CN111777038A - Waste heat recovery system and method for hydrogen production converter - Google Patents
Waste heat recovery system and method for hydrogen production converter Download PDFInfo
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- 239000002918 waste heat Substances 0.000 title claims abstract description 49
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 39
- 239000001257 hydrogen Substances 0.000 title claims abstract description 39
- 238000011084 recovery Methods 0.000 title claims abstract description 39
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 21
- 239000002994 raw material Substances 0.000 claims abstract description 179
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 65
- 239000003546 flue gas Substances 0.000 claims abstract description 65
- 238000006243 chemical reaction Methods 0.000 claims abstract description 62
- 238000001704 evaporation Methods 0.000 claims abstract description 31
- 230000008020 evaporation Effects 0.000 claims abstract description 31
- 239000002737 fuel gas Substances 0.000 claims abstract description 12
- 238000007670 refining Methods 0.000 claims description 18
- 238000002407 reforming Methods 0.000 claims description 17
- 230000008569 process Effects 0.000 claims description 8
- 238000013021 overheating Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 description 11
- 230000005855 radiation Effects 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 239000000446 fuel Substances 0.000 description 6
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 150000001336 alkenes Chemical class 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000002336 sorption--desorption measurement Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- -1 steam Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- 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
- C01B3/34—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
- C01B3/38—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 catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
- C01B2203/0816—Heating by flames
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0872—Methods of cooling
- C01B2203/0883—Methods of cooling by indirect heat exchange
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1258—Pre-treatment of the feed
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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
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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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- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention provides a waste heat recovery system and a method for a hydrogen production converter, wherein the waste heat recovery system comprises: the waste heat recovery system comprises a conversion raw material preheating section, a steam superheating section, a high-temperature air preheating section, an evaporation section and a low-temperature air preheating section which are sequentially connected in series through a flue, and the waste heat recovery system also comprises a raw material preheating section which is connected in series with the evaporation section and/or the low-temperature air preheating section through the flue; the preheating medium of the raw material preheating section is the conversion raw material and/or the fuel gas of the hydrogen production conversion furnace. After the technical scheme is adopted, the waste heat of the flue gas can be fully utilized, and the temperature of the flue gas is reduced to 70-120 ℃.
Description
Technical Field
The invention relates to the technical field of waste heat recovery, in particular to a waste heat recovery system and method for a hydrogen production converter.
Background
The hydrogen production process by light hydrocarbon steam conversion is widely used in petrochemical industry, and high-purity hydrogen products are produced to be used as hydrogen raw materials for oil product hydrotreatment (refining, cracking, synthesis and the like). The process uses light hydrocarbon (natural gas, refinery gas, liquefied gas, naphtha, etc.) as raw material, and through water vapor conversion reaction, transformation reaction and pressure swing adsorption purification, 99.9% purity hydrogen product is obtained.
The core equipment of the process is a hydrogen production converter, raw material gas and water vapor are mixed and then enter a converter tube of a radiation section in the converter, a conversion catalyst is filled in the tube, and the conversion reaction is completed at the temperature of about 850 ℃. The pressure swing adsorption desorption gas is used as the main fuel of the reformer, and the shortage is supplemented by a factory fuel gas pipe network. In order to improve the heat efficiency of the reformer, the outlet of the radiation section is provided with a convection section for recovering the waste heat of the flue gas, the industrial device is respectively provided with a part or all of waste heat recovery facilities such as a water protection section, a reforming raw material preheating section, a pre-reforming raw material preheating section, a steam superheating section, a high-temperature air preheating section, an evaporation section, a low-temperature air preheating section and the like, and the schematic diagram of the heat exchange process is shown in figure 1. The high-temperature flue gas in the radiation chamber of the hydrogen production reforming furnace is subjected to heat exchange by the device, the temperature of the flue gas is reduced to 140-180 ℃, and the flue gas enters a chimney through a draught fan and is discharged, so that the thermal efficiency is about 90%.
The main reasons that the conventional waste heat recovery facility cannot realize lower smoke emission temperature are as follows: the pressure swing adsorption desorption gas flow is large, the heat value is low (the content of CO2 is as high as 50-55%), the quantity of flue gas formed after combustible components are completely combusted is 28-30% more than that of flue gas generated by combustion of factory fuel gas, the flue gas is influenced by the temperature of saturated water after being recovered by the waste heat of all sections, the temperature of the flue gas discharged from an evaporation section is generally 270-320 ℃ and cannot be further reduced, the air is adopted for recovering the flue gas waste heat in the last section of low-temperature air preheating section, the air quantity is only 60-80% of the flue gas quantity, the influence of the heat exchange balance of the flue gas and the air and the temperature of an air inlet is avoided, the temperature of the flue gas cannot be reduced to a lower temperature due to insufficient cold sources, no more low-temperature.
