CN108931150B - Integrated heat exchange equipment in natural gas hydrogen production system - Google Patents
Integrated heat exchange equipment in natural gas hydrogen production system Download PDFInfo
- Publication number
- CN108931150B CN108931150B CN201810302819.1A CN201810302819A CN108931150B CN 108931150 B CN108931150 B CN 108931150B CN 201810302819 A CN201810302819 A CN 201810302819A CN 108931150 B CN108931150 B CN 108931150B
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- CN
- China
- Prior art keywords
- heat exchange
- flue gas
- tube bundle
- natural gas
- gas tube
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- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 132
- 239000003345 natural gas Substances 0.000 title claims abstract description 63
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 18
- 239000001257 hydrogen Substances 0.000 title claims abstract description 18
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 16
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 13
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 90
- 239000003546 flue gas Substances 0.000 claims abstract description 89
- 239000007789 gas Substances 0.000 claims abstract description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 238000006243 chemical reaction Methods 0.000 claims abstract description 26
- 239000002994 raw material Substances 0.000 claims abstract description 11
- 239000000203 mixture Substances 0.000 claims description 12
- 238000009413 insulation Methods 0.000 claims description 4
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000002918 waste heat Substances 0.000 description 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- 238000006477 desulfuration reaction Methods 0.000 description 5
- 230000023556 desulfurization Effects 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 238000010276 construction Methods 0.000 description 2
- QDOXWKRWXJOMAK-UHFFFAOYSA-N dichromium trioxide Chemical compound O=[Cr]O[Cr]=O QDOXWKRWXJOMAK-UHFFFAOYSA-N 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 231100000572 poisoning Toxicity 0.000 description 2
- 230000000607 poisoning effect Effects 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The invention provides integrated heat exchange equipment in a natural gas hydrogen production system, which comprises a first heat exchange part and a second heat exchange part which are integrally manufactured; the first heat exchange part comprises a flue gas cylinder, a raw material natural gas coil and a natural gas steam mixed gas coil, and the second heat exchange part comprises a conversion gas tube bundle, a first flue gas tube bundle and a boiler water supply shell; the first flue gas tube bundle is connected in series to the outlet of the flue gas cylinder. The integrated heat exchange equipment disclosed by the invention reasonably optimizes and effectively integrates a plurality of heat exchange equipment in the natural gas hydrogen production process, so that the equipment investment can be saved, the heat exchange efficiency of a system is improved, the heat loss of a device is reduced, and the energy consumption of the device is finally reduced.
Description
Technical Field
The invention relates to heat exchange equipment, in particular to integrated heat exchange equipment applied to a natural gas hydrogen production system.
Background
At present, heat utilization of high-temperature flue gas in a natural gas hydrogen production device generally adopts a convection section, and the convection section consists of a plurality of independent heat exchange tubes. When the high-temperature flue gas passes through the convection section, the high-temperature flue gas exchanges heat with the natural gas steam mixed gas, the raw material natural gas, the boiler water supply, the air and the like in sequence, and finally is discharged into the atmosphere through an induced draft fan. The heat recovery of the conversion gas is performed by an independent conversion gas waste heat boiler, wherein the waste heat boiler is generally a tube type heat exchange device, the tube side of the waste heat boiler is used for removing the conversion gas, the shell side of the waste heat boiler is used for removing the boiler feed water, and saturated steam is generated after the heat exchange of the conversion gas and the boiler feed water.
For a small device, more than 50% of each heat exchange tube in the smoke convection section is positioned in the heat insulation layer of the tube box and does not directly contact with smoke for heat exchange; in order to ensure the utilization rate of the heat of the flue gas, the heat exchange tube array of the convection section has the defects of large number of heat exchange tubes, large area, high investment, large occupied area and the like.
In addition, in the existing scheme, a flue gas waste heat boiler is arranged in the flue gas convection section, residual flue gas heat is exchanged with boiler feed water, and converted gas is exchanged with the boiler feed water through an independent converted gas waste heat boiler, so that equipment and resources are repeated and wasted.
Disclosure of Invention
In order to solve the problems, the invention provides integrated heat exchange equipment in a natural gas hydrogen production system, which combines various mediums such as raw natural gas, natural gas steam mixture, conversion gas, flue gas, boiler water supply and the like to exchange heat, and different mediums are in different heat exchange channels, so that the respective heat exchange purposes are finally achieved.
