CN219433266U - Combustor capable of simultaneously combusting pulverized coal and organic wastewater - Google Patents

Abstract

The utility model provides a burner capable of burning pulverized coal and organic wastewater simultaneously, which comprises a cavity, wherein a first sleeve layer, a cooling water jacket layer and a second sleeve layer are sequentially sleeved in the cavity from inside to outside, the first sleeve layer, the second sleeve layer and the cavity are hollow and are opened at the lower end, the first sleeve layer, the cooling water jacket layer and the second sleeve layer penetrate through the upper end of the cavity, the protruding heights of the first sleeve layer, the cooling water jacket layer and the second sleeve layer relative to the cavity are gradually reduced, a second gasifying agent channel is formed in the first sleeve layer, and an organic wastewater channel, a first gasifying agent channel and a pulverized coal channel are sequentially formed among the first sleeve layer, the cooling water jacket layer, the second sleeve layer and the cavity from inside to outside. The burner capable of burning pulverized coal and organic wastewater simultaneously provided by the utility model not only can treat the organic wastewater, but also can improve the carbon conversion rate of the gasifier, greatly reduce the energy consumption and the operation cost, and meet the environment-friendly requirement.

Description

Combustor capable of simultaneously combusting pulverized coal and organic wastewater

Technical Field

The utility model belongs to the technical field of energy conservation and environmental protection in coal chemical industry, and relates to a burner capable of burning pulverized coal and organic wastewater simultaneously.

Background

At present, an economical and effective practical method for industrial organic wastewater such as dye, pesticide, pharmacy and the like is still lacking for the low concentration, complex structure, large impurity content, poor biodegradability and high toxicity. Due to technical and economic reasons, the treatment difficulty is great by utilizing the traditional wastewater treatment methods such as an adsorption method, an extraction method and a biochemical method, and the higher and higher environmental protection requirements cannot be met. Therefore, there is an urgent need to develop techniques and methods for effectively treating highly toxic, difficult-to-biologically treated organic wastewater.

The organic wastewater mainly has the following characteristics: (1) high organic matter concentration. Its COD is generally above 2000mg/L, some are even up to several tens of thousands to hundreds of thousands mg/L, BOD is lower, and many waste water has poor biodegradability. (2) the component (A) is complex. Often contains production raw materials, side reaction products and various inorganic salts, and contains more toxic substances such as sulfide, cyanide, nitride, carbohydrate and the like. (3) high chroma and peculiar smell. Some waste waters emit a pungent malodor. Causing adverse effects to the surrounding environment. (4) acid, alkali and salts. The organic sewage has more compounds with strong acid or strong alkalinity, and has very strong corrosiveness and tends to have strong acid or strong alkalinity.

From the development trend of coal gasification technology in recent years, the dry powder coal feed gasification furnace has higher carbon conversion rate, low oxygen consumption and coal quality adaptability, and gradually occupies more gasification furnace technology markets. The dry powdered coal is fed into the gasifier and mixed with organic wastewater, and the organic wastewater is decomposed at high temperature by the gasifier to generate effective synthesis gas. The utility model can combine the advantages of treating organic wastewater and gasifying pulverized coal, is used in combination with a gasifier, and is core equipment in the field of coal gasification.

Disclosure of Invention

In view of the above-mentioned drawbacks of the prior art, the present utility model aims to provide a burner capable of burning pulverized coal and organic wastewater simultaneously, which is capable of disposing organic wastewater while pursuing a high carbon conversion rate, low oxygen consumption and coal quality adaptability, and has great significance in improving comprehensive energy efficiency of gasification furnaces in the field of coal chemical industry, reducing system investment and reducing carbon emission.

