CN113955718B - Direct reforming process and system for non-catalytic partial oxidation of high-temperature raw gas - Google Patents
Direct reforming process and system for non-catalytic partial oxidation of high-temperature raw gas Download PDFInfo
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- CN113955718B CN113955718B CN202111255603.2A CN202111255603A CN113955718B CN 113955718 B CN113955718 B CN 113955718B CN 202111255603 A CN202111255603 A CN 202111255603A CN 113955718 B CN113955718 B CN 113955718B
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
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- C01B3/346—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using heat generated by superheated steam
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- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0211—Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step
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Abstract
The invention relates to a non-catalytic partial oxidation direct reforming process and a system of high-temperature raw gas, wherein the system comprises a reforming furnace, a waste heat boiler, a dust removing device, a heat exchanger, a supercharging device, a final cooling tower and a desulfurizing device; the invention fully utilizes the heat of the high-temperature raw gas to prepare the synthesis gas with low cost and sufficient quantity, and provides a guarantee for the development and application of carbon emission reduction technology.
Description
Technical Field
The invention relates to the technical field of energy conservation and environmental protection in coking production, in particular to a non-catalytic partial oxidation direct reforming process and system for high-temperature raw gas.
Background
In order to cope with global climate change, the emission of carbon dioxide gas in the industrial production process is effectively reduced, and the demand for hydrogen is rapidly increased. In particular to the steel industry accounting for 15 percent of the carbon emission, in order to realize carbon emission reduction, the development of a hydrogen-rich blast furnace smelting technology and a hydrogen direct reduction iron technology is carried out in a dispute, and the future requirement for hydrogen is predicted to be increased. However, the current hydrogen production and transportation costs are high, which forms a prominent contradiction with the urgent demand for hydrogen. For this purpose, the skilled worker turns his eyes towards coke oven gas enriched with hydrogen.
Coke oven gas is known to be an important by-product in coking production. In the traditional coking process, coal is subjected to high-temperature carbonization in a coke oven carbonization chamber to prepare coke, and meanwhile, generated raw gas escapes from the top of the coke oven and enters a gas purification workshop. After the raw gas is purified by the gas, one part of the raw gas is used as heating fuel to return to the coke oven to provide heat for the coking process, and the other part of the raw gas is subjected to deep processing or is used as fuel to be conveyed to other process workshops. The purified coke oven gas mainly comprises hydrogen, methane, carbon monoxide and a small amount of C2-C3 hydrocarbons, wherein the volume ratio of the hydrogen is more than 50%. Considerable hydrogen can be prepared by using coke oven gas at low cost, and the cost is low; in addition, because the hydrogen production area is distributed around the country along with the existing coking enterprises, the high transportation cost after the hydrogen is prepared can be avoided, and the consumption requirement of regional hydrogen can be well met.
In the steel combined enterprises, part of hydrogen is usually separated from the purified coke oven gas through a pressure swing adsorption process, but the obtained hydrogen is difficult to meet the requirements of enterprises on reducing gas, and in order to further improve the hydrogen yield, the coke oven gas is required to be subjected to reforming treatment, and methane in the purified coke oven gas is prepared into the reducing gas, namely carbon monoxide and hydrogen through incomplete oxidation. From the current technical process, the coke oven raw gas is cooled and purified firstly after escaping from the coke oven, and then is heated for reforming to obtain the reducing gas, so that the heat carried by the coke oven raw gas is not fully utilized, the energy consumption is high, and meanwhile, the hydrocarbon such as tar, crude benzene and the like in the raw gas cannot be fully converted and utilized.
