JPS6020645B2 - Solid hydrocarbon combustion treatment method - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a combustion treatment method for solid hydrocarbons, such as fossil fuels or solid hydrocarbons produced by pyrolysis or catalytic cracking. The present invention relates to a method for burning the solid hydrocarbons described above, which can reduce nitrogen oxides contained in gas to nitrogen.

When fossil fuels or solid wastes are burned in industrial combustion equipment, significant amounts of nitrogen oxides are generally produced and are a major source of pollution to the environment. For this reason, it is necessary to remove the dilute nitrogen oxide in the combustion gas, but ``Currently,
As methods for removing nitrogen oxides from this combustion gas, there are two known methods: converting nitrogen oxides into nitrogen using a catalyst and converting nitrogen oxides into nitrogen using a reducing agent such as ammonia gas. In many cases, the catalyst is poisoned by substances in the combustion gas that act as catalyst poisons, reducing its performance.In order to remove this catalyst poisoning, the combustion gas is cooled to separate harmful substances. ~ A method of reheating the purified combustion gas and sending it to the denitrification reactor has been used, but it has the disadvantage of causing a large loss of thermal energy and requiring a huge amount of heat exchange equipment.On the other hand, the latter method The method requires the introduction of a considerable amount of ammonia in order to reduce nitrogen oxides with ammonia etc., resulting in a large waste from the standpoint of resources and energy.The purpose of the present invention is to overcome the drawbacks of the above-mentioned prior art. Removal of nitrogen oxides, such as nitrogen oxides, generated during the combustion of hydrocarbons, can be efficiently reduced and removed in the system without using reduction treatment with ammonia or catalysts. An object of the present invention is to provide a combustion treatment method.

In order to achieve the above object, the present invention aims to provide oxygen depletion by supplying part or all of the solid hydrocarbon to the first combustion zone when solid nitrogen-containing hydrocarbon is combusted in a reaction tower. The undigested solid hydrocarbons in the first combustion zone are then introduced into the second combustion zone to produce oxygen in excess of the theoretical combustion oxygen amount of the hydrocarbons, or equivalent air or air and oxygen. The combustion gas in the second combustion zone is further introduced into the first combustion zone, and the nitrogen oxides in the combustion gas are reduced by the solid hydrocarbons in the combustion zone. It is characterized by removal.

In the present invention, the solid nitrogen-containing hydrocarbons supplied to the first combustion zone may be a mixture of solid carbon and hydrocarbons, such as coal, coke, char obtained by carbonizing coal, petroleum refined Examples include coke-adhered catalysts.

In the present invention, in order to divide the reaction tower into a first combustion zone and a second combustion zone, a perforated plate or the like is provided at the boundary between these zones, and an overflow pipe is used to connect both zones, or a hole is placed near the boundary. An interpolation as described later may be provided.

It is preferable that pressurized gas is blown into both of the combustion zones from below the reaction tower to form a fluidized bed of solid nitrogen-containing hydrocarbons. The solid nitrogen-containing hydrocarbons supplied to the first combustion zone react with nitrogen oxides in the combustion gas supplied from the second combustion zone, and the nitrogen oxides in the combustion gas are converted into nitrogen. , is transferred from the first combustion zone to the second combustion zone, where it is completely combusted at an excess air ratio of 1.0 or more.

According to the present invention, it is no longer necessary to post-process the exhaust gas containing nitrogen oxide generated by the combustion of nitrogen-containing hydrocarbons as in the past, and the nitrogen-containing hydrocarbons can be efficiently combusted in-house along with the exhaust gas treatment. be able to. Hereinafter, typical embodiments of the present invention will be described with reference to the drawings. Figure 1 is a front sectional view of a combustion regeneration tower for a coked catalyst obtained during catalytic cracking of petroleum-based hydrocarbons.

