking, the industrial sludge such as brewages, and containing hydrocarbon wet solid fuel;

3) combination drying system: the high-temperature flue gas after dedusting enters combination drying system, high-temperature flue gas is in the carrier gas interchanger of the dry subsystem of first step air flow bed and the heat exchange of cycling hot carrier gas partition, hot carrier gas absorbs heat temperature and is improved, and high-temperature flue-gas enters flue gas waste heat recovery system and continues to reclaim heat after reducing;

In the dry subsystem of each air flow bed: the hot carrier gas after drying air fan pressurization is divided into two-way, and wherein a road is sent into after the input thermal source partition heat exchange of the gentle fluidized bed drying subsystem of carrier gas interchanger, sends into air flow bed drying machine sludge-drying, add the wet mud of air flow bed drying machine after inner dispersion mechanism breaks up, the strong convection current direct heating of the hot carrier gas mummification of being heated by carrier gas interchanger, in wet mud, moisture evaporation becomes superheated vapour, hot carrier gas temperature is reduced simultaneously, hot carrier gas after cooling is carried all dewatered sludges and is entered drying, dedusting device and carry out gas solid separation, mud is after drying discharged this subsystem and is delivered to fluidized bed incinerator burning or send into the dry subsystem of all the other air flow bed and continue depth drying, finally deliver to the dewatered sludge water-content 5～40% that fluidized bed incinerator burns, preferred water-content 5～25%, hot carrier gas suction drying air fan after drying, dedusting device gas solid separation again pressurized circulation is dry, the hot carrier gas in another road after drying air fan pressurization is expelled to dry gas condenser condenses, heat of condensation offers the dry subsystem of next stage air flow bed as input thermal source, condensed air-water mixture is after the separated moisture of air water separator, and non-condensable gas is sent into fluidized bed incinerator and burned deodorizing,

In the dry subsystem of adjacent two-stage air flow bed, upper level dry gas condenser is simultaneously as next stage carrier gas interchanger; Vapor condensation heat in 1～hot carrier gas that (N-1) the dry subsystem of level air flow bed is discharged, be the dry subsystem sludge-drying of next stage air flow bed heat is provided, and in hot carrier gas at different levels, vapor condensation temperature reduces gradually, and heat energy obtains cascade utilization, and utilization ratio greatly improves; The dry subsystem of last step air flow bed is discharged steam in gas, by water coolant is indirectly or directly cooling, carrys out condensation separation, and the non-condensable gas after separation goes fluidized bed incinerator burning deodorizing;

The condensed hot water that the dry subsystem dry gas condenser of air flow bed at different levels is discharged is directly discharged into sewage network and processes, and also can be used as absorption refrigeration or heat pump set provides low-temperature receiver or thermal source to supply heating or refrigeration outward, cold-heat combined with feasible region.

4) flue gas waste heat recovery system: the carrier gas heat exchanger exit flue gas in the dry subsystem of first step air flow bed enters steam boiler, the heat exchange of flue gas partition is to water medium in boiler, and steam boiler water medium evaporates the outer heat supply of the steam producing or further with steam turbine, generates electricity; Steam boiler outlet flue gas enters air preheater, the secondary air partition heating that the flue gas primary air that outlet comes to primary air fan, overfire air fan outlet come, it is interior as fluidisation and combustion-supporting gas that a wind after heating is sent into fluidized bed incinerator air compartment, and the secondary air after heating is sent into fluidized bed incinerator temperature adjustment; If burn the heat of auxiliary fuel and dewatered sludge generation only for meeting wet sludge anhydration institute heat requirement, can not establish steam boiler;

5) flue gas is processed blowdown system: air preheater outlet flue gas enters flue gas and processes blowdown system, at flue gas, process flue gas in blowdown system and reach environmental protection standard through purifying treatment such as dedusting, de-Dioxins, desulphurization and denitration, depicklings, qualified flue gas harmless emission enters atmosphere;

Described combination drying system, is characterized in that:

The high-temperature flue gas that the dry subsystem input of first step air flow bed thermal source is incineration system, the dry subsystem input of all the other air flow bed at different levels thermal source is the heat of condensation that the dry subsystem of upper level air flow bed is discharged steam in hot carrier gas, and input thermal source is all in carrier gas interchanger and the heat exchange of hot carrier gas partition; The dry subsystem of the level Four air flow bed of take is example, the high-temperature flue gas that the dry subsystem input of first step air flow bed thermal source is incineration system, the dry subsystem input of second stage air flow bed thermal source is the heat of condensation that the dry subsystem of first step air flow bed is discharged steam in hot carrier gas, the dry subsystem input of third stage air flow bed thermal source is the heat of condensation that air flow bed dry subsystem in the second stage is discharged steam in hot carrier gas, the dry subsystem input of fourth stage air flow bed thermal source is the heat of condensation that the dry subsystem of third stage air flow bed is discharged steam in hot carrier gas, by that analogy;