The invention provides a non-catalytic partial oxidation direct reforming process of high-temperature raw coke oven gas from the viewpoints of energy conservation and full utilization of raw coke oven gas resources, and the raw coke oven gas is directly subjected to non-catalytic partial oxidation reforming at a high temperature, so that methane in the raw coke oven gas can be incompletely oxidized into carbon monoxide and hydrogen, meanwhile, tar and crude benzene in the raw coke oven gas can be prepared into carbon monoxide and hydrogen through non-catalytic partial oxidation, the yield of reducing gas is greatly improved, low-cost and sufficient hydrogen resources can be provided for carbon emission reduction, and impurities such as organic sulfur which are originally difficult to remove in the raw coke oven gas are oxidized into inorganic sulfur which is easy to remove, so that the purification cost is greatly reduced. As organic matters such as crude benzene, tar and the like are oxidized to generate carbon monoxide and hydrogen, the process wastewater only contains a small amount of inorganic pollutants, and the one-time construction investment of the purification device and the sewage treatment device is saved.
Disclosure of Invention
The invention provides a non-catalytic partial oxidation direct reforming process and a system for high-temperature raw gas, which fully utilize the heat of the high-temperature raw gas, prepare low-cost and sufficient-quantity synthesis gas and provide guarantee for development and application of carbon emission reduction technology.
In order to achieve the above purpose, the invention is realized by adopting the following technical scheme:
a non-catalytic partial oxidation direct reforming process of high-temperature raw gas comprises the following steps:
1) Raw gas escaping from the top of the coke oven carbonization chamber enters a raw gas pipeline after being collected;
2) Raw gas with the temperature of 550-900 ℃ is conveyed by a raw gas pipeline and enters the upper part of a reforming furnace, pure oxygen is introduced into the top of the reforming furnace, the pure oxygen and the raw gas are subjected to incomplete oxidation reaction in the reforming furnace, and methane, crude benzene and tar in the raw gas are converted into reducing gas under the negative pressure condition of 1150-1300 ℃ and the pressure value of-20-0 kpa; simultaneously, continuously or intermittently introducing carbon dioxide into the reforming furnace, and forming carbon black after insufficient oxidation of the carbon dioxide and polyaromatic macromolecules in the tar and further carrying out carbon melting reaction to generate carbon monoxide;
3) Reducing gas generated in the reformer enters a tube side of the waste heat boiler, preheated boiler feed water enters a shell side of the waste heat boiler, the reducing gas in the waste heat boiler exchanges heat with the boiler feed water to generate saturated steam of 0.8-8 Mpa, and the saturated steam is sent out from the waste heat boiler;
4) The temperature of the reducing gas after waste heat recovery by the waste heat boiler is 160-280 ℃, dust is removed by a dust removing device, and the reducing gas enters a shell side of a heat exchanger to preheat boiler water, and the temperature is reduced to 60-80 ℃;
5) Reducing gas discharged by the dust removing device is pressurized by the pressurizing device and then enters the final cooling tower for cooling;
6) The reducing gas cooled by the final cooling tower enters a desulfurization device, hydrogen sulfide gas is separated from the reducing gas, and the desulfurized reducing gas comprises hydrogen and carbon monoxide and is sent to a subsequent working section.
The inner wall of the raw gas pipeline is lined with an inner heat-insulating layer, and the inner heat-insulating layer is composed of refractory bricks or refractory castable; an insulating layer is arranged on the outer wall of the raw gas pipeline.
The pure oxygen is introduced from the top of the reformer, and the carbon dioxide gas is introduced from the periphery of the burner of the reformer.
The dust removing device adopts a cyclone dust remover or a cloth bag dust remover.
The lower part of the heat exchanger is provided with a condensate outlet.