In the figure, the regeneration tower 1 is equipped with an introduction pipe 2 for the coke-adhered catalyst from the reaction tower for catalyst decomposition, and a delivery pipe 3 for discharging the regenerated catalyst.
A perforated plate 4 forms a first combustion zone in the upper part of the tower, and a second combustion zone is formed between the perforated plate 4 and the perforated plate 4 for completely regenerating the coke-adhered catalyst, that is, completely burning the coke adhering to the catalyst. An overflow pipe 7 is provided to transport the coke-adhered catalyst 6 held by the perforated plate 4 to the combustion zone. The regeneration tower 1 also has a combustion gas supply port 8 at the bottom and a combustion gas discharge port 9 at the top. In the catalytic cracking of petroleum hydrocarbons, the amount of coke produced in the reaction tower ranges from 1% to over 30%, and an example of its composition is 8% by weight of carbon, 8% by weight of sulfur, Hydrogen 32% by weight, nitrogen 0. It also contains several hundred to dozens of other metals such as vanadium and nickel based on the weight of the neck.

This coke deposits on the catalyst surface within the reaction tower and reduces the catalytic reaction activity. At Z, the coke-adhered catalyst is moved and scaled through an inlet pipe 2 that connects the reaction tower and regeneration tower 1 in the illustrated apparatus, and is transferred to the first combustion zone (reduction zone). The perforated plate 4 prevents the coke-adhered catalyst from the reaction tower from being sent directly to the 22nd combustion zone below, and disperses the nitrogen monoxide-containing combustion gas from the lower part in the direction of the cross-sectional area inside the tower.
Fluidize the coke-adhered catalyst that has entered the cyclic zone. That is, nitrogen monoxide gas in the combustion gas that enters from the lower part of the porous plate 4 is dispersed within the combustion gas by the two porous plates 4, contacts the coke-adhered catalyst in a fluid state, and becomes nitrogen through the next reaction. is 00C → C020N2 However, this reaction takes place at a temperature of 40
It occurs when the temperature is above 000 and does not progress below that.

Theoretically, the reaction involves 2 moles of N03 and 1 mole of C, but the reaction in a fluidized state is preferably carried out in the presence of 4 moles or more of C per 1 mole of NO. In addition, the combustion gas from the second combustion zone usually contains about 1 to 33% oxygen in order to complete combustion in the second combustion zone, and this oxygen also prevents coke. Therefore, the amount of carbon in the coke on the perforated plate 4 is preferably maintained at least four times the amount consumed by oxygen and the molar amount of NO.In other words, on the perforated plate 4, oxygen and monoxide from below A carbon layer is formed which is larger than the amount of nitrogen gas by 4 and acts as a reduction zone.Furthermore, the temperature required for the reaction to occur is brought in by the combustion gas (600 to 10,000C) from the bottom, and the overflow reaction continues. The flow tube 7 is a first combustion zone (reduction zone).
The coke-adhered particles supplied to the overflow pipe are fed to the second combustion zone, and the particles are supplied to the second combustion zone by overflow from the upper end of the overflow pipe. Carbon substances not consumed by oxygen and nitric oxide in the first combustion zone fall through this overflow pipe 7 and enter the second combustion zone at the bottom, where they are combusted at an excess air ratio of 1.0 or more. The adhering coke is completely removed from the catalyst, or the coke is removed to a level where the catalytic activity returns, and the coke is returned to the original reaction stage through the delivery pipe 3. Although the above embodiment is a case in which a fluidized bed is formed in the reaction tower, the first combustion zone (reduction zone) does not need to be a fluidized bed, and may be a moving bed or a solid bed.

It should be noted that the coke-adhered catalyst introduced into the reduction zone does not need to be supplied in its entirety from the reaction tower; some of the coke-adhered catalyst is sent to the first combustion zone, and the rest is directly sent to the second combustion zone. The supply method of sending is fine. That is, the coked catalyst may be supplied to the first combustion zone so that carbon is present in an amount approximately four times the mole of NO and oxygen in the combustion gas, and the remaining carbon may be sent to the combustion zone for combustion treatment. . Next, an embodiment using an insert instead of an overflow pipe will be described.