In order to achieve the above and other related objects, the utility model provides a burner capable of burning pulverized coal and organic wastewater simultaneously, comprising a cavity, wherein a first sleeve layer, a cooling water jacket layer and a second sleeve layer are sequentially sleeved in the cavity from inside to outside, the first sleeve layer, the second sleeve layer and the cavity are hollow and are open at the lower end, the first sleeve layer, the cooling water jacket layer and the second sleeve layer penetrate through the upper end of the cavity, the protruding heights of the first sleeve layer, the cooling water jacket layer and the second sleeve layer relative to the cavity are gradually reduced, a second gasifying agent channel is formed in the first sleeve layer, and an organic wastewater channel, a first gasifying agent channel and a pulverized coal channel are sequentially formed among the first sleeve layer, the cooling water jacket layer, the second sleeve layer and the cavity from inside to outside.

As described above, the burner capable of simultaneously burning pulverized coal and organic wastewater provided by the utility model has the following beneficial effects:

(1) The burner capable of simultaneously burning pulverized coal and organic wastewater combines the advantages of treating organic wastewater and pulverized coal gasification, can simultaneously burn dry pulverized coal and organic wastewater, can treat organic wastewater, can improve the carbon conversion rate of a gasification furnace, greatly reduces energy consumption, reduces operation cost and meets the green environment-friendly requirement.

(2) The multifunctional burner provided by the utility model can burn pulverized coal and organic wastewater simultaneously, and can perform harmless treatment on the organic wastewater under the condition of ensuring the safe operation of the gasifier. The organic matters are completely decomposed in the high-temperature (1350-1550 ℃) environment in the gasification furnace. Does not produce secondary pollution and harmful substances. And the organic matters and oxygen are subjected to chemical reaction, so that synthesis gas (CO and H2) can be generated, the method belongs to the green environment-friendly technology, and meets the energy-saving environment-friendly requirements.

(3) The multifunctional burner provided by the utility model can burn pulverized coal and organic wastewater simultaneously, the organic wastewater can reduce heat flux, the burner is protected, and the steam addition amount can be reduced.

(4) The multifunctional burner provided by the utility model can burn pulverized coal and organic wastewater simultaneously, the organic wastewater is sprayed into the hearth of the gasification furnace from the organic wastewater channel of the burner, and the initial thickness of the organic wastewater serosity is low, so that the organic wastewater serosity is easy to atomize. The inner side of the device is provided with a second gasifying agent flowing at a high speed and forms a certain intersection angle with the organic wastewater; the second gasifying agent atomizes the organic wastewater by means of impact, vibration and the like. The burner structure enables the organic wastewater to be fully chemically reacted with the gasifying agent.

Drawings

FIG. 1 is a schematic view showing the overall structure of a burner for simultaneously burning pulverized coal and organic wastewater according to the present utility model.

FIG. 2 shows a cross-sectional view of the region A-A of FIG. 1 in accordance with the present utility model.

Fig. 3 shows an enlarged cross-sectional view of the end of the region A-A of fig. 2 in the present utility model.

FIG. 4 is a schematic view showing the structure of a coaxial sleeve using a cooling water jacket layer as an outer sleeve of a burner capable of simultaneously burning pulverized coal and organic wastewater in the present utility model.

FIG. 5 is a schematic view of the region B-B of FIG. 4 in accordance with the present utility model.

Reference numerals

1A first Cooling Water Inlet

1B first Cooling Water Outlet

2 (2A, 2B) pulverized coal inlet

3 (3A, 3B) first gasifying agent inlet

4A second Cooling Water Inlet

4B second Cooling Water Outlet

5. Organic wastewater inlet

6. Second gasifying agent inlet

7. Coal dust channel

8. First gasifying agent channel

9. Organic waste water channel

10. Second gasifying agent channel

11. Cavity body

111. A first cavity section

112. A second chamber section

12. First sleeve layer

13. Cooling water jacket layer

14. Second sleeve layer

15. Inner isolation plate layer

16. Cooling water pipeline

Included angle between side wall of alpha second cavity section and central axis

Included angle between outlet end pipe wall and central axis of beta cooling water jacket layer

