CN102179131A - Three-group simultaneously-running pressure swing absorption process for increasing recovery rate - Google Patents
Three-group simultaneously-running pressure swing absorption process for increasing recovery rate Download PDFInfo
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- CN102179131A CN102179131A CN2011101057075A CN201110105707A CN102179131A CN 102179131 A CN102179131 A CN 102179131A CN 2011101057075 A CN2011101057075 A CN 2011101057075A CN 201110105707 A CN201110105707 A CN 201110105707A CN 102179131 A CN102179131 A CN 102179131A
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Abstract
The invention discloses a pressure swing absorption gas separating process for increasing the recovery rate of effective gas, which is characterized in that three groups of absorption columns are provided; the first group of absorption columns and the second group of absorption columns are used for pressure swing absorption gas separation in the common sense; and the third group of additionally provided absorption columns is particularly used for recovering effective ingredients in the desorption gas from the first group of the absorption columns and the second group of absorption columns, the recovered effective gas ingredients are returned to the first group of absorption columns and the second group of absorption columns in a pressure equalizing way for pressure swing absorption, therefore, the pressure swing absorption gas separating efficiency and the recovery rate of the effective gas are increased.
Description
One, technical field
The present invention relates to chemical field, is that a kind of mist separates pressure swing absorption process, and this method is mainly used in the device of conversion gas separating carbon dioxide component.
Two, background technology
For the technology of conversion gas separating carbon dioxide, the method for usually using is wet method decarburization and pressure swing adsorption decarbonization.
The wet method decarburization technique, using maximum is propene carbonate decarburization technique and NHD decarburization technique, this technology is the solvent absorbing carbon dioxide under high pressure, desorb carbon dioxide under the low-pressure, the carbon dioxide desorb generally is divided into two stages, first stage tradition is called high the sudden strain of a muscle, gas concentration lwevel is lower in the desorption gas, be generally 45-85%, mean concentration is 65%, present most of wet method decarbonization device is provided with separator (for example carbonization in addition, transformation absorption) recycle the effective hydrogen in this flash gas, nitrogen, gases such as carbon monoxide, the second stage tradition is called low the sudden strain of a muscle, and gas concentration lwevel is higher in the desorption gas, is generally 95-100%, mean concentration is 97.5%, is directly used in the synthetic use of urea or produces liquid CO 2.The wet method decarburization, has solvent consumption etc. to become insoluble problem at operating cost height, energy consumption height.
Conversion gas transformation absorption decarbonizing urea technology, using maximum is the two-stage method technology.First stage pressure swing adsorption apparatus, be called enriching section, carbon dioxide about 85% is absorbed, second stage pressure swing adsorption apparatus, be called rectifying section, have about 15% carbon dioxide to absorb at second section, second section exit gas gas concentration lwevel directly send compressor smaller or equal to 0.2%.
Absorbing carbon dioxide under common first section adsorbent high pressure, desorb carbon dioxide under the low-pressure, the final desorb of carbon dioxide generally is divided into two stages, first stage tradition is called along putting (or adding displacement), gas concentration lwevel is lower in the desorption gas, be generally 45-85%, mean concentration is 65%, at present the pressure swing adsorption decarbonization device is not provided with separator in addition and recycles gases such as effective hydrogen in this emptying gas, nitrogen, carbon monoxide, has only report to use this emptying gas to be used for the report of blowing-out gas combustion system; The second stage tradition is called finds time and washes, and gas concentration lwevel is higher in the desorption gas, is generally 95-99%, and mean concentration is 97.5%, is directly used in that urea is synthetic to use or produce liquid CO 2; Use the flushing flow process, flushing back segment stripping gas gas concentration lwevel is low, is generally 45-90%, has only report to use this emptying gas to be used for the report of blowing-out gas combustion system.
Absorbing carbon dioxide under common second section adsorbent high pressure, desorb carbon dioxide under the low-pressure, the final desorb of carbon dioxide generally is divided into two stages, first stage tradition is called contrary putting, gas concentration lwevel is lower in the desorption gas, be generally 25-55%, mean concentration is 35%, at present the pressure swing adsorption decarbonization device is not provided with separator in addition and recycles gases such as effective hydrogen in this emptying gas, nitrogen, carbon monoxide, has only report to use this emptying gas to be used for the report of blowing-out gas combustion system or is directly used in the phase I body of all calming the anger; The second stage tradition is called finds time or washes, gas concentration lwevel is higher in the desorption gas, be generally 55-70%, mean concentration is 65%, at present the pressure swing adsorption decarbonization device is not provided with separator in addition and recycles gases such as effective hydrogen in this emptying gas, nitrogen, carbon monoxide, has only report to use this emptying gas to be used for the report of blowing-out gas combustion system or is directly used in the phase I body of all calming the anger.
