CN111139088A - Method for recycling and reusing energy - Google Patents
Method for recycling and reusing energy Download PDFInfo
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- CN111139088A CN111139088A CN202010012204.2A CN202010012204A CN111139088A CN 111139088 A CN111139088 A CN 111139088A CN 202010012204 A CN202010012204 A CN 202010012204A CN 111139088 A CN111139088 A CN 111139088A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B21/00—Heating of coke ovens with combustible gases
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Gasification And Melting Of Waste (AREA)
Abstract
The invention provides a method for recycling and reusing energy. In the technical scheme, the high-level heat energy gas is circulated by using a thermal circulator, and is mixed with fresh high-temperature furnace gas after combustion to increase the temperature, and the two gases are combined for large circulation to accelerate the flow velocity, so that the temperature of each point of the pyrolysis reactor is uniform, and the yield and the utilization rate of equipment are improved. The shunted high-level heat energy furnace gas is fully transferred to combustion air; the energy can be saved by more than 60%. The pyrolysis process conditions depend on the difference of the inlet temperature and the outlet temperature of the heating gas and the heat transfer area, and the pyrolysis process can be satisfied by utilizing the hot furnace gas circulation and the heat exchange process. The discharged waste heat furnace gas is subjected to heat recovery on the second component in unit volume, heated air is combusted to increase temperature and then mixed with circulating hot furnace gas in unit volume of eighty components to increase temperature, and then the mixture enters a pyrolysis system; therefore, the unit volume of furnace gas is only discharged about two times, and is only 1/4-1/5 of the smoke discharge amount in the conventional process.
Description
Technical Field
The invention relates to the technical field of chemical processes, in particular to a method for recycling energy.
Background
Pyrolysis is a common treatment method in chemical engineering and environmental engineering, and is used for heating solid substances to a certain temperature to cause decomposition reaction. A pyrolyzer is a chemical plant that performs pyrolysis processes to provide an enclosed space and serves as a site for the pyrolysis processes. The temperature of furnace gas discharged from the heating furnace of the fluidized pyrolyzer is about 500 ℃, in the prior art, the furnace gas is directly discharged into the atmosphere, which not only causes environmental pollution, but also can not utilize the waste heat.
In order to solve the problem, a typical treatment method is to exchange heat with furnace gas to fully cool the furnace gas, and then perform a waste gas treatment process to discharge the waste gas after the waste gas reaches the discharge standard. The treatment mode can only realize waste heat utilization to a certain extent, and the heat recovery efficiency is relatively low; moreover, the introduced waste gas treatment process can significantly prolong the overall process flow, and at the same time bring about treatment cost. Under the circumstances, if the furnace gas can be recycled, the technical problems are expected to be overcome, however, how to design the furnace gas recycling method and the energy recovery method according to the requirements of the pyrolysis process does not have a mature solution in the prior art.
Disclosure of Invention
The invention aims to provide a method for recycling energy aiming at the technical defects of the prior art, and aims to solve the technical problems of large waste gas discharge and large energy consumption of a heating furnace of a fluidized pyrolyzer in the prior art.
The invention also aims to solve the technical problem of how to recover and recycle energy of furnace gas discharged from the heating furnace of the fluidized pyrolyzer.
In order to achieve the technical purpose, the invention adopts the following technical scheme:
a method for energy recovery and recycling comprises the following steps:
1) conveying 75-85% of furnace gas quantity discharged from a heating furnace of the convection state pyrolyzer to the tail end of a combustion furnace through a thermal circulator to be uniformly mixed with high-temperature combustion gas, and using the obtained mixed high-temperature gas for pyrolysis reaction;
2) shunting 15-25% of furnace gas quantity discharged from a heating furnace of the fluidized pyrolyzer into a first heat exchanger, heating air, feeding the heated air into a combustion furnace, combusting the heated air with byproduct non-condensable combustible gas, mixing high-temperature combustion gas with circulating furnace gas, and using the mixed gas for pyrolysis reaction; and the split-flow furnace gas flowing through the first heat exchanger enters a second heat exchanger, and the desulfurized wet furnace gas is heated.
Preferably, the temperature of furnace gas discharged from the heating furnace of the fluidized pyrolyzer is 450-550 ℃; further preferably, the temperature is 500 ℃.
Preferably, the amount of furnace gas diverted is equal to the make-up gas amount of the fluidized pyrolyzer furnace.
Preferably, the first heat exchanger and the second heat exchanger are both located in a heat recovery system.
Preferably, in the step 2), the temperature of the heated air is 400-440 ℃; further preferably, the temperature is 420 ℃.