The raw materials of the hydrogen production device need olefin saturation and deep desulfurization pretreatment before entering the converter, the temperature is required to be above 320 ℃, a heating furnace or superheated steam is generally adopted for heating in practical application, and additionally, the consumption of fuel gas or medium-pressure superheated steam of the device is increased.
With the continuous improvement of the national requirements for carbon emission, if the thermal efficiency of the hydrogen production converter in the actual industrial production is operated at a lower efficiency for a long time, not only the waste of fuel is caused and the economic benefit of enterprises is influenced, but also the requirements of national relevant standards can not be met, and the development of the enterprises is seriously restricted.
The invention aims to provide a waste heat recovery system and a waste heat recovery method for a hydrogen production converter, which have lower exhaust gas temperature and higher waste heat recovery efficiency.
Disclosure of Invention
In order to overcome the technical defects, the invention utilizes the temperature level of the flue gas and combines the flow and heat load requirements of waste heat media such as raw material gas, steam, air and boiler feed water inside the device to carry out reasonable heat exchange flow optimization, so that the flue gas waste heat is fully utilized, and the waste heat recovery system and the method for the hydrogen production conversion furnace have lower exhaust gas temperature and higher waste heat recovery efficiency.
The invention discloses a waste heat recovery system for a hydrogen production converter, which comprises: the waste heat recovery system comprises a conversion raw material preheating section, a steam superheating section, a high-temperature air preheating section, an evaporation section and a low-temperature air preheating section which are sequentially connected in series through a flue, and the waste heat recovery system also comprises a raw material preheating section which is connected in series with the evaporation section and/or the low-temperature air preheating section through the flue;
the preheating medium of the raw material preheating section is the conversion raw material and/or the fuel gas of the hydrogen production conversion furnace.
Preferably, the raw material preheating section is connected in series between the high-temperature air preheating section and the evaporation section through a flue;
or the raw material preheating section is connected in series between the steam superheating section and the high-temperature air preheating section through a flue;
or the raw material preheating section is connected in series between the conversion raw material preheating section and the steam superheating section through a flue;
or the raw material preheating section is connected in series between the evaporation section and the low-temperature air preheating section through a flue;
or the raw material preheating section is connected in series between the low-temperature air preheating section and the chimney through a flue.
Preferably, the feed preheating section comprises a first high temperature feed preheating section and a first low temperature feed preheating section;
the first high-temperature raw material preheating section is connected in series between the high-temperature air preheating section and the evaporation section through a flue, and the first low-temperature raw material preheating section is connected in series between the evaporation section and the low-temperature air preheating section through a flue.
Preferably, the preheating medium outlet of the first low-temperature raw material preheating section is connected with the preheating medium inlet of the first high-temperature raw material preheating section through a pipeline.
Preferably, the feed preheating section comprises a second high temperature feed preheating section and a second low temperature feed preheating section;
the second high-temperature raw material preheating section is connected in series between the high-temperature air preheating section and the evaporation section through a flue,
the second low-temperature raw material preheating section is connected in series between the low-temperature air preheating section and the chimney through a flue.
Preferably, the positions of the steam superheating section and the high-temperature air preheating section in the process can be interchanged;
preferably, the preheating medium outlet of the second low-temperature raw material preheating section is connected with the preheating medium inlet of the second high-temperature raw material preheating section through a pipeline.
Preferably, the preheating medium of the feedstock preheating section is a conversion feedstock;
a preheating medium outlet of the raw material preheating section is connected with a raw material refining device;
and a medium outlet of the raw material refining device is connected with a conversion raw material preheating section.