The integrated heat exchange equipment comprises a first heat exchange part and a second heat exchange part which are integrally manufactured; the first heat exchange part comprises a flue gas cylinder, a raw material natural gas coil and a natural gas steam mixed gas coil, and the second heat exchange part comprises a conversion gas tube bundle, a first flue gas tube bundle and a boiler water supply shell; the first flue gas tube bundle is connected in series to the outlet of the flue gas cylinder.
Preferably, the raw material natural gas coil and the natural gas steam mixed gas coil are embedded in the flue gas cylinder, and the natural gas steam mixed gas coil is located between the inlet of the flue gas cylinder and the raw material natural gas coil.
Preferably, the inner wall of the flue gas cylinder is provided with a heat insulation layer.
Preferably, a plurality of baffle plates are arranged in the flue gas cylinder along the length direction of the cylinder.
Preferably, the second heat exchange part further comprises a second flue gas tube bundle, and the second heat exchange part is used for enabling the flue gas output by the first flue gas tube bundle to exchange heat with boiler feed water again.
Preferably, the layout of the first flue gas tube bundle, the second flue gas tube bundle and the conversion gas tube bundle is adapted to the cylindrical boiler feedwater housing, so that the volume or the floor space of the integrated heat exchange device is minimized.
Specifically, the second flue gas tube bundle is located on the upper side or the lower side of the first flue gas tube bundle.
Specifically, the conversion gas tube bundle is located at the front side or the rear side of the first flue gas tube bundle and the second flue gas tube bundle.
Through the integrated heat exchange equipment, various mediums such as raw natural gas, natural gas steam mixed gas, converted gas, flue gas, boiler water supply and the like are combined for heat exchange, and a plurality of heat exchange equipment in the natural gas hydrogen production process are reasonably optimized and effectively integrated, so that equipment investment can be saved, the heat exchange efficiency of a system is improved, the heat loss of a device is reduced, and finally the energy consumption of the device is reduced.
Drawings
FIG. 1 is a schematic illustration of an exemplary natural gas hydrogen production process flow;
FIG. 2A is a schematic front view of an integrated heat exchange device according to an exemplary embodiment;
FIG. 2B is a schematic top view of an integrated heat exchange device according to an exemplary embodiment;
fig. 2C is a schematic left-hand view of an integrated heat exchange device according to an example embodiment.
Detailed Description
The invention is explained in more detail below with reference to the drawings.
Referring to fig. 1, the conventional natural gas hydrogen production process includes the following steps.
Desulfurizing: preheating raw natural gas to about 300-400 ℃ and then carrying out desulfurization treatment. The raw natural gas in this example is methane-based natural gas, contains various impurities, and generally contains trace amounts of sulfur. The purpose of desulfurization is to avoid poisoning of the catalyst in later steps, and the conversion catalyst is extremely susceptible to poisoning and loss of activity during use, and strict requirements are placed on the impurity content in the raw material, particularly the sulfur content. Since natural gas contains a trace amount of sulfur, it is necessary to first desulfurize natural gas.
The conversion step: the conversion process is carried out in a reformer. The common reformer comprises a convection section and a radiation section, and the natural gas and steam mixture after desulfurization treatment is preheated to about 500-600 ℃ in the convection section of the reformer and then enters the radiation section of the reformer for conversion reaction. The heat required for the reformer is provided by a fuel gas comprising raw natural gas. The conversion reaction comprises, under the action of a catalyst, preferably metallic nickel:
CH4+H2O＝CO+3H2，
CO+3H2＝CH4+H2O，
CO+H2O＝CO2+H2，
the generated conversion gas mainly comprises hydrogen, methane, carbon monoxide, carbon dioxide and water vapor.
It should be noted that the preheating of the raw natural gas mentioned in the desulfurization step is also performed in one of the convection sections of the reformer. The temperature of the flue gas generated by combustion heating in the reformer is 800-900 ℃.
A transformation step: the high temperature converted gas (generally between 750 and 850 ℃) is subjected to heat exchange by a converted gas steam generator (waste heat boiler), then the temperature is reduced, the converted gas enters a conversion process, and the medium temperature conversion temperature is 330 to 360 ℃. The shift reaction is carried out under the action of a catalyst Fe2O3.Cr2O3: co+h2o=co2+h2. The CO content in the gas is reduced to below 2% through medium temperature shift reaction, and meanwhile, the hydrogen is continuously produced. The medium-shift gas is cooled and split by a cooler after part of waste heat is recovered by heat exchange, and then enters the PSA part.
