CN114321945A - Incineration method and system for high-water-content organic waste liquid - Google Patents
Incineration method and system for high-water-content organic waste liquid Download PDFInfo
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Abstract
The application relates to the field of environmental protection recycling, in particular to a method and a system for incinerating high-water-content organic waste liquid; the method comprises the following steps: obtaining high-water content organic waste liquid; concentrating the high-water-content organic waste liquid to obtain a concentrated solution of the organic waste liquid; adding coal powder into the concentrated solution of the organic waste liquid, stirring and mixing to obtain mixed slurry of water-coal-organic waste liquid concentrated solution; atomizing the mixed slurry, and then burning to obtain the flue gas waste heat; introducing N-grade air in the combustion stage; the system comprises: a waste liquid storage unit; the waste liquid storage unit is communicated with the waste liquid concentration unit; the stirring and mixing unit comprises a coal powder feeding part and a pulping part, the waste liquid concentration unit is communicated with the pulping part, and the coal powder feeding part is communicated with the pulping part; the combustion unit comprises a combustion furnace and an atomizer, and the atomizer is arranged in the combustion furnace; the air inlet unit is communicated with the combustion unit; realize the combustion of organic waste liquid and heat recovery.
Description
Technical Field
The application relates to the field of environmental protection recycling, in particular to a method and a system for incinerating high-water-content organic waste liquid.
Background
Along with the development of national economy and the increasing improvement of the living standard of people, various industries in China are rapidly developed, and the problem of the discharge of the waste water is increasingly obvious, wherein, in the industries of medicine, textile, petroleum, paper making and the like, thousands of tons of high-concentration and difficult-to-degrade industrial waste liquid are discharged; generally, wastewater contains BOD (Biochemical Oxygen Demand, abbreviated as BOD) and COD (chemical Oxygen Demand), and BOD is generally used5＞1000mg·L-1And COD > 2000 mg.L-1The waste water is called organic waste liquid, and the treatment method aiming at the organic waste liquid at present comprises a physical treatment method, a chemical treatment method, a biological treatment method and the like, but the methods all have the defects that the methods are possibly limited by equipment, materials, economy or high-concentration organic matters, salts and the like in the organic waste liquid, so that the organic waste liquid cannot be effectively treated in a large-scale, economical and reasonable mode.
However, the difficulty of large-scale treatment of organic waste liquid by the current incineration method is as follows:
(1) the water content is high, and the untreated organic waste liquid cannot be ignited at all because the water content in the waste liquid is up to more than 70 percent;
(2) the heat value is low, and because the content of combustible substances in the waste liquid is low, even if the concentrated liquid containing the concentrated organic waste liquid can be combusted, the combustion temperature is low, and harmful substances such as dioxin and the like are easily generated in the combustion process.
In order to overcome the above difficulties, when organic waste liquid is incinerated, auxiliary fuel is often required to be added to ensure the sufficient combustion of the organic waste liquid, and natural gas is generally considered as an ideal auxiliary fuel because of the advantages of high calorific value, low pollutant emission and the like. However, because natural gas resources in China are deficient and the price is high, the natural gas is used as an auxiliary fuel, the treatment cost is inevitably increased due to combustion, and the large-scale treatment of organic waste liquid is limited.
Therefore, how to treat the organic waste liquid on a large scale at low cost is a technical problem which needs to be solved urgently at present.
Disclosure of Invention
The application provides a method and a system for incinerating high-water-content organic waste liquid, which aim to solve the technical problem that the organic waste liquid is difficult to treat in a large scale with low cost in the prior art.
In a first aspect, the present application provides a method for incinerating a high-water content organic waste liquid, the method comprising:
obtaining high-water content organic waste liquid;
concentrating the high-water-content organic waste liquid to obtain a concentrated solution of the organic waste liquid;
adding coal powder into the concentrated solution, stirring and mixing to obtain mixed slurry of water-coal-organic waste liquid concentrated solution;
atomizing the mixed slurry, and then burning to obtain the waste heat of the burnt flue gas;
wherein N-grade air is introduced into the combustion stage, N is more than or equal to 3, and N is an integer.
Optionally, the number of air stages introduced in the combustion stage is three, and the total amount of air introduced in the combustion stage comprises the air volume of primary air, the air volume of secondary air) and the air volume of tertiary air; the air volume of the primary air accounts for 45-55% of the total air volume, the air volume of the secondary air accounts for 35-45% of the total air volume, and the air volume of the tertiary air accounts for 5-15% of the total air volume.
Optionally, the excess air coefficient of the air introduced in the combustion stage is 1.1-1.3.
Optionally, the mass ratio of water to coal powder in the mixed slurry is 30-40% to 60-70%;
the mass ratio of water to the organic waste liquid in the mixed slurry is 10-20% to 80-90%.
Optionally, the water content of the high-water content organic waste liquid is more than 70%, and the water content of the concentrated solution is 10% -20%.