FIG. 2 is a sectional view of a solid hydrocarbon fuel combustion furnace according to the invention. The lower part of the combustion furnace 1 is provided with a refueling gas supply port such as air or oxygen, a combustion gas discharge port 9 in the upper part, and a solid fuel supply port 2 and an ash extraction port 3 in the side wall.
An insert 12 is inserted between the solid fuel supply port 2 and the ash removal port 3 of the combustion furnace 1. Also, the insert 12 in the combustion furnace
A rectifying plate 5 is provided below. In the combustion furnace configured as described above, the solid fuel 6 is supplied from a quantitative supply device such as a screw feeder or a rotary valve through the fuel supply port 2 to the upper fluidized bed (first fluidized bed) of the internal poison 12. Due to the insert 12, the majority of the solid particles fed into the first fluidized bed are not able to move directly to the fluidized bed (second fluidized bed) located below the insert; Stagnant in a fluidized bed. The average grain size is 35 mm in a fluidized bed in a furnace with an inner diameter of 960 mm.
According to the experimental results of filling particles with a specific gravity of 3.2 and measuring the stagnation situation, it was found that the particles from the first fluidized bed to the second fluidized bed when the Uchiko Toxic Substance 12 was not placed in the waste. The amount of movement was 38 kg per second per cross-sectional area of the layer, and the similar amount of movement when the inner poison was installed was 4k9/s. In other words, the first fluidized bed particles cannot quickly move downward due to the interpolation material 12, and in the above experimental example, if 4 kg/s of solid fuel is supplied from the fuel supply port 2, the first fluidized bed particles cannot move downward quickly. The balance in the fluidized bed is balanced, and a fluidized bed with a constant bed height is formed. On the other hand, the solid fuel that has moved from the first fluidized bed to the second fluidized bed is fluidized and combusted by a combustion auxiliary gas such as air or oxygen supplied from the gas supply port 8. This auxiliary gas is supplied to the solid fuel present in the second fluidized bed in an amount greater than the generally known theoretical value required for the next reaction. C10Q → C02 4th 102 → 2LO S+Q → S02 2N102-? 2NO At this time, nitrogen in the solid fuel reacts with oxygen, albeit in a small amount, to generate nitrogen oxides.

In other words, the composition of the combustion gas generated in the second fluidized bed is C0
2, ratio ○, S02, NO, etc., and this combustion gas enters the first fluidized bed separated by an interpolant. In the first fluidized bed, a solid fuel mainly composed of carbon forms a fluidized bed, and the combustion gas from the second fluidized bed undergoes the following known reaction. C10C02ヱ2CO C10.

21C.

2 LO CH40 CO C1 QO CO 10 days C 12 NO KO C02 0 N2' Therefore, in the first fluidized bed, nitrogen monoxide in the combustion gas can be converted to nitrogen.

Furthermore, the gas leaving the first fluidized bed contains CO5C ratio, etc., but this can be easily converted to C02 and QO by introducing combustion-supporting gas from the upper part of the first fluidized bed. . The insert turtle 2 installed in the fluidized bed is used to divide the first fluidized bed and the second fluidized bed, and to introduce the solid hydrocarbon from the first fluidized bed to the second fluidized bed. It is established to adjust the speed to match the income and expenditure.

The shape of the insert is as shown in the cross-sectional view and plan view of FIGS. 3A and 3B.
Conical vane type pipes are formed by stacking many pipes in the same circular shape, as shown in Fig. 4 A and B.
A pipe grid type thing made by stacking bamboo in a grid pattern.
As shown in FIGS. 5A and 5B, a structure in which a large number of U-shaped tubes arranged in parallel in two stages is preferably used.
The insert 12 shown in FIG. 6 consists of a donut-shaped box 16 connected to both ends of two U-shaped tubes 16 arranged in parallel, and water holes provided on opposite sides of the box 16. Feed pipe 18
It is composed of a water delivery pipe 19, and a cutting board IT of the box body 16 for feeding and sending water to and from the two stages of U-shaped pipes 15, respectively. Since the combustion temperature (second fluidized bed zero temperature) of the insert is 700 to 1000 qo, it is generally preferable to cool the insert, and for this reason, the pipe 20 of the insert shown in FIG. Water, pressurized steam, or the like is passed as a coolant through the pipe tube 4 in the figure and the U-shaped pipe 15 in FIG. No need to feed by mouth;
In the first fluidized bed, oxygen and nitrogen monoxide in the combustion gas entering from the second fluidized bed are supplied so that the amount of carbon is about 4 times the mole, and the rest is directly fed to the second fluidized bed. It's okay.