The invention also discloses a waste heat recovery method for the hydrogen production converter, which comprises the following steps:
flue gas from a hydrogen production reforming furnace exchanges heat sequentially through a reforming raw material preheating section, a steam superheating section and a high-temperature air preheating section, and the flue gas is subjected to heat exchange to 450-550 ℃;
the flue gas discharged from the high-temperature air preheating section exchanges heat through the evaporation section, the low-temperature air preheating section and the raw material preheating section, and the heat of the flue gas is exchanged to below 70-120 ℃;
wherein, the raw material preheating section is connected with the evaporation section and/or the low-temperature air preheating section in series through a flue; the preheating medium of the raw material preheating section is the conversion raw material and/or the fuel gas of the hydrogen production conversion furnace.
Preferably, the temperature of the preheating medium of the raw material preheating section entering the raw material preheating section is not more than 50 ℃;
the temperature of the preheating medium after heat exchange in the raw material preheating section is 300-400 ℃.
Preferably, the preheating medium of the feedstock preheating section is a conversion feedstock; a preheating medium outlet of the raw material preheating section is connected with a raw material refining device; the medium outlet of the raw material refining device is connected with a conversion raw material preheating section;
the temperature of the conversion raw material after heat exchange in the raw material preheating section is 300-400 ℃;
the converted raw material enters a raw material refining device for refining after heat exchange in a raw material preheating section;
the refined conversion raw material enters a conversion raw material preheating section to exchange heat with the flue gas, and the temperature of the conversion raw material after heat exchange is 530-630 ℃.
After the technical scheme is adopted, compared with the prior art, the method has the following beneficial effects:
1. the consumption of extra energy is reduced by adding a raw material preheating section, and meanwhile, due to the low-temperature property of the raw material preheating section, a low-temperature cold source in a flue gas waste heat recovery system is added, so that the flue gas waste heat can be fully utilized, the exhaust gas temperature is reduced to 70-120 ℃, and the thermal efficiency of 93-95% is realized;
2. the outlet temperature of the original conversion raw material is about 520 ℃, the flue gas with higher temperature level directly enters the conversion raw material preheating section to heat the conversion raw material by canceling the water protection section, and the outlet temperature of the conversion raw material is raised to 530-630 ℃ to enter the radiation section of the converter, so that the overall load of the radiation section is reduced, the fuel gas consumption of the converter is reduced from the source, and the energy conservation and emission reduction are realized.
3. The air preheating section and the raw material preheating section are both in two sections (or in one section when the temperature meets the requirement), the waste heat of the flue gas is absorbed to the maximum extent, the heat absorption capacity of the steam superheating section and the evaporation section is reduced, and the unnecessary steam yield is reduced, so that the overall heat load of the reformer is reduced, and the fuel gas consumption is reduced.
Drawings
FIG. 1 is a schematic flow diagram of a flue gas waste heat recovery system of a hydrogen production reformer in the prior art
FIG. 2 is a schematic flow diagram of a waste heat recovery system of a hydrogen production reformer according to an embodiment of the present invention;
FIG. 3 is a schematic flow diagram of a waste heat recovery system of a hydrogen production reformer in another embodiment of the present invention.
Reference numerals:
1-high temperature flue gas in a radiation chamber of a hydrogen production reforming furnace, 2-a reforming raw material preheating section, 3-a steam superheating section, 4-a high temperature air preheating section, 5-a high temperature raw material preheating section, 6-an evaporation section, 7-a low temperature raw material preheating section, and 8-a low temperature air preheating section.
Detailed Description
The advantages of the invention are further illustrated in the following description of specific embodiments in conjunction with the accompanying drawings.
Reference will now be made in detail to the exemplary embodiments, examples of which are illustrated in the accompanying drawings. When the following description refers to the accompanying drawings, like numbers in different drawings represent the same or similar elements unless otherwise indicated. The implementations described in the exemplary embodiments below are not intended to represent all implementations consistent with the present disclosure. Rather, they are merely examples of apparatus and methods consistent with certain aspects of the present disclosure, as detailed in the appended claims.
The terminology used in the present disclosure is for the purpose of describing particular embodiments only and is not intended to be limiting of the disclosure. As used in this disclosure and the appended claims, the singular forms "a," "an," and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise. It should also be understood that the term "and/or" as used herein refers to and encompasses any and all possible combinations of one or more of the associated listed items.
In the description of the present invention, unless otherwise specified and limited, it is to be noted that the terms "mounted," "connected," and "connected" are to be interpreted broadly, and may be, for example, a mechanical connection or an electrical connection, a communication between two elements, a direct connection, or an indirect connection via an intermediate medium, and specific meanings of the terms may be understood by those skilled in the art according to specific situations.