Optionally, the ratio of the heat input power of the concentrated solution to the heat input power of the pulverized coal is 1: 2-5;
and/or the ratio of the flow rate of the concentrated solution to the flow rate of the pulverized coal is 2-10: 1.
Optionally, the mixed slurry is atomized and then combusted to obtain the flue gas waste heat after combustion, and then the heat exchange between the flue gas waste heat after combustion and the air for combustion is carried out to obtain the air after heat exchange.
The temperature of the air after heat exchange is 373K-473K.
In a second aspect, the present application provides a system for incinerating a high water content organic waste stream, said system being adapted to the method of the first aspect, said system comprising:
the waste liquid storage unit is used for storing the high-water-content organic waste liquid;
the liquid outlet of the waste liquid storage unit is communicated with the liquid inlet of the waste liquid concentration unit and is used for converting the high-water-content organic waste liquid into concentrated liquid containing concentrated organic waste liquid;
the liquid outlet of the waste liquid concentration unit is communicated with the liquid inlet of the stirring and mixing unit and is used for fully mixing the pulverized coal and the concentrated solution; the stirring and mixing unit comprises a coal powder feeding part and a pulping part, the pulping part comprises a first feeding hole and a second feeding hole, a discharge hole of the waste liquid concentration unit is communicated with the first feeding hole of the pulping part, and a discharge hole of the coal powder feeding part is communicated with the second feeding hole of the pulping part;
the combustion unit is provided with a feed inlet communicated with the discharge hole of the pulping part and comprises a combustion furnace and an atomizer, the feed inlet of the atomizer is communicated with the discharge hole of the pulping part, and the atomizer is arranged in the combustion furnace and used for atomizing and combusting mixed slurry;
the air inlet unit is used for providing air required by the combustion unit for combustion, and an air outlet of the air inlet unit is communicated with an air inlet of the combustion unit; the air inlet unit comprises a blower, a heat exchanger and N sections of ventilation pipelines, the heat exchanger comprises a first air inlet and a second air inlet, an air outlet of the blower is communicated with the first air inlet of the heat exchanger, an air outlet of the combustion furnace is communicated with the second air inlet of the heat exchanger, an air outlet of the heat exchanger is communicated with the air inlets of the N sections of ventilation pipelines, wherein N is more than or equal to 3 and is an integer.
Optionally, the N sections of ventilation ducts include a first ventilation duct, a second ventilation duct, and a third ventilation duct, air inlets of the first ventilation duct, the second ventilation duct, and the third ventilation duct are all communicated with an air outlet of the heat exchanger, and air outlets of the first ventilation duct, the second ventilation duct, and the third ventilation duct are all communicated with an air inlet of the combustion furnace.
Optionally, the heat exchanger includes first gas outlet and second gas outlet, the system still includes the tail gas processing unit, the air inlet intercommunication of tail gas processing unit the second gas outlet of heat exchanger, the first gas outlet intercommunication of heat exchanger first air pipe the second air pipe with the air intake of third air pipe.
Compared with the prior art, the technical scheme provided by the embodiment of the application has the following advantages:
according to the incineration method of the high-water-content organic waste liquid, the high-water-content organic waste liquid is concentrated into the low-water-content organic waste liquid, the coal powder is added into the concentrated liquid containing the concentrated organic waste liquid to form the water-coal-waste liquid compound, and the water-coal-waste liquid compound is atomized, so that the organic waste liquid is conveniently combusted and is fully combusted, the coal powder is used for replacing natural gas, and the low-cost large-scale treatment of the organic waste liquid is realized.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the invention and together with the description, serve to explain the principles of the invention.
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.
Fig. 1 is a schematic flow chart of a method provided in an embodiment of the present application;
fig. 2 is a schematic logical structure diagram of a system according to an embodiment of the present application;
fig. 3 is a schematic physical structure diagram of a system according to an embodiment of the present application;
the system comprises a waste liquid storage unit 1, a waste liquid concentration unit 2, a stirring and mixing unit 3, a coal powder feeding unit 31, a pulping unit 32, a combustion unit 4, a combustion furnace 41, an atomizer 42, an air inlet unit 5, a blower 51, a heat exchanger 52, a ventilation pipeline 53-N, a first ventilation pipeline 531, a second ventilation pipeline 532, a third ventilation pipeline 533, and a tail gas treatment unit 6.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present application clearer, the technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application, and it is obvious that the described embodiments are some embodiments of the present application, but not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
In one embodiment of the present application, as shown in fig. 1, a method for incinerating a high water content organic waste liquid, the method comprises:
s1, obtaining high-water-content organic waste liquid;
s2, concentrating the high-water-content organic waste liquid to obtain a concentrated solution of the organic waste liquid;
s3, adding coal powder into the concentrated solution, stirring and mixing to obtain mixed slurry of water-coal-organic waste liquid concentrated solution;
s4, atomizing the mixed slurry, and then burning to obtain the waste heat of the burned flue gas;
wherein N-grade air is introduced into the combustion stage, N is more than or equal to 3, and N is an integer.
