METHOD FOR DRYING CATALYTIC OXIDATION FURNACE

Abstract

A method for drying a catalytic oxidation furnace, the method including: 1) charging a feed gas including oxygen and natural gas, and a temperature control gas to a catalytic oxidation furnace loaded with a catalyst; 2) preheating a mixed gas including the feed gas and the temperature control gas to increase the temperature of the mixed gas, and stopping the preheating when the temperature of the mixed gas achieves a temperature adapted to trigger the oxidation reaction of the mixed gas; and 3) within the molar ratio of the temperature control gas to the feed gas being 0.1-7:1.3-1.6, reducing the molar ratio of the temperature control gas to the feed gas such that the rise of the temperature of the mixed gas conforms to the temperature rising rate of the drying-out curve of a heat insulation refractory material of the catalytic oxidation furnace.

Claims

1. A method for drying a catalytic oxidation furnace, the method comprising: 1) charging a feed gas comprising oxygen and natural gas, and a temperature control gas capable of reducing a reaction temperature rising rate to a catalytic oxidation furnace loaded with a catalyst, wherein a molar ratio of the oxygen to the natural gas in the feed gas is 0.3-0.6:1, and a molar ratio of the temperature control gas to the feed gas is 0.1-7:1.3-1.6; 2) preheating a mixed gas comprising the feed gas and the temperature control gas to increase a temperature of the mixed gas, and stopping the preheating when the temperature of the mixed gas achieves a temperature adapted to trigger an oxidation reaction of the mixed gas; and 3) within the molar ratio of the temperature control gas to the feed gas being 0.1-7:1.3-1.6, reducing the molar ratio of the temperature control gas to the feed gas so that a rise of the temperature of the mixed gas conforms to a temperature rising rate of a drying-out curve of a heat insulation refractory material of the catalytic oxidation furnace, and stopping charging the temperature control gas when the reaction temperature achieves the working temperature of the catalytic oxidation furnace.

2. The method of claim 1, wherein 3) further comprises adjusting the molar ratio of the oxygen to the natural gas in the feed gas while reducing the molar ratio of the temperature control gas to the feed gas.

3. The method of claim 1, wherein in 1), the temperature control gas is an inert gas, N.sub.2, CO.sub.2, water vapor, or a mixture thereof.

4. The method of claim 2, wherein in 1), the temperature control gas is an inert gas, N.sub.2, CO.sub.2, water vapor, or a mixture thereof.

5. The method of claim 1, wherein in 2), the temperature adapted to trigger an oxidation reaction of the mixed gas is between 300 and 600° C.

6. The method of claim 2, wherein in 2), the temperature adapted to trigger an oxidation reaction of the mixed gas is between 300 and 600° C.

7. The method of claim 1, wherein 3) further comprises increasing the molar ratio of the oxygen to the natural gas in the feed gas while reducing the molar ratio of the temperature control gas to the feed gas.

8. The method of claim 2, wherein 3) further comprises increasing the molar ratio of the oxygen to the natural gas in the feed gas while reducing the molar ratio of the temperature control gas to the feed gas.

9. The method of claim 1, wherein in 3), the molar ratio of the temperature control gas to the feed gas is reduced from 7:1.3-1.6 to 0-5:1.3-1.6 when the temperature of the mixed gas is increased to 750° C. from 280° C.

10. The method of claim 2, wherein in 3), the molar ratio of the temperature control gas to the feed gas is reduced from 7:1.3-1.6 to 0-5:1.3-1.6 when the temperature of the mixed gas is increased to 750° C. from 280° C.

11. The method of claim 1, wherein in 3), the molar ratio of the temperature control gas to the feed gas is reduced from 5.1-7:1.4-1.6 to 0-5:1.4-1.6, and the molar ratio of the oxygen to the natural gas in the feed gas is increased from 0.3-0.4:1 to 0.41-0.6:1 when the temperature of the mixed gas is increased to 750° C. from 280° C.