A broken tower tray is arranged in the final cooling tower to divide the final cooling tower into an upper tower body and a lower tower body; an upper cooling water circulating pipeline is arranged outside the upper tower body, and an upper cooling water circulating pump and a low-temperature water heat exchanger are arranged on the upper cooling water circulating pipeline; a lower cooling water circulating pipeline is arranged outside the lower tower body, and a lower cooling water circulating pump and a circulating water heat exchanger are arranged on the lower cooling water circulating pipeline; cooling water in the lower tower body is pressurized by a lower cooling water circulating pump and then cooled by a circulating water heat exchanger, and then returns to the lower tower body; the cooling water in the upper tower body is pressurized by an upper cooling water circulating pump and then cooled by a low-temperature water heat exchanger, and is mixed with the supplementary cooling water and then returned to the upper tower body; reducing gas enters from the lower tower body and is discharged from the top of the final cooling tower; condensate generated by reducing the temperature of the reducing gas in the upper tower body is collected on the broken tower tray and flows into the lower tower body through accumulation overflow.
And the condensate generated in the heat exchanger and the condensate generated in the final cooling tower are converged and then enter a sewage treatment system.
The desulfurization device adopts PDS desulfurization, vacuum carbonate desulfurization, alcohol amine desulfurization or low-temperature methanol washing desulfurization.
A non-catalytic partial oxidation direct reforming system of high-temperature raw gas comprises a reforming furnace, a waste heat boiler, a dust removing device, a heat exchanger, a supercharging device, a final cooling tower and a desulfurizing device; the upper part of the reforming furnace is provided with a raw gas inlet connected with a raw gas pipeline, the top of the reforming furnace is provided with a gas inlet pipe, and the gas inlet pipe is provided with a pure oxygen inlet and a carbon dioxide inlet; the lower part of the reforming furnace is provided with a reducing gas outlet which is connected with a tube side inlet of the waste heat boiler, the tube side outlet of the waste heat boiler is connected with a gas inlet at the upper part of the dust removing device, and the gas outlet at the lower part of the dust removing device is connected with a shell side inlet of the heat exchanger; the tube side inlet of the heat exchanger is connected with a boiler water supply pipeline, the tube side outlet of the heat exchanger is connected with the shell side inlet of the waste heat boiler, and the shell side outlet of the waste heat boiler is connected with a saturated steam pipeline; a broken tower tray is arranged in the final cooling tower to divide the final cooling tower into an upper tower body and a lower tower body; an upper cooling water circulating pipeline is arranged outside the upper tower body, and an upper cooling water circulating pump, a low-temperature water heat exchanger and a supplementary cooling water inlet are sequentially arranged on the upper cooling water circulating pipeline along the flowing direction of cooling water; a lower cooling water circulating pipeline is arranged outside the lower tower body, and a lower cooling water circulating pump and a circulating water heat exchanger are sequentially arranged on the lower cooling water circulating pipeline along the flowing direction of cooling water; the shell side outlet of the heat exchanger is connected with the reducing gas inlet of the lower tower body through a supercharging device; the top of the final cooling tower is provided with a reducing gas outlet which is connected with a desulfurization device, and the desulfurization device is provided with a hydrogen sulfide gas outlet and a reducing gas outlet.
The bottom of the waste heat boiler is provided with a drain outlet connected with a drain pipeline, and the drain pipeline is provided with a valve.
Compared with the prior art, the invention has the beneficial effects that:
1) The yield of reducing gases (including hydrogen and carbon monoxide) is improved;
2) The process flow is optimized, the gas purifying part is reduced, and the primary investment is saved;
3) The organic sulfur which is difficult to remove is largely converted into inorganic sulfur while the raw gas is subjected to incomplete oxidation to generate reducing gas, so that the raw gas is favorable for treatment by a desulfurization device; meanwhile, a large amount of organic matters are converted into inorganic matters through oxidization, so that the phenol-cyanogen sewage treatment process is avoided, and the investment is saved;
4) Because the oxidation reaction sewage does not contain organic matters, the phenol-cyanogen sewage treatment is omitted, the occupied area and one-time investment are saved, and the energy consumption is greatly reduced;
5) The repeated cooling and heating process of the coal gas in the purifying process is avoided, so that the energy consumption of the whole process is further optimized and reduced.