Preferably, in the step 2), after the high-temperature combustion gas is mixed with the circulating furnace gas, the temperature of the combustion gas is adjusted to 580-620 ℃; further preferably, the temperature thereof is adjusted to 600 ℃.
Preferably, in the step 2), the temperature of the flow-dividing furnace gas flowing through the first heat exchanger is 130-170 ℃; further preferably, the temperature is 150 ℃.
Preferably, in the step 2), the desulfurized wet furnace gas is heated to 75-85 ℃; further preferably, the temperature is heated to 80 ℃.
The invention provides a method for recycling and reusing energy. In the technical scheme, the high-level heat energy gas is circulated by using a thermal circulator, and is mixed with fresh high-temperature furnace gas after combustion to increase the temperature, and the two gases are combined for large circulation to accelerate the flow velocity, so that the temperature of each point of the pyrolysis reactor is uniform, and the yield and the utilization rate of equipment are improved. The shunted high-level heat energy furnace gas is fully transferred to combustion air; the energy can be saved by more than 60%. The pyrolysis process conditions depend on the difference of the inlet temperature and the outlet temperature of the heating gas and the heat transfer area, and the pyrolysis process can be satisfied by utilizing the hot furnace gas circulation and the heat exchange process. The discharged waste heat furnace gas is subjected to heat recovery on the second component in unit volume, heated air is combusted to increase temperature and then mixed with circulating hot furnace gas in unit volume of eighty components to increase temperature, and then the mixture enters a pyrolysis system; therefore, the unit volume of furnace gas is only discharged about two times, and is only 1/4-1/5 of the smoke discharge amount in the conventional process.
The invention has outstanding technical advantages in the aspects of energy saving and emission reduction. Wherein, in the aspect of energy saving: the high-level heat energy gas is circulated by using a thermal circulator, so that the yield and the utilization rate of equipment are improved, and the energy can be saved by over 60 percent; in the aspect of emission reduction: the pyrolysis process can be satisfied by utilizing hot furnace gas circulation and heat exchange processes, so that the emission of the invention is only 1/4-1/5 of the conventional emission.
The invention effectively overcomes the defects of large energy consumption, large waste gas discharge and the like in the conventional process; by applying the process disclosed by the invention, energy conservation and emission reduction can be effectively realized, and the production efficiency is improved.
Detailed Description
Hereinafter, specific embodiments of the present invention will be described in detail. Well-known structures or functions may not be described in detail in the following embodiments in order to avoid unnecessarily obscuring the details. Approximating language, as used herein in the following examples, may be applied to identify quantitative representations that could permissibly vary in number without resulting in a change in the basic function. Unless defined otherwise, technical and scientific terms used in the following examples have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
Example 1
A method for energy recovery and cyclic utilization comprises the following steps:
1. the temperature of furnace gas discharged from the heating furnace of the fluidized pyrolyzer is about 500 ℃, 80% of the furnace gas quantity enters a heat circulation system, and 20% of the furnace gas quantity is shunted to enter a heat recovery system (equal to the make-up gas quantity).
2. The furnace gas enters a thermal circulator and is sent to the tail end of a combustion furnace to be uniformly mixed with the high-temperature combustion gas, and the obtained mixed high-temperature gas can meet the heat and temperature provided by the reaction of the pyrolyzer.
3. The split high-level heat energy furnace gas enters a No. 1 heat exchanger, air is heated to about 420 ℃, hot air enters a combustion furnace to be combusted with byproduct non-condensable combustible gas, the high-temperature combustion gas is mixed with circulating furnace gas, the temperature is adjusted to about 600 ℃, and the requirements of a pyrolysis reaction process are met.
4. The temperature of the split-flow furnace gas is reduced to about 150 ℃ after the heat exchange between the split-flow furnace gas and the air in the No. 1 heat exchanger, the split-flow furnace gas enters the No. 2 heat exchanger, the temperature of the desulfurized wet furnace gas is increased to 80 ℃, the dew point of the flue gas is improved, and a good foundation is provided for the next step of furnace gas purification.
The method has the following technical advantages:
1. energy conservation: the high-level heat energy gas is circulated by using a thermal circulator, and is mixed with the combusted fresh high-temperature furnace gas for heating, and the two gases are combined for large circulation to accelerate the flow velocity, so that the temperature of each point of the pyrolysis reactor is uniform, and the yield and the utilization rate of equipment are improved. The shunted high-level heat energy furnace gas is fully transferred to combustion air. The energy can be saved by more than 60%.