The inner drying air fan that adopts of the dry subsystem of air flow bed at different levels circulates by carrier gas interchanger raising carrier gas temperature, the direct transmission of heat by convection of wet mud after the hot carrier gas after temperature raising and diverting device are broken up, and wet mud heat absorption obtains mummification, and carrier gas temperature is reduced;

Described hot carrier gas is the mixture that superheated vapour and non-condensable gas form, and superheated vapour is produced by wet sludge anhydration transpiring moisture;

Described non-condensable gas is that in drying process, drying sludge decomposes generation and entered in the dry subsystem of air flow bed by external complement;

Described by external complement, to enter in the dry subsystem of air flow bed non-condensable gas be air, flue gas one of them or its gas mixture, and preferred non-condensable gas is flue gas;

In the hot carrier gas that the dry subsystem of 1～N level air flow bed is discharged, vapor condensation temperature reduces step by step, by air flow bed, is dried the working pressure of the hot carrier gas of subsystem inner drying and is sneaked into non-condensable gas content and control;

Along with the working pressure raising of the dry heat carrier gas in the dry subsystem of air flow bed at different levels, the dry subsystem of air flow bed at different levels is arranged the corresponding raising of vapor condensation temperature in carrier gas outward; Along with the working pressure reduction of the dry heat carrier gas in the dry subsystem of air flow bed at different levels, the dry subsystem of air flow bed at different levels is arranged the corresponding reduction of vapor condensation temperature in carrier gas outward.Along with the raising of non-condensable gas content in the dry heat carrier gas in the dry subsystem of air flow bed at different levels, the dry subsystem of air flow bed at different levels is arranged the corresponding reduction of vapor condensation temperature in carrier gas outward.Along with the reduction of non-condensable gas content in the dry heat carrier gas in the dry subsystem of air flow bed at different levels, the dry subsystem of air flow bed at different levels is arranged the corresponding raising of vapor condensation temperature in carrier gas outward.

Compared with prior art, tool of the present invention has the following advantages:

1, partition-wall heat transfer of sludge incineration high-temperature flue gas is to dry heat carrier gas, and the high equipment volume of heat transfer efficiency is little, and the dry exhaust steam producing is convenient to repeatedly utilize, and dryly containing smelly non-condensable gas, sends into fluidized bed incinerator and obtains complete deodorization and process.

2, adopt the combination drying system that comprises the dry subsystem of Multi-stage airflow bed, the high-temperature flue gas that the dry subsystem input of primary airstream bed thermal source is fluidized bed incinerator, all the other input thermals source at different levels are the heat of condensation that the dry subsystem of upper level air flow bed is discharged steam in hot carrier gas, thermal energy step is utilized, and drying energy saving is effective.

3, adopt the dry superheated vapour mixing non-condensable gas producing of mud self as the air flow bed drying process of hot carrier gas, throughput is large, and drying efficiency is high, safety anti-explosive, and sludge treatment equipment maximization investment is low.

The present invention can be widely used in various field of sludge treatment.

Accompanying drawing explanation

Fig. 1 is one-piece construction schematic diagram of the present invention

Fig. 2 is the combination drying system architecture schematic diagram being comprised of the dry subsystem of two-stage air flow bed of the present invention

Fig. 3 is the combination drying system architecture schematic diagram being comprised of the dry subsystem of three grades of air flow bed of the present invention

Embodiment

Below in conjunction with drawings and Examples, the present invention is described in detail.

As shown in Figure 1, the present invention includes an incineration system 1, a combination drying system 2, a flue gas waste heat recovery system 3, a flue gas processing blowdown system 4.Incineration system 1 comprises fluidized bed incinerator 11, hot precipitator 12; Flue gas waste heat recovery system 3 comprises steam boiler 31, air preheater 32;

As shown in Figure 2, the combination drying system 2 being formed by the dry subsystem of two-stage air flow bed of the present invention, first step air flow bed is dried subsystem 21, and second stage air flow bed is dried subsystem 22.The dry subsystem 21 of first step air flow bed is comprised of carrier gas interchanger 211, air flow bed moisture eliminator 212, drying, dedusting device 213, drying air fan 214, dry gas condenser 215, air water separator 216; Air flow bed dry subsystem 22 in the second stage is comprised of carrier gas interchanger 221, air flow bed moisture eliminator 222, drying, dedusting device 223, drying air fan 224, dry gas condenser 225, air water separator 226; In the dry subsystem 21 of the dry subsystem first step air flow bed of adjacent two-stage air flow bed and the dry subsystem 22 of second stage air flow bed, upper level dry gas condenser 215 is simultaneously as next stage carrier gas interchanger 221, be that dry gas condenser 215 and carrier gas interchanger 221 are same heat-exchange equipments, the both sides of interchanger partition are walked respectively in the hot carrier gas of the dry subsystem 21 of first step air flow bed and the dry subsystem 22 of second stage air flow bed.

As shown in Figure 3, the combination drying system 2 being formed by the dry subsystem of three grades of air flow bed of the present invention, first step air flow bed is dried subsystem 21, and second stage air flow bed is dried subsystem 22, and third stage air flow bed is dried subsystem 23.

