CN101664629A - Pressure swing absorption process for improving recovery rate with two groups running simultaneously - Google Patents
Pressure swing absorption process for improving recovery rate with two groups running simultaneously Download PDFInfo
- Publication number
- CN101664629A CN101664629A CN200910167773A CN200910167773A CN101664629A CN 101664629 A CN101664629 A CN 101664629A CN 200910167773 A CN200910167773 A CN 200910167773A CN 200910167773 A CN200910167773 A CN 200910167773A CN 101664629 A CN101664629 A CN 101664629A
- Authority
- CN
- China
- Prior art keywords
- gas
- group
- pressure swing
- pressure
- recovery rate
- 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.)
- Granted
Links
Landscapes
- Separation Of Gases By Adsorption (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
The invention discloses a pressure swing absorption gas separation process for improving active gas recovery rate, which is characterized in that two groups of adsorption towers are arranged, whereinthe first group is used for pressure swing adsorption gas separation in common sense, the second group is arranged to be specially used for recovering active ingredients in the first group reverse deabsorption gas, the recovered active gas ingredients are returned to the first group for pressure swing absorption in a pressure equalizing way, thereby improving pressure swing adsorption gas separation efficiency and active gas recovery rate.
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, solvent desorption 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, gas concentration lwevel is higher in the desorption gas, be generally 95-100%, mean concentration is 97.5%, can be directly used in the synthetic use of urea or produce liquid CO 2.The wet method decarburization, has solvent consumption etc. to become insoluble problem at operating cost height, energy consumption height, and is higher but gas recovery ratio is compared common pressure swing adsorption technique.
The pressure swing adsorption decarbonization technology, using maximum is one-stage process technology, this technology is absorbing carbon dioxide under the high pressure adsorbent, 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 45-85%, mean concentration is 65%, at present the pressure swing adsorption decarbonization device is not provided with separator in addition and recycles effective hydrogen in this contrary venting body, nitrogen, gases such as carbon monoxide have 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 or washes, and gas concentration lwevel is higher in the desorption gas, is generally 95-99%, and mean concentration is 97.5%, can be directly used in that urea is synthetic to use or produce liquid CO 2.The contrary venting of this technology body loss of effective components is serious, becomes the deadly defect of this technology, almost is difficult to overcome.
Three, summary of the invention
For the better active ingredient (hydrogen, carbon monoxide and nitrogen) that reclaims in the contrary venting of the decarburization body, utilization of the present invention is provided with the strategy of one group of a plurality of adsorption tower again, is used for improving gas reclaiming rate.
Adsorption tower is set to two groups, wherein first group of transformation adsorbed gas that is used on the common meaning separates, be specifically designed to first group of contrary active ingredient of putting in the desorption gas of recovery and be provided with second group in addition, the available gas composition that reclaims returns first 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 the active ingredient in the contrary venting fully be reclaimed, 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 similar wet method decarburization simultaneously and reclaim the high system of dodging gas, promptly other one group of adsorption tower, this system continues carbon dioxide to separate to obtain the gaseous mixture that gas concentration lwevel is not higher than conversion gas concentration.
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 24000NM
3/ H.
First group of pressure swing adsorption technique that sets up standard, nine towers three advance three equal technologies, contrary put initial pressure 0.10MPa, the end pressure-0.06MPa that finds time, and conversion gas import carbon dioxide 28%, the Ammonia Production requirement is satisfied in outlet 0.2%.
Second group is provided with the recovery pressure swing adsorption technique, four towers one advance an equal technology, air inlet initial pressure-0.04MPa, air inlet end pressure 0.08MPa, end pressure-the 0.06MPa that finds time, contrary venting import carbon dioxide 45-85%, outlet 5%, exit gas uses the mode of all pressing to return main system, satisfies first group of body composition requirement of all calming the anger.
Embodiment 2: conversion atmospheric pressure 1.4MPa, flow 24000NM
3/ H.
First group of pressure swing adsorption technique that sets up standard, nine towers three advance three equal technologies, contrary put initial pressure 0.26MPa, the end pressure-0.06MPa that finds time, and conversion gas import carbon dioxide 28%, the Ammonia Production requirement is satisfied in outlet 0.2%.
Second group is provided with the recovery pressure swing adsorption technique, it is one equal that four towers one advance, air inlet initial pressure-0.04MPa, air inlet end pressure 0.18MPa, end pressure-the 0.06MPa that finds time, contrary venting import carbon dioxide 35-55%, outlet 3%, exit gas uses the mode of all pressing to return main system, satisfies first group of body composition requirement of all calming the anger.
Embodiment 3: conversion atmospheric pressure 2.7MPa, flow 24000NM
3/ H.
First group of pressure swing adsorption technique that sets up standard, 16 towers three advance nine equal technologies, contrary put initial pressure 0.54MPa, the end pressure-0.06MPa that finds time, and conversion gas import carbon dioxide 28%, the Ammonia Production requirement is satisfied in outlet 0.2%.
Second group is provided with the recovery pressure swing adsorption technique, it is one equal that four towers one advance, air inlet initial pressure-0.04MPa, air inlet end pressure 0.42MPa, end pressure-the 0.06MPa that finds time, contrary venting import carbon dioxide 15-35%, outlet 2%, exit gas uses the mode of all pressing to return main system at twice, satisfies first group of body composition requirement of all calming the anger.