2. Emission reduction: the pyrolysis process conditions depend on the difference of the inlet temperature and the outlet temperature of the heating gas and the heat transfer area, and the pyrolysis process can be satisfied by utilizing the hot furnace gas circulation and the heat exchange process. The discharged waste heat furnace gas occupies two components in unit volume for heat recovery, and the heated air is mixed with the circulating hot furnace gas occupying eight components in unit volume for temperature rise after being combusted and heated, and then enters a pyrolysis system. Therefore, the unit volume of furnace gas only discharges about two times, and the emission of flue gas is reduced by 4-5 times compared with the conventional emission.
Example 2
A method for energy recovery and recycling comprises the following steps:
1) conveying 75% of furnace gas quantity discharged from the heating furnace of the convection state pyrolyzer to the tail end of the combustion furnace through a thermal circulator to be uniformly mixed with high-temperature combustion gas, and using the obtained mixed high-temperature gas for pyrolysis reaction;
2) shunting 25% of furnace gas quantity discharged from a heating furnace of the fluidized pyrolyzer into a first heat exchanger to heat air, feeding the heated air into a combustion furnace to be combusted with byproduct non-condensable combustible gas, and mixing high-temperature combustion gas with circulating furnace gas for pyrolysis reaction; and the split-flow furnace gas flowing through the first heat exchanger enters a second heat exchanger, and the desulfurized wet furnace gas is heated.
Wherein the temperature of the furnace gas discharged from the heating furnace of the fluidized pyrolyzer is 450 ℃. The amount of the furnace gas which is shunted is equal to the amount of the make-up gas of the heating furnace of the fluidized pyrolyzer. The first heat exchanger and the second heat exchanger are both located in a heat recovery system. In step 2), the temperature of the heated air was 400 ℃. In the step 2), after the high-temperature combustion gas is mixed with the circulating furnace gas, the temperature is adjusted to 580 ℃. In the step 2), the temperature of the split-flow furnace gas flowing through the first heat exchanger is 130 ℃. In the step 2), the desulfurized wet furnace gas is heated to 75 ℃.
Example 3
A method for energy recovery and recycling comprises the following steps:
1) sending 85% of furnace gas quantity discharged from the heating furnace of the convection state pyrolyzer to the tail end of the combustion furnace through a thermal circulator to be uniformly mixed with high-temperature combustion gas, and using the obtained mixed high-temperature gas for pyrolysis reaction;
2) shunting 15% of furnace gas quantity discharged from a heating furnace of the fluidized pyrolyzer into a first heat exchanger to heat air, feeding the heated air into a combustion furnace to be combusted with byproduct non-condensable combustible gas, and mixing high-temperature combustion gas with circulating furnace gas for pyrolysis reaction; and the split-flow furnace gas flowing through the first heat exchanger enters a second heat exchanger, and the desulfurized wet furnace gas is heated.
Wherein the temperature of the furnace gas discharged from the heating furnace of the fluidized pyrolyzer is 550 ℃. In step 2), the temperature of the heated air was 440 ℃. In the step 2), after the high-temperature combustion gas is mixed with the circulating furnace gas, the temperature is adjusted to 620 ℃. In the step 2), the temperature of the split-flow furnace gas flowing through the first heat exchanger is 170 ℃. In the step 2), the desulfurized wet furnace gas is heated to 85 ℃.
Example 4
A method for energy recovery and recycling comprises the following steps:
1) conveying 80% of furnace gas quantity discharged from the heating furnace of the convection state pyrolyzer to the tail end of the combustion furnace through a thermal circulator to be uniformly mixed with high-temperature combustion gas, and using the obtained mixed high-temperature gas for pyrolysis reaction;
2) shunting 20% of furnace gas quantity discharged from a heating furnace of the fluidized pyrolyzer into a first heat exchanger to heat air, feeding the heated air into a combustion furnace to be combusted with byproduct non-condensable combustible gas, and mixing high-temperature combustion gas with circulating furnace gas for pyrolysis reaction; and the split-flow furnace gas flowing through the first heat exchanger enters a second heat exchanger, and the desulfurized wet furnace gas is heated.
The embodiments of the present invention have been described in detail, but the description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention. Any modification, equivalent replacement, and improvement made within the scope of the application of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. A method for energy recovery and recycling is characterized by comprising the following steps:
1) conveying 75-85% of furnace gas quantity discharged from a heating furnace of the convection state pyrolyzer to the tail end of a combustion furnace through a thermal circulator to be uniformly mixed with high-temperature combustion gas, and using the obtained mixed high-temperature gas for pyrolysis reaction;
2) shunting 15-25% of furnace gas quantity discharged from a heating furnace of the fluidized pyrolyzer into a first heat exchanger, heating air, feeding the heated air into a combustion furnace, combusting the heated air with byproduct non-condensable combustible gas, mixing high-temperature combustion gas with circulating furnace gas, and using the mixed gas for pyrolysis reaction; and the split-flow furnace gas flowing through the first heat exchanger enters a second heat exchanger, and the desulfurized wet furnace gas is heated.