And (3) purification: a PSA purification process is employed. Specifically, the medium-temperature gas after cooling and water separation enters a PSA unit to adsorb and remove other impurities (CH 4, CO2, H2O and the like) except hydrogen, so that the product hydrogen is purified, and the impurity is desorbed and then sent to a reformer to be used as fuel gas.
It should be further noted that in the above process flow of producing hydrogen from natural gas, after heat exchange with the mixture of natural gas and natural gas steam, a great amount of waste heat remains, and in the general flow, the heat-enriched flue gas further passes through a waste heat boiler (for heat exchange with boiler water supply) and an air heat exchange device (for heat exchange with air) in sequence, and is then discharged from a chimney.
Based on the background description of the natural gas hydrogen production process, the invention provides integrated heat exchange equipment, which combines various mediums such as raw material natural gas, natural gas steam mixed gas, converted gas, flue gas, boiler water supply and the like for heat exchange, and different mediums pass through different heat exchange channels to finally achieve respective heat exchange purposes.
Specifically, please refer to fig. 2A, fig. 2B and fig. 2C together.
The integrated heat exchange device comprises a first heat exchange part and a second heat exchange part which are integrally manufactured. Wherein the first heat exchange part comprises a flue gas cylinder 212, a raw natural gas coil 214 and a natural gas steam mixed gas coil 216; the second heat exchange section includes a reformed gas tube bundle 224, a first flue gas tube bundle 226, and a boiler feedwater housing 222; the first flue gas tube bundle 226 is connected in series with the outlet of the flue gas cylinder 212.
The heat exchange process of the integrated heat exchange device is as follows.
The flue gas from the reformer is passed through flue gas drum 212 and exchanges heat with the raw natural gas in raw natural gas coil 214 and the natural gas vapor mixture in natural gas vapor mixture coil 216. Wherein the raw natural gas absorbs the heat of the flue gas to enter the desulfurization step, and the natural gas steam mixture absorbs the heat of the flue gas to enter the conversion step.
The flue gas in the flue gas cylinder 212 enters a first flue gas tube bundle 226 of the second heat exchange part after passing through the heat exchange process of the first heat exchange part; the boiler feed water in the boiler feed water housing 222 exchanges heat with the flue gas in the first flue gas bundle 226 and the reformed gas in the reformed gas bundle 224, and a portion of the steam generated during the heat exchange process may be used to form a natural gas steam mixture with the sweetened natural gas as a reaction gas in the reformer.
In the second heat exchange part, boiler feed water exchanges heat with flue gas passing through the first flue gas tube bundle and conversion gas passing through the conversion gas tube bundle, compared with the traditional heat exchange design scheme, the reuse rate of waste heat boiler equipment and boiler feed water resources is improved, the number of heat exchange equipment of the whole system is further reduced, the heat exchange pipeline layout is optimized, and the occupied area and the running cost of the whole system are reduced.
Because the heat exchange temperature of the natural gas vapor mixture is higher than that of the raw material natural gas, preferably, the natural gas vapor mixture coil 216 is embedded between the inlet of the flue gas cylinder 212 and the raw material natural gas coil 214, so that the natural gas vapor mixture exchanges heat with the high-temperature flue gas output by the reformer preferentially, thereby more reasonably utilizing the heat of the flue gas and reducing the energy loss of the system.
Preferably, the inner wall of the flue gas drum 212 is provided with a thermal insulation layer 218, such as a silicate material layer having a thickness of 50-100 mm, to allow the high temperature flue gas to exchange heat only with the raw natural gas and natural gas steam mixture, the heat exchange temperature being unaffected by the relatively low temperature water in the boiler feedwater housing 222.
Preferably, a plurality of baffles (not shown) are arranged in the flue gas cylinder 212 along the length direction of the cylinder so as to increase the residence time of the flue gas in the cylinder and reduce the length of the flue gas cylinder 212, thereby reducing the occupied area of the whole heat exchange equipment. The baffle plates are stainless steel annular baffle plates with high temperature resistance.
Because the temperature of the flue gas in the whole system is higher, the initial temperature is 800-900 ℃, and the temperature before entering the air for heat exchange after boiler water supply heat exchange generally needs to reach about 250 ℃; preferably, in order to control the length of the first flue gas tube bundle 226 to reduce the occupied area of the whole integrated heat exchange device, a second flue gas tube bundle 228 is additionally arranged, wherein the second flue gas tube bundle 228 is positioned on the upper side of the first flue gas tube bundle 226, and flue gas output by the first flue gas tube bundle 226 enters the second flue gas tube bundle 228 to exchange heat with boiler feedwater after passing through a flue gas hood 232.