Included angle between outlet end pipe wall and central axis of gamma first sleeve layer

Angle of rotation angle between theta rotational flow sheet and central axis

Detailed Description

Please refer to fig. 1 to 5. It should be understood that the structures, proportions, sizes, etc. shown in the drawings are for illustration purposes only and should not be construed as limiting the utility model to the extent that it can be practiced, since modifications, changes in the proportions, or otherwise, used in the practice of the utility model, are not intended to be critical to the essential characteristics of the utility model, but are intended to fall within the spirit and scope of the utility model. Also, the terms such as "upper," "lower," "left," "right," "middle," and "a" and the like recited in the present specification are merely for descriptive purposes and are not intended to limit the scope of the utility model, but are intended to provide relative positional changes or modifications without materially altering the technical context in which the utility model may be practiced.

The utility model provides a burner capable of burning pulverized coal and organic wastewater simultaneously, as shown in fig. 1-5, which comprises a cavity 11, wherein a first sleeve layer 12, a cooling water jacket layer 13 and a second sleeve layer 14 are sleeved in the cavity 11 from inside to outside in sequence, the first sleeve layer 12, the second sleeve layer 14 and the cavity 11 are hollow and open at the lower end, the first sleeve layer 12, the cooling water jacket layer 13 and the second sleeve layer 14 penetrate through the upper end of the cavity 11, the protruding heights of the first sleeve layer 12, the cooling water jacket layer 13 and the second sleeve layer 14 relative to the cavity 11 are gradually reduced, a second gasifying agent channel 10 is formed in the first sleeve layer 12, and the first sleeve layer 12, the cooling water jacket layer 13, the second sleeve layer 14 and the cavity 11 are sequentially formed with an organic wastewater channel 9, a first gasifying agent channel 8 and a pulverized coal channel 7 from inside to outside.

In the above burner, as shown in fig. 1-3, the first sleeve layer 12 is disposed at the central axis of the cavity 11.

In the above burner, as shown in fig. 1-5, the first sleeve layer 12, the cooling water jacket layer 13, and the second sleeve layer 14 are concentrically arranged in the cavity 11.

In the above-described burner, as shown in fig. 1 and 4, the first sleeve layer 12, the cooling water jacket layer 13, and the second sleeve layer 14 are flanged as coaxial sleeves.

In the above burner, as shown in fig. 2 and 3, the cavity 11 is sequentially provided with a first cavity section 111 and a second cavity section 112 from top to bottom, the cross-sectional area of the first cavity section 111 is kept unchanged from top to bottom, and the cross-sectional area of the second cavity section 112 is gradually reduced from top to bottom.

In one embodiment, as shown in fig. 3, the included angle α between the sidewall of the second cavity section 112 and the central axis is 10 ° to 40 °, preferably 20 °.

In the above-mentioned burner, as shown in fig. 1 and 2, a cooling water pipeline 16 is disposed around the outer sidewall of the cavity 11, and a first cooling water inlet 1A and a first cooling water outlet 1B are respectively disposed on the cooling water pipeline 16. The outer side wall of the cavity 11 is surrounded by a cooling water pipeline 16, and a layer of protection metal wall is arranged on the periphery of the cooling water pipeline 16 in a coil pipe type cooling mode. The cooling water pipe 16 is connected to the outside through the first cooling water inlet 1A and the first cooling water outlet 1B. The cooling water can avoid the influence of high temperature on the burner, and cool the fire surface metal.

In one embodiment, as shown in fig. 1, the first cooling water inlet 1A and the first cooling water outlet 1B are provided on a cooling water pipe 16 located outside an upper outer sidewall of the cavity 11.

In a preferred embodiment, as shown in fig. 1, the first cooling water inlet 1A and the first cooling water outlet 1B are provided on a cooling water line 16 located outside an upper outer sidewall of the first chamber section 111.