The dry subsystem 21 of first step air flow bed is comprised of carrier gas interchanger 211, air flow bed moisture eliminator 212, drying, dedusting device 213, drying air fan 214, dry gas condenser 215, air water separator 216; Air flow bed dry subsystem 22 in the second stage is comprised of carrier gas interchanger 221, air flow bed moisture eliminator 222, drying, dedusting device 223, drying air fan 224, dry gas condenser 225, air water separator 226; The dry subsystem 23 of third stage air flow bed is comprised of carrier gas interchanger 231, air flow bed moisture eliminator 232, drying, dedusting device 233, drying air fan 234, dry gas condenser 235, air water separator 236;

In the dry subsystem 21 of the dry subsystem first step air flow bed of adjacent two-stage air flow bed and the dry subsystem 22 of second stage air flow bed, upper level dry gas condenser 215 is simultaneously as next stage carrier gas interchanger 221, be that dry gas condenser 215 and carrier gas interchanger 221 are same heat-exchange equipments, the both sides of interchanger partition are walked respectively in the hot carrier gas of the dry subsystem 21 of first step air flow bed and the dry subsystem 22 of second stage air flow bed;

In the dry subsystem 22 of the dry subsystem of adjacent two-stage air flow bed second stage air flow bed and the dry subsystem 23 of third stage air flow bed, upper level dry gas condenser 225 is simultaneously as next stage carrier gas interchanger 231, be that dry gas condenser 225 and carrier gas interchanger 231 are same heat-exchange equipments, the both sides of interchanger partition are walked respectively in the hot carrier gas of the dry subsystem 22 of second stage air flow bed and the dry subsystem 23 of third stage air flow bed.

Embodiment mono-

The employing of the present embodiment combination drying system comprises the dry subsystem of 2 grades of air flow bed and comes dewatered sludge then to carry out burning disposal.

Technical process connects as follows:

See Fig. 1, Fig. 2: comprise an incineration system 1, a combination drying system 2, a flue gas waste heat recovery system 3, a flue gas processing blowdown system 4.Incineration system 1 comprises fluidized bed incinerator 11, hot precipitator 12; Flue gas waste heat recovery system 3 comprises steam boiler 31, air preheater 32;

The combination drying system 2 that the present embodiment is comprised of the dry subsystem of two-stage air flow bed, first step air flow bed is dried subsystem 21, and second stage air flow bed is dried subsystem 22.The dry subsystem 21 of first step air flow bed is comprised of carrier gas interchanger 211, air flow bed moisture eliminator 212, drying, dedusting device 213, drying air fan 214, dry gas condenser 215, air water separator 216; Air flow bed dry subsystem 22 in the second stage is comprised of carrier gas interchanger 221, air flow bed moisture eliminator 222, drying, dedusting device 223, drying air fan 224, dry gas condenser 225, air water separator 226; In the dry subsystem 21 of the dry subsystem first step air flow bed of adjacent two-stage air flow bed and the dry subsystem 22 of second stage air flow bed, upper level dry gas condenser 215 is simultaneously as next stage carrier gas interchanger 221, be that dry gas condenser 215 and carrier gas interchanger 221 are same heat-exchange equipments, the both sides of interchanger partition are walked respectively in the hot carrier gas of the dry subsystem 21 of first step air flow bed and the dry subsystem 22 of second stage air flow bed.

Described 11 wind interfaces of fluidized bed incinerator connect a wind outlet of air preheater 32 in flue gas waste heat recovery system 3, the boiling section dewatered sludge interface of fluidized bed incinerator 11 connects the dewatered sludge outlet of combination drying system 2, fluidized bed incinerator 11 non-condensable gas interfaces connect air water separator non-condensable gas outlet in combination drying system 2, fluidized bed incinerator 11 exhanst gas outlets connect hot precipitator 12 gas approachs, hot precipitator 12 exhanst gas outlets connect dry subsystem carrier gas interchanger 211 gas approachs of first step air flow bed in combination drying system 2, dry subsystem carrier gas interchanger 211 exhanst gas outlets of first step air flow bed connect the gas approach of steam boiler 31 in flue gas waste heat recovery system 3, the exhanst gas outlet of steam boiler 31 connects air preheater 32 gas approachs, an air preheater 32 exhanst gas outlets road in parallel is connected to each drying air fan import in combination drying system 2, an air preheater 32 exhanst gas outlets road simultaneously in parallel connects flue gas and processes blowdown system 4 imports, flue gas is processed blowdown system 4 outlets and is entered atmosphere,

A wind entrance of the air preheater 32 of described flue gas waste heat recovery system 3 connects primary air fan air vout, a wind outlet of air preheater 32 connects a wind interface of fluidized bed incinerator 11, the secondary air entrance connecting secondary blower air outlet of air preheater 32, the secondary air outlet of air preheater 32 connects the secondary air interface of fluidized bed incinerator 11;