In some optional embodiments, the number of air stages introduced in the combustion stage is three, and the total amount of air introduced in the combustion stage comprises the air volume of the primary air, the air volume of the secondary air and the air volume of the tertiary air; the air volume of the primary air accounts for 45-55% of the total air volume, the air volume of the secondary air accounts for 35-45% of the total air volume, and the air volume of the tertiary air accounts for 5-15% of the total air volume.
In the application, the positive effect that the air volume of the primary air accounts for 45% -55% of the total air volume is that in the range of the proportion, the primary combustion of the mixed slurry containing the water-coal-waste liquid compound can be ensured, the heat after the primary combustion can be conveniently and rapidly transferred, and further the combustion of the organic waste liquid and the primary recovery of the energy are preliminarily realized; when the value of the ratio is larger than the maximum value of the end point of the range, the adverse effect is that the air volume of excessive primary air can cause the mixed slurry to be burnt too fully, the heat is released too fast, and the heat is not recovered favorably.
The positive effect that the air quantity of the secondary air accounts for 35-45% of the total air quantity is that within the range of the proportion, the further combustion of the mixed slurry containing the water-coal-waste liquid compound can be ensured on the basis of the primary combustion, the heat after the further combustion can be conveniently and rapidly transferred, and further the combustion of the organic waste liquid and the further recovery of the energy are further realized; when the value of the ratio is larger than the maximum value of the end point of the range, the adverse effect is that the mixed slurry is burnt too fully due to the excessive air volume of the secondary air, the heat is released too fast, and the heat recovery is not facilitated, and when the value of the ratio is smaller than the minimum value of the end point of the range, the adverse effect is that the mixed slurry cannot be further burnt due to the excessively low air volume of the secondary air.
The positive effect that the air volume of the tertiary air accounts for 5% -15% of the total air volume is that within the range of the proportion, the mixed slurry containing the water-coal-waste liquid compound can be fully combusted, the heat after the full combustion can be conveniently and quickly transferred, and the complete combustion of the organic waste liquid and the full recovery of the energy are further realized; when the value of the ratio is larger than the maximum value of the end point of the range, the adverse effect is that the temperature of the mixed slurry is too low due to the excessive air volume of the tertiary air, meanwhile, part of heat is taken away by the excessive air volume of the tertiary air, the recovery of the heat is affected, and when the value of the ratio is smaller than the minimum value of the end point of the range, the adverse effect is that the excessive air volume of the tertiary air cannot promote the mixed slurry to be fully combusted.
In some optional embodiments, the excess air factor of the air introduced in the combustion stage is 1.1-1.3.
In the application, the positive effect that the excess air coefficient of the air introduced in the combustion stage is 1.1-1.3 is that in the excess air coefficient, the sufficient ventilation quantity in the combustion stage can be ensured, and meanwhile, the heat is not taken away by excessive air, so that the recovery of energy and the full operation of combustion are ensured; when the value of the coefficient is larger than the maximum value of the end point of the range, the adverse effect is that too much air takes away a large amount of heat, so that the energy cannot be effectively recovered, and the cost is increased; when the value of the coefficient is less than the minimum value at the end of the range, the adverse effect will be that too low a coefficient will result in low air content and no guarantee of adequate ventilation during the combustion phase.
In some alternative embodiments, the ratio of the mass of water to the mass of coal fines in the mixed slurry is 30% to 40% to 60% to 70%;
the mass ratio of water to the organic waste liquid in the mixed slurry is 10-20% to 80-90%.
In the application, the positive effect that the mass ratio of the water to the coal powder in the mixed slurry is 30-40% to 60-70% is that in the mass ratio range, the proper ratio of the water to the coal powder in the mixed slurry can be ensured, so that the coal powder can be fully combusted in the subsequent combustion stage, the water is changed into a steam state, the subsequent energy recovery is convenient, and the production cost is reduced; when the mass ratio is greater than the maximum of the end of the range, an adverse effect will result in too high a water content that will result in insufficient combustion of the mixed slurry and more difficult heat recovery, and when the mass ratio is less than the minimum of the end of the range, an adverse effect will be that too much coal fines will increase the cost of the auxiliary fuel required for combustion.
The mass ratio of the water to the organic waste liquid in the mixed slurry is 30-40% to 60-70%, and the positive effect is that the proper ratio of the water to the organic waste liquid can be ensured within the range of the mass ratio, so that the organic waste liquid can be fully combusted in the subsequent combustion stage, water is changed into a steam state, the subsequent energy recovery is facilitated, and the production cost is reduced; when the value of the mass ratio is larger than the maximum value of the end point of the range, the adverse effect is that the organic waste liquid of the mixed slurry cannot be sufficiently combusted due to excessively high water content, and the heat recovery is difficult.
In some optional embodiments, the high water content organic waste liquid has a moisture content of > 70% and the concentrated liquid has a moisture content of 10% to 20%.
In the application, the positive effect that the moisture content of the concentrated organic waste liquid is 10-20% is to ensure that the moisture content in the concentrated liquid containing the concentrated organic waste liquid is in a proper range, so as to ensure that the organic waste liquid can be combusted; when the value of moisture content is greater than the end point maximum value of this scope, the adverse effect that will lead to is too much moisture will lead to organic waste liquid can't burn, and when the content of moisture is less than the end point minimum value of this scope, the adverse effect that will lead to is too low moisture will lead to the unable conversion of organic waste liquid post-combustion heat to can't be by effectual recycle, lead to the heat waste, increase manufacturing cost.
In some optional embodiments, the ratio of the heat input power of the concentrated solution to the heat input power of the pulverized coal is 1: 2-5;
and/or the ratio of the flow rate of the concentrated solution to the flow rate of the pulverized coal is 2-10: 1.
In the application, the positive effect that the ratio of the heat input power of the concentrated solution containing the concentrated organic waste liquid to the heat input power of the pulverized coal is 1: 2-5 is that the organic waste liquid and the pulverized coal can be fully combusted in the ratio range, so that the organic waste liquid is fully combusted; when the value of the ratio is larger or smaller than the end value of the range, the adverse effect that the pulverized coal and the organic waste liquid cannot be sufficiently combusted is caused.
The positive effect that the ratio of the flow of the concentrated solution containing the concentrated organic waste liquid to the flow of the pulverized coal is 2-10: 1 is that the organic waste liquid and the pulverized coal can be fully mixed in the ratio range, and the subsequent combustion is fully guaranteed; when the value of the ratio is larger or smaller than the end value of the range, the adverse effect is that the organic waste liquid and the pulverized coal cannot be sufficiently mixed.
In some optional embodiments, the atomizing and post-combusting the mixed slurry to obtain the residual heat of the flue gas after combustion, and then, the method comprises:
s5, exchanging heat between the burnt flue gas waste heat and the air for combustion to obtain heat exchanged air;
the temperature of the air after heat exchange is 373K-473K.
In the application, the positive effect that the end point temperature of the air after heat recovery is 373K-473K is that under the condition of the temperature, the air before combustion next time can be sufficiently heated, and meanwhile, the heat can be recycled after combustion.
In one embodiment of the present application, as shown in fig. 2 and 3, there is provided a system for incinerating a high water content organic waste liquid, said system being adapted to said method, said system comprising:
the waste liquid storage unit 1 is used for storing high-water-content organic waste liquid, wherein the waste liquid storage unit 1 can be a waste liquid storage tank, a waste liquid storage tank or a waste liquid storage bottle;
a liquid outlet of the waste liquid storage unit 1 is communicated with a liquid inlet of the waste liquid concentration unit 2, and is used for converting the high-water-content organic waste liquid into a concentrated liquid containing the concentrated organic waste liquid, wherein the waste liquid concentration unit 2 can be a rotary evaporator;
the liquid outlet of the waste liquid concentration unit 2 is communicated with the liquid inlet of the stirring and mixing unit 3, and the stirring and mixing unit is used for fully mixing the pulverized coal and the concentrated solution; the stirring and mixing unit 3 comprises a coal powder feeding part 31 and a pulping part 32, the pulping part 32 comprises a first feeding hole and a second feeding hole, a discharge hole of the waste liquid concentration unit 2 is communicated with the first feeding hole of the pulping part 32, a discharge hole of the coal powder feeding part 31 is communicated with the second feeding hole of the pulping part 32, the pulping part 32 can be a pulping device such as a pulping device or a pulping tank, the coal powder feeding part 31 comprises a coal bunker and a coal mill, a discharge hole of the coal bunker is communicated with a feeding hole of the coal mill, and a discharge hole of the coal mill is communicated with a feeding hole of the pulping part 32;
the combustion unit 4, the feed inlet of the combustion unit 4 is communicated with the discharge outlet of the slurry preparing part 32, the combustion unit 4 comprises a combustion furnace 41 and an atomizer 42, the feed inlet of the atomizer 42 is communicated with the discharge outlet of the slurry preparing part 32, and the atomizer 42 is arranged in the combustion furnace 41 and is used for atomizing and combusting the mixed slurry;
the air inlet unit 5 is used for providing air required by the combustion unit 4 for combustion, and an air outlet of the air inlet unit 5 is communicated with an air inlet of the combustion unit 4; the air inlet unit 5 comprises a blower 51, a heat exchanger 52 and N sections of ventilation pipelines 53, the heat exchanger 52 comprises a first air inlet and a second air inlet, an air outlet of the blower 51 is communicated with the first air inlet of the heat exchanger 52, an air outlet of the combustion furnace 41 is communicated with the second air inlet of the heat exchanger 52, an air outlet of the heat exchanger 52 is communicated with the air inlets of the N sections of ventilation pipelines 53, wherein N is more than or equal to 3 and is an integer.
In some optional embodiments, the N sections of ventilation ducts 53 include a first ventilation duct 531, a second ventilation duct 532, and a third ventilation duct 533, air inlets of the first ventilation duct 531, the second ventilation duct 532, and the third ventilation duct 533 are all communicated with an air outlet of the heat exchanger 52, and air outlets of the first ventilation duct 531, the second ventilation duct 532, and the third ventilation duct 533 are all communicated with an air inlet of the combustion furnace 41.
In this application, through N section air pipe 53 including first air pipe 531, second air pipe 532 and third air pipe 533, utilize to realize the burning to the different degree of organic waste liquid to different air pipe control, for example: mix the thick liquid atomizing after, open first air pipe 531 and make the air get into, again will mix the thick liquid burning, realize the preliminary burning of mixing the thick liquid, open second air pipe 532 again, can close or maintain according to actual conditions and open first air pipe 531 this moment, thereby be the preliminary burning back of mixing the thick liquid and further burning, the rethread opens third air pipe 533, this moment can close or maintain and open first air pipe 531 and second air pipe 532 according to actual conditions, thereby make the organic waste liquid burning complete, and utilize the air pipe of different sections to realize thermal not equidimension's cyclic utilization.
In some optional embodiments, the heat exchanger 52 includes a first air outlet and a second air outlet, the system further includes an exhaust gas treatment unit 6, an air inlet of the exhaust gas treatment unit 6 is communicated with the second air outlet of the heat exchanger 52, and a first air outlet of the heat exchanger 52 is communicated with air inlets of the first ventilation duct 531, the second ventilation duct 532 and the third ventilation duct 533, wherein the exhaust gas treatment unit 6 may be a chimney, an exhaust gas kiln or an exhaust gas purifier.
In this application, through adopting tail gas processing unit 6, pass through the exhaust gas treatment unit with the waste gas after the organic waste liquid burning and discharge to guarantee steam or burning waste gas and discharge through tail gas processing unit 6, realize energy-concerving and environment-protective.
Example 1
As shown in fig. 1, a method for incinerating a high-water content organic waste liquid, the method comprising:
s1, obtaining high-water-content organic waste liquid;
s2, concentrating the high-water-content organic waste liquid to obtain a concentrated solution of the organic waste liquid;
s3, adding the coal powder into the concentrated solution containing the concentrated organic waste liquid, stirring and mixing to obtain mixed slurry of water-coal-organic waste liquid concentrated solution;
s4, atomizing the mixed slurry, and then burning to obtain the waste heat of the burned flue gas;
s5., exchanging heat between the waste heat of the burnt flue gas and the air for combustion to obtain the air after heat exchange;
the temperature of the air after heat exchange is 450K;
wherein N-grade air is introduced into the combustion stage, N is more than or equal to 3, and N is an integer.
The air stage number introduced in the combustion stage is three, and the total amount of air introduced in the combustion stage comprises the air volume of primary air, the air volume of secondary air and the air volume of tertiary air; the air volume of the primary air accounts for 50% of the total air volume, the air volume of the secondary air accounts for 40% of the total air volume, and the air volume of the tertiary air accounts for 10% of the total air volume.
The excess air ratio of the air introduced in the combustion stage was 1.2.
The mass ratio of water to coal powder in the mixed slurry is 35 percent to 65 percent;
the mass ratio of water to organic waste liquid in the mixed slurry is 15 percent to 85 percent.
The water content of the high-water content organic waste liquid is more than 70 percent, and the water content of the concentrated solution containing the concentrated organic waste liquid is 15 percent.
The ratio of the heat input power of the concentrated solution containing the concentrated organic waste liquid to the heat input power of the coal powder is 1: 3;
the ratio of the flow rate of the concentrated liquid containing the concentrated organic waste liquid to the flow rate of the pulverized coal is 6: 1.
