CN210979798U - Low-temperature waste heat recycling device for variable gas in hydrogen production device - Google Patents
Low-temperature waste heat recycling device for variable gas in hydrogen production device Download PDFInfo
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- CN210979798U CN210979798U CN201921642787.6U CN201921642787U CN210979798U CN 210979798 U CN210979798 U CN 210979798U CN 201921642787 U CN201921642787 U CN 201921642787U CN 210979798 U CN210979798 U CN 210979798U
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Abstract
The utility model discloses a become gas low temperature waste heat recovery and recycle device among hydrogen generator, including dry gas hydrogen generator and fuel gas heater, dry gas hydrogen generator has well gas of change/deoxidation water heat exchanger and well gas desalination heat exchanger, the well gas of change that comes from the well reaction gets into well gas of change first minute fluid reservoir after the heat transfer of well gas of change/deoxidation water heat exchanger, the well gas of the first minute fluid reservoir of the in process gas of change after dividing the liquid feeds through steam generator's heat source import through first steam conduit, steam generator's heat source export feeds through well gas desalination heat exchanger through the second steam conduit, again with the demineralized water that comes from the pipe network heat transfer in well gas desalination heat exchanger and divide the liquid in well gas second minute fluid reservoir; and the steam generated by the steam generator is communicated to the fuel gas heater through a third steam pipeline. The utility model discloses utilize the low temperature waste heat in the change gas among the dry gas hydrogen plant, replace original 1.0MPa steam heat source system, practice thrift steam consumption and power consumption to reduce the device energy consumption.
Description
Technical Field
The utility model relates to a low temperature waste heat recovery recycles device of changing gas among hydrogen plant.
Background
In the dry gas hydrogen production device, the temperature of the medium-temperature transformed gas after heat exchange and steam generation is still as high as 170 +/-5 ℃, and after heat exchange with the desalted water entering the device, the temperature of the medium-temperature transformed gas before entering the device reaches 145 ℃, so that the temperature of the deaerated water is too high, the steam exhaust of the deaerator is increased, the pressure of the deaerator is increased, and a large amount of desalted water is evaporated and lost. And the middle variable air inlet variable air/demineralized water heat exchanger bypass is slightly opened, the heat is fully absorbed, and the middle variable air cooling load is increased. The process not only wastes the deaerated water, but also increases the power consumption, so that the production cost of the whole system is increased.
The fuel gas heater of the device mainly aims at improving the temperature of the fuel gas before entering the furnace, improving the temperature of the fuel, reducing the heat required by combustion and reducing the fuel consumption of the device. The temperature of the fuel gas is usually 30 ℃, the fuel gas is heated to 60-80 ℃ by a fuel gas heater, the heat source is 1.0MPa pipe network steam, and the produced condensed water is sent to a condensed water pipe network.
Disclosure of Invention
The to-be-solved technical problem of the utility model is to utilize the low temperature waste heat in the change gas among the dry gas hydrogen plant, directly supply the fuel gas heater as the heat source, replace original 1.0MPa steam heat source system, the energy consumption of whole optimization device is balanced, fully retrieves the low temperature heat energy in the product, and reducing device fuel consumption practices thrift steam consumption and power consumption to the reducing device energy consumption.
In order to solve the technical problem, the utility model discloses a dry gas hydrogen manufacturing installation and fuel gas heater, dry gas hydrogen manufacturing installation has well gas conversion/deoxidation water heat exchanger and well gas conversion demineralized water heat exchanger, well gas conversion that well gas conversion reaction comes enters well gas conversion first minute fluid reservoir after well gas conversion/deoxidation water heat exchanger heat transfer, its structural feature is that well gas conversion after the first minute fluid reservoir of well gas conversion divides the liquid feeds through steam generator's heat source import through first steam line, well gas conversion from steam generator's heat source export after steam generator heats feeds through well gas conversion demineralized water heat exchanger through second steam line, again with the demineralized water that comes from the pipe network heat transfer in well gas conversion demineralized water heat exchanger and in well gas conversion second minute fluid reservoir; and the steam generated by the steam generator is communicated to the fuel gas heater through a third steam pipeline.
And a fourth steam pipeline is arranged between the first steam pipeline and the second steam pipeline, and a gate valve is arranged on the fourth steam pipeline.
The medium-pressure gas/deoxygenation water heat exchanger is supplied with liquid by a deoxygenator through a deoxygenation water pump, and the steam generator is also supplied with liquid by the deoxygenator through the deoxygenation water pump.