In an embodiment, as shown in fig. 1, the first cooling water inlet 1A and the first cooling water outlet 1B are symmetrically distributed along the central axis of the cavity 11.

In the above-mentioned burner, as shown in fig. 1, the cavity 11 is further provided with a plurality of pulverized coal inlets 2, and the pulverized coal inlets 2 are communicated with the pulverized coal channel 7. The pulverized coal channel 2 is used for outputting pulverized coal through a burner.

In one embodiment, as shown in FIG. 1, the pulverized coal inlets 2 are 2-4.

In one embodiment, as shown in FIG. 1, the pulverized coal inlet 2 is provided on the top surface of the cavity 11.

In one embodiment, as shown in FIG. 1, the pulverized coal inlets 2 are symmetrically and uniformly distributed along the central axis of the cavity 11. And a space is kept between the adjacent pulverized coal inlets 2.

In the above burner, as shown in fig. 1 and 2, the second sleeve layer 14 is provided with a plurality of first gasifying agent inlets 3, and the first gasifying agent inlets 3 are communicated with the first gasifying agent channels 8. The first gasifying agent channel 8 is used for outputting a first gasifying agent through the burner, wherein the first gasifying agent is used for uniformly dispersing pulverized coal on one hand, fully mixing the pulverized coal and the gasifying agent, and carrying out chemical reaction with the pulverized coal on the other hand.

In one embodiment, as shown in fig. 1, the number of the first gasifying agent inlets 3 is 2-4.

In one embodiment, as shown in fig. 1, the first gasifying agent inlet 3 is disposed on the pipe wall of the pipe section of the cavity 11, where the second casing layer 14 protrudes.

In one embodiment, as shown in fig. 1, the first gasifying agent inlets 3 are symmetrically distributed along the central axis of the second casing layer 14. A space is kept between the adjacent first gasifying agent inlets 3.

In the above-mentioned burner, as shown in fig. 1, 2 and 3, the cooling water jacket layer 13 is hollow and has an inner separator layer 15 therein to form a circulation water path, the cooling water jacket layer 13 has a second cooling water inlet 4A and a second cooling water outlet 4B, and the second cooling water inlet 4A and the second cooling water outlet 4B are in communication with the circulation water path. The cooling water jacket layer 13 is used for inputting cooling water to cool the burner, specifically, the second cooling water inlet 4A and the second cooling water outlet 4B are connected with the outside. By adopting the jacket cooling mode, cooling water enters the cooling water jacket layer 13 through the second cooling water inlet 4A to cool the burner to fire surface metal, and is discharged from the second cooling water outlet 4B.

In an embodiment, as shown in fig. 1 and 4, the second cooling water inlet 4A and the second cooling water outlet 4B are disposed on the pipe wall of the pipe section of the cavity 11, where the cooling water jacket layer 13 protrudes from the pipe section of the cavity 11, and the second cooling water outlet 4B is located higher than the second cooling water inlet 4A.

In the above-mentioned burner, as shown in fig. 1, 2 and 4, the cooling water jacket layer 13 is further provided with an organic wastewater inlet 5, and the organic wastewater inlet 5 is communicated with the organic wastewater channel 9.

The organic wastewater channel 9 is used for spraying organic wastewater through a burner. Specifically, the organic wastewater is sprayed out of the organic wastewater channel 9, so that the thickness of a liquid film can be reduced, the atomization of the liquid is facilitated, the contact area with a gasifying agent is increased, and the conversion rate is improved.

In one embodiment, as shown in fig. 1 and 4, the organic wastewater inlet 5 is disposed on the pipe wall of the pipe section of the cavity 11, where the cooling water jacket layer 13 protrudes.

In the above burner, as shown in fig. 1, 2, 3 and 4, the upper end of the first casing layer 12 is provided with a second gasifying agent inlet 6, and the second gasifying agent inlet 6 is communicated with a second gasifying agent channel 10. The second gasifying agent channel 10 is used for outputting a second gasifying agent, namely combustion-supporting gas, through a combustor, so that on one hand, the organic wastewater is atomized through the modes of impact, vibration and the like, and on the other hand, combustion-supporting gas and the organic wastewater are provided for combustion reaction.