As shown in fig. 2 and 3, a system for incinerating a high water content organic waste liquid, said system being adapted to said method, said system comprising:
the waste liquid storage unit 1 is used for storing high-water-content organic waste liquid;
the liquid outlet of the waste liquid storage unit 1 is communicated with the liquid inlet of the waste liquid concentration unit 2 and is used for converting the high-water-content organic waste liquid into concentrated liquid containing the concentrated organic waste liquid;
the liquid outlet of the waste liquid concentration unit 2 is communicated with the liquid inlet of the stirring and mixing unit 3 and is used for fully mixing the coal powder and the concentrated solution containing the concentrated organic waste liquid; the stirring and mixing unit 3 comprises a coal powder feeding part 31 and a pulping part 32, the pulping part 32 comprises a first feeding hole and a second feeding hole, a discharge hole of the waste liquid concentration unit 2 is communicated with the first feeding hole of the pulping part 32, and a discharge hole of the coal powder feeding part 31 is communicated with the second feeding hole of the pulping part 32;
the combustion unit 4, the feed inlet of the combustion unit 4 communicates with the discharge outlet of the pulping part 32, the combustion unit 4 includes a combustion furnace 41 and an atomizer 42, the feed inlet of the atomizer 42 communicates with the discharge outlet of the pulping part 32, the atomizer 42 is arranged in the combustion furnace 41, is used for carrying on the atomization and burning to mix the slurry;
the air inlet unit 5 is used for providing air required by the combustion unit 4 for combustion, and an air outlet of the air inlet unit 5 is communicated with an air inlet of the combustion unit 4; the air inlet unit 5 comprises a blower 51, a heat exchanger 52 and N sections of ventilation pipelines 53, the heat exchanger 52 comprises a first air inlet and a second air inlet, an air outlet of the blower 51 is communicated with the first air inlet of the heat exchanger 52, an air outlet of the combustion furnace 41 is communicated with the second air inlet of the heat exchanger 52, an air outlet of the heat exchanger 52 is communicated with the air inlets of the N sections of ventilation pipelines 53, wherein N is more than or equal to 3 and is an integer.
The N-section ventilation duct 53 includes a first ventilation duct 531, a second ventilation duct 532, and a third ventilation duct 533, air inlets of the first ventilation duct 531, the second ventilation duct 532, and the third ventilation duct 533 are all communicated with an air outlet of the heat exchanger 52, and air outlets of the first ventilation duct 531, the second ventilation duct 532, and the third ventilation duct 533 are all communicated with an air inlet of the combustion furnace 41.
The heat exchanger 52 comprises a first air outlet and a second air outlet, the system further comprises a tail gas processing unit 6, an air inlet of the tail gas processing unit 6 is communicated with the second air outlet of the heat exchanger 52, and a first air outlet of the heat exchanger 52 is communicated with air inlets of a first ventilating pipeline 531, a second ventilating pipeline 532 and a third ventilating pipeline 533.
Example 2
Comparing example 2 with example 1, example 2 differs from example 1 in that:
the temperature of the air after heat exchange is 373K;
the air volume of the primary air accounts for 55% of the total air volume, the air volume of the secondary air accounts for 40% of the total air volume, and the air volume of the tertiary air accounts for 5% of the total air volume.
The excess air ratio of the air introduced in the combustion stage was 1.1.
The mass ratio of water to coal powder in the mixed slurry is 30 percent to 60 percent;
the mass ratio of water to organic waste liquid in the mixed slurry is 10 percent to 90 percent.
The water content of the concentrated solution containing the concentrated organic waste liquid was 10%.
The ratio of the heat input power of the concentrated solution containing the concentrated organic waste liquid to the heat input power of the coal powder is 1: 5;
the ratio of the flow rate of the concentrated liquid containing the concentrated organic waste liquid to the flow rate of the pulverized coal is 2: 1.
Example 3
Comparing example 3 with example 1, example 3 differs from example 1 in that:
the temperature of the air after heat exchange is 473K;
the air volume of the primary air accounts for 45% of the total air volume, the air volume of the secondary air accounts for 40% of the total air volume, and the air volume of the tertiary air accounts for 15% of the total air volume.
The excess air ratio of the air introduced in the combustion stage was 1.3.
The mass ratio of water to coal powder in the mixed slurry is 40 percent to 70 percent;
the mass ratio of water to organic waste liquid in the mixed slurry is 20 percent to 80 percent.
The water content of the high-water content organic waste liquid is more than 70 percent, and the water content of the concentrated solution containing the concentrated organic waste liquid is 20 percent.
The ratio of the heat input power of the concentrated solution containing the concentrated organic waste liquid to the heat input power of the coal powder is 1: 2;
the ratio of the flow rate of the concentrated liquid containing the concentrated organic waste liquid to the flow rate of the pulverized coal is 10: 1.
Comparative example 1
Comparative example 1 and example 1 were compared, and comparative example 1 and example 1 were distinguished in that:
one-time ventilation is adopted.
Comparative example 2
Comparative example 2 is compared with example 1, and comparative example 2 differs from example 1 in that:
the air volume of the primary air accounts for 45% of the total air volume, the air volume of the secondary air accounts for 45% of the total air volume, and the air volume of the tertiary air accounts for 10% of the total air volume.
The excess air ratio of the air introduced in the combustion stage was 1.0.
The mass ratio of water to coal powder in the mixed slurry is 20 percent to 80 percent;
the mass ratio of water to organic waste liquid in the mixed slurry is 5 percent to 95 percent.
The water content of the organic waste liquid after the condensation is 5%.
The ratio of the heat input power of the concentrated solution containing the concentrated organic waste liquid to the heat input power of the coal powder is 1: 1;
the ratio of the flow rate of the concentrated liquid containing the concentrated organic waste liquid to the flow rate of the pulverized coal is 1: 1.
Comparative example 3
Comparative example 3 is compared with example 1, and comparative example 3 differs from example 1 in that:
the air volume of the primary air accounts for 55% of the total air volume, the air volume of the secondary air accounts for 35% of the total air volume, and the air volume of the tertiary air accounts for 10% of the total air volume.
The excess air ratio of the air introduced in the combustion stage was 1.5.
The mass ratio of water to coal powder in the mixed slurry is 50 percent to 50 percent;
the mass ratio of water to organic waste liquid in the mixed slurry is 30 percent to 70 percent.
The water content of the concentrated solution containing the concentrated organic waste liquid was 25%.
The ratio of the heat input power of the concentrated solution containing the concentrated organic waste liquid to the heat input power of the coal powder is 1: 6;
the ratio of the flow rate of the concentrated liquid containing the concentrated organic waste liquid to the flow rate of the pulverized coal is 11: 1.
Related experiments:
the heat loss rate and the organic waste liquid residue rate in the processes of examples 1 to 3 and comparative examples 1 to 2 were counted, and the results are shown in table 1.
Test methods of the related experiments:
heat loss rate: the heat generated by the post-combustion furnace 41, the heat exchanged by the heat exchanger 52, the heat loss amount of the pipe itself, and the theoretical total combustion amount of the organic waste liquid are counted, respectively, and the heat loss rate is 1- (theoretical total combustion amount-heat generated by the combustion furnace 41-heat exchanged by the heat exchanger 52-heat loss amount of the pipe itself)/theoretical total combustion amount.
Organic waste liquid residual rate: the weight of the concentrated solution containing the concentrated organic waste liquid added before the combustion and the weight of the organic waste liquid after the combustion treatment are counted, and the organic waste liquid residual rate is the weight of the organic waste liquid after the combustion treatment/the weight of the concentrated solution containing the concentrated organic waste liquid.
TABLE 1
| Categories | Heat loss Rate (%) | Residual rate (%) of organic waste liquid |
| Example 1 | 15 | 0.5 |
| Example 2 | 17 | 0.4 |
| Example 3 | 18 | 0.8 |
| Comparative example 1 | 31 | 3.2 |
| Comparative example 2 | 25 | 2.3 |
| Comparative example 3 | 24 | 2.5 |
Table 1 specific analysis:
the heat loss rate refers to the loss condition of heat generated by combustion of the organic waste liquid after the organic waste liquid is treated by the method and the system, and when the heat loss rate is lower, the higher the utilization degree of the heat in the method and the system is.
The organic waste liquid residual rate refers to the residual degree of the organic waste liquid after being treated by the method and the system, and the lower the organic waste liquid residual rate is, the more complete the combustion degree of the organic waste liquid is.
From the data of examples 1-3, it can be seen that:
by adopting the method, the high-water-content organic waste liquid is concentrated into the low-water-content organic waste liquid, the coal powder is added into the concentrated liquid containing the concentrated organic waste liquid to form a water-coal-waste liquid compound, the water-coal-waste liquid compound is atomized and then combusted, the combusted heat is fully utilized, the heat is fully recovered, and meanwhile, the organic waste liquid is completely combusted.
From the data of comparative examples 1-3, it can be seen that:
if the ventilation mode of the application is not adopted or the technological condition parameters of the application are exceeded, the heat loss after the organic waste liquid is combusted is caused, and part of the organic waste liquid is incompletely combusted.
One or more technical solutions in the embodiments of the present application at least have the following technical effects or advantages:
(1) according to the method provided by the embodiment of the application, the high-water-content organic waste liquid is concentrated into the low-water-content organic waste liquid, the coal powder is added into the concentrated liquid containing the concentrated organic waste liquid to form the water-coal-waste liquid compound, and the water-coal-waste liquid compound is atomized, so that the organic waste liquid is conveniently combusted and is fully combusted, and the coal powder is used for replacing natural gas, so that the low-cost large-scale treatment of the organic waste liquid is realized.
(2) According to the method provided by the embodiment of the application, as the pulverized coal is used as the auxiliary fuel, most of the pulverized coal in China is the low-grade coal or the surface coal, the pulverized coal is converted into the pulverized coal, and the effective utilization of the low-grade coal or the surface coal can be increased.
(3) The system that this application embodiment provided, through adopting N section air pipe 53 including first air pipe 531, second air pipe 532 and third air pipe 533, can effectually provide the air in the organic waste liquid combustion process, make the organic waste liquid fully burn.
(4) The system provided by the embodiment of the application realizes heat control of air entering the combustion furnace 41 through the heat exchanger 52, and can further improve the recovery and utilization degree of heat.
It is noted that, in this document, relational terms such as "first" and "second," and the like, may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.