12. The method of claim 2, wherein in 3), the molar ratio of the temperature control gas to the feed gas is reduced from 5.1-7:1.4-1.6 to 0-5:1.4-1.6, and the molar ratio of the oxygen to the natural gas in the feed gas is increased from 0.3-0.4:1 to 0.41-0.6:1 when the temperature of the mixed gas is increased to 750° C. from 280° C.

13. The method of claim 7, wherein in 3), the molar ratio of the temperature control gas to the feed gas is reduced from 5.1-7:1.4-1.6 to 0-5:1.4-1.6, and the molar ratio of the oxygen to the natural gas in the feed gas is increased from 0.3-0.4:1 to 0.41-0.6:1 when the temperature of the mixed gas is increased to 750° C. from 280° C.

14. The method of claim 8, wherein in 3), the molar ratio of the temperature control gas to the feed gas is reduced from 5.1-7:1.4-1.6 to 0-5:1.4-1.6, and the molar ratio of the oxygen to the natural gas in the feed gas is increased from 0.3-0.4:1 to 0.41-0.6:1 when the temperature of the mixed gas is increased to 750° C. from 280° C.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0020] FIG. 1 is a drying-out curve of a heat insulation refractory material in the prior art;

[0021] FIG. 2 is a change chart of temperature of a gas discharged from a catalyst bed with the variation of the flow rate of N.sub.2 in Example 1;

[0022] FIG. 3 is a change chart of temperature of a gas discharged from a catalyst bed with the variation of the flow rate of Helium in Example 2;

[0023] FIG. 4 is a change chart of temperature of a gas discharged from a catalyst bed with the variation of the flow rate of CO.sub.2 in Example 3;

[0024] FIG. 5 is a change chart of temperature of a gas discharged from a catalyst bed with the variation of the flow rate of N.sub.2 in Example 4;

[0025] FIG. 6 is a change chart of temperature of a gas discharged from a catalyst bed with the variation of the flow rate of H.sub.2O in Example 5; and

[0026] FIG. 7 is a change chart of temperature of a gas discharged from a catalyst bed with the variation of the flow rate of Argon in Example 6.

DETAILED DESCRIPTION OF THE EMBODIMENTS

[0027] For further illustrating the invention, experiments detailing a method for drying an adiabatic catalytic oxidation furnace are described hereinbelow combined with the drawings. It should be noted that the following examples are intended to describe and not to limit the invention.

EXAMPLE 1

[0028] First, N.sub.2, natural gas and oxygen were injected to a dried catalytic oxidation furnace loaded with a noble metal catalyst, where the natural gas comprised more than 99.9% (v/v) methane; the flow rate of the natural gas was 1 kmol/h; the purity of the oxygen exceeded 99.9%; the flow rate of the oxygen was 0.6 kmol/h; the purity of the N.sub.2 exceeded 99.9%; and the flow rate of the N.sub.2 was 7 kmol/h. Thereafter, the mixed gas comprising the N.sub.2, natural gas and oxygen was preheated to 300° C. to trigger the catalytic oxidation; stop preheating, and gradually reduce the flow rate of the nitrogen until the flow rate of the nitrogen became 0, such that the rise of the reaction temperature of the mixed gas conforms to the temperature rising rate of the designed drying-out curve of the heat insulation refractory material of the catalytic oxidation furnace of natural gas. Specifically, the temperature rose steadily to 1115° C. which was the normal working temperature of the catalytic oxidation furnace. The drying-out curve of the heat insulation refractory material of the catalytic oxidation furnace of natural gas is shown in FIG. 1.

[0029] During the drying stage, with the reduction of the flow rate of the N.sub.2, the temperature of the gas discharged from the catalyst bed is shown in FIG. 2 when the flow rates of the N.sub.2 are 7 kmol/h, 6 kmol/h, 5 kmol/h, 4 kmol/h, 3 kmol/h, 2 kmol/h, 1 kmol/h and 0.1 kmol/h. As shown in FIG. 2, the gas temperature in the furnace increases steadily with the reduction of the flow rate of the N.sub.2, without shock heating; and the molar ratio of the natural gas to the oxygen to the N.sub.2 is shown in Table 1 in each insulating stage of drying.