In the above burner, as shown in fig. 3, the included angle β between the outlet end pipe wall of the cooling water jacket layer 13 and the central axis is 10 to 30 °, preferably 20 °.

In the above burner, as shown in fig. 3, the included angle γ between the wall of the outlet end of the first casing layer 12 and the central axis is 5 ° to 20 °, preferably 10 °.

In the above-mentioned burner, as shown in fig. 5, a swirl plate is provided in the first gasifying agent passage 8, and the rotation angle θ of the swirl plate with respect to the central axis is 10 ° to 30 °, preferably 13 °. The swirl plate is welded in the first gasifying agent channel 8 by using a coaxial sleeve taking the cooling water jacket layer 13 as an outer sleeve.

The burner is installed on gasification furnace equipment.

The following describes a specific use of a burner for simultaneously burning pulverized coal and organic wastewater according to the present utility model with reference to FIGS. 1 to 5.

When a user obtains a burner capable of burning pulverized coal and organic wastewater simultaneously as shown in fig. 1-5, the burner is arranged on a gasification furnace, pulverized coal is sprayed into a reaction chamber of the gasification furnace through a pulverized coal channel of the burner, a first gasifying agent is sprayed into the reaction chamber of the gasification furnace through a first gasifying agent channel 8 of the burner, then organic wastewater is sprayed into the reaction chamber through an organic wastewater channel 9 of the burner, a second gasifying agent is sprayed into the reaction chamber through a second gasifying agent channel 10 of the burner, and gasification reaction is carried out, so that high-temperature coarse synthetic gas and molten ash slag are obtained. In use, the burner can be prevented from being influenced by high temperature through the cooling water pipeline 16, and the burner can be cooled by inputting cooling water through the cooling water jacket layer 13 to cool the fire surface metal.

Specifically, the pulverized coal is dry pulverized coal. The particle size of the pulverized coal is not smaller than 90 mu m and not smaller than 90wt% and the particle size of the pulverized coal is not smaller than 5 mu m and not smaller than 10wt%, preferably the particle size of the pulverized coal is not smaller than 90 mu m and not smaller than 90wt% and the particle size of the pulverized coal is not smaller than 5 mu m and not smaller than 10wt%. The water content of the pulverized coal is less than or equal to 5wt%.

Specifically, the first gasifying agent is a mixture of pure oxygen and steam, and the mass ratio of the steam to the pure oxygen is 0-6%, specifically, 0-3% and 3-6%. The steam is water vapor.

Specifically, the organic wastewater refers to organic wastewater or a mixture of coal dust and organic wastewater.

For example, the organic wastewater comprises the following components in percentage by mass: 0-65% of pulverized coal; 35-100% of organic wastewater.

Specifically, the second gasifying agent is pure oxygen. The pure oxygen refers to oxygen with purity of more than or equal to 99V percent.

Specifically, the mass ratio of the first gasifying agent to the pulverized coal is 0.6-1: 1kg/kg, specifically for example 0.6 to 0.8: 1. 0.8 to 1:1.

specifically, the volume ratio of the second gasifying agent (the volume is calculated according to the standard state) to the organic wastewater is 50-500 Nm ³ /m ³ Specifically according to the mass percentage of the combustible organic wastewater.

Specifically, the ratio of the organic wastewater to the pulverized coal is 0.05-0.6: 1, specifically, for example, 0.05 to 0.2: 1. 0.2 to 0.4: 1. 0.4 to 0.6:1.

in particular, all material flows can be independently regulated.

The gasification reaction is carried out in a conventional gasification furnace by mixing a proper amount of oxygen and steam. The reaction prolongs the residence time and the reaction time of the reaction materials in the reaction chamber, improves the turbulence effect of carbon particles in the gasification furnace, and improves the decomposition rate of organic volatile matters and organic wastewater in coal and the carbon conversion rate.