After adopting above-mentioned structure, because in the dry gas hydrogen manufacturing installation, the heat that well change gas carried has certain heat source optimization space, through the balanced optimization of the interior energy consumption of device, through adding a steam generator, tak away the partial heat of 170 ℃ left and right temperature level in the well change gas, produce 0.30MPa saturated steam, directly supply the fuel gas heater as the heat source, replace original 1.0MPa steam heat source system, the energy consumption of whole optimization device is balanced, fully retrieve the low temperature heat energy in the product, reduce device fuel consumption, practice thrift steam consumption and power consumption, thereby reduce device energy consumption. Meanwhile, the heat of the medium-pressure gas changing air cooler is taken away to reduce the inlet temperature (reduced to about 125 ℃) and the temperature of the deaerated water of the medium-pressure gas changing air cooler, so that the fan load of the medium-pressure gas changing air cooler can be reduced, and the air cooling power consumption of the medium-pressure gas changing air cooler is reduced.
Drawings
The following detailed description of embodiments of the present invention is provided with reference to the accompanying drawings:
FIG. 1 is a schematic structural diagram of a dry gas hydrogen production plant in the prior art;
FIG. 2 is a schematic diagram of a fuel gas heater of a prior art device;
fig. 3 is a schematic structural diagram of the present invention.
Detailed Description
In the dry gas hydrogen production device shown in figure 1, medium gas produced from a medium shift reaction enters a medium shift first liquid separation tank 2 after heat exchange through a medium shift gas/deoxidized water heat exchanger 1, exchanges heat with desalted water in a medium shift gas/desalted water heat exchanger 16 after liquid separation, separates liquid in a medium shift second liquid separation tank 19, and finally enters a medium shift gas third liquid separation tank (not shown in the figure) after being cooled to 30-40 ℃ through a medium shift gas cooler 20. The device is 10000Nm3The flow of the medium gas before full load passing through the medium air cooler is 15000Nm3About/h, wherein the heat at the temperature of 170 ℃ is used for supplying the medium-temperature-shift gas/desalted water heat exchanger 16 and then is sent to the deaerator 13, wherein the inlet temperature of the desalted water at the cold end of the medium-temperature-shift gas/desalted water heat exchanger 16 is about 40 ℃, the outlet temperature is 145 ℃, the deaerator deoxygenated water temperature is controlled to be 102 ℃, the temperature enters the deaerator to generate a large amount of evaporated steam, the deaerator causes impact, the temperature of the shifted gas in the subsequent flow of the device is reduced by increasing the load of the medium-temperature-shift gas cooler 20, and therefore the heat of the shifted gas is transferred or absorbed, and the heat can be realized only by reducing the heat source temperature of the. In conclusion, the low-temperature waste heat utilization in the temperature range medium-temperature exhaust gas has a large optimization and adjustment space.
Demineralized water from a pipe network 17 is subjected to heat exchange through a medium gas/demineralized water heat exchanger 16 and then enters a deaerator 13 for deaerating, then is subjected to pressure boosting through a deaerating water pump 12 to reach required pressure, is subjected to heat exchange with the medium gas/deaerated water heat exchanger 1 and then enters a conversion steam drum, steam required by the deaerator 13 comes from a pipe network 14, and the heat source is 1.0MPa steam.
In the fuel gas warmer for the device shown in fig. 2, fuel gas from an external fuel gas pipe network 25 enters a fuel gas buffer tank 24 for liquid separation, then enters a shell pass of the fuel gas warmer 21, 1.0MPa steam from a steam pipe network enters a pipe pass of the fuel gas warmer for warming the fuel gas, the fuel gas is warmed to 60-80 ℃ and then enters a heating furnace system for burning, and condensed water generated by the fuel gas warmer 21 is removed to a condensed water pipe network.