In the dry subsystem 21 of the 1st grade of air flow bed of described combination drying system: drying air fan 214 outlet carrier gas interchanger 211 carrier gas inlet in parallel and the outer row's carrier gas inlet of dry gas condenser 215, the 211 carrier gas outlets of carrier gas interchanger connect air flow bed moisture eliminator 212 carrier gas inlet, 212 outlets of air flow bed moisture eliminator connect drying, dedusting device 213, the 213 carrier gas outlets of drying, dedusting device are connected to drying air fan 214 imports, 215 outlets of dry gas condenser connect air water separator 216, and air water separator 216 non-condensable gas outlets connect fluidized bed incinerator 11 non-condensable gas imports;

In the dry subsystem 22 of the 2nd grade of air flow bed of described combination drying system: drying air fan 224 outlet carrier gas interchanger 221 carrier gas inlet in parallel and the outer row's carrier gas inlet of dry gas condenser 225, the 221 carrier gas outlets of carrier gas interchanger connect air flow bed moisture eliminator 222 carrier gas inlet, 222 outlets of air flow bed moisture eliminator connect drying, dedusting device 223, the 223 carrier gas outlets of drying, dedusting device are connected to drying air fan 224 imports, 225 outlets of dry gas condenser connect air water separator 226, and air water separator 226 non-condensable gas outlets connect fluidized bed incinerator 11 non-condensable gas imports;

The present embodiment using method is as follows:

Incineration system: with the mud after auxiliary fuel and mummification in the interior common burning of fluidized bed incinerator 11; In the air compartment of fluidized bed incinerator 11, pass into the heat primary air of flue gas waste heat recovery system 3, auxiliary fuel and dewatered sludge are at the interior fluidized bed combustion of fluidized bed incinerator 11; Freeboard of fluidized bed at fluidized bed incinerator, the hot secondary air that adds flue gas waste heat recovery system 3, carry out flue gas disturbance oxygenating and strengthen burning, what pass into 2 generations of combination drying system carries out high temperature incineration deodorizing containing smelly non-condensable gas simultaneously, and 850～1100 ℃ of high-temperature flue gas of temperature that fluidized bed incinerator 11 produces enter hot precipitator 12 and carry out dedusting;

Described auxiliary fuel comprises coal water slurry that coal, coal gangue, high-concentration waste water make, oil fuel, combustible gas, biomass fuel one of them or its mixture; The coal water slurry that the high-concentration waste water of usining is made during as auxiliary fuel fluidized bed incinerator processed high-concentration waste water simultaneously; Described mud comprises domestic sludge, oil, chemical industry, printing and dyeing, papermaking, the industrial sludge such as brewages, and containing hydrocarbon wet solid fuel;

Combination drying system: the high-temperature flue gas after dedusting enters combination drying system 2, high-temperature flue gas in the carrier gas interchanger 211 of the dry subsystem 21 of the 1st grade of air flow bed with the heat exchange of cycling hot carrier gas partition, hot carrier gas absorbs heat temperature and is improved to 650～900 ℃, and high-temperature flue-gas enters flue gas waste heat recovery system 3 and continues to reclaim heat after being reduced to 250 ℃;

In the dry subsystem 21 of the 1st grade of air flow bed: the hot carrier gas after drying air fan 214 pressurizations is divided into two-way, wherein a road is sent into after input thermal source (high-temperature flue gas of hot precipitator 12) the partition heat exchange of the gentle fluidized bed drying subsystem 21 of carrier gas interchanger 211, sends into air flow bed drying machine 212 sludge-dryings, add the wet mud of air flow bed drying machine 212 after inner dispersion mechanism breaks up, by the strong convection current direct heating of the hot carrier gas mummification of carrier gas interchanger 211 heating, in wet mud, moisture evaporation becomes superheated vapour, hot carrier gas temperature is reduced simultaneously, hot carrier gas after cooling is carried all dewatered sludges and is entered drying, dedusting device 213 and carry out gas solid separation, mud is after drying discharged this subsystem and is delivered to fluidized bed incinerator 11 burnings or send into the dry subsystem of all the other air flow bed and continue depth drying, finally deliver to the dewatered sludge water-content 5～40% that fluidized bed incinerator 11 burns, preferred water-content 5～25%, hot carrier gas suction drying air fan 214 after drying, dedusting device 213 gas solid separation again pressurized circulation is dry, the hot carrier gas in another road after drying air fan 214 pressurizations is expelled to 215 condensations of dry gas condenser, heat of condensation offers the dry subsystem of next stage air flow bed (the 2nd grade of dry subsystem 22 of air flow bed) as input thermal source, condensed air-water mixture is after the separated moisture of air water separator 216, and non-condensable gas is sent into fluidized bed incinerator 11 and burned deodorizing,