TABLE-US-00001 TABLE 1 Drying temperature/° C. 125 280 650 750 1100 Example 1 1:0.6:7 1:0.6:7 1:0.6:6.5 1:0.6:3 1:0.6:0.05 CH.sub.4:O.sub.2:N.sub.2 Example 2 1:0.3:7 1:0.3:7 1:0.3:5 1:0.3:0.3 — CH.sub.4:O.sub.2:He Example 3 1:0.4:7 1:0.4:7 1:0.4:1 1:0.4:0.1 — CH.sub.4:O.sub.2:CO.sub.2 Example 4 1:0.4:4 1:0.4:4 1:0.45:3 1:0.51:1 1:0.6:0.05 CH.sub.4:O.sub.2:N.sub.2 Example 5 1:0.4:4 1:0.4:4 1:0.4:2 1:0.47:1.5 1:0.56:0.3 CH.sub.4:O.sub.2:H.sub.2O Example 6 1:0.4:3.5 1:0.4:3.5 1:0.4:3 1:0.5:1.2 1:0.6:0.1 CH.sub.4:O.sub.2:Ar

EXAMPLE 2

[0030] First, Helium, natural gas and oxygen were injected to a dried catalytic oxidation furnace loaded with a noble metal catalyst, where the natural gas comprised more than 99.9% (v/v) methane; the flow rate of the natural gas was 1 kmol/h; the purity of the oxygen exceeded 99.9%; the flow rate of the oxygen was 0.3 kmol/h; the purity of the Helium exceeded 99.9%; and the flow rate of the Helium was 7 kmol/h. Thereafter, the mixed gas comprising the Helium, natural gas and oxygen was preheated to 550° C. to trigger the catalytic oxidation; stop preheating, and gradually reduce the flow rate of the

[0031] Helium until the flow rate of the Helium became 0, such that the rise of the reaction temperature of the mixed gas conforms to the temperature rising rate of the designed drying-out curve of the heat insulation refractory material of the catalytic oxidation furnace of natural gas. Specifically, the temperature rose steadily to 760° C. which was the normal working temperature of the catalytic oxidation furnace. The drying-out curve of the heat insulation refractory material of the catalytic oxidation furnace of natural gas is shown in FIG. 1.

[0032] During the drying stage, with the reduction of the flow rate of the Helium, the temperature of the gas discharged from the catalyst bed is shown in FIG. 3 when the flow rates of the Helium are 7 kmol/h, 6 kmol/h, 5 kmol/h, 4 kmol/h, 3 kmol/h, 2 kmol/h, 1 kmol/h and 0.1 kmol/h. As shown in FIG. 3, the gas temperature in the furnace increases steadily with the reduction of the flow rate of the Helium, without shock heating; and the molar ratio of the natural gas to the oxygen to the Helium is shown in Table 1 in each insulating stage of drying.

EXAMPLE 3

[0033] First, CO.sub.2, natural gas and oxygen were injected to a dried catalytic oxidation furnace loaded with a noble metal catalyst, where the natural gas comprised more than 99.9% (v/v) methane; the flow rate of the natural gas was 1 kmol/h; the purity of the oxygen exceeded 99.9%; the flow rate of the oxygen was 0.4 kmol/h; the purity of the CO.sub.2 exceeded 99.9%; and the flow rate of the CO.sub.2 was 7 kmol/h. Thereafter, the mixed gas comprising the CO.sub.2, natural gas and oxygen was preheated to 600° C. to trigger the catalytic oxidation; stop preheating, and gradually reduce the flow rate of the CO.sub.2 until the flow rate of the CO.sub.2 became 0, such that the rise of the reaction temperature of the mixed gas conforms to the temperature rising rate of the designed drying-out curve of the heat insulation refractory material of the catalytic oxidation furnace of natural gas. Specifically, the temperature rose steadily to 760° C. which was the normal working temperature of the catalytic oxidation furnace. The drying-out curve of the heat insulation refractory material of the catalytic oxidation furnace of natural gas is shown in FIG. 1.

