CN102951609A - New utilization technology of shift gas heat in hydrogen production device - Google Patents
New utilization technology of shift gas heat in hydrogen production device Download PDFInfo
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- CN102951609A CN102951609A CN2011102545860A CN201110254586A CN102951609A CN 102951609 A CN102951609 A CN 102951609A CN 2011102545860 A CN2011102545860 A CN 2011102545860A CN 201110254586 A CN201110254586 A CN 201110254586A CN 102951609 A CN102951609 A CN 102951609A
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Abstract
The invention relates to the field of petrifaction energy conservation, and particularly relates to a new utilization technology of shift gas heat in a hydrogen production device. The technology comprises a lean amine liquid pump, a solvent regeneration tower, a medium temperature shift gas-lean amine liquid heat exchanger, a lean amine liquid reboiler and a lean liquid pump. Compared with the prior art, the invention provides a technological flow of transporting the lean amine liquid easy to transport for long distance into the hydrogen generation device and performing heat exchange with the medium temperature shift gas, the problem that the medium temperature shift gas cannot be transported for long distance is solved, and the heat integration mode between the medium temperature shift gas in hydrogen production and the hot traps such as lean amine liquid and the like is widely applied.
Description
Technical field
The present invention relates to the petrochemical industry energy-saving field, specifically become gas Btu utilization novel process in a kind of device for producing hydrogen.
Background technology
Along with crude oil in poor quality and oil quality upgrading trend, the refinery is increasing to the demand of hydrogen.Device for producing hydrogen is one of main device of hydrogen making, also is main energy-dissipating device.Reasonable, the abundant utilization that becomes the gas heat in the device for producing hydrogen is one of important factor that affects device for producing hydrogen energy consumption and refining energy consumption.At present, become in most of device for producing hydrogen gas through with the heat exchange such as hydrogen feedstock gas, oiler feed, de-mineralized water after, the temperature when entering air cooler still up to 140 ℃～160 ℃, waste heat is further recycling not.By the heat integration technology, the hot trap that becomes gas and other oil refining apparatus in the device for producing hydrogen is carried out heat integration, become the heat of gas in can further recycling, thereby reduce the refining energy consumption of full factory.
In the oil refining apparatus, can with hydrogen manufacturing in become the gas heat integration hot trap comprise at the bottom of the charging of desulfurizer solvent regeneration tower, sewage stripping device Wastewater Stripping Tower or the tower liquid etc.The heat integration mode of taking at present is after middle change pneumatic transmission is replaced heat to other dress, returns the middle change gas air cooler of device for producing hydrogen.There is a difficult problem in this heat integration mode, namely installs when distant when device for producing hydrogen and other, and middle change gas is carried at a distance and can be produced larger pressure drop, can be influential to follow-up PSA purifying plant, and hydrogen product can not be transported to the hydrogen pipe network.As seen, this heat integration mode since be subject to device space from restriction, can not be widely used.Therefore, it is vital becoming gas Btu utilization novel process in a kind of device for producing hydrogen that can avoid middle change gas to carry at a distance of design.
Summary of the invention
The objective of the invention is to overcome the deficiencies in the prior art, provide a kind of can avoiding to become gas Btu utilization novel process in the remote device for producing hydrogen of carrying of middle change gas.
In order to achieve the above object, the present invention includes poor amine liquid pump, solvent regeneration tower, middle change gas-poor amine liquid interchanger, poor amine liquid reboiler and lean pump, it is characterized in that: poor amine liquid is drawn at the bottom of the tower of solvent regeneration tower, after poor amine liquid pump pressurization, be delivered to device for producing hydrogen, enter the shell side entrance of middle change gas-poor amine liquid interchanger; Middle change gas therefrom becomes gas air cooler entrance draws, and enters the tube side entrance of middle change gas-poor amine liquid interchanger; Poor amine liquid and middle change gas carry out heat exchange in middle change gas-poor amine liquid interchanger, in the heat transfer process, poor amine liquid is partly vaporized, form liquid and vapor capacity, the vapor phase exit that vapour phase therefrom becomes gas-poor amine liquid interchanger is back to the shell side outlet of poor amine liquid reboiler, liquid phase therefrom becomes the liquid-phase outlet of gas-poor amine liquid interchanger draws, and after the lean pump pressurization, is back to the shell side outlet of poor amine liquid reboiler; Middle change gas after the heat exchange is back to middle change gas air cooler entrance.