In the following description, suffixes such as "module", "component", or "unit" used to denote elements are used only for facilitating the explanation of the present invention, and have no specific meaning in themselves. Thus, "module" and "component" may be used in a mixture.
Referring to the attached drawing 2, in the embodiment of the present invention, a flow schematic diagram of a waste heat recovery system of a hydrogen production reformer is shown, in which a reforming raw material preheating section 2, a steam superheating section 3, a high temperature air preheating section 4, a high temperature raw material preheating section 5, an evaporation section 6, a low temperature raw material preheating section 7, and a low temperature air preheating section 8 are sequentially connected by a flue, and flue gas after heat exchange in the low temperature air preheating section 8 is introduced into a chimney through an induced draft fan and discharged. High-temperature flue gas 1 coming out from the radiation section of the hydrogen-making reformer sequentially passes through a reforming raw material preheating section 2, a steam superheating section 3, a high-temperature air preheating section 4, a high-temperature raw material preheating section 5, an evaporation section 6, a low-temperature raw material preheating section 7 and a low-temperature air preheating section 8 for heat exchange. Air is firstly introduced into the low-temperature air preheating section 8 to exchange heat with the flue gas, then is subjected to heat exchange with the flue gas through the high-temperature air preheating section 4, and is then introduced into the hydrogen production reforming furnace. Raw materials (light hydrocarbon: natural gas, refinery gas, liquefied gas, naphtha and the like) of the hydrogen production conversion furnace are firstly introduced into the low-temperature raw material preheating section 7 to exchange heat with the flue gas, and then introduced into the high-temperature raw material preheating section 5 to exchange heat with the flue gas, the conversion raw material after heat exchange in the high-temperature raw material preheating section 5 is introduced into the raw material refining device to be refined, the raw material refining device can be used for carrying out olefin saturation and deep desulfurization pretreatment on the conversion raw material, the refined conversion raw material is introduced into the conversion raw material preheating section 2 to exchange heat with the flue gas, and the conversion raw material after heat exchange in the conversion raw material preheating section. In this embodiment, the preheating medium of the low-temperature raw material preheating section 7 and the high-temperature raw material preheating section 5 is the conversion raw material of the hydrogen-production converter, and in other embodiments, the preheating medium may also be the fuel of the hydrogen-production converter, such as supplementary fuel, which is preheated by the low-temperature raw material preheating section 7 and the high-temperature raw material preheating section 5 in sequence and then introduced into the hydrogen-production converter. In other embodiments, the preheating mediums of the low temperature feedstock preheating section 7 and the high temperature feedstock preheating section 5 may be different, such as preheating the fuel and reforming feedstock of the hydrogen-producing reformer by the low temperature feedstock preheating section 7 and the high temperature feedstock preheating section 5, respectively. In this embodiment, the high temperature flue gas 1 coming out from the radiation section of the hydrogen generation reformer is about 800-1100 ℃, and the temperature of the flue gas after heat exchange in the preheating section 2 of the reforming raw material is as follows: 700-800 ℃, wherein the heat exchange medium for heat exchange with the flue gas in the heat exchanger type tube/finned tube heat exchange section of the conversion raw material preheating section 2 is a conversion raw material of the hydrogen production converter, and comprises light hydrocarbon and water vapor. The flue gas temperature after heat exchange in the steam superheating section 3 is as follows: the heat exchanger type of the steam superheating section 3 is a tubular/finned tube heat exchange section at 550-650 ℃. The flue gas temperature after heat exchange in the high-temperature air preheating section 4 is as follows: the heat exchanger type of the high-temperature air preheating section 4 can be various types of air preheaters at 450-550 ℃. The flue gas temperature after heat exchange by the high-temperature raw material preheater 5 is as follows: the temperature of 350-450 ℃ and the type of the heat exchanger of the high-temperature raw material preheater 5 are tube/finned tube heat exchange sections. The flue gas temperature after heat exchange in the low-temperature raw material preheating section 7 is as follows: the heat exchanger type of the low-temperature raw material preheating section 7 is a tubular/finned tube heat exchanger at 140-180 ℃. The flue gas temperature after heat exchange in the low-temperature air preheating section 8 is as follows: the heat exchanger type of the low-temperature air preheating section 8 is various air preheaters at 70-120 ℃. Air is introduced into the low-temperature air preheating section 8 from normal temperature through the air blower to exchange heat with the flue gas to 120-150 ℃, and then introduced into the high-temperature air preheating section 4 to exchange heat with the flue gas to 450-600 ℃. The conversion raw material is introduced into a low-temperature raw material preheating section 7 from the temperature of not more than 50 ℃ (preferably 40 ℃) to exchange heat with flue gas to 200-250 ℃, then introduced into a high-temperature raw material preheating section 5 to exchange heat with the flue gas to 300-400 ℃, and then introduced into a raw material refining device to be refined, the refined conversion raw material is introduced into a conversion raw material preheating section 2 to exchange heat with the flue gas, and the temperatures of the conversion raw material before and after heat exchange of the conversion raw material preheating section 2 are 350-450 ℃ and 530-630 ℃ respectively.