[0034] During the drying stage, with the reduction of the flow rate of the CO.sub.2, the temperature of the gas discharged from the catalyst bed is shown in FIG. 4 when the flow rates of the CO.sub.2 are 7 kmol/h, 6 kmol/h, 5 kmol/h, 4 kmol/h, 3 kmol/h, 2 kmol/h, 1 kmol/h and 0.1 kmol/h. As shown in FIG. 4, the gas temperature in the furnace increases steadily with the reduction of the flow rate of the CO.sub.2, without shock heating; and the molar ratio of the natural gas to the oxygen to the CO.sub.2 is shown in Table 1 in each insulating stage of drying.

EXAMPLE 4

[0035] First, N.sub.2, natural gas and oxygen were injected to a dried catalytic oxidation furnace loaded with a noble metal catalyst, where the natural gas comprised more than 99.9% (v/v) methane; the flow rate of the natural gas was 1 kmol/h; the purity of the oxygen exceeded 99.9%; the flow rate of the oxygen was 0.3 kmol/h; the purity of the N.sub.2 exceeded 99.9%; and the flow rate of the N.sub.2 was 7 kmol/h. Thereafter, the mixed gas comprising the N.sub.2, natural gas and oxygen was preheated to 300° C. to trigger the catalytic oxidation; stop preheating, and gradually reduce the flow rate of the nitrogen and regulate the molar ratio of the natural gas to the oxygen, such that the rise of the reaction temperature of the mixed gas conforms to the temperature rising rate of the designed drying-out curve of the heat insulation refractory material of the catalytic oxidation furnace of natural gas. Specifically, the temperature rose steadily to 1115° C. which was the normal working temperature of the catalytic oxidation furnace, the flow rate of the nitrogen became 0, and the molar ratio of the natural gas to the oxygen was 1:0.6. The drying-out curve of the heat insulation refractory material of the catalytic oxidation furnace of natural gas is shown in FIG. 1.

[0036] During the drying stage, with the reduction of the flow rate of the N.sub.2 and the increase of the flow rate of the oxygen, the temperature of the gas discharged from the catalyst bed is shown in FIG. 5 when the flow rates of the N.sub.2 are 7 kmol/h, 6 kmol/h, 5 kmol/h, 4 kmol/h, 3 kmol/h, 2 kmol/h, 1 kmol/h and 0.1 kmol/h, and the flow rates of the oxygen are 0.3 kmol/h, 0.4 kmol/h, 0.5 kmol/h, and 0.6 kmol/h. As shown in FIG. 5, the gas temperature in the furnace increases steadily with the reduction of the flow rate of the N.sub.2 and the increase of the flow rate of the oxygen, without shock heating; and the molar ratio of the natural gas to the oxygen to the N.sub.2 is shown in Table 1 in each insulating stage of drying.

EXAMPLE 5

[0037] First, water vapor, natural gas and oxygen were injected to a dried catalytic oxidation furnace loaded with a noble metal catalyst, where the natural gas comprised more than 99.9% (v/v) methane; the flow rate of the natural gas was 1 kmol/h; the purity of the oxygen exceeded 99.9%; the flow rate of the oxygen was 0.3 kmol/h; the purity of the water vapor exceeded 99.9%; and the flow rate of the water vapor was 7 kmol/h. Thereafter, the mixed gas comprising the water vapor, natural gas and oxygen was preheated to 600° C. to trigger the catalytic oxidation; stop preheating, and gradually reduce the flow rate of the water vapor and regulate the molar ratio of the natural gas to the oxygen, that is, gradually increase the molar percentage of the oxygen, such that the rise of the reaction temperature of the mixed gas conforms to the temperature rising rate of the designed drying-out curve of the heat insulation refractory material of the catalytic oxidation furnace of natural gas. Specifically, the temperature rose steadily to 1342° C. which was the normal working temperature of the catalytic oxidation furnace, the flow rate of the water vapor became 0, and the molar ratio of the natural gas to the oxygen was 1:0.6. The drying-out curve of the heat insulation refractory material of the catalytic oxidation furnace of natural gas is shown in FIG. 1.