Described poor amine liquid initial temperature is between 120 ℃-130 ℃, between 125 ℃-135 ℃ of the vaporization temperatures of poor amine liquid.
Described middle change gas initial temperature is between 140 ℃-160 ℃, and the middle change temperature degree after heat exchange is finished is between 130 ℃-140 ℃.
The liquid level of described middle change gas-poor amine liquid interchanger is by the poor amine flow quantity control of middle change gas-poor amine liquid interchanger liquid-phase outlet.
The poor amine liquid vaporization temperature of described middle change gas-poor amine liquid interchanger is by the middle change gas feed rate control of middle change gas-poor amine liquid interchanger.
The present invention compares with prior art, having proposed to be easy to the remote poor amine liquid of carrying is delivered to device for producing hydrogen and carries out the technical process of thermal exchange with middle change gas, solved the problem that middle change gas can not be carried at a distance, thereby the heat integration mode that becomes the hot traps such as gas and poor amine liquid in the hydrogen manufacturing is used widely.
Description of drawings
Fig. 1 is structural representation of the present invention.
Referring to Fig. 1,1 is poor amine liquid pump; 2 is solvent regeneration tower; 3 is middle change gas-poor amine liquid interchanger; 4 is vapor phase exit; 5 is poor amine liquid reboiler, and 6 is lean pump; 7 is liquid-phase outlet.
Embodiment
Now by reference to the accompanying drawings the present invention is described further.
Referring to Fig. 1, the present invention proposes a kind of novel process that is not subjected in the device for producing hydrogen to become distance limit between gas and the hot trap, be about to hot trap fluid and be transported to device for producing hydrogen, the technique of carrying out heat exchange with change gas in the hydrogen manufacturing.Hot trap includes but not limited to the poor amine liquid of desulfurizer, comprises that also temperature is at various solution and oil product below 180 ℃.Now in poor amine liquid and device for producing hydrogen, become the gas heat integration as example, the idiographic flow of this technique is described.This flow process comprises poor amine liquid pump, solvent regeneration tower, middle change gas-poor amine liquid interchanger, poor amine liquid reboiler and lean pump.Wherein, middle change gas-poor amine liquid interchanger 3 is a kind of shell side also can carry out level gauging with the liquid and vapor capacity separated space interchanger.The poor amine liquid of initial temperature between 120 ℃-130 ℃ is drawn at the bottom of the tower of solvent regeneration tower 2, after poor amine liquid pump 1 pressurization, is delivered to device for producing hydrogen, enters the shell side entrance of middle change gas-poor amine liquid interchanger 3.The middle change gas of initial temperature between 140 ℃-160 ℃ therefrom becomes the tube side entrance that middle change gas-poor amine liquid interchanger 3 was drawn and entered to gas air cooler entrance.Poor amine liquid and middle change gas carry out heat exchange in middle change gas-poor amine liquid interchanger 3, in the heat transfer process, poor amine liquid is partly vaporized, and form vapour item and liquid phase.The vapor phase exit 4 that vapour phase therefrom becomes gas-poor amine liquid interchanger 3 is back to the shell side outlet of poor amine liquid reboiler 5.Liquid phase therefrom becomes the liquid-phase outlet 7 of gas-poor amine liquid interchanger 3 draws, and is back to the shell side outlet of poor amine liquid reboiler 5 after lean pump 6 pressurizations.The vaporization temperature of middle change gas-poor amine liquid interchanger 3 is controlled by middle change gas feed rate, and liquid level is by the poor amine flow quantity control of outlet.Middle change temperature degree after the heat exchange is back to middle change gas air cooler entrance between 130 ℃-140 ℃.So far, end-of-job of the present invention.