The second stage desorption gas is directly used in the phase I and all presses, and causes that active ingredient increases in the phase I desorption gas, in fact can not fine recovery available gas, just the emptying position is changed.Simultaneously, the adsorbent use amount of phase I is increased a lot, cause unnecessary waste.
Whether no matter use the second stage desorption gas directly to return the phase I and all press, facts have proved, this technology gas loss is serious, become the deadly defect of this technology, almost is difficult to overcome.
Three, summary of the invention
Reclaim first section along active ingredient hydrogen, carbon monoxide and nitrogen in venting body and the second section contrary venting body for better, utilization of the present invention is provided with the strategy of a group and above a plurality of recovery pressure-swing absorbers again, is used for improving gas reclaiming rate.
Adsorption tower is set to three groups or above group, wherein first group, second group transformation adsorbed gas that is used on the common meaning separates, be specifically designed to and reclaim first group and be provided with the 3rd group or the 4th group, the 5th group in addition along the active ingredient of putting in desorption gas and the second group of contrary desorption gas of putting, find time, the available gas composition that reclaims returns first group and second group of transformation absorption by the mode of all pressing, and improves transformation adsorbed gas separative efficiency thus and improves the available gas rate of recovery.
By this technology, active ingredient in can giving vent to anger first group of suitable venting, second group of contrary venting, flushing flow fully reclaims, and, reclaim find time again born density of carbon dioxide gas even can reach more than 97% of adsorption tower group, satisfy the synthetic needs of urea or produce liquid CO 2.
The technology of the present invention following characteristics of comparing with the wet method decarbonization process.
Main piece-rate system adopts the pressure swing adsorption technique system; The relative wet method decarbonization system of this process as main system have the investment little, energy consumption is low, convenience operation.
Have the similar high system of dodging gas that reclaims simultaneously, this system continues carbon dioxide to separate to obtain gas concentration lwevel and be not higher than all the calm the anger gaseous mixture of concentration of equal pressure.
The technology of the present invention following characteristics of comparing with the pressure-swing absorption apparatus on the independent meaning.
Gas recovery ratio improves greatly.Can meet or exceed the recovery level of wet method decarburization fully.
Four, the specific embodiment
Embodiment 1: conversion atmospheric pressure 0.8MPa, flow 48000NM
3/ H.
First group of pressure swing adsorption technique that sets up standard, ten towers three advance three equal replacing process, along putting initial pressure 0.10MPa, and the end pressure-0.06MPa that finds time, conversion gas import carbon dioxide 28%, outlet 5.2% enters second group and continues absorption.
Second group of pressure swing adsorption technique that sets up standard, eight towers three advance three technologies of all finding time, and contraryly put initial pressure 0.20MPa, the end pressure-0.06MPa that finds time, and import carbon dioxide 5.2%, the Ammonia Production requirement is satisfied in outlet 0.2%.
The 3rd group is provided with the recovery pressure swing adsorption technique, it is two equal that six towers one advance, air inlet initial pressure-0.04MPa, air inlet end pressure 0.18MPa, end pressure-0.06MPa finds time, second group of contrary venting import carbon dioxide 15-35%, first group of suitable venting import carbon dioxide 45-60%, outlet all pushes back second section carbon dioxide 1.5%, and outlet all pushes back first section carbon dioxide 4.5%, exit gas uses the mode of all pressing to return main system, satisfies first group and second group of body composition requirement of all calming the anger respectively.
Embodiment 2: conversion atmospheric pressure 1.4MPa, flow 48000NM
3/ H.
First group of pressure swing adsorption technique that sets up standard, 12 towers three advance five equal replacing process, along putting initial pressure 0.20MPa, and the end pressure-0.06MPa that finds time, conversion gas import carbon dioxide 28%, outlet 3.2% enters second group and continues absorption.
Second group of pressure swing adsorption technique that sets up standard, ten towers three advance three technologies of all finding time, and contraryly put initial pressure 0.40MPa, the end pressure-0.06MPa that finds time, and import carbon dioxide 3.2%, the Ammonia Production requirement is satisfied in outlet 0.2%.