The low-temperature waste heat recycling device for the transformer gas in the hydrogen production device shown in figure 3 comprises a dry gas hydrogen production device and a fuel gas heater 21, wherein the dry gas hydrogen production device is 10000Nm3The flow of the medium gas before full load passing through the medium air cooler is 15000Nm3About/h, the dry gas hydrogen production device is provided with a middle variable gas/deoxidized water heat exchanger 1 and a middle variable gas desalted water heat exchanger 16, middle variable gas from the middle variable gas reaction enters a middle variable gas first liquid separation tank 2 after heat exchange of the middle variable gas/deoxidized water heat exchanger 1, and middle variable gas after liquid separation of the middle variable gas first liquid separation tank 2 is communicated with steam through a first steam pipeline 3The heat source inlet of the generator 5, the heat source outlet of the steam generator 5 is communicated to the medium-pressure gas-shift desalted water heat exchanger 16 through the second steam pipeline 7, then exchanges heat with desalted water from the pipe network 17 in the medium-pressure gas-shift desalted water heat exchanger 16 and divides liquid in the medium-pressure gas-shift second liquid dividing tank 19, the bottoms of the medium-pressure gas-shift first liquid dividing tank 2 and the medium-pressure gas-shift second liquid dividing tank 19 are provided with acid water discharge pipes, the acid water discharge pipes are provided with gate valves, and acid water generated by the medium-pressure gas-shift first liquid dividing tank 2 and the medium-pressure gas-shift second liquid dividing tank. Steam generated by the steam generator 5 is communicated to the fuel gas heater 21 through the third steam pipeline 6, the steam generator 5 is a 0.3MPa steam generator, 0.30MPa saturated steam (about 1 t/h) is generated, and enters the fuel gas heater 21 tube pass to heat shell pass fuel gas under the regulation of the outlet pressure control valve, and the first steam pipeline 3 and the third steam pipeline 6 are 0.3MPa steam pipelines. A fourth steam pipeline 4 is arranged between the first steam pipeline 3 and the second steam pipeline 7, and a gate valve is arranged on the fourth steam pipeline 4 to adjust the inlet air temperature and pressure of the medium-pressure gas desalting water heat exchanger 16. Demineralized water from a pipe network 17 is subjected to heat exchange by a medium-pressure gas/demineralized water heat exchanger 16, then enters a deaerator 13 through a demineralized water pipeline 15 for deaerating, then is subjected to pressure boosting by a deaerating water pump 12 until required pressure is subjected to heat exchange and temperature rise by a deaerating water pipeline 11 and the medium-pressure gas/deaerating water heat exchanger 1, and then enters a conversion steam pocket, steam required by the deaerator 13 comes from a pipe network 14, and a heat source is 1.0MPa steam. The deaerated water (about 1 t/h) after being deaerated by the deaerator 13 is boosted to the required pressure through the deaerating water pump 12 and is conveyed to the steam generator 5 through another pipeline 9, the pipeline 9 is provided with a gate valve, and the bottom of the steam generator 5 is provided with a sewage discharge pipeline 8 to discharge sewage regularly and prevent impurity deposition. The medium gas from the second steam pipeline 7 is subjected to heat exchange by a medium gas desalting water heat exchanger 16, liquid separation in a medium gas second liquid separation tank 19, is communicated with a medium gas cooler 20 through a second liquid separation tank steam pipeline 18, and finally enters a medium gas third liquid separation tank (not shown in the figure) for liquid separation after being cooled to 30-40 ℃ by the medium gas cooler 20. Fuel gas from an external fuel gas pipe network 25 enters a fuel gas buffer tank 24 for liquid separation, then enters a fuel gas heater 21 shell pass through a pipeline 23 at the top of the buffer tank, and 0 comes from a steam generator 5 through a third steam pipeline 63MPa steam enters the tube pass of the fuel gas warmer 21 to heat the fuel gas, the fuel gas is heated to 60-80 ℃ and then enters the heating furnace system for combustion, condensed water generated by the fuel gas warmer 21 is removed to a condensed water pipe network through a condensed water pipeline 22, a condensate discharging pipe 26 is arranged at the bottom of the fuel gas buffer tank 24, and a gate valve is arranged on the condensate discharging pipe 26.
The utility model discloses a theory of operation is:
the medium gas from the medium gas shift reaction enters a medium gas shift first liquid separation tank 2 after heat exchange through a medium gas shift/deoxygenation water heat exchanger 1, the medium gas after liquid separation is used as a heat source of a steam generator 5 to heat deoxygenation water from a deoxygenation water pump 12 through a 0.3MPa first steam pipeline 3, 0.3MPa steam is generated by controlling the temperature of the medium gas shift, and the generated 0.3MPa steam is sent to a fuel gas heater 21 through pressure control to heat the fuel gas to 60-80 ℃.
The medium gas after being heated by the 0.3MPa steam generator 5 exchanges heat with desalted water in the medium gas desalting heat exchanger 16, is separated in a medium gas second liquid separation tank 19, is cooled to 30-40 ℃ by a medium gas cooler 20, and then enters a medium gas third liquid separation tank (not shown in the figure) for liquid separation.
The desalted water from the pipe network 17 enters the deaerator 13 for deaerating after being subjected to heat exchange by the medium gas/desalted water heat exchanger 16, then is boosted to the required pressure by the deaerating water pump 12, and enters the conversion steam drum after being subjected to heat exchange and temperature rise by the medium gas/desalted water heat exchanger 1, and is conveyed to the steam generator 5 through another pipeline 9.