Claims (5)
1. become gas Btu utilization novel process in a device for producing hydrogen, comprise poor amine liquid pump, solvent regeneration tower, middle change gas-poor amine liquid interchanger, poor amine liquid reboiler and lean pump, it is characterized in that: poor amine liquid is drawn at the bottom of the tower of solvent regeneration tower (2), after poor amine liquid pump (1) pressurization, be delivered to device for producing hydrogen, enter the shell side entrance of middle change gas-poor amine liquid interchanger (3); Middle change gas therefrom becomes gas air cooler entrance draws, and enters the tube side entrance of middle change gas-poor amine liquid interchanger (3); Poor amine liquid and middle change gas carry out heat exchange in middle change gas-poor amine liquid interchanger (3), in the heat transfer process, poor amine liquid is partly vaporized, form liquid and vapor capacity, the vapor phase exit (4) that vapour phase therefrom becomes gas-poor amine liquid interchanger (3) is back to the shell side outlet of poor amine liquid reboiler (5), liquid phase therefrom becomes the liquid-phase outlet (7) of gas-poor amine liquid interchanger (3) draws, and after lean pump (6) pressurization, is back to the shell side outlet of poor amine liquid reboiler (5); Middle change gas after the heat exchange is back to middle change gas air cooler entrance.
2. become gas Btu utilization novel process in a kind of device for producing hydrogen according to claim 1, it is characterized in that: described poor amine liquid initial temperature is between 120 ℃-130 ℃, between 125 ℃-135 ℃ of the vaporization temperatures of poor amine liquid.
3. become gas Btu utilization novel process in a kind of device for producing hydrogen according to claim 1, it is characterized in that: described middle change gas initial temperature is between 140 ℃-160 ℃, and the middle change temperature degree after heat exchange is finished is between 130 ℃-140 ℃.
4. become gas Btu utilization novel process in a kind of device for producing hydrogen according to claim 1, it is characterized in that: the liquid level of described middle change gas-poor amine liquid interchanger (3) is by the poor amine flow quantity control of middle change gas-poor amine liquid interchanger (3) liquid-phase outlet (7).
5. become gas Btu utilization novel process in a kind of device for producing hydrogen according to claim 1, it is characterized in that: the poor amine liquid vaporization temperature of described middle change gas-poor amine liquid interchanger (3) is by the middle change gas feed rate control of middle change gas-poor amine liquid interchanger (3).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110254586.0A CN102951609B (en) | 2011-08-31 | 2011-08-31 | New utilization technology of shift gas heat in hydrogen production device |
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| CN201110254586.0A CN102951609B (en) | 2011-08-31 | 2011-08-31 | New utilization technology of shift gas heat in hydrogen production device |
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| CN102951609A true CN102951609A (en) | 2013-03-06 |
| CN102951609B CN102951609B (en) | 2014-08-13 |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201040718Y (en) * | 2007-04-18 | 2008-03-26 | 中国科学院工程热物理研究所 | Solar energy medium low temperature heat driving thermochemical reaction hydrogen producing system |
| JP2008069017A (en) * | 2006-09-12 | 2008-03-27 | Matsushita Electric Ind Co Ltd | Method for producing hydrogen |
| CN101318620A (en) * | 2007-06-06 | 2008-12-10 | 中国科学院工程热物理研究所 | Chemical industry power multi-generation energy resource system and method for separating C02 |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008069017A (en) * | 2006-09-12 | 2008-03-27 | Matsushita Electric Ind Co Ltd | Method for producing hydrogen |
| CN201040718Y (en) * | 2007-04-18 | 2008-03-26 | 中国科学院工程热物理研究所 | Solar energy medium low temperature heat driving thermochemical reaction hydrogen producing system |
| CN101318620A (en) * | 2007-06-06 | 2008-12-10 | 中国科学院工程热物理研究所 | Chemical industry power multi-generation energy resource system and method for separating C02 |
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