Drawings
FIG. 1 is a schematic diagram of a non-catalytic partial oxidation direct reforming system for high temperature raw gas according to the present invention.
In the figure: 1. reformer 2, waste heat boiler 3, dust collector 4, heat exchanger 5, booster 6, final cooling tower 7, desulfurizing unit 8, lower cooling water circulating pump 9, circulating water heat exchanger 10, upper cooling water circulating pump 11, low temperature water heat exchanger 12, valve 13, raw gas pipe 14, inner heat insulating layer 15, outer heat insulating layer
Detailed Description
The following is a further description of embodiments of the invention, taken in conjunction with the accompanying drawings:
as shown in FIG. 1, the non-catalytic partial oxidation direct reforming process of the high-temperature raw coke oven gas comprises the following steps:
1) Raw gas escaping from the top of the coke oven carbonization chamber enters a raw gas pipeline 13 after being collected;
2) Raw gas with the temperature of 550-900 ℃ after being conveyed by a raw gas pipeline 13 enters the upper part of a reformer 1, pure oxygen is introduced into the top of the reformer 1, the pure oxygen and the raw gas undergo incomplete oxidation reaction in the reformer 1, and methane, crude benzene and tar in the raw gas are converted into reducing gas under the negative pressure condition of 1150-1300 ℃ and the pressure value of-20 kpa-0 kpa; simultaneously, continuously or intermittently introducing carbon dioxide into the reformer 1, and forming carbon black after insufficient oxidation of the carbon dioxide and polyaromatic macromolecules in tar and further carrying out carbon melting reaction to generate carbon monoxide;
3) Reducing gas generated in the reformer 1 enters a tube pass of the waste heat boiler 2, preheated boiler feed water enters a shell pass of the waste heat boiler 2, and after heat exchange between the reducing gas in the waste heat boiler 2 and the boiler feed water, saturated steam of 0.8-8 Mpag is generated and sent out from the waste heat boiler 2;
4) The temperature of the reducing gas after waste heat recovery by the waste heat boiler 2 is 160-280 ℃, dust is removed by the dust removing device 3, and the reducing gas enters a shell pass of the heat exchanger 4 to preheat boiler water, and the temperature is reduced to 60-80 ℃;
5) Reducing gas discharged by the dust removing device 3 is pressurized by the pressurizing device 5 and then enters the final cooling tower 6 for cooling;
6) The reducing gas cooled by the final cooling tower 6 enters a desulfurization device 7, hydrogen sulfide gas is separated from the reducing gas, and the desulfurized reducing gas comprises hydrogen and carbon monoxide and is sent to a subsequent working section.
The inner wall of the raw gas pipeline 13 is lined with an inner heat-insulating layer 14, and the inner heat-insulating layer 14 is composed of refractory bricks or refractory castable; an insulating layer 15 is arranged on the outer wall of the raw gas pipeline.
The pure oxygen is introduced from the top of the reformer 1, and the carbon dioxide gas is introduced from the periphery of the burner of the reformer 1.
The dust removing device 3 adopts a cyclone dust remover or a cloth bag dust remover.
The lower part of the heat exchanger 4 is provided with a condensate outlet.
A broken tray is arranged in the final cooling tower 6 to divide the final cooling tower 6 into an upper tower body and a lower tower body; an upper cooling water circulating pipeline is arranged outside the upper tower body, and an upper cooling water circulating pump 10 and a low-temperature water heat exchanger 11 are arranged on the upper cooling water circulating pipeline; a lower cooling water circulating pipeline is arranged outside the lower tower body, and a lower cooling water circulating pump 8 and a circulating water heat exchanger 9 are arranged on the lower cooling water circulating pipeline; the cooling water in the lower tower body is pressurized by a lower cooling water circulating pump 8 and then cooled by a circulating water heat exchanger 9, and then returns to the lower tower body; the cooling water in the upper tower body is pressurized by an upper cooling water circulating pump 10 and then cooled by a low-temperature water heat exchanger 11, and is mixed with the supplementary cooling water and then returned to the upper tower body; reducing gas enters from the lower tower body and is discharged from the top of the final cooling tower 6; condensate generated by reducing the temperature of the reducing gas in the upper tower body is collected on the broken tower tray and flows into the lower tower body through accumulation overflow.