The foregoing are merely exemplary embodiments of the present invention, which enable those skilled in the art to understand or practice the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. A method for incinerating a high-water content organic waste liquid, comprising:
obtaining high-water content organic waste liquid;
concentrating the high-water-content organic waste liquid to obtain a concentrated solution of the organic waste liquid;
adding coal powder into the concentrated solution, stirring and mixing to obtain mixed slurry of water-coal-organic waste liquid concentrated solution;
atomizing the mixed slurry, and then burning to obtain the waste heat of the burnt flue gas;
wherein N-grade air is introduced into the combustion stage, N is more than or equal to 3, and N is an integer.
2. The method according to claim 1, wherein the number of the air stages introduced in the combustion stage is three, and the total amount of the air introduced in the combustion stage comprises the air volume of primary air, the air volume of secondary air and the air volume of tertiary air;
the air volume of the primary air accounts for 45-55% of the total air volume, the air volume of the secondary air accounts for 35-45% of the total air volume, and the air volume of the tertiary air accounts for 5-15% of the total air volume.
3. The method according to claim 1 or 2, wherein the excess air ratio of the air introduced in the combustion stage is 1.1 to 1.3.
4. The method according to claim 1, wherein the mass ratio of water to coal powder in the mixed slurry is 30-40% to 60-70%;
the mass ratio of water to the organic waste liquid in the mixed slurry is 10-20% to 80-90%.
5. The method according to claim 1, wherein the high water content organic waste liquid has a moisture content of > 70% and the concentrate has a moisture content of 10% to 20%.
6. The method according to claim 1, wherein the ratio of the heat input power of the concentrated solution to the heat input power of the pulverized coal is 1: 2-5;
and/or the ratio of the flow rate of the concentrated solution to the flow rate of the pulverized coal is 2-10: 1.
7. The method according to claim 1, wherein the mixing slurry is atomized and post-combusted to obtain the residual heat of the flue gas after combustion, and then the method comprises the following steps:
exchanging heat between the waste heat of the combusted flue gas and the air for combustion to obtain air after heat exchange;
the temperature of the air after heat exchange is 373K-473K.
8. A system for incineration of high water content organic waste liquid, characterized in that the system is adapted to the method according to any of claims 1-7, the system comprising:
the waste liquid storage unit (1) is used for storing high-water-content organic waste liquid;
the liquid outlet of the waste liquid storage unit (1) is communicated with the liquid inlet of the waste liquid concentration unit (2) and is used for converting the high-water-content organic waste liquid into concentrated liquid containing concentrated organic waste liquid;
the liquid outlet of the waste liquid concentration unit (2) is communicated with the liquid inlet of the stirring and mixing unit (3) and is used for fully mixing the pulverized coal and the concentrated solution; the stirring and mixing unit (3) comprises a coal powder feeding part (31) and a pulping part (32), the pulping part (32) comprises a first feeding hole and a second feeding hole, a discharge hole of the waste liquid concentrating unit (2) is communicated with the first feeding hole of the pulping part (32), and a discharge hole of the coal powder feeding part (31) is communicated with the second feeding hole of the pulping part (32);
the combustion unit (4), the feed inlet of the combustion unit (4) is communicated with the discharge outlet of the slurry making part (32), the combustion unit (4) comprises a combustion furnace (41) and an atomizer (42), the feed inlet of the atomizer (42) is communicated with the discharge outlet of the slurry making part (32), and the atomizer (42) is arranged in the combustion furnace (41) and is used for atomizing and combusting the mixed slurry;
the air inlet unit (5), the air outlet of the air inlet unit (5) is communicated with the air inlet of the combustion unit (4) and is used for providing air required by the combustion unit (4) for combustion; the air inlet unit (5) comprises a blower (51), a heat exchanger (52) and N sections of ventilation pipelines (53), wherein the heat exchanger (52) comprises a first air inlet and a second air inlet, an air outlet of the blower (51) is communicated with the first air inlet of the heat exchanger (52), an air outlet of the combustion furnace (41) is communicated with the second air inlet of the heat exchanger (52), an air outlet of the heat exchanger (52) is communicated with the air inlets of the N sections of ventilation pipelines (53), wherein N is more than or equal to 3, and N is an integer.
9. The system of claim 8, wherein the N-segment ventilation duct (53) comprises a first ventilation duct (531), a second ventilation duct (532) and a third ventilation duct (533), wherein air inlets of the first ventilation duct (531), the second ventilation duct (532) and the third ventilation duct (533) are communicated with an air outlet of the heat exchanger (52), and air outlets of the first ventilation duct (531), the second ventilation duct (532) and the third ventilation duct (533) are communicated with an air inlet of the burner (41).
10. The system of claim 9, wherein the heat exchanger (52) comprises a first air outlet and a second air outlet, the system further comprising an exhaust gas treatment unit (6), wherein an air inlet of the exhaust gas treatment unit (6) is communicated with the second air outlet of the heat exchanger (52), and wherein the first air outlet of the heat exchanger (52) is communicated with air inlets of the first ventilation duct (531), the second ventilation duct (532) and the third ventilation duct (533).
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