Also, it goes without saying that when inserting a boiler tube for heat recovery into the first or second fluidized bed, the projected area per column cross-sectional area of the insert must be larger than that of the boiler tube. is desirable. Furthermore, there is no problem even if the insert is the boiler tube itself. In the above embodiment as well, nitrogen monoxide generated when nitrogen-containing solid fuel is burned is reduced with carbon in the solid fuel and converted into nitrogen, reducing nitrogen oxides in the combustion gas while reducing the amount of solid fuel. It can be burned.

Hereinafter, the present invention will be explained in more detail using examples.

Example 1 A reaction tower with an inner diameter of 10 and a length of 2,000 mm and an inner wall of 160 mm.
In a two-stage circulating flow reactor consisting of a regeneration tower with a length of 3,000 m and a catalyst circulation line connecting both devices, the lower part of the regeneration tower has a porosity of 1% and 20 holes with 20 pitches. Install a straightening plate raised above the straightening plate, connect a regenerated catalyst delivery pipe with a hole made of 24 willow ◇ at an angle of 30 degrees to the vertical on the side wall of the straightening slope 60 square meters above the straightening plate, and then install a rectifier plate 1,50 square meters above the straightening plate. A perforated plate with a porosity of 4% and 4 side holes at 20 pitches was installed at the position, and a coke-adhered catalyst introduction pipe with 24 holes was connected to the 10-board side wall of the perforated slope.

Inside the regeneration tower, a 24-square overflow pipe was provided through a perforated plate at a position opposite to the connection direction of the catalyst introduction pipe and delivery pipe, and at a distance of 5 m from the center of the melt. The lower end of the overflow pipe is connected to the 10th point on the rectifying slope, and the upper end is connected to the 40th point on the perforated plate. The temperature measurement seat was installed at a position 3 broadsides from the tower wall, 200 meters above the perforated plate and 25 meters above the rectifier plate, and the temperature was measured with a PR thermocouple. The catalyst has an average particle size of 2
The coke composition on the coke-adhered catalyst entering the regeneration tower from the inlet pipe is 87% carbon and 8% sulfur.
%, hydrogen 4% and nitrogen 0.8% (both by weight)
It is. The amount of coke on the catalyst is 4.5% by weight based on the catalyst.
It is. A combustion regeneration test of a coke-adhered catalyst was conducted using the above equipment specifications and under the following conditions.

Air supply amount to the second combustion zone: 12h3/h (converted to standard conditions) Excess air ratio Amount of catalyst discharged from the L03 delivery pipe: 30k9/h Fluidized bed temperature of the second combustion zone: 850pm ○ Second combustion zone combustion gas composition (Dry basis %) N2
C02 S02 0281.0 17.
5 0. Ridge 0.86 CNO○ of the first combustion zone (
molar ratio) 444 C/(NO10 of the first combustion zone)
2) (Molar ratio) 21 Under the above conditions, when the temperature (fluidized bed temperature) of the first combustion zone (reduction zone) was set to 700°C, the amount of NO in the dry combustion gas at the gas discharge port at the exit of the reduction zone was It was zero.

Example 2 Using the same equipment as in Example 1, when the fluidized bed temperature in the second combustion zone was set to 700 pm, the NO content in the dry combustion gas was 35 μm; When the temperature of the zone was set to 590 qo, the NO content in the dry combustion gas at the gas discharge port at the outlet of the zone was zero.

Example 3 A cap-type porous plate 4 (cap 1) as shown in FIG.
0 outside diameter 12 side, height 1 hole, wall thickness 3, with 3 holes 1 and 1 raised in 4 directions on the circumference at 5 feet in height) conducted a combustion test under the following conditions using the same equipment as in Example 1, and found that the NO content at the first combustion zone outlet gas outlet was zero.