The condensate generated in the heat exchanger 4 and the condensate generated in the final cooling tower 6 are converged and then enter a sewage treatment system.
The desulfurization device 7 adopts PDS desulfurization, vacuum carbonate desulfurization, alcohol amine desulfurization or low-temperature methanol washing desulfurization.
A high-temperature raw gas non-catalytic partial oxidation direct reforming system comprises a reforming furnace 1, a waste heat boiler 2, a dust removing device 3, a heat exchanger 4, a supercharging device 5, a final cooling tower 6 and a desulfurizing device 7; the upper part of the reforming furnace 1 is provided with a raw gas inlet connected with a raw gas pipeline 13, the top of the reforming furnace 1 is provided with a gas inlet pipe, and the gas inlet pipe is provided with a pure oxygen inlet and a carbon dioxide inlet; the lower part of the reforming furnace 1 is provided with a reducing gas outlet which is connected with a tube side inlet of the waste heat boiler 2, the tube side outlet of the waste heat boiler 2 is connected with a gas inlet at the upper part of the dust removing device 3, and the gas outlet at the lower part of the dust removing device 3 is connected with a shell side inlet of the heat exchanger 4; the tube side inlet of the heat exchanger 4 is connected with a boiler water supply pipeline, the tube side outlet of the heat exchanger 4 is connected with the shell side inlet of the waste heat boiler 2, and the shell side outlet of the waste heat boiler 2 is connected with a saturated steam pipeline; a broken tower tray is arranged in the final cooling tower 6 to divide the final cooling tower into an upper tower body and a lower tower body; an upper cooling water circulating pipeline is arranged outside the upper tower body, and an upper cooling water circulating pump 10, a low-temperature water heat exchanger 11 and a supplementary cooling water inlet are sequentially arranged on the upper cooling water circulating pipeline along the flowing direction of cooling water; a lower cooling water circulating pipeline is arranged outside the lower tower body, and a lower cooling water circulating pump 8 and a circulating water heat exchanger 9 are sequentially arranged on the lower cooling water circulating pipeline along the flowing direction of cooling water; the lower tower body is also provided with a reducing gas inlet, and a shell side outlet of the heat exchanger 4 is connected with the reducing gas inlet of the lower tower body through a supercharging device 5; the top of the final cooling tower 6 is provided with a reducing gas outlet which is connected with a desulfurizing device 7, and the desulfurizing device 7 is provided with a hydrogen sulfide gas outlet and a reducing gas outlet.
The bottom of the waste heat boiler 2 is provided with a drain outlet connected with a drain pipeline, and the drain pipeline is provided with a valve 12.
The invention discloses a non-catalytic partial oxidation direct reforming system of high-temperature raw gas, which consists of a reforming furnace 1, a waste heat boiler 2, a dust removing device 3, a heat exchanger 4, a supercharging device 5, a final cooling tower 6, a desulfurizing device 7 and other devices.
The reformer 1 is provided with a pure oxygen inlet, a carbon dioxide inlet, a raw gas inlet, and a reducing gas outlet. The raw gas inlet is connected with a raw gas pipeline 13, and the other end of the raw gas pipeline 13 is connected with a rising pipe of each carbonization chamber of the coke oven; raw gas escaping from the coking chamber of the coke oven enters the raw gas pipeline 13 through the ascending pipe and is then sent to the reformer 1. The pure oxygen inlet is connected with a pure oxygen pipeline, and the carbon dioxide inlet is connected with a carbon dioxide pipeline.
