CN101670221A - Pressure swing adsorption technique for improving coefficient of recovery through simultaneous running of three groups - Google Patents
Pressure swing adsorption technique for improving coefficient of recovery through simultaneous running of three groups Download PDFInfo
- Publication number
- CN101670221A CN101670221A CN200910167774A CN200910167774A CN101670221A CN 101670221 A CN101670221 A CN 101670221A CN 200910167774 A CN200910167774 A CN 200910167774A CN 200910167774 A CN200910167774 A CN 200910167774A CN 101670221 A CN101670221 A CN 101670221A
- Authority
- CN
- China
- Prior art keywords
- group
- gas
- swing adsorption
- pressure
- pressure swing
- Prior art date
- 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.)
- Pending
Links
Abstract
The invention discloses a pressure swing adsorption gas separation technique for effectively improving the coefficient of gas recovery, which is characterized in that three groups of adsorption towersare arranged, wherein the first group and second group are used for pressure swing adsorption gas separation on common sense; however, the third group is additionally arranged to specially recover effective components in the desorbed gas of the first group and the second group; and the recovered effective gas components are returned to the first group and the second group for pressure swing adsorption through a pressure equalizing mode, thus improving the separation efficiency of the pressure swing adsorption gas and improving the coefficient of recovery of effective gas.
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%, and present most of wet method decarbonization devices are provided with separator (for example carbonization, transformation absorption) in addition and recycle gases such as effective hydrogen in this flash gas, nitrogen, 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%, and 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 contrary putting, and gas concentration lwevel is higher in the desorption gas, is generally 95-99%, and mean concentration is 97.5%, is directly used in the synthetic use of urea or produces liquid CO 2.
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, gas concentration lwevel is higher in the desorption gas, be generally 55-70%, mean concentration is 47.5%, 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 one group of a plurality of pressure-swing absorber again, is used for improving gas reclaiming rate.
Adsorption tower is set to three groups, 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 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, can fully reclaim along the active ingredient in venting, second group of contrary venting, the exhaust first group, and the density of carbon dioxide gas of finding time to produce even can reach more than 97% satisfies the synthetic needs of urea or produces 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, a kind of adsorption gas separating technology that improves the available gas rate of recovery, it is characterized in that: adsorption tower is set to 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 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 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910167774A CN101670221A (en) | 2009-09-27 | 2009-09-27 | Pressure swing adsorption technique for improving coefficient of recovery through simultaneous running of three groups |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910167774A CN101670221A (en) | 2009-09-27 | 2009-09-27 | Pressure swing adsorption technique for improving coefficient of recovery through simultaneous running of three groups |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101670221A true CN101670221A (en) | 2010-03-17 |
Family
ID=42017767
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200910167774A Pending CN101670221A (en) | 2009-09-27 | 2009-09-27 | Pressure swing adsorption technique for improving coefficient of recovery through simultaneous running of three groups |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101670221A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102179131A (en) * | 2011-04-27 | 2011-09-14 | 杨皓 | Three-group simultaneously-running pressure swing absorption process for increasing recovery rate |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4790858A (en) * | 1988-01-29 | 1988-12-13 | Air Products And Chemicals, Inc. | Fractionation of multicomponent gas mixtures by pressure swing adsorption |
| CN1334135A (en) * | 2001-07-31 | 2002-02-06 | 成都天立化工科技有限公司 | Process for removing CO2 from conversion gas by pressure swing adsorption method |
| CN1334136A (en) * | 2001-07-31 | 2002-02-06 | 成都天立化工科技有限公司 | Two-stage pressure swing adsorption process for decarbonizing urea |
| 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 |
-
2009
- 2009-09-27 CN CN200910167774A patent/CN101670221A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4790858A (en) * | 1988-01-29 | 1988-12-13 | Air Products And Chemicals, Inc. | Fractionation of multicomponent gas mixtures by pressure swing adsorption |
| CN1334135A (en) * | 2001-07-31 | 2002-02-06 | 成都天立化工科技有限公司 | Process for removing CO2 from conversion gas by pressure swing adsorption method |
| CN1334136A (en) * | 2001-07-31 | 2002-02-06 | 成都天立化工科技有限公司 | Two-stage pressure swing adsorption process for decarbonizing urea |
| 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 |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102179131A (en) * | 2011-04-27 | 2011-09-14 | 杨皓 | Three-group simultaneously-running pressure swing absorption process for increasing recovery rate |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2017166943A1 (en) | Full-temperature-range pressure swing adsorption gas separation, refinement and purification method | |
| CN101596391B (en) | Method for pressure swing adsorption and staged concentration of low concentration gas | |
| CN100400142C (en) | Stripped gas method for recovering C2 and higher carbon content hydrocarbon constituent | |
| CN101628198A (en) | Pressure-swing adsorption method of directly enriching methane from coal bed gas | |
| CN107433107B (en) | Two-stage concentration PSA method for recovering C2+ from refinery dry gas | |
| CN102491292A (en) | Low-consumption and low-emission nitric acid production method and production equipment thereof | |
| CN109294645A (en) | It is a kind of to utilize coke-stove gas synthesis of methanol with joint production LNG, richness H2Device and method | |
| CN101664629B (en) | Pressure swing absorption process for improving recovery rate with two groups running simultaneously | |
| CN109437234B (en) | Compound semiconductor epitaxy tail gas recycling device and method | |
| CN202355997U (en) | CO2 absorption tower and low-temperature methanol washing equipment comprising same | |
| CN102489120A (en) | Low temperature methanol wash method and equipment | |
| CN105498449B (en) | A kind of CO2Absorbent solution | |
| CN101637694B (en) | Method for separating and recycling CO2 from mixed gas containing CO2 | |
| CN102179131A (en) | Three-group simultaneously-running pressure swing absorption process for increasing recovery rate | |
| CN112678773A (en) | Process for producing hydrogen and coproducing LNG (liquefied Natural gas) by using raw gas | |
| CN102861509A (en) | Biogas decarburization and tertiary desorption process | |
| CN209052640U (en) | It is a kind of to utilize coke-stove gas synthesis of methanol with joint production LNG, richness H2Device | |
| CN101670221A (en) | Pressure swing adsorption technique for improving coefficient of recovery through simultaneous running of three groups | |
| CN101015761A (en) | Pressure-swing-adsorption purging regeneration method without using vacuum pump | |
| CN111013382A (en) | Tail gas treatment device and method for adipic acid production device | |
| CN107754558B (en) | Desulfurization and concentration method of polyethylene glycol dimethyl ether | |
| CN110201487A (en) | High-purity high-yield methane causes steady gas purification and reuse method in a kind of ethylene process epoxy ethane | |
| CN103991845B (en) | A kind of method of hydrogen production process conversion gas carbon dioxide removal | |
| CN202786165U (en) | Energy-saving methane decarburization device | |
| CN102876412A (en) | Energy-saving decarbonization process for biogas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20100317 |