Specifically, the reaction formula in the gasification reaction is as follows:

C+O ₂ →CO ₂

C+CO ₂ →2CO

C+1/2O ₂ →CO

S+O ₂ +3H ₂ →H ₂ S+2H ₂ O

specifically, the temperature of the high-temperature crude synthesis gas is 1300-1700 ℃. The high temperature raw synthesis gas is high temperature raw synthesis gas containing hydrogen and carbon monoxide.

Specifically, the melting ash is formed by burning coal in a gasification furnace at high temperature and performing chemical reaction, volatile matters of organic matters in the coal and organic wastewater become gaseous products, and the residual ash forms flowable melting ash in a high-temperature state.

Further advantages and effects of the present utility model will become apparent to those skilled in the art from the disclosure of the present utility model, which is described by the following specific examples.

Example 1

The combustor is adopted to treat organic wastewater, pulverized coal and a first gasifying agent are sprayed into an existing gasifier through the combustor, the organic wastewater and a second gasifying agent are sprayed into the combustor, gasification reaction is carried out under the pressure of 4.3MPa (g) and the temperature of 1500 ℃, and high-temperature crude synthesis gas and molten ash with the temperature of 1450 ℃ are obtained. Wherein the pulverized coal is dry pulverized coal, the particle size of the pulverized coal is less than or equal to 90 mu m and less than or equal to 5 mu m and less than or equal to 10wt%, and the moisture content of the pulverized coal is less than or equal to 5wt%. The first gasifying agent is a mixture of pure oxygen and steam, and the mass ratio of the steam to the pure oxygen is 5%. The second gasifying agent is pure oxygen (oxygen content 99.7V%). The organic wastewater comprises the following components in percentage by mass: 60% of coal dust; 40% of organic wastewater. The mass ratio of the first gasifying agent to the pulverized coal is 0.787:1, kg/kg; the volume ratio of the second gasifying agent to the organic wastewater is 450:1Nm ³ /m ³ . The mass ratio of the organic wastewater to the coal dust is 0.13:1, kg/kg.

Example 2

The burner is adopted to treat organic wastewater, pulverized coal and a first gasifying agent are sprayed into an existing gasifier through the burner, the organic wastewater and a second gasifying agent are sprayed into the burner, gasification reaction is carried out at the pressure of 4.3MPa (g) and the temperature of 1400 ℃, and high-temperature crude synthesis gas and molten ash with the temperature of 1350 ℃ are obtained. Wherein the pulverized coal is dry pulverized coal, the particle size of the pulverized coal is less than or equal to 90 mu m and less than or equal to 5 mu m and less than or equal to 10wt%, and the water content of the pulverized coal is typically less than or equal to 5wt%. Both the first gasifying agent and the second gasifying agent are pure oxygen (oxygen content 99.7V%). The organic wastewater comprises the following components in percentage by mass: 0% of coal dust; 100% of organic wastewater. First airThe mass ratio of the chemical agent to the coal powder is 0.787:1, a step of; the volume ratio of the second gasifying agent to the organic wastewater is 50:1Nm ³ /m ³ . The mass ratio of the organic wastewater to the coal dust is 0.05:1, kg/kg.

Example 3

The high-temperature raw synthesis gas and the molten ash slag with the temperature of 1450 ℃ obtained in the example 1 are cooled after the reaction waste heat is recovered in the existing gasification furnace, and the medium-temperature raw synthesis gas and the medium-temperature ash slag are obtained. The temperature of the medium temperature raw synthesis gas was 700 ℃.

And (3) primarily washing the intermediate-temperature crude synthesis gas and the intermediate-temperature ash in the existing gasifier, cooling to obtain crude synthesis gas 1# and ash 1#, outputting the crude synthesis gas 1# and discharging the ash 1 #. Wherein the washing reagent is grey water. The mass ratio of raw synthesis gas # 1 to scrubbing agent addition was 0.825:1. the temperature of the raw synthesis gas output was 198 ℃.