[0038] During the drying stage, with the reduction of the flow rate of the water vapor and the increase of the flow rate of the oxygen, the temperature of the gas discharged from the catalyst bed is shown in FIG. 6 when the flow rates of the water vapor are 7 kmol/h, 6 kmol/h, 5 kmol/h, 4 kmol/h, 3 kmol/h, 2 kmol/h, 1 kmol/h and 0.1 kmol/h, and the flow rates of the oxygen are 0.3 kmol/h, 0.4 kmol/h, 0.5 kmol/h, and 0.6 kmol/h. As shown in FIG. 6, the gas temperature in the furnace increases steadily with the reduction of the flow rate of the water vapor and the increase of the flow rate of the oxygen, without shock heating; and the molar ratio of the natural gas to the oxygen to the water vapor is shown in Table 1 in each insulating stage of drying.

EXAMPLE 6

[0039] First, Argon, natural gas and oxygen were injected to a dried catalytic oxidation furnace loaded with a noble metal catalyst, where the natural gas comprised more than 99.9% (v/v) methane; the flow rate of the natural gas was 1 kmol/h; the purity of the oxygen exceeded 99.9%; the flow rate of the oxygen was 0.3 kmol/h; the purity of the Argon exceeded 99.9%; and the flow rate of the Argon was 7 kmol/h. Thereafter, the mixed gas comprising the Argon, natural gas and oxygen was preheated to 300° C. to trigger the catalytic oxidation; stop preheating, and gradually reduce the flow rate of the Argon and regulate the molar ratio of the natural gas to the oxygen, that is, gradually increase the molar percentage of the oxygen, such that the rise of the reaction temperature of the mixed gas conforms to the temperature rising rate of the designed drying-out curve of the heat insulation refractory material of the catalytic oxidation furnace of natural gas. Specifically, the temperature rose steadily to 1115° C. which was the normal working temperature of the catalytic oxidation furnace, the flow rate of the Argon became 0, and the molar ratio of the natural gas to the oxygen was 1:0.6. The drying-out curve of the heat insulation refractory material of the catalytic oxidation furnace of natural gas is shown in FIG. 1.

[0040] During the drying stage, with the reduction of the flow rate of the Argon and the increase of the flow rate of the oxygen, the temperature of the gas discharged from the catalyst bed is shown in FIG. 7 when the flow rates of the Argon are 7 kmol/h, 6 kmol/h, 5 kmol/h, 4 kmol/h, 3 kmol/h, 2 kmol/h, 1 kmol/h and 0.1 kmol/h, and the flow rates of the oxygen are 0.3 kmol/h, 0.4 kmol/h, 0.5 kmol/h, and 0.6 kmol/h. As shown in FIG. 7, the gas temperature in the furnace increases steadily with the reduction of the flow rate of the Argon and the increase of the flow rate of the oxygen, without shock heating; and the molar ratio of the natural gas to the oxygen to the Argon is shown in Table 1 in each insulating stage of drying.

[0041] Unless otherwise indicated, the numerical ranges involved in the invention include the end values. While particular embodiments of the invention have been shown and described, it will be obvious to those skilled in the art that changes and modifications may be made without departing from the invention in its broader aspects, and therefore, the aim in the appended claims is to cover all such changes and modifications as fall within the true spirit and scope of the invention.