The top of the waste heat boiler 2 is provided with a saturated steam outlet (shell side outlet), the lower part is provided with a reducing gas inlet (tube side inlet), a reducing gas outlet (tube side outlet), a boiler water inlet (shell side inlet) and the bottom is provided with a sewage outlet. The reducing gas outlet at the lower part of the reformer 1 is connected with the reducing gas inlet of the waste heat boiler 2, the saturated steam outlet at the top of the waste heat boiler 2 is connected with a saturated steam pipeline, the sewage outlet at the bottom of the waste heat boiler 2 is connected with a sewage pipeline, and the sewage pipeline is provided with a valve 12.
The dust removing device 3 is provided with a reducing gas inlet, a reducing gas outlet and a dust removing outlet. The reducing gas outlet of the waste heat boiler 2 is connected to the reducing gas inlet of the dust removing device 3.
The heat exchanger 4 is provided with a reducing gas inlet (shell side inlet), a reducing gas outlet (shell side outlet), a condensate outlet, a boiler feed water inlet (tube side inlet), and a boiler feed water outlet (tube side outlet). The reducing gas outlet of the dust removing device 3 is connected with the reducing gas inlet of the heat exchanger 4, the boiler water inlet of the heat exchanger 4 is connected with the boiler water inlet pipe, the boiler water outlet of the heat exchanger 4 is connected with the boiler water inlet of the waste heat boiler 2, and the condensate outlet is connected with the sewage pipe.
The pressurizing device 5 is provided with a reducing gas inlet and a reducing gas outlet, and the reducing gas inlet is connected with the reducing gas outlet of the heat exchanger 4.
The lower tower body of the final cooling tower 6 is provided with a reducing gas inlet, a lower cooling water outlet and a lower cooling water inlet, the upper tower body is provided with a cooling water outlet and an upper cooling water inlet, the top is provided with a reducing gas outlet, and the bottom is provided with a condensate outlet. The reducing gas outlet of the supercharging device 5 is connected with the reducing gas inlet of the final cooling tower 6, and the condensate outlet at the bottom of the final cooling tower 6 is connected with a sewage pipeline; the lower cooling water outlet of the final cooling tower 6 is connected with the inlet of the lower cooling water circulating pump 8, the outlet of the lower cooling water circulating pump 8 is connected with the cooling water inlet of the circulating water heat exchanger 9, and the cooling water outlet of the circulating water heat exchanger 9 is connected with the lower cooling water inlet. The upper cooling water outlet of the final cooling tower 6 is connected with the inlet of the upper cooling water circulating pump 10, the outlet of the upper cooling water circulating pump 10 is connected with the cooling water inlet of the low-temperature water heat exchanger 11, the cooling water outlet of the low-temperature water heat exchanger 11 is connected with the upper cooling water inlet, and the section of connecting pipeline is provided with a supplementary cooling water inlet which is connected with a supplementary cooling water pipeline.
The desulfurization device 7 is provided with a reducing gas inlet, a reducing gas outlet, and a hydrogen sulfide gas outlet. The reducing gas inlet of the desulfurizing device 7 is connected with the reducing gas outlet of the final cooling tower 6, the hydrogen sulfide gas outlet is connected with a hydrogen sulfide pipeline, and the reducing gas outlet of the desulfurizing device 7 is connected with a reducing gas outlet pipeline.
The inner wall of the raw gas pipeline 13 is lined with refractory bricks or refractory castable to serve as an inner heat preservation layer 14, heat dissipation is reduced, meanwhile, damage to the raw gas pipeline 13 due to overhigh temperature is avoided, the outer wall of the raw gas pipeline 13 is wrapped with heat preservation materials to serve as an outer heat preservation layer 15, and therefore heat loss in the raw gas conveying process is reduced.
Pure oxygen is introduced into the top of the reformer 1 as combustion-supporting gas, a certain amount of carbon dioxide gas is introduced into the periphery of the burner, carbon dioxide and carbon black generated by incomplete oxidation of tar undergo carbon melting reaction, and carbon black deposition is prevented.