2. The method according to claim 1, wherein the temperature of the furnace gas discharged from the fluidized pyrolyzer heating furnace is 450-550 ℃.
3. The method of claim 1, wherein the amount of furnace gas diverted is equal to the amount of make-up gas for the fluidized pyrolyzer furnace.
4. A method of energy recovery and recycling according to claim 1, wherein said first heat exchanger and said second heat exchanger are both located in a heat recovery system.
5. The method for energy recovery and recycling according to claim 1, wherein the temperature of the heated air in step 2) is 400-440 ℃.
6. The method according to claim 1, wherein the temperature of the combustion gas with high temperature in step 2) is adjusted to 580-620 ℃ after mixing with the circulating furnace gas.
7. The method for energy recovery and recycling according to claim 1, wherein in the step 2), the temperature of the split-flow furnace gas after flowing through the first heat exchanger is 130-170 ℃.
8. The method for recycling energy of claim 1, wherein in the step 2), the desulfurized wet furnace gas is heated to 75-85 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010012204.2A CN111139088A (en) | 2020-01-07 | 2020-01-07 | Method for recycling and reusing energy |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202010012204.2A CN111139088A (en) | 2020-01-07 | 2020-01-07 | Method for recycling and reusing energy |
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| CN111139088A true CN111139088A (en) | 2020-05-12 |
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Citations (8)
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|---|---|---|---|---|
| CN101761920A (en) * | 2009-12-16 | 2010-06-30 | 上海理工大学 | Method and device for burning low NOx by utilizing reburning of pulverized coal pyrolysis gas |
| US20100314235A1 (en) * | 2009-06-16 | 2010-12-16 | Exxonmobil Research And Engineering Company | High temperature hydropyrolysis of carbonaceous materials |
| CN204138600U (en) * | 2014-08-19 | 2015-02-04 | 湖南华银能源技术有限公司 | High-temperature hot is vented one's spleen recycling system |
| CN205061978U (en) * | 2015-09-15 | 2016-03-02 | 农业部规划设计研究院 | Living beings pyrolysis gas firing and heat retrieval and utilization device |
| CN107163965A (en) * | 2017-06-26 | 2017-09-15 | 农业部规划设计研究院 | Turn round pyrolysis oven combination decoking and hot blast recycling system |
| CN206970532U (en) * | 2017-07-19 | 2018-02-06 | 山东拓普环境科技有限公司 | A kind of energy-saving environmental protection device of oil sludge and sand pyrolytic process |
| GB2553919A (en) * | 2016-09-20 | 2018-03-21 | Phan Anthony | Biomass treatment process and apparatus |
| CN108977211A (en) * | 2018-08-03 | 2018-12-11 | 浙江工业大学 | A kind of solid waste pyrolysis system that coupling high temperature pyrolysis gas are directly burnt |
-
2020
- 2020-01-07 CN CN202010012204.2A patent/CN111139088A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100314235A1 (en) * | 2009-06-16 | 2010-12-16 | Exxonmobil Research And Engineering Company | High temperature hydropyrolysis of carbonaceous materials |
| CN101761920A (en) * | 2009-12-16 | 2010-06-30 | 上海理工大学 | Method and device for burning low NOx by utilizing reburning of pulverized coal pyrolysis gas |
| CN204138600U (en) * | 2014-08-19 | 2015-02-04 | 湖南华银能源技术有限公司 | High-temperature hot is vented one's spleen recycling system |
| CN205061978U (en) * | 2015-09-15 | 2016-03-02 | 农业部规划设计研究院 | Living beings pyrolysis gas firing and heat retrieval and utilization device |
| GB2553919A (en) * | 2016-09-20 | 2018-03-21 | Phan Anthony | Biomass treatment process and apparatus |
| CN107163965A (en) * | 2017-06-26 | 2017-09-15 | 农业部规划设计研究院 | Turn round pyrolysis oven combination decoking and hot blast recycling system |
| CN206970532U (en) * | 2017-07-19 | 2018-02-06 | 山东拓普环境科技有限公司 | A kind of energy-saving environmental protection device of oil sludge and sand pyrolytic process |
| CN108977211A (en) * | 2018-08-03 | 2018-12-11 | 浙江工业大学 | A kind of solid waste pyrolysis system that coupling high temperature pyrolysis gas are directly burnt |
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Application publication date: 20200512 |
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