In the dry subsystem 22 of the 2nd grade of air flow bed: the hot carrier gas after drying air fan 224 pressurizations is divided into two-way, wherein a road is sent into after input thermal source (vapor condensation heat in the hot carrier gas of the 1st grade of dry subsystem 21 discharges of air flow bed) the partition heat exchange of the gentle fluidized bed drying subsystem 22 of carrier gas interchanger 221, sends into air flow bed drying machine 222 sludge-dryings, add the wet mud of air flow bed drying machine 222 after inner dispersion mechanism breaks up, by the strong convection current direct heating of the hot carrier gas mummification of carrier gas interchanger 221 heating, in wet mud, moisture evaporation becomes superheated vapour, hot carrier gas temperature is reduced simultaneously, hot carrier gas after cooling is carried all dewatered sludges and is entered drying, dedusting device 223 and carry out gas solid separation, mud is after drying discharged this subsystem and is delivered to fluidized bed incinerator 11 burnings or send into the dry subsystem of all the other air flow bed and continue depth drying, finally deliver to the dewatered sludge water-content 5～40% that fluidized bed incinerator 11 burns, preferred water-content 5～25%, hot carrier gas suction drying air fan 224 after drying, dedusting device 223 gas solid separation again pressurized circulation is dry, the hot carrier gas in another road after drying air fan 224 pressurizations is expelled to 225 condensations of dry gas condenser, because the dry subsystem of the 2nd grade of air flow bed is the dry subsystem of last step air flow bed in the present embodiment, heat of condensation no longer offers the dry subsystem of next stage air flow bed as input thermal source, so steam is indirect or directly cooling by water coolant in discharge gas, condensed air-water mixture is after the separated moisture of air water separator 226, non-condensable gas is sent into fluidized bed incinerator 11 and is burned deodorizing,

In the dry subsystem of the adjacent two-stage air flow bed of this implementation column, vapor condensation heat in the hot carrier gas of the 1st grade of dry subsystem 21 discharges of air flow bed, provides heat as dry subsystem 22 sludge-dryings of next stage (the 2nd grade) air flow bed.The hot carrier gas temperature of the 1st grade of dry subsystem 21 discharges of air flow bed is 150 ℃, 110 ℃ of vapor condensation temperature, and main component is that superheated vapour contains a small amount of non-condensable gas; In the hot carrier gas of the 2nd grade of dry subsystem 22 discharges of air flow bed, vapor condensation temperature is 65 ℃, and main component is a large amount of non-condensable gas flue gases and part superheated vapour;

When the dry subsystem of all air flow bed is driven, all first to filling into flue gas in system, circulate.The dry generation after a large amount of superheated vapours of the dry subsystem 21 of first step air flow bed, along with the discharge of non-condensable gas gradually become take superheated vapour as cycling hot carrier gas dry.The dry generation after a large amount of superheated vapours of the dry subsystem 22 of second stage air flow bed, also will be to filling into flue gas or hot secondary air in system, to reduce the vapor condensation temperature in outer row's carrier gas, keep the heat transfer temperature difference of the carrier gas interchanger 221 hot carrier gas in both sides, simultaneously the heat of recovered flue gas and hot secondary air.Because vapor condensation temperature in the outer heat extraction carrier gas of the dry subsystem of two-stage air flow bed reduces gradually, heat energy obtains cascade utilization, and utilization ratio greatly improves.

The condensed hot water Yin Wendu of the 1st grade of dry subsystem 21 discharges of air flow bed is higher, and can be used as absorption refrigeration or heat pump set provides low-temperature receiver or thermal source to supply heating or refrigeration outward, cold-heat combined with feasible region.The condensed hot water temperature of the 2nd grade of dry subsystem 22 discharges of air flow bed is lower, is directly discharged into sewage network and processes.

Flue gas waste heat recovery system: the carrier gas interchanger 211 outlet flue gases in the dry subsystem 21 of first step air flow bed enter steam boiler 31, the heat exchange of flue gas partition is to water medium in boiler, and steam boiler 31 water mediums evaporate the outer heat supply of the steam producing or further with steam turbine, generate electricity; Steam boiler 31 outlet flue gases enter air preheater 32, the secondary air partition heating that the flue gas primary air that outlet comes to primary air fan, overfire air fan outlet come, it is interior as fluidisation and combustion-supporting gas that a wind after heating is sent into fluidized bed incinerator 11 air compartments, and the secondary air after heating is sent into fluidized bed incinerator 11 temperature adjustments; If the present embodiment burns the heat of auxiliary fuel and dewatered sludge generation only for meeting wet sludge anhydration institute heat requirement, can not establish steam boiler 31, if sludge calorific value is high, can be without auxiliary fuel;

Flue gas is processed blowdown system: air preheater 32 outlet flue gases enter flue gas and process blowdown system 4, at flue gas, process flue gas in blowdown system 4 and reach environmental protection standard through purifying treatment such as dedusting, de-Dioxins, desulphurization and denitration, depicklings, qualified flue gas harmless emission enters atmosphere;

Embodiment bis-

The employing of the present embodiment combination drying system comprises the dry subsystem of 3 grades of air flow bed and comes dewatered sludge then to carry out burning disposal.