0.3MPa steam from the steam generator 5 through the third steam pipeline 6 enters the tube pass of the fuel gas heater 21 to heat the fuel gas, the fuel gas is heated to 60-80 ℃ and then enters the heating furnace system to be combusted, and condensed water generated by the fuel gas heater 21 is sent to a condensed water pipe network through a condensed water pipeline 22.
In the utility model, the structures of the medium gas/deoxidized water heat exchanger 1 (model: E-101), the medium gas first liquid separation tank 2 (model: D-108), the medium gas desalted water heat exchanger 16 (model: E-102), the medium gas second liquid separation tank 19 (model: D-109), the deaerator 13 (model: D-124), the steam generator 5 (model: E-102), the medium gas cooler 20 (model: A-101), the fuel gas heater 21 (model: E-104) and the fuel gas buffer tank 24 (model: D-111) are known structures, and are not described herein.
In summary, in 10000Nm3In the dry gas hydrogen production device, heat carried by medium-to-medium gas has a certain heat source optimization space, a steam generator is additionally arranged through balance optimization of energy consumption in the device, partial heat of about 170 ℃ in the medium-to-medium gas is taken away, 0.30MPa saturated steam is produced, and a direct fuel gas heater is used as a heat source to replace the original 1.0MPa steam. After the improvement, the fuel heater does not need to consume 1.0MPa steam; meanwhile, the heat of the medium-pressure gas changing air cooler is taken away to reduce the inlet temperature (reduced to about 125 ℃) and the temperature of the deaerated water of the medium-pressure gas changing air cooler, so that the fan load of the medium-pressure gas changing air cooler can be reduced, and the air cooling power consumption of the medium-pressure gas changing air cooler is reduced.
Claims (3)
1. A low-temperature waste heat recycling device for variable gas in a hydrogen production device comprises a dry gas hydrogen production device and a fuel gas heater (21), wherein the dry gas hydrogen production device is provided with a medium variable gas/deoxidized water heat exchanger (1) and a medium variable gas desalted water heat exchanger (16), medium variable gas generated by a medium variable gas reaction enters a medium variable gas first liquid separation tank (2) after heat exchange through the medium variable gas/deoxidized water heat exchanger (1), the system is characterized in that the medium shift gas subjected to liquid separation by the medium shift gas first liquid separation tank (2) is communicated to a heat source inlet of a steam generator (5) through a first steam pipeline (3), the medium shift gas subjected to heat extraction by the steam generator (5) is communicated to a medium shift gas desalted water heat exchanger (16) from a heat source outlet of the steam generator (5) through a second steam pipeline (7), and then exchanges heat with desalted water from a pipe network in the medium shift gas desalted water heat exchanger (16) and separates liquid in a medium shift gas second liquid separation tank (19); the steam generated by the steam generator (5) is communicated to the fuel gas heater (21) through a third steam pipeline (6).
2. The variable gas low-temperature waste heat recycling device in the hydrogen production device according to claim 1, characterized in that a fourth steam pipeline (4) is arranged between the first steam pipeline (3) and the second steam pipeline (7), and a gate valve is arranged on the fourth steam pipeline (4).
3. The low-temperature waste heat recycling device for the shift gas in the hydrogen production device according to claim 1, characterized in that the shift gas/deoxidized water heat exchanger (1) is supplied with liquid by a deaerator (13) through a deoxidized water pump (12), and the steam generator (5) is also supplied with liquid by the deaerator (13) through the deoxidized water pump (12).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921642787.6U CN210979798U (en) | 2019-09-29 | 2019-09-29 | Low-temperature waste heat recycling device for variable gas in hydrogen production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921642787.6U CN210979798U (en) | 2019-09-29 | 2019-09-29 | Low-temperature waste heat recycling device for variable gas in hydrogen production device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210979798U true CN210979798U (en) | 2020-07-10 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921642787.6U Expired - Fee Related CN210979798U (en) | 2019-09-29 | 2019-09-29 | Low-temperature waste heat recycling device for variable gas in hydrogen production device |
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| Country | Link |
|---|---|
| CN (1) | CN210979798U (en) |
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2019
- 2019-09-29 CN CN201921642787.6U patent/CN210979798U/en not_active Expired - Fee Related
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Granted publication date: 20200710 Termination date: 20210929 |
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| CF01 | Termination of patent right due to non-payment of annual fee |