In the above examples, the feed preheating section includes a low temperature feed preheating section and a high temperature feed preheating section. In other embodiments, the raw material preheating section can be provided with only one section and is connected in series between the high-temperature air preheating section and the evaporation section through a flue; or the flue is connected in series between the evaporation section and the low-temperature air preheating section; or the low-temperature air preheating section is connected in series between the low-temperature air preheating section and the chimney through a flue. In other embodiments, more than two feed preheating sections can be provided in series with the evaporation section and/or the low temperature air preheating section.
Referring to the attached drawing 3, in the embodiment of the present invention, a flow schematic diagram of a waste heat recovery system of a hydrogen production reformer is shown, in which a reforming raw material preheating section 2, a steam superheating section 3, a high temperature air preheating section 4, a high temperature raw material preheating section 5, an evaporation section 6, a low temperature air preheating section 8, and a low temperature raw material preheating section 7 are sequentially connected by a flue, and flue gas after heat exchange in the low temperature raw material preheating section 7 is introduced into a chimney through an induced draft fan and discharged. High-temperature flue gas 1 coming out from the radiation section of the hydrogen-making reformer sequentially passes through a reforming raw material preheating section 2, a steam superheating section 3, a high-temperature air preheating section 4, a high-temperature raw material preheating section 5, an evaporation section 6, a low-temperature air preheating section 8 and a low-temperature raw material preheating section 7 for heat exchange. Air is firstly introduced into the low-temperature air preheating section 8 to exchange heat with the flue gas, then is subjected to heat exchange with the flue gas through the high-temperature air preheating section 4, and is then introduced into the hydrogen production reforming furnace. The conversion raw material of the hydrogen production conversion furnace is firstly introduced into the low-temperature raw material preheating section 7 to exchange heat with the flue gas, then introduced into the high-temperature raw material preheating section 5 to exchange heat with the flue gas, the conversion raw material after heat exchange in the high-temperature raw material preheating section 5 is introduced into the raw material refining device to be refined, the raw material refining device can be used for olefin saturation and deep desulfurization pretreatment on the conversion raw material, the refined conversion raw material is introduced into the conversion raw material preheating section 2 to exchange heat with the flue gas, and the conversion raw material after heat exchange in the conversion raw material preheating section 2 is introduced into the.
According to the technical scheme, the flue gas waste heat of the converter can be deeply utilized, the temperature of the flue gas can be reduced to 70-120 ℃, the heat efficiency of the converter can be stably improved to 93-95% for a long period, and the energy consumption of the device is greatly reduced. And the waterless protection section is cancelled, so that the temperature of the conversion raw material entering the conversion furnace can be effectively increased by using the high-temperature flue gas, the load of the heating furnace and the consumption of fuel gas are reduced from the source, and the operation cost is reduced. Meanwhile, the process medium can be heated by fully utilizing the flue gas waste heat at different temperature positions, so that the fuel energy consumption or superheated steam energy consumption of the original raw material to be preheated is directly reduced, the energy consumption of the device is reduced, the medium in the system is utilized to the maximum extent for flue gas waste heat recovery, the extra steam yield is reduced, the operation load of the hydrogen production reformer is integrally reduced, and the unnecessary fuel gas consumption is reduced. The invention has simple process flow and low investment cost, and can ensure long-period operation of the whole process equipment.
It should be noted that the embodiments of the present invention have been described in terms of preferred embodiments, and not by way of limitation, and that those skilled in the art can make modifications and variations of the embodiments described above without departing from the spirit of the invention.