Conditions: Amount of coke adhering catalyst introduced from the introduction pipe 30 [9/h Amount of coke adhering on the catalyst 3. a Weight % Combined amount of air supply in the second combustion zone 9.0 h3/h (converted to standard conditions) Excess air ratio 1.11 2nd
Fluidized bed temperature in the combustion zone Composition of combustion gas in the second combustion zone (% on dry basis) N2 C0
2 S02 0280.0 16.9
0.6 2.5 N clam pulp in dry scale gas
Fluidized bed temperature of 4-component first combustion zone 500
C/N in the first combustion zone (molar ratio) 361 C/(NO+02) in the first combustion zone (molar ratio) 1○ Example 4 Part of the combustion gas generated in the second combustion zone in Example 1 A part of the stainless steel pipe with an inner diameter of 6 mm is continuously air-filled, and the inner diameter is 25 mm.
The coke-adhered catalyst used in Example 1 (however, the coke adhesion amount is about 1% by weight to about 0.
Inlet NO for the amount of coke inside the regeneration tube when the fluidized bed temperature inside the regeneration tube is varied from 400 to 950 qo by filling the layer with 105% by weight of 105 qo from the outside of the tube and heating it from outside the tube in an electric furnace.
The molar ratio of the amount (C/NO) and the N at the inlet and outlet of the regeneration tube
O molar concentration ratio ([NO]OUT/[NO]rN: NO removal
Figure 7 shows the results of determining the relationship between

In addition, the regenerated cylinder speed in this case is 41 to 51 m/s.
It is. From the above results, it can be seen that generally the higher the temperature, the higher the C
It is clear that the higher the /NO molar ratio, the higher the denitrification rate. Example 5 Using the same equipment as in Example 4, the regeneration tube was filled with Pacific coal with an average particle size of 350 mm and a static bed height of 10 mm, and from the bottom of the pipe, the NO containing gas generated in the second combustion zone of Example 1 was charged. A quantity of combustion gas of 41 mm is passed through the cylinder at a cylinder velocity of 1 m/s, and is heated from outside the regeneration tube in an electric furnace to bring the temperature inside the regeneration tower to 900.
℃, the NO concentration at the outlet of the regeneration tube was zero.

Further, when the char produced by carbonizing the Pacific coal at 500° C. for 18 minutes in a nitrogen atmosphere was filled under the above conditions and treated under the above conditions, the NQ formicity at the outlet of the regeneration tube was zero.
Example 6 At the bottom of a combustion furnace with an inner diameter of 16 ribs and a length of 3,000 mm, a rectifier plate with a perforation ratio of 08%, 2 vertical holes and 20 pitches with perforations at the apex of a square was installed, and 200 combustion chambers were placed on the rectifier plate. Connect the ash removal pipe with a hole on the 24th side to the side wall of the adjacent furnace, and pass the gate valve on one side of the pipe to make the inner volume 2.

5 The pots are connected through holes.

As an insert, the conical vane type shown in Figure 3 was installed at a position 60 m above the current plate.The dimensions of the insert were 49 vane angles, 20 vane spacing, and a height of 40 m. It's an enemy ~ Is there two enemy mosquitoes at the intersection in the center of the vane? It has a hole. Additionally, each vane is fixed with a 1/4 inch pipe arranged in a cross shape at the top. Also, 1,0 on the rectifier plate of the combustion furnace
A fuel supply V pipe with 24 arm holes is connected to the side wall at the 00th rib at an angle of 30 degrees to the vertical, and one side of the pipe connects the gate valve, rotor refider, and fuel hopper. . In addition, nitrogen gas is supplied to the fuel hopper under pressure.
This prevents moisture in the combustion gas from adhering to the fuel supply pipe. Air was used as combustion auxiliary gas from the bottom of the rectifier plate. The temperature inside the combustion furnace was measured by inserting thermocouples into the center of the furnace at 30 and 80 points above the current plate. The height of the outside of the combustion furnace is 15 cm.
A zero temperature electric furnace was installed above the rectifier plate to raise the temperature and control the temperature inside the furnace.