The 3rd group is provided with the recovery pressure swing adsorption technique, it is two equal that six towers one advance, air inlet initial pressure-0.04MPa, air inlet end pressure 0.32MPa, the contrary pressure 0.05MPa of putting, end pressure-0.06MPa finds time, second group of contrary venting import carbon dioxide 15-35%, first group along venting import carbon dioxide 45-60%, outlet all pushes back second section carbon dioxide 0.5%, outlet all pushes back first section carbon dioxide 4.5%, and exit gas uses the mode of all pressing to return main system, satisfies first group and second group of body composition requirement of all calming the anger respectively.
Embodiment 3: conversion atmospheric pressure 2.7MPa, flow 72000NM
3/ H.
First group of pressure swing adsorption technique that sets up standard, 16 towers three advance ten equal replacing process, along putting initial pressure 0.45MPa, and the end pressure-0.06MPa that finds time, conversion gas import carbon dioxide 28%, outlet 3.2% enters second group and continues absorption.
Second group of pressure swing adsorption technique that sets up standard, 16 towers three advance ten technologies of all finding time, and contraryly put initial pressure 0.60MPa, the end pressure-0.06MPa that finds time, and import carbon dioxide 3.2%, the Ammonia Production requirement is satisfied in outlet 0.2%.
The 3rd group is provided with the recovery pressure swing adsorption technique, it is two equal that six towers one advance, air inlet initial pressure-0.04MPa, air inlet end pressure 0.50MPa, the contrary pressure 0.15MPa of putting, end pressure-the 0.06MPa that finds time, contrary venting import carbon dioxide 15-35% is along venting import carbon dioxide 45-60%, outlet all pushes back second section carbon dioxide 0.5%, outlet all pushes back first section carbon dioxide 4.5%, and exit gas uses the mode of all pressing to return main system, satisfies first group and second group of body composition requirement of all calming the anger respectively.
This patent uses at conversion gas decarbonization plant modification through actual, and effect is fairly obvious, effectively reduces the available gas loss, has saved cost.
Claims (1)
1. adsorption gas separating technology that improves the available gas rate of recovery, it is characterized in that, adsorption tower is set to more than three groups, wherein first group is separated with second group of two-stage method transformation adsorbed gas that is used on the common meaning, and be provided with in addition the 3rd group or the 4th group or the 5th group be specifically designed to reclaim first group with second group of desorption gas in active ingredient, the available gas composition that reclaims returns first group or second group of transformation absorption by the mode of all pressing, and improves transformation adsorbed gas separative efficiency thus and improves the available gas rate of recovery.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108126516A (en) * | 2017-12-21 | 2018-06-08 | 宁夏宝塔化工中心实验室(有限公司) | A kind of plasma combustion technology purifying calcium carbide furnace tail gas process |
| CN110559799A (en) * | 2019-06-27 | 2019-12-13 | 杨皓 | Improved pressure swing adsorption reverse air discharge, scavenging gas, forward air discharge and air pumping recovery process |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1557528A (en) * | 2004-01-18 | 2004-12-29 | 成都天立化工科技有限公司 | Process for removing CO2 from conversion gas by three-stage pressure swing adsorption device |
| CN101664629A (en) * | 2009-09-27 | 2010-03-10 | 杨皓 | Pressure swing absorption process for improving recovery rate with two groups running simultaneously |
| CN101670221A (en) * | 2009-09-27 | 2010-03-17 | 杨皓 | Pressure swing adsorption technique for improving coefficient of recovery through simultaneous running of three groups |
-
2011
- 2011-04-27 CN CN2011101057075A patent/CN102179131A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1557528A (en) * | 2004-01-18 | 2004-12-29 | 成都天立化工科技有限公司 | Process for removing CO2 from conversion gas by three-stage pressure swing adsorption device |
| CN101664629A (en) * | 2009-09-27 | 2010-03-10 | 杨皓 | Pressure swing absorption process for improving recovery rate with two groups running simultaneously |
| CN101670221A (en) * | 2009-09-27 | 2010-03-17 | 杨皓 | Pressure swing adsorption technique for improving coefficient of recovery through simultaneous running of three groups |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108126516A (en) * | 2017-12-21 | 2018-06-08 | 宁夏宝塔化工中心实验室(有限公司) | A kind of plasma combustion technology purifying calcium carbide furnace tail gas process |
| CN110559799A (en) * | 2019-06-27 | 2019-12-13 | 杨皓 | Improved pressure swing adsorption reverse air discharge, scavenging gas, forward air discharge and air pumping recovery process |
| CN110559799B (en) * | 2019-06-27 | 2022-06-10 | 杨皓 | Improved pressure swing adsorption reverse air discharge, scavenging gas, forward air discharge and air pumping recovery process |
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Application publication date: 20110914 |