Comparative example 1

The biological treatment technology is adopted to treat the organic wastewater. The biological treatment technology is to remove pollutant materials of the wastewater through self degradation of microorganisms, and is the most economical and effective treatment method for wastewater treatment at present. Biological processes generally employ activated sludge processes and biological membrane processes. The process operation of the activated sludge process (oxidation ditch, SBR and plug flow aeration tank) is stable and mature. The biomembrane method comprises a biological rotating disc and a contact oxidant biological aerated filter. The biological wastewater treatment technology is described by taking the main processes of anoxic, aerobic, flocculation precipitation, biological filtration and disinfection as examples.

The wastewater is pressurized by a pump and is sent to a regulating tank of a sewage treatment plant. The wastewater enters an adjusting tank for homogenizing and homogenizing, the adjusted wastewater enters an A/O system, enters an accident tank during an accident, and then gradually and controllably enters the adjusting tank. The regulated wastewater enters an A/O system to remove most of organic matters, ammonia nitrogen and TP in the wastewater, and the A/O effluent enters a secondary sedimentation tank to carry out mud-water separation. And (3) enabling the supernatant in the secondary sedimentation tank to enter a flocculation system, returning sludge to the anoxic tank, and nitrifying and returning sludge in the aerobic tank to the anoxic tank. And discharging the excess sludge into a sludge concentration tank.

And a flocculating agent and a coagulant aid are added into the flocculation reaction tank, so that COD and SS in the wastewater are further reduced. And (3) the effluent of the flocculation reaction tank enters a flocculation sedimentation tank for mud-water separation, and the sludge is discharged into a sludge concentration tank. And (3) enabling the effluent of the flocculation sedimentation tank to enter BAF, further removing COD and SS, and performing ultraviolet disinfection on the effluent of the BAF and discharging the effluent after reaching the standard.

BAF adopts effluent pool waste water as backwash water, and backwash effluent enters a backwash pool. After the wastewater is precipitated in the backwashing water tank, the supernatant fluid is pumped into a flocculation reaction tank, and the sludge-containing sewage is stirred and discharged to a sludge concentration tank.

Supernatant fluid of the sludge concentration tank enters an anoxic tank, and the sludge is dewatered and then is transported outwards.

Comparative test example 1

Comparing example 3 with the method of treating organic wastewater in comparative example 1, it can be found that the method in comparative example 1 has the following usage defects: (1) high requirements on organic wastewater: has lower COD, better biodegradability and low suspended matter and oil content. (2) The operation cost is high, the power consumption is high, the operation management is complex, the sludge is easy to deactivate after the sludge is cultured for a long time, and the sludge is required to be cultured again after the sewage treatment plant is operated again. (3) the occupied area is large.

While the method in example 3 forms organic wastewater by mixing the wastewater with pulverized coal by the burner, the organic wastewater is pyrolyzed into synthesis gas (CO+H) in the gasifier ₂ ) The synthesis gas is an important chemical raw material, and can be used for producing methanol, acetic acid, ethylene glycol, synthetic ammonia and other chemical raw materials. The method is a method for changing waste into valuable. The burner can decompose organic matters at the reaction temperature of the gasifier above 1350 ℃, so that tar, medium oil, phenol and heterocyclic organic matters can not be generated, and secondary pollution to the environment can not be caused. In addition, the method has low treatment operation cost, is not influenced by external factors, and is stable and reliable in operation.

In summary, the present utility model effectively overcomes the disadvantages of the prior art and has high industrial utility value.