The solid fuel used was Pacific coal, whose properties and composition are as follows. Grain: 0.4-0.7 Rib composition (dry weight%) C Day NS ○ Ash content 66.9 5.4 1.1 0.4 13.2
13.0 Furthermore, ``Pacific coal, which is a solid fuel, is
It was carbonized at 50°C for 3 hours.

. The amount of fuel supplied is 500g/, and the fuel has a particle size of 10
The ash content generated by Pacific coal combustion of 4 to 589 fm is 9
0% mixed. Fill the combustion furnace with a mixture of 11k9 internal fuel and ash, and 3. Air is supplied at a constant rate of 3 m3, heated from outside the furnace in an electric furnace, and when good combustion starts at the second fluidized bed temperature of about 60,000, a mixture of fuel and ash is supplied at a rate of 5,900 m, and the ash is removed from the ash extraction port. More than 4.58k
The ash was taken out at 9/h and the temperature at the bottom of the insert was 850°C.
When the NO concentration in the combustion furnace outlet gas was measured at a steady state at an upper temperature of 79,000, it was found to be zero. For comparison, when combustion was performed under the above conditions without installing an insert in the combustion furnace, the NG concentration in the combustion furnace outlet gas during steady state was 41%. At this time, each fluidized bed temperature was All 850o
It was o. Example 7 In the same combustion furnace as in Example 6, stainless steel tubes with a diameter of 8 sides as shown in the attached schematic diagram were stacked in 4 stages vertically and horizontally at a pitch of 15 candles each with a "stage spacing IQ". A pipe grid-shaped insert with a stainless steel plate and 155 mm diameter was installed as a shipboard, and combustion was performed under the same conditions as in Example 6. ``The NO concentration in the exhaust gas at the combustion furnace outlet was zero.

At this time, the temperature of the fluidized bed above and below the inner horizontal object was 700oC.
and 870:00. Example 8 As an insert for the combustion furnace of Example 6, a U-shaped tube shown in the attached FIG. 5 was used.

The U-shaped pipe has an outer i90 fence and an inner i90 fence, and a height of 30
The ribs are connected to hollow donut boxes. The interior of the donut box is divided into four rooms by partition plates in a direction perpendicular to the circumferential direction of the box,
A pair of water inlet pipes and a pair of water outlet pipes are open-connected to the central outer peripheral wall between the partition plates. On the top of this donut box is a fence from the inner diameter 4 side to the outer diameter 8 at the position of 15 m. Both ends of the U-shaped tube are open-connected to the top wall of the donut box so that it is located parallel to the partition plate at a 41Q side and a height of 10 meters, and then the inner diameter is Both ends of the U-shaped tube on the 4th side and the 8th outside diameter side are drilled into the upper wall of the donut box so that it is located parallel to the partition plate with a pitch of IQ and a height of 8mm. This insert is connected by a flange to a position on the rectifier plate on the 500 Yanagi side.As a solid fuel, Gatchi Saran vacuum residual oil is used at a decomposition temperature of 54,000 Yanagi.
The coke produced when the contact fraction was simulated was used. The composition ratio (weight %) of the coke is as follows. C H
N S Fe Ni SiQ Mg04.5 0
．． 2 0.04 0.4 14.4 3.3 49.9
6 27.2 The coke-adhered particles had an average particle size of 210 mm and a specific gravity of 3.4.

A combustion furnace was filled with 26 kg of the above particles, and air was supplied for 4Nm3noh from the lower gas supply port of the combustion furnace. While fluidizing, the temperature was raised in an external electric furnace. When the coke started burning at 480 oo, the fuel 1 of the coke-adhering particles from the supply port
The fuel was supplied at a rate of 8k9/h, and on the other hand, the regenerated particles were taken out from the ash outlet at 17k9/h, and the NO concentration in the gas at the combustion furnace outlet was measured at steady state after about 1 hour and found to be zero.