Those skilled in the art will readily appreciate that, without being limited to the disclosure of the present embodiment, the second flue gas tube bundle 228 may also be disposed below the first flue gas tube bundle 226, and may be flexibly designed according to the specific construction environment.
According to the examples of the present disclosure, the conversion gas tube bundles 224 are disposed on the rear sides of the first and second flue gas tube bundles 226 and 228, and those skilled in the art will readily recognize that the conversion gas tube bundles 224 may also be disposed on the front sides of the first and second flue gas tube bundles 226 and 228, and may be flexibly designed according to the specific construction environment.
In particular, the layout of the reforming gas tube bundle 224, the first flue gas tube bundle 226 and the second flue gas tube bundle 228 is considered to be compatible with the cylindrical boiler feedwater housing, so that the volume or footprint of the integrated heat exchange apparatus is minimized.
By the mode, a plurality of discrete heat exchange devices in the natural gas hydrogen production process are highly integrated, so that the equipment investment is saved, the heat exchange efficiency of the system is improved, and the heat loss and the energy consumption of the device are reduced.
Claims (8)
1. An integrated heat exchange device in a natural gas hydrogen production system is characterized by comprising a first heat exchange part and a second heat exchange part which are integrally manufactured; the first heat exchange part comprises a flue gas cylinder, a raw material natural gas coil and a natural gas steam mixed gas coil, the raw material natural gas coil and the natural gas steam mixed gas coil are embedded in the flue gas cylinder, the second heat exchange part comprises a conversion gas tube bundle, a first flue gas tube bundle and a boiler water supply shell, and the flue gas cylinder is arranged in the boiler water supply shell; the first flue gas tube bundle is connected in series to the outlet of the flue gas cylinder, and the first flue gas tube bundle and the conversion gas tube bundle are both arranged in the boiler water supply shell.
2. The integrated heat exchange device of claim 1, wherein the natural gas vapor mixture coil is located between the inlet of the flue gas cartridge and the feed natural gas coil.
3. The integrated heat exchange device of claim 2, wherein the inner wall of the flue gas cartridge is provided with a thermal insulation layer.
4. An integrated heat exchange device according to claim 3, wherein the interior of the flue gas cartridge is provided with baffles along the length of the cartridge.
5. The integrated heat exchange device of any one of claims 1-4, wherein the second heat exchange section further comprises a second flue gas tube bundle for exchanging the flue gas output by the first flue gas tube bundle with boiler feedwater again.
6. The integrated heat exchange device of claim 5, wherein the layout of the first flue gas tube bundle, the second flue gas tube bundle, and the conversion gas tube bundle is adapted to a cylindrical boiler feedwater housing such that the volume or footprint of the integrated heat exchange device is minimized.
7. The integrated heat exchange device of claim 6, wherein the second flue gas tube bundle is located on an upper side or a lower side of the first flue gas tube bundle.
8. The integrated heat exchange device of claim 7, wherein the conversion gas tube bundle is located on a front side or a rear side of the first and second flue gas tube bundles.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810302819.1A CN108931150B (en) | 2018-04-06 | 2018-04-06 | Integrated heat exchange equipment in natural gas hydrogen production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810302819.1A CN108931150B (en) | 2018-04-06 | 2018-04-06 | Integrated heat exchange equipment in natural gas hydrogen production system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108931150A CN108931150A (en) | 2018-12-04 |
| CN108931150B true CN108931150B (en) | 2023-10-24 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
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| CN201810302819.1A Active CN108931150B (en) | 2018-04-06 | 2018-04-06 | Integrated heat exchange equipment in natural gas hydrogen production system |
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| Country | Link |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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-
2018
- 2018-04-06 CN CN201810302819.1A patent/CN108931150B/en active Active
Patent Citations (9)
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| CN2674292Y (en) * | 2004-01-08 | 2005-01-26 | 上海理工大学 | Energy source waste heat boiler |
| CN101487630A (en) * | 2009-02-26 | 2009-07-22 | 北京航空航天大学 | Heat-exchange intensification apparatus and method for indirect medium heating furnace |
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| CN108931150A (en) | 2018-12-04 |
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