Technical process connects as follows:

See Fig. 1, Fig. 3: comprise an incineration system 1, a combination drying system 2, a flue gas waste heat recovery system 3, a flue gas processing blowdown system 4.Incineration system 1 comprises fluidized bed incinerator 11, hot precipitator 12; Flue gas waste heat recovery system 3 comprises steam boiler 31, air preheater 32;

The combination drying system 2 that the present embodiment is comprised of the dry subsystem of three grades of air flow bed, first step air flow bed is dried subsystem 21, and second stage air flow bed is dried subsystem 22, and third stage air flow bed is dried subsystem 23.

Whole system connects sees Fig. 1, connects identical with embodiment 1, detailed description no longer, different is the intrasystem connection of combination drying:

In the dry subsystem 23 of 3rd level air flow bed of described combination drying system: drying air fan 234 outlet carrier gas interchanger 231 carrier gas inlet in parallel and the outer row's carrier gas inlet of dry gas condenser 235, the 231 carrier gas outlets of carrier gas interchanger connect air flow bed moisture eliminator 232 carrier gas inlet, 232 outlets of air flow bed moisture eliminator connect drying, dedusting device 233, the 233 carrier gas outlets of drying, dedusting device are connected to drying air fan 234 imports, 235 outlets of dry gas condenser connect air water separator 236, and air water separator 236 non-condensable gas outlets connect fluidized bed incinerator 11 non-condensable gas imports;

The using method of the present embodiment is as follows:

Incineration system: with embodiment 1

Combination drying system: the high-temperature flue gas after dedusting enters combination drying system 2, high-temperature flue gas in the carrier gas interchanger 211 of the dry subsystem of the 1st grade of air flow bed with the heat exchange of cycling hot carrier gas partition, hot carrier gas absorbs heat temperature and is improved, and high-temperature flue-gas enters flue gas waste heat recovery system 3 and continues to reclaim heat after reducing;

In the dry subsystem of the 2nd grade of air flow bed 22: the hot carrier gas after drying air fan 224 pressurizations is divided into two-way, wherein a road is sent into after input thermal source (vapor condensation heat in the hot carrier gas of the 1st grade of dry subsystem 21 discharges of air flow bed) the partition heat exchange of the gentle fluidized bed drying subsystem 22 of carrier gas interchanger 221, sends into air flow bed drying machine 222 sludge-dryings, add the wet mud of air flow bed drying machine 222 after inner dispersion mechanism breaks up, by the strong convection current direct heating of the hot carrier gas mummification of carrier gas interchanger 221 heating, in wet mud, moisture evaporation becomes superheated vapour, hot carrier gas temperature is reduced simultaneously, hot carrier gas after cooling is carried all dewatered sludges and is entered drying, dedusting device 223 and carry out gas solid separation, mud is after drying discharged this subsystem and is delivered to fluidized bed incinerator 11 burnings or send into the dry subsystem of all the other air flow bed and continue depth drying, finally deliver to the dewatered sludge water-content 5～40% that fluidized bed incinerator 11 burns, preferred water-content 5～25%, hot carrier gas suction drying air fan 224 after drying, dedusting device 223 gas solid separation again pressurized circulation is dry, the hot carrier gas in another road after drying air fan 224 pressurizations is expelled to 225 condensations of dry gas condenser, heat of condensation offers the dry subsystem (3rd level air flow bed is dried subsystem 23) of next stage air flow bed as input thermal source, condensed air-water mixture is after the separated moisture of air water separator 236, and non-condensable gas is sent into fluidized bed incinerator 11 and burned deodorizing,

In the dry subsystem of 3rd level air flow bed 23: the hot carrier gas after drying air fan 234 pressurizations is divided into two-way, wherein a road is sent into after input thermal source (vapor condensation heat in the hot carrier gas of the 2nd grade of dry subsystem 22 discharges of air flow bed) the partition heat exchange of the gentle fluidized bed drying subsystem 23 of carrier gas interchanger 231, sends into air flow bed drying machine 232 sludge-dryings, add the wet mud of air flow bed drying machine 232 after inner dispersion mechanism breaks up, by the strong convection current direct heating of the hot carrier gas mummification of carrier gas interchanger 231 heating, in wet mud, moisture evaporation becomes superheated vapour, hot carrier gas temperature is reduced simultaneously, hot carrier gas after cooling is carried all dewatered sludges and is entered drying, dedusting device 233 and carry out gas solid separation, mud is after drying discharged this subsystem and is delivered to fluidized bed incinerator 11 burnings or send into the dry subsystem of all the other air flow bed and continue depth drying, finally deliver to the dewatered sludge water-content 5～40% that fluidized bed incinerator 11 burns, preferred water-content 5～25%, hot carrier gas suction drying air fan 234 after drying, dedusting device 233 gas solid separation again pressurized circulation is dry, the hot carrier gas in another road after drying air fan 234 pressurizations is expelled to 235 condensations of dry gas condenser, because the dry subsystem of 3rd level air flow bed is the dry subsystem of last step air flow bed in the present embodiment, heat of condensation no longer offers the dry subsystem of next stage air flow bed as input thermal source, so steam is indirect or directly cooling by water coolant in discharge gas, condensed air-water mixture is after the separated moisture of air water separator 236, non-condensable gas is sent into fluidized bed incinerator 11 and is burned deodorizing,

In the dry subsystem of the adjacent three grades of air flow bed of this implementation column, vapor condensation heat in the hot carrier gas of the 1st grade of dry subsystem 21 discharges of air flow bed, as dry subsystem 22 sludge-dryings of next stage (the 2nd grade) air flow bed, provide heat, vapor condensation heat in the hot carrier gas of the 2nd grade of dry subsystem 22 discharges of air flow bed, provides heat as dry subsystem 23 sludge-dryings of next stage (3rd level) air flow bed.

The hot carrier gas temperature of the 1st grade of dry subsystem 21 discharges of air flow bed is 200 ℃, 150 ℃ of vapor condensation temperature, and main component is that superheated vapour contains a small amount of non-condensable gas; In the hot carrier gas of the 2nd grade of dry subsystem 22 discharges of air flow bed, vapor condensation temperature is 100 ℃, and main component is that superheated vapour contains a small amount of non-condensable gas; In the hot carrier gas that the dry subsystem 23 of 3rd level air flow bed is discharged, vapor condensation temperature is 65 ℃, and main component is a large amount of non-condensable gas flue gases and part superheated vapour;

When the dry subsystem of all air flow bed is driven, all first to filling into flue gas in system, circulate.The dry generation after a large amount of superheated vapours of the dry subsystem 22 of the dry subsystem 21 of first step air flow bed and second stage air flow bed, along with the discharge of non-condensable gas gradually become take superheated vapour as cycling hot carrier gas dry.The dry generation after a large amount of superheated vapours of the dry subsystem 23 of third stage air flow bed, also will be to filling into flue gas or hot secondary air in system, to reduce the vapor condensation temperature in outer row's carrier gas, keep the heat transfer temperature difference of the carrier gas interchanger 231 hot carrier gas in both sides, simultaneously the heat of recovered flue gas and hot secondary air.Because vapor condensation temperature in the outer heat extraction carrier gas of the dry subsystem of three grades of air flow bed reduces gradually, heat energy obtains cascade utilization, and utilization ratio greatly improves.

The condensed hot water Yin Wendu that the dry subsystem 22 of the dry subsystem 21 of first step air flow bed and second stage air flow bed is discharged is higher, and can be used as absorption refrigeration or heat pump set provides low-temperature receiver or thermal source to supply heating or refrigeration outward, cold-heat combined with feasible region.The condensed hot water temperature that the dry subsystem 23 of third stage air flow bed is discharged is lower, is directly discharged into sewage network and processes.

Flue gas waste heat recovery system: with embodiment 1

Flue gas is processed blowdown system: with embodiment 1

The various embodiments described above are only the preferred embodiment of the present invention, and in the art, every changes and improvements based in technical solution of the present invention, should not get rid of outside protection scope of the present invention.

Claims

1. a mud multiple-effect anhydration burning processing system, is characterized in that: comprise an incineration system, a combination drying system, a flue gas waste heat recovery system, a flue gas processing blowdown system;

In the dry subsystem of each air flow bed of described combination drying system, drying air fan exports carrier gas interchanger carrier gas inlet in parallel and dry gas condenser is arranged carrier gas inlet outward, carrier gas interchanger carrier gas outlet connects air flow bed moisture eliminator carrier gas inlet, air flow bed dryer export connects drying, dedusting device, drying, dedusting device carrier gas outlet is connected to drying air fan import, dry gas condensator outlet connects air water separator, and the outlet of air water separator non-condensable gas connects the import of fluidized bed incinerator non-condensable gas; In the dry subsystem of adjacent two-stage air flow bed, upper level dry gas condenser is simultaneously as next stage carrier gas interchanger.

2. mud multiple-effect anhydration burning processing system as claimed in claim 1, is characterized in that: the dry subsystem of described N level air flow bed, N=1～5, preferred N=2.

3. a using method for mud multiple-effect anhydration burning processing system as claimed in claim 1 or 2, is characterized in that:

The dry subsystem of described N level air flow bed, N=1～5, preferred N=2;

3) combination drying system: the high-temperature flue gas after dedusting enters combination drying system, high-temperature flue gas is in the carrier gas interchanger of the dry subsystem of the first air flow bed and the heat exchange of cycling hot carrier gas partition, hot carrier gas absorbs heat temperature and is improved, and high-temperature flue-gas enters flue gas waste heat recovery system and continues to reclaim heat after reducing;