The dust removing device 3 is preferably a cyclone dust collector or a bag dust collector, but is not limited thereto.
The supercharging device 5 is a fan or a compressor.
A breaking tray is arranged in the middle of the final cooling tower 6 to divide the tower body into an upper tower body and a lower tower body. The cooling water in the lower tower body is pressurized by the lower cooling water circulating pump 8, cooled by the circulating water heat exchanger 9 and then returned to the lower tower body. The cooling water in the upper tower body is pressurized by the upper cooling water circulating pump 10, cooled by the low-temperature water heat exchanger 11, and then mixed with the supplementary cooling water to return to the upper tower body. In the upper tower body, condensate generated by reducing the temperature of the reducing gas is collected on the broken tower tray and then overflows into the lower tower body through accumulation.
The desulfurization unit 7 may employ a conventional desulfurization method such as PDS desulfurization, vacuum carbonate desulfurization, alcohol amine desulfurization, low-temperature methanol washing desulfurization, or the like, but is not limited to the above method.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (10)
1. The non-catalytic partial oxidation direct reforming process of the high-temperature raw gas is characterized by comprising the following steps of:
1) Raw gas escaping from the top of the coke oven carbonization chamber enters a raw gas pipeline after being collected;
2) Raw gas with the temperature of 550-900 ℃ after being conveyed by a raw gas pipeline enters the upper part of a reforming furnace, pure oxygen is introduced into the top of the reforming furnace, the pure oxygen and the raw gas are subjected to incomplete oxidation reaction in the reforming furnace, and methane, crude benzene and tar in the raw gas are converted into reducing gas under the negative pressure condition that the temperature of 1150-1300 ℃ and the pressure value of-20 kPaG-0 kPaG are not included; simultaneously, continuously or intermittently introducing carbon dioxide into the reforming furnace, and forming carbon black after insufficient oxidation of the carbon dioxide and polyaromatic macromolecules in the tar and further carrying out carbon melting reaction to generate carbon monoxide;
3) Reducing gas generated in the reformer enters a tube side of the waste heat boiler, preheated boiler feed water enters a shell side of the waste heat boiler, the reducing gas in the waste heat boiler exchanges heat with the boiler feed water to generate saturated steam of 0.8-8 MPaG, and the saturated steam is sent out from the waste heat boiler;
4) The temperature of the reducing gas after waste heat recovery by the waste heat boiler is 160-280 ℃, dust is removed by a dust removing device, and the reducing gas enters a shell side of a heat exchanger to preheat boiler water, and the temperature is reduced to 60-80 ℃;
5) Reducing gas discharged by the dust removing device is pressurized by the pressurizing device and then enters the final cooling tower for cooling;
6) The reducing gas cooled by the final cooling tower enters a desulfurization device, hydrogen sulfide gas is separated from the reducing gas, and the desulfurized reducing gas comprises hydrogen and carbon monoxide and is sent to a subsequent working section.
2. The direct reforming process for non-catalytic partial oxidation of high-temperature raw gas according to claim 1, wherein the inner wall of the raw gas pipeline is lined with an inner heat-insulating layer, and the inner heat-insulating layer is composed of refractory bricks or refractory castable; an insulating layer is arranged on the outer wall of the raw gas pipeline.
3. The direct reforming process for non-catalytic partial oxidation of high-temperature raw gas according to claim 1, wherein the pure oxygen is introduced from the top of the reformer and the carbon dioxide is introduced from the periphery of the burner of the reformer.
4. The non-catalytic partial oxidation direct reforming process for high-temperature raw gas according to claim 1, wherein the dust removing device adopts a cyclone dust remover or a cloth bag dust remover.
5. The non-catalytic partial oxidation direct reforming process for high temperature raw gas according to claim 1, wherein the lower part of the heat exchanger is provided with a condensate outlet.
6. The direct reforming process for non-catalytic partial oxidation of high-temperature raw gas according to claim 1, wherein a broken tray is arranged in the final cooling tower to divide the final cooling tower into an upper tower body and a lower tower body; an upper cooling water circulating pipeline is arranged outside the upper tower body, and an upper cooling water circulating pump and a low-temperature water heat exchanger are arranged on the upper cooling water circulating pipeline; a lower cooling water circulating pipeline is arranged outside the lower tower body, and a lower cooling water circulating pump and a circulating water heat exchanger are arranged on the lower cooling water circulating pipeline; cooling water in the lower tower body is pressurized by a lower cooling water circulating pump and then cooled by a circulating water heat exchanger, and then returns to the lower tower body; the cooling water in the upper tower body is pressurized by an upper cooling water circulating pump and then cooled by a low-temperature water heat exchanger, and is mixed with the supplementary cooling water and then returned to the upper tower body; reducing gas enters from the lower tower body and is discharged from the top of the final cooling tower; condensate generated by reducing the temperature of the reducing gas in the upper tower body is collected on the broken tower tray and flows into the lower tower body through accumulation overflow.
7. The direct reforming process for non-catalytic partial oxidation of high-temperature raw gas according to claim 1, wherein the condensate generated in the heat exchanger is merged with the condensate generated in the final cooling tower and then enters the sewage treatment system.
8. The direct reforming process for non-catalytic partial oxidation of high-temperature raw gas according to claim 1, wherein the desulfurization device adopts PDS desulfurization, vacuum carbonate desulfurization, alcohol amine desulfurization or low-temperature methanol washing desulfurization.
9. The direct reforming system for non-catalytic partial oxidation of high-temperature raw gas for realizing the process of any one of claims 1 to 8, which is characterized by comprising a reformer, a waste heat boiler, a dust removal device, a heat exchanger, a supercharging device, a final cooling tower and a desulfurization device; the upper part of the reforming furnace is provided with a raw gas inlet connected with a raw gas pipeline, the top of the reforming furnace is provided with a gas inlet pipe, and the gas inlet pipe is provided with a pure oxygen inlet and a carbon dioxide inlet; the lower part of the reforming furnace is provided with a reducing gas outlet which is connected with a tube side inlet of the waste heat boiler, the tube side outlet of the waste heat boiler is connected with a gas inlet at the upper part of the dust removing device, and the gas outlet at the lower part of the dust removing device is connected with a shell side inlet of the heat exchanger; the tube side inlet of the heat exchanger is connected with a boiler water supply pipeline, the tube side outlet of the heat exchanger is connected with the shell side inlet of the waste heat boiler, and the shell side outlet of the waste heat boiler is connected with a saturated steam pipeline; a broken tower tray is arranged in the final cooling tower to divide the final cooling tower into an upper tower body and a lower tower body; an upper cooling water circulating pipeline is arranged outside the upper tower body, and an upper cooling water circulating pump, a low-temperature water heat exchanger and a supplementary cooling water inlet are sequentially arranged on the upper cooling water circulating pipeline along the flowing direction of cooling water; a lower cooling water circulating pipeline is arranged outside the lower tower body, and a lower cooling water circulating pump and a circulating water heat exchanger are sequentially arranged on the lower cooling water circulating pipeline along the flowing direction of cooling water; the shell side outlet of the heat exchanger is connected with the reducing gas inlet of the lower tower body through a supercharging device; the top of the final cooling tower is provided with a reducing gas outlet which is connected with a desulfurization device, and the desulfurization device is provided with a hydrogen sulfide gas outlet and a reducing gas outlet.
10. The direct reforming system for non-catalytic partial oxidation of high-temperature raw gas according to claim 9, wherein a drain outlet is arranged at the bottom of the waste heat boiler and is connected with a drain pipe, and a valve is arranged on the drain pipe.
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