The above embodiments are merely illustrative of the principles of the present utility model and its effectiveness, and are not intended to limit the utility model. Modifications and variations may be made to the above-described embodiments by those skilled in the art without departing from the spirit and scope of the utility model. Accordingly, it is intended that all equivalent modifications and variations of the utility model be covered by the claims, which are within the ordinary skill of the art, be within the spirit and scope of the present disclosure.

Claims (10)

1. The utility model provides a combustor that can burn fine coal and organic waste water simultaneously, its characterized in that, including cavity (11), first sleeve pipe layer (12), cooling water jacket layer (13), second sleeve pipe layer (14) have been cup jointed in proper order from interior to exterior in cavity (11), first sleeve pipe layer (12), second sleeve pipe layer (14), cavity (11) cavity and lower extreme opening, first sleeve pipe layer (12), cooling water jacket layer (13), second sleeve pipe layer (14) run through cavity (11) upper end just first sleeve pipe layer (12), cooling water jacket layer (13), second sleeve pipe layer (14) are for the protrusion height of cavity (11) gradually reduces in proper order, form second gasification agent passageway (10) in first sleeve pipe layer (12), cooling water jacket layer (13), second sleeve pipe layer (14), cavity (11) between form organic waste water passageway (9), first gasification agent passageway (8), buggy passageway (7) from interior to exterior in proper order.

2. The burner capable of simultaneously burning pulverized coal and organic wastewater according to claim 1, wherein the cavity (11) is provided with a first cavity section (111) and a second cavity section (112) in sequence from top to bottom, the cross-sectional area of the first cavity section (111) is kept unchanged from top to bottom, and the cross-sectional area of the second cavity section (112) is gradually reduced from top to bottom.

3. Burner for simultaneous combustion of pulverized coal and organic waste water according to claim 2, characterized in that the angle α between the side wall of the second chamber section (112) and the central axis is 10-40 °.

4. Burner capable of simultaneously burning pulverized coal and organic wastewater according to claim 1, wherein a cooling water pipeline (16) is arranged around the outer side wall of the cavity (11), and a first cooling water inlet (1A) and a first cooling water outlet (1B) are respectively arranged on the cooling water pipeline (16);

and/or the cavity (11) is also provided with a plurality of pulverized coal inlets (2), and the pulverized coal inlets (2) are communicated with the pulverized coal channel (7).

5. Burner for simultaneous combustion of pulverized coal and organic waste water according to claim 1, wherein the second casing layer (14) is provided with a plurality of first gasifying agent inlets (3), the first gasifying agent inlets (3) being in communication with the first gasifying agent channels (8).

6. Burner capable of burning pulverized coal and organic wastewater simultaneously according to claim 1, characterized in that the cooling water jacket layer (13) is hollow and internally provided with an inner isolation plate layer (15) to form a circulating waterway, the cooling water jacket layer (13) is provided with a second cooling water inlet (4A) and a second cooling water outlet (4B), and the second cooling water inlet (4A) and the second cooling water outlet (4B) are communicated with the circulating waterway.

7. Burner for simultaneous combustion of pulverized coal and organic waste water according to claim 1, characterized in that the cooling water jacket layer (13) is further provided with an organic waste water inlet (5), the organic waste water inlet (5) being in communication with the organic waste water channel (9).

8. Burner for simultaneous combustion of pulverized coal and organic waste water according to claim 1, wherein the upper end of the first casing layer (12) is provided with a second gasifying agent inlet (6), the second gasifying agent inlet (6) being in communication with a second gasifying agent channel (10);

and/or the included angle gamma between the outlet end pipe wall of the first sleeve layer (12) and the central axis is 5-20 degrees.

9. Burner for simultaneous combustion of pulverized coal and organic waste water according to claim 1, wherein the angle β between the outlet end wall of the cooling water jacket layer (13) and the central axis is 10-30 °.

10. Burner for simultaneous combustion of pulverized coal and organic waste water according to claim 1, characterized in that the first gasifying agent channel (8) is provided with swirl vanes, the angle of rotation θ of the swirl vanes to the central axis being 10-30 °.