In the dry subsystem of each air flow bed: the hot carrier gas after drying air fan pressurization is divided into two-way, and wherein a road is sent into after the input thermal source partition heat exchange of the gentle fluidized bed drying subsystem of carrier gas interchanger, sends into air flow bed drying machine sludge-drying, add the wet mud of air flow bed drying machine after inner mud diverting device is broken up, the strong convection current direct heating of the hot carrier gas mummification of being heated by carrier gas interchanger, in wet mud, moisture evaporation becomes superheated vapour, hot carrier gas temperature is reduced simultaneously, hot carrier gas after cooling is carried all dewatered sludges and is entered drying, dedusting device and carry out gas solid separation, mud is after drying discharged this subsystem and is delivered to fluidized bed incinerator burning or send into the dry subsystem of all the other air flow bed and continue depth drying, finally deliver to the dewatered sludge water-content 5～40% that fluidized bed incinerator burns, preferred water-content 5～25%, hot carrier gas suction drying air fan after drying, dedusting device gas solid separation again pressurized circulation is dry, the hot carrier gas in another road after drying air fan pressurization is expelled to dry gas condenser condenses, heat of condensation offers the dry subsystem of next stage air flow bed as input thermal source, condensed air-water mixture is after the separated moisture of air water separator, and non-condensable gas is sent into fluidized bed incinerator and burned deodorizing,

In the dry subsystem of adjacent two-stage air flow bed, upper level dry gas condenser is simultaneously as next stage carrier gas interchanger; Vapor condensation heat in 1～hot carrier gas that (N-1) the dry subsystem of level air flow bed is discharged, is the dry subsystem sludge-drying of next stage air flow bed heat is provided, and in hot carrier gas at different levels, vapor condensation temperature reduces gradually, and heat energy obtains cascade utilization; The dry subsystem of last step air flow bed is discharged steam in gas, by water coolant is indirectly or directly cooling, carrys out condensation separation, and the non-condensable gas after separation goes fluidized bed incinerator burning deodorizing;

The condensed hot water that the dry subsystem dry gas condenser of air flow bed at different levels is discharged is directly discharged into sewage network and processes, and also can be used as absorption refrigeration or heat pump set provides low-temperature receiver or thermal source cold-heat combined with feasible region for heating or refrigeration outward;

4) flue gas waste heat recovery system: the carrier gas heat exchanger exit flue gas in the dry subsystem of the first air flow bed enters steam boiler, the heat exchange of flue gas partition is to water medium in boiler, and steam boiler water medium evaporates the outer heat supply of the steam producing or further with steam turbine, generates electricity; Steam boiler outlet flue gas enters air preheater, the secondary air partition heating that the flue gas primary air that outlet comes to primary air fan, overfire air fan outlet come, it is interior as fluidisation and combustion-supporting gas that a wind after heating is sent into fluidized bed incinerator air compartment, and the secondary air after heating is sent into fluidized bed incinerator temperature adjustment; If burn the heat of auxiliary fuel and dewatered sludge generation only for meeting wet sludge anhydration institute heat requirement, can not establish steam boiler;

5) flue gas is processed blowdown system: air preheater outlet flue gas enters flue gas and processes blowdown system, at flue gas, process flue gas in blowdown system and reach environmental protection standard through purifying treatment such as dedusting, de-Dioxins, desulphurization and denitration, depicklings, qualified flue gas harmless emission enters atmosphere.

4. the using method of mud multiple-effect anhydration burning processing system as claimed in claim 3, is characterized in that:

Described combination drying system: the high-temperature flue gas that the dry subsystem input of first step air flow bed thermal source is fluidized bed incinerator, the dry subsystem input of all the other air flow bed at different levels thermal source is the heat of condensation that the dry subsystem of upper level air flow bed is discharged steam in hot carrier gas, and input thermal source is all in carrier gas interchanger and the heat exchange of hot carrier gas partition; The inner drying air fan that adopts of the dry subsystem of air flow bed at different levels circulates by carrier gas interchanger raising carrier gas temperature, the direct transmission of heat by convection of wet mud after hot carrier gas after temperature raising and mud diverting device are broken up, wet mud heat absorption obtains mummification, and carrier gas temperature is reduced; In the hot carrier gas that the dry subsystem of 1～N level air flow bed is discharged, vapor condensation temperature reduces step by step, by air flow bed, is dried the working pressure of the hot carrier gas of subsystem inner drying and is sneaked into non-condensable gas content and control.

5. the using method of the mud multiple-effect anhydration burning processing system as described in claim 3 or 4, is characterized in that:

Described hot carrier gas is the mixture that superheated vapour and non-condensable gas form, and superheated vapour is produced by wet sludge anhydration transpiring moisture.

6. the using method of the mud multiple-effect anhydration burning processing system as described in claim 3 or 4, is characterized in that:

Described by external complement, to enter in the dry subsystem of air flow bed non-condensable gas be air, flue gas one of them or its gas mixture, and preferred non-condensable gas is flue gas.

7. the using method of the mud multiple-effect anhydration burning processing system as described in claim 3 or 4, is characterized in that:

Described auxiliary fuel comprises coal water slurry that coal, coal gangue, high-concentration waste water make, oil fuel, combustible gas, biomass fuel one of them or its mixture.

8. the using method of the mud multiple-effect anhydration burning processing system as described in claim 3 or 4, is characterized in that:

Described mud comprises domestic sludge, oil, chemical industry, printing and dyeing, papermaking, the industrial sludge such as brewages, and containing hydrocarbon wet solid fuel.