The fluidized bed temperature at steady state is 805q0 at the bottom and 750q0 at the top.
It was oo. In addition, 3.5X9 from the water supply pipe of the insert
When water at 13°C was introduced at a speed of 120°C from the delivery pipe
℃ water vapor was obtained. The temperatures of the upper and lower fluidized beds at this time were 703° C. and 000° C., respectively. At this time, the NO concentration in the combustion furnace outlet gas was zero. For comparison, the nitrogen concentration in the combustion furnace outlet gas under the above-mentioned conditions without the interpolator installed was 430 degrees, and the temperature of the upper and lower fluidized beds at this time was 0° C. in total. that's all,
According to the present invention, "solid hydrocarbons (or a mixture of solid hydrocarbons and carbon) are efficiently combusted, and the generated harmful gases such as nitrogen monoxide are reduced within the system to render them harmless." can do.

[Brief explanation of the drawing]

FIG. 1 is a cross-sectional view of a catalyst regeneration device showing one embodiment of the present invention, and FIG. 2 is a cross-sectional view of a combustion furnace showing another embodiment of the present invention. Figures A, B and Figure 5 A, B'
Also, a side sectional view and a plan view of the main parts showing various examples of the insert used in the combustion furnace shown in FIG. 2, respectively, and FIG.
A cross-sectional view showing an example of a perforated plate used in the device shown in the figure, No. 7
The figure is a diagram showing the experimental results of the method of the present invention. 1... Regeneration tower or combustion furnace, 2... Inlet pipe, 3...
Sending pipe, 4... Porous plate, 5... Rectifying plate, 8...
Coke adhesion catalyst, 7... Overflow pipe, 8... Combustion auxiliary gas supply port, 9... Combustion gas discharge port, 12...
・Interpolation. Younger brother's figure 2 figure 3 figure 4 figure 5 figure 5 figure 7

Claims (1)

[Claims] 1. When solid nitrogen-containing hydrocarbons are burned in a reaction tower, part or all of the solid hydrocarbons are supplied to the first combustion zone and reacted in an oxygen-deficient environment. Then, the undigested solid hydrocarbons in the first combustion zone are introduced into the second combustion zone, and the solid hydrocarbons that have not been digested in the first combustion zone are introduced into the second combustion zone, and are heated with oxygen in excess of the theoretical combustion oxygen amount of the hydrocarbons, or with an equivalent amount of air or a mixture of air and oxygen. Complete combustion is performed, and the combustion gas in the second combustion zone is further introduced into the first combustion zone to reduce and remove nitrogen oxides in the combustion gas with solid hydrocarbons in the combustion zone. A method for combustion treatment of solid hydrocarbons. 2. The solid hydrocarbon combustion treatment method according to claim 1, characterized in that the solid hydrocarbons in the first combustion zone are transferred to the second combustion zone by overflow. 3
Solid according to claim 1, characterized in that the introduction of solid hydrocarbons from the first combustion zone into the second combustion zone takes place via an interpolation separating the two zones. Hydrocarbon combustion treatment method. 4. The method for combustion treatment of solid hydrocarbons according to claim 1, characterized in that the combustion zone consists of a fluidized bed of solid hydrocarbons. 5. In claim 4, the fluidizing gas of the fluidized bed is combustion gas from a second combustion zone in the first combustion zone, and air or a mixed gas of oxygen and air in the second combustion zone. A method for combustion treatment of solid hydrocarbons, characterized in that: 6 In claim 5, it is provided that the amount of nitrogen monoxide and oxygen in the combustion gas supplied into the first combustion zone is
A method for combustion treatment of solid hydrocarbons, characterized in that solid hydrocarbons are supplied so that twice the molar amount or more of carbon is present in the first combustion zone. 7. The method for combustion treatment of solid hydrocarbons according to claim 3, characterized in that the insert comprises a conical vane. 8. A method for combustion treatment of solid hydrocarbons according to claim 3, characterized in that the insert comprises a pipe grid. 9. The method for combustion treatment of solid hydrocarbons according to claim 9, characterized in that a coolant is passed through the pipe or tube.