Claims (12)
1. A waste heat recovery system for a hydrogen-producing reformer, comprising: a conversion raw material preheating section, a steam superheating section, a high-temperature air preheating section, an evaporation section and a low-temperature air preheating section which are sequentially connected in series through a flue,
the waste heat recovery system also comprises a raw material preheating section, and the raw material preheating section is connected with the evaporation section and/or the low-temperature air preheating section in series through a flue;
the preheating medium of the raw material preheating section is the conversion raw material and/or the fuel gas of the hydrogen production conversion furnace.
2. The waste heat recovery system of claim 1,
the raw material preheating section is connected in series between the high-temperature air preheating section and the evaporation section through a flue;
or the raw material preheating section is connected in series between the steam superheating section and the high-temperature air preheating section through a flue;
or the raw material preheating section is connected in series between the conversion raw material preheating section and the steam superheating section through a flue;
or the raw material preheating section is connected in series between the evaporation section and the low-temperature air preheating section through a flue;
or the raw material preheating section is connected in series between the low-temperature air preheating section and the chimney through a flue.
3. The waste heat recovery system of claim 1,
the raw material preheating section comprises a first high-temperature raw material preheating section and a first low-temperature raw material preheating section;
the first high-temperature raw material preheating section is connected in series between the high-temperature air preheating section and the evaporation section through a flue, and the first low-temperature raw material preheating section is connected in series between the evaporation section and the low-temperature air preheating section through a flue.
4. The waste heat recovery system of claim 3,
and a preheating medium outlet of the first low-temperature raw material preheating section is connected with a preheating medium inlet of the first high-temperature raw material preheating section through a pipeline.
5. The waste heat recovery system of claim 1,
the raw material preheating section comprises a second high-temperature raw material preheating section and a second low-temperature raw material preheating section;
the second high-temperature raw material preheating section is connected in series between the high-temperature air preheating section and the evaporation section through a flue,
the second low-temperature raw material preheating section is connected in series between the low-temperature air preheating section and the chimney through a flue.
6. The waste heat recovery system of claim 5,
and a preheating medium outlet of the second low-temperature raw material preheating section is connected with a preheating medium inlet of the second high-temperature raw material preheating section through a pipeline.
7. The waste heat recovery system of claim 5,
the positions of the steam overheating section and the high-temperature air preheating section in the process can be interchanged.
8. The waste heat recovery system of claim 1,
the preheating medium of the raw material preheating section is a device raw material;
a preheating medium outlet of the raw material preheating section is connected with a raw material refining device;
and a medium outlet of the raw material refining device is connected with a conversion raw material preheating section.
9. A waste heat recovery method for a hydrogen production converter is characterized by comprising the following steps:
flue gas from a hydrogen production reforming furnace exchanges heat sequentially through a reforming raw material preheating section, a steam superheating section and a high-temperature air preheating section, and the flue gas is subjected to heat exchange to 450-550 ℃;
the flue gas discharged from the high-temperature air preheating section exchanges heat through the evaporation section, the low-temperature air preheating section and the raw material preheating section, and the heat of the flue gas is exchanged to 70-120 ℃;
wherein, the raw material preheating section is connected with the evaporation section and/or the low-temperature air preheating section in series through a flue; the preheating medium of the raw material preheating section is the conversion raw material and/or the fuel gas of the hydrogen production conversion furnace.
10. The waste heat recovery method according to claim 9,
the temperature of the preheating medium of the raw material preheating section entering the raw material preheating section is not more than 50 ℃;
the temperature of the preheating medium after heat exchange in the raw material preheating section is 300-400 ℃.
11. The waste heat recovery method according to claim 10,
the preheating medium of the raw material preheating section is a conversion raw material; a preheating medium outlet of the raw material preheating section is connected with a raw material refining device; the medium outlet of the raw material refining device is connected with a conversion raw material preheating section;
the temperature of the raw material is 300-400 ℃ after heat exchange in the raw material preheating section;
after heat exchange in the raw material preheating section, the raw material enters a raw material refining device for refining;
and mixing the refined raw material with steam to form a conversion raw material, entering a conversion raw material preheating section to exchange heat with flue gas, wherein the temperature of the conversion raw material after heat exchange is 530-630 ℃.
12. The waste heat recovery method according to claim 1,
the high-temperature air preheating section, the high-temperature raw material preheating section, the low-temperature air preheating section and the low-temperature raw material preheating section can distribute flue gas in a parallel flow or counter flow mode to obtain heat and control the outlet temperature of a medium.
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