This patent uses at conversion gas decarbonization device 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 two groups, wherein first group of transformation adsorbed gas that is used on the common meaning separates, be specifically designed to first group of contrary active ingredient of putting in the desorption gas of recovery and be provided with second group in addition, the available gas composition that reclaims returns first 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 |
|---|---|---|---|
| CN200910167773.8A CN101664629B (en) | 2009-09-27 | 2009-09-27 | Pressure swing absorption process for improving recovery rate with two groups running simultaneously |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910167773.8A CN101664629B (en) | 2009-09-27 | 2009-09-27 | Pressure swing absorption process for improving recovery rate with two groups running simultaneously |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101664629A true CN101664629A (en) | 2010-03-10 |
| CN101664629B CN101664629B (en) | 2015-06-24 |
Family
ID=41801504
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200910167773.8A Active CN101664629B (en) | 2009-09-27 | 2009-09-27 | Pressure swing absorption process for improving recovery rate with two groups running simultaneously |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101664629B (en) |
Cited By (4)
| 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 |
| CN102627259A (en) * | 2012-03-27 | 2012-08-08 | 成都赛普瑞兴科技有限公司 | Method for preparing hydrogen by methanol-water reforming |
| CN105413394A (en) * | 2015-12-25 | 2016-03-23 | 杨皓 | Method of combined preparation of acidic gas and pure nitrogen from flue gas through pressure swinging adsorption process |
| CN105967184A (en) * | 2016-05-10 | 2016-09-28 | 杨皓 | Process for combined production of ammonia and sodium carbonate by using shift gas |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN1879943A (en) * | 2006-05-10 | 2006-12-20 | 杨皓 | Pressure-variable adsorption decarbonization improved process for carbamide and methanol |
-
2009
- 2009-09-27 CN CN200910167773.8A patent/CN101664629B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN1879943A (en) * | 2006-05-10 | 2006-12-20 | 杨皓 | Pressure-variable adsorption decarbonization improved process for carbamide and methanol |
Cited By (6)
| 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 |
| CN102627259A (en) * | 2012-03-27 | 2012-08-08 | 成都赛普瑞兴科技有限公司 | Method for preparing hydrogen by methanol-water reforming |
| CN105413394A (en) * | 2015-12-25 | 2016-03-23 | 杨皓 | Method of combined preparation of acidic gas and pure nitrogen from flue gas through pressure swinging adsorption process |
| CN105413394B (en) * | 2015-12-25 | 2019-01-15 | 杨皓 | A method of combined using pressure swing adsorption technique from flue gas and produces sour gas and purity nitrogen |
| CN105967184A (en) * | 2016-05-10 | 2016-09-28 | 杨皓 | Process for combined production of ammonia and sodium carbonate by using shift gas |
| CN105967184B (en) * | 2016-05-10 | 2018-02-23 | 杨皓 | A kind of technique of conversion gas combined production of ammonia and soda ash |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101664629B (en) | 2015-06-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2017166943A1 (en) | Full-temperature-range pressure swing adsorption gas separation, refinement and purification method | |
| CN109999618B (en) | System and method for separating carbon dioxide from medium-high pressure gas source | |
| CN103011198B (en) | Process for preparing synthetic ammonia with coke-oven gas | |
| 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 | |
| CN112625761B (en) | Process for removing low-partial pressure acid gas in low-pressure feed gas by using low-temperature methanol | |
| 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 | |
| CN113877371A (en) | Catalytic cracking regeneration method with zero emission of carbon dioxide | |
| CN108970332A (en) | A kind of decarbonization method of converter and/or blast furnace gas | |
| CN107778124B (en) | Full-temperature range adsorption extraction separation method for recovering H2 and C2+ from refinery dry gas | |
| CN102491292A (en) | Low-consumption and low-emission nitric acid production method and production equipment thereof | |
| CN102489120A (en) | Low temperature methanol wash method and equipment | |
| CN202355997U (en) | CO2 absorption tower and low-temperature methanol washing equipment comprising same | |
| CN100400142C (en) | Stripped gas method for recovering C2 and higher carbon content hydrocarbon constituent | |
| CN105498449B (en) | A kind of CO2Absorbent solution | |
| CN102049174A (en) | Method for partially separating carbon dioxide from gas mixture | |
| CN103991845B (en) | A kind of method of hydrogen production process conversion gas carbon dioxide removal | |
| CN102179131A (en) | Three-group simultaneously-running pressure swing absorption process for increasing recovery rate | |
| CN101015761A (en) | Pressure-swing-adsorption purging regeneration method without using vacuum pump | |
| CN101670221A (en) | Pressure swing adsorption technique for improving coefficient of recovery through simultaneous running of three groups | |
| CN107754558B (en) | Desulfurization and concentration method of polyethylene glycol dimethyl ether | |
| CN113368663B (en) | Treatment method of Fischer-Tropsch synthesis decarbonized tail gas and equipment system for implementing method | |
| CN202786165U (en) | Energy-saving methane decarburization device | |
| CN210410096U (en) | Separation system for carbon dioxide in medium-high pressure gas source |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |