CN105967184B - A kind of technique of conversion gas combined production of ammonia and soda ash - Google Patents
A kind of technique of conversion gas combined production of ammonia and soda ash Download PDFInfo
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- CN105967184B CN105967184B CN201610300798.0A CN201610300798A CN105967184B CN 105967184 B CN105967184 B CN 105967184B CN 201610300798 A CN201610300798 A CN 201610300798A CN 105967184 B CN105967184 B CN 105967184B
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
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Abstract
The present invention relates to a kind of technique that synthesis ammonia and soda ash are produced using conversion gas, 90%~95%CO that conversion gas separates through PSA12Referred to as rich CO2Gas one, while obtain the CO that concentration is less than 0.2%2For synthesizing ammonia, rich CO2Gas two is passed through weight carbon calcining furnace, after extraction with rich CO2Gas one mixes, compressed to enter joint carbonators production connection alkali, and the tail gas of discharge uses PSA2 separating and concentratings CO2To more than 90%, referred to as rich CO2Gas two, while obtain 0.28MPa CO2Concentration is less than 5% poor CO2Tail gas, poor CO2Tail gas separates through PSA3, obtains 0.25MPa CO2Concentration is less than 0.2% recovery gas, and the recovery equal force feed of gas enters PSA1, and PSA3 has part 0.01MPa 25% CO2Air is discharged into, PSA1 separation CO can be reduced2Process N2Loss, the pressure energy of joint carbonators tail gas are also recycled utilization.
Description
Technical field
The present invention relates to chemical industry and field of Environment Protection, is that a kind of effectively utilize produces waste gas reduction energy consumption with reducing raw material
The method of consumption.
Background technology
1st, the method for being used to produce connection alkali for conversion gas decarbonization, typically uses liquid phase decarburization technique, is because liquid phase takes off
Carbon technique nitrogen losses are small, and the resolution gas gas concentration lwevel of acquisition is up to 96%~99%, but liquid phase decarburization technique energy consumption
Height, and generally environment-friendly degree is not so good as pressure swing adsorption.The technology for being used to produce connection alkali for conversion gas decarbonization, is used
Two-stage method decarburization, 96%~99% concentration carbon dioxide gas can be obtained in first paragraph, be directly used in joint carbonization and liquid
Phase carbon rejection processes are compared to identical.But the rate of recovery of carbon dioxide is not so good as liquid phase carbon rejection processes.Because pressure-variable adsorption second segment is net
To change gas and reach less than 0.2%, stripping gas gas concentration lwevel is general all 55% or so, and is rich in hydrogen and carbon monoxide,
Joint carbonization is cannot be used for, because potential safety hazard be present.And nitrogen losses are very big in two sections of stripping gas, to be mended in Gas-making
Nitrogen more more than liquid phase method decarburization are filled, compressor is have impact on and goes out power.One-stage process conversion gas pressure-changeable adsorption decarbonization device desorbs
Air carbon dioxide concentration reaches 90~95%, and carbon dioxide almost all is carbonized using to do joint, purified gas dense carbon dioxide
Degree can reach less than 0.2%, but nitrogen losses are very big, it is necessary to supplement nitrogen more more than liquid phase method decarburization in Gas-making
Gas, it have impact on compressor and go out power.
2nd, the air inducing process of weight alkali calcining stove is generally negative pressure extraction, can directly introduce air into calcining tail gas.Make originally
The gas carbon dioxide concentration of carbon dioxide decomposition gas more than 99% is reduced to 60~80%, contains oxygen and nitrogen.
3rd, join alkali carbonators using decarbonization gas stripping gas or the gas concentration lwevel of resolution gas more than 96% and calcining gas 60~
80% gas concentration lwevel is mixed, and mixed pressure is reduced under 0.35~0.4MPa, into carbonators, carbonators outlet tail gas
0.3MPa gas concentration lwevels 28% or so, this gas contains oxygen and nitrogen, can not comprehensively utilize.
The content of the invention
It is a kind of to produce synthesis ammonia with joining the technique of alkali using conversion gas, carbon dioxide is separated using one section of pressure swing adsorption method,
Characterized in that, the density of carbon dioxide gas control that conversion gas pressure-variable adsorption 1 is separated is referred to as richness 90%~95%
Carbon dioxide gas one, while obtain ammonia synthesis gas of the gas concentration lwevel less than 0.2% and be used to produce synthesis ammonia, it is carbon dioxide enriched
It is nitrogen that hydrogen in gas one controls remaining below 0.5% with carbonomonoxide concentration, and carbon dioxide enriched gas one goes out pressure-variable adsorption 1
Stress control in 0.01MPa, it is not high that the pressure-variable adsorption so set up avoids two-stage method carbon dioxide yield, while 55% is dense
The stripping gas of degree can not utilize big difficult situation.Investment is also significantly less than two-stage method pressure-variable adsorption.And operation is than two-stage method letter
Just, invest also lower.The method of the present invention, nitrogen do not supplement in Gas-making, it is not required that purity nitrogen is supplemented using external enwergy, and
It is to be worked off one's feeling vent one's spleen supplement nitrogen using carbonators, greatlys save work done during compression, and ensure that gas compression pump goes out power rate.If
The carbon dioxide enriched gas two for not setting up the present invention is passed through weight alkali calcining stove positive pressure protection, or does not recycle carbonators tail gas, and one
Section method decarburization loss is lost more than effective gas of two-stage method, will be more unreasonable.
Carbon dioxide enriched gas two is passed through weight alkali calcining stove positive pressure protection calcining air inducing process, air inducing process is not sucked sky
Gas, so as to overcome calcining furnace exhaust gas oxygenous not convenient the problem of using.Carbon dioxide enriched gas two mixes with weight caustic digestion gas, from
Calcining furnace is drawn, and referred to as gaseous mixture is mixed with carbon dioxide enriched gas one, is compressed to 0.35~0.4MPa, into joint carbonators life
Congress of Industrial Organizations's alkali, gaseous mixture carbon dioxide in alkali carbonisation is joined largely are absorbed, and the tail gas of discharge is about in 0.3MPa, tail gas
Major gaseous component is carbon dioxide 28%, also a large amount of nitrogen, a small amount of hydrogen and carbon monoxide.
Carbonization tail gas has 0.3MPa pressure, gas concentration lwevel 28%, using pressure-variable adsorption 2 the carbon dioxide in tail gas
Separating and concentrating is to more than 90% and hydrogen and carbon monoxide, this technology are not routine techniques.It is if carbon dioxide is net
Change to 0.2%, stripping gas gas concentration lwevel can only have 50% or so, and circulation is compressed to 0.3MPa, and the energy of consumption can compare
Greatly, and the hydrogen and nitrogen gas rate of recovery is not high enough, and purifying carbon dioxide concentration is brought up to 5% or so, stripping gas dense carbon dioxide
Degree can reach 90~95%, referred to as carbon dioxide enriched gas two, while it is poor less than 5% to obtain 0.28MPa, gas concentration lwevel
Carbon dioxide tail gas.
The poor carbon dioxide tail gas of 5% concentration, which directly pushes back the device of pressure-variable adsorption 1, can destroy adsorption process, therefore continue
Separated using pressure-variable adsorption 3, obtain nitrogen hydrogen carbon monoxide gas of the 0.25MPa gas concentration lwevels less than 0.2% and be referred to as reclaiming gas,
The equal force feed of recovery gas enter the device of conversion gas separation carbon dioxide pressure-variable adsorption 1 some corresponding to press step, thus
Most of nitrogen of the device of pressure-variable adsorption 1 loss is reclaimed, so as to avoid gas making stage supplement nitrogen or supplement in addition pure
The process of nitrogen.The 0.3MPa energy separations recovery nitrogen of the invention that rationally make use of carbonators outlet vent gas, avoids energy
Amount wastes.
The gas of still some 0.01MPa of pressure-variable adsorption 3 of loss gas concentration lwevel 25% or so is discharged into greatly
Gas, the gas still can be with pressure recovery nitrogen and carbon dioxide, but needs to compress, more worthwhile not as directly emptying.
Embodiment
Embodiment 1：Certain 180,000 tons/year of ammonia and 500,000 tons of connection alkali devices, 100,000 mark sides/hour conversion gas 1.6MPa transformation are inhaled
Attached 1 evacuates technique separation carbon dioxide, and purified gas gas concentration lwevel is 0.15%, send ammonia synthesis system.Stripping gas titanium dioxide
Concentration of carbon 93%.Weight alkali calcining stove is changed to the carbon dioxide enriched positive pressure protection of gas two by original negative pressure induced wind and blown, carbon dioxide
Concentration is increased to more than 95% by original 80%, and oxygen content is less than 0.2%.Calciner exit gas and pressure-variable adsorption
1 device stripping gas mixes, and send connection alkali carbon-dioxide gas compressor.Pressurized carbon dioxide is reduced to 0.35MPa and send connection alkali carbonators.It is carbonized out
Gas gas concentration lwevel 33%, pressure 0.3MPa.
Carbonization exit gas is sent into the device of pressure-variable adsorption 2, the nitrogen hydrogen one that the concentration of carbon dioxide 5% is obtained from outlet aoxidizes
Carbon gas, oxygen concentration are less than 0.3%.The gas for obtaining the concentration of carbon dioxide 90% simultaneously send weight alkali calcining stove to do positive pressure protection
Gas.
The nitrogen hydrogen carbon monoxide gas of the concentration of carbon dioxide 5% come out from the device of pressure-variable adsorption 2, pressure 0.28MPa, send
Enter the device of pressure-variable adsorption 3, obtain the nitrogen hydrogen of exit concentration 0.2%, oxygen concentration is less than 0.4%, is pressed into change at twice
Pressure rises for the first time after the evacuation of pressure 1 device of absorption and third time pressure rises.
From the stripping gas gas concentration lwevel about 27% of the device of pressure-variable adsorption 3 outflow, air is discharged directly into.
Embodiment 2：Certain 280,000 tons/year of ammonia and 700,000 tons of connection alkali devices, 150,000 mark sides/hour conversion gas 2.6MPa transformation are inhaled
Attached 1 purging+recovery process separation carbon dioxide, purified gas gas concentration lwevel is 0.1%, send ammonia synthesis system.Stripping gas two
Concentration of carbon 92% is aoxidized, desorbs atmospheric pressure 0.005MPa,.Weight alkali calcining stove is changed to carbon dioxide enriched gas by original negative pressure induced wind
Two positive pressure protections are blown, and gas concentration lwevel is increased to more than 95% by original 70%, and oxygen content is less than 0.2%.
Calciner exit gas mixes with the device stripping gas of pressure-variable adsorption 1, send connection alkali carbon-dioxide gas compressor.Pressurized carbon dioxide is reduced to
0.35MPa send connection alkali carbonators.Be carbonized exit gas gas concentration lwevel 28%, pressure 0.3MPa.
Carbonization exit gas is sent into the device of pressure-variable adsorption 2, the nitrogen hydrogen one that the concentration of carbon dioxide 5% is obtained from outlet aoxidizes
Carbon gas, oxygen concentration are less than 0.3%.The gas for obtaining the concentration of carbon dioxide 90% simultaneously send weight alkali calcining stove to do positive pressure protection
Gas.
The nitrogen hydrogen carbon monoxide gas of the concentration of carbon dioxide 5% come out from the device of pressure-variable adsorption 2, pressure 0.28MPa, send
Enter the device of pressure-variable adsorption 3, obtain the nitrogen hydrogen of exit concentration 0.2%, oxygen concentration is less than 0.4%, is pressed into change at twice
Pressure rises for the first time after the evacuation of pressure 1 device of absorption and pressure rises for the second time.
From the stripping gas gas concentration lwevel about 27% of the device of pressure-variable adsorption 3 outflow, air is discharged directly into.
Embodiment 3：Certain 90,000 tons/year of ammonia and 250,000 tons of connection alkali devices, 5.4 ten thousand mark sides/hour conversion gas 0.9MPa transformation are inhaled
Attached 1 evacuates technique separation carbon dioxide, and purified gas gas concentration lwevel is 0.25%, send ammonia synthesis system.Stripping gas titanium dioxide
Concentration of carbon 89%, atmospheric pressure 0.005MPa is desorbed,.Weight alkali calcining stove is being changed to carbon dioxide enriched gas two just by original negative pressure induced wind
Pressure protection air-supply, gas concentration lwevel is increased to more than 95% by original 70%, and oxygen content is less than 0.2%.Calcining
Outlet of still gas mixes with the device stripping gas of pressure-variable adsorption 1, send connection alkali carbon-dioxide gas compressor.Pressurized carbon dioxide is reduced to
0.35MPa send connection alkali carbonators.Be carbonized exit gas gas concentration lwevel 27%, pressure 0.3MPa.
Carbonization exit gas is sent into the device of pressure-variable adsorption 2, the nitrogen hydrogen one that the concentration of carbon dioxide 5% is obtained from outlet aoxidizes
Carbon gas, oxygen concentration are less than 0.3%.The gas for obtaining the concentration of carbon dioxide 90% simultaneously send weight alkali calcining stove to do positive pressure protection
Gas.
The nitrogen hydrogen carbon monoxide gas of the concentration of carbon dioxide 5% come out from the device of pressure-variable adsorption 2, pressure 0.28MPa, send
Enter the device of pressure-variable adsorption 3, obtain the nitrogen hydrogen of exit concentration 0.2%, oxygen concentration is less than 0.4%, is pressed into change at twice
Pressure rises for the first time after the evacuation of pressure 1 device of absorption and third time pressure rises.
From the stripping gas gas concentration lwevel about 27% of the device of pressure-variable adsorption 3 outflow, air is discharged directly into.
Pressure swing adsorption method will be reduced using the present invention to invest, while reduce the consumption of synthesis ammonia.
Claims (1)
1. a kind of technique for producing synthesis ammonia and connection alkali using conversion gas, it is characterised in that conversion gas pressure-variable adsorption 1 is isolated
The density of carbon dioxide gas control come is referred to as carbon dioxide enriched gas one 90%~95%, while it is low to obtain gas concentration lwevel
Ammonia synthesis gas in 0.2% synthesizes ammonia for producing, and the hydrogen in carbon dioxide enriched gas one controls with carbonomonoxide concentration to exist
Less than 0.5% remaining be nitrogen, carbon dioxide enriched gas one goes out the Stress control of pressure-variable adsorption 1 in 0.01MPa, carbon dioxide enriched gas
Two are passed through weight carbon calcining furnace positive pressure protection calcining air inducing process, air inducing process is not sucked air, are drawn and richness from calcining furnace
The mixing of carbon dioxide gas one is referred to as gaseous mixture, is compressed to 0.35~0.4MPa, and into joint carbonators production connection alkali, gaseous mixture exists
Carbon dioxide is largely absorbed in connection alkali carbonisation, and for the tail gas of discharge in 0.3MPa, tail gas major gaseous component is dioxy
Change carbon 28%, also a large amount of nitrogen, a small amount of hydrogen and carbon monoxide, using pressure-variable adsorption 2 the carbon dioxide separation in tail gas
Concentrate is to more than 90% and not hydrogen and carbon monoxide, referred to as carbon dioxide enriched gas two, while obtain 0.28MPa, dioxy
Change the poor carbon dioxide tail gas that concentration of carbon is less than 5%, poor carbon dioxide tail gas is continuing with pressure-variable adsorption 3 and separated, and obtains
Nitrogen hydrogen carbon monoxide gas of the 0.25MPa gas concentration lwevels less than 0.2% is referred to as reclaiming gas, and the equal force feed of recovery gas is entered conversion gas
Separate the device of carbon dioxide pressure-variable adsorption 1, the gas row of some 0.01MPa of pressure-variable adsorption 3 gas concentration lwevel 25%
Enter air, thus reduce the nitrogen losses that conversion gas pressure swing adsorption method 1 separates carbon dioxide process, combine the pressure of carbonators tail gas
Power can also be recycled utilization.
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| CN201610300798.0A CN105967184B (en) | 2016-05-10 | 2016-05-10 | A kind of technique of conversion gas combined production of ammonia and soda ash |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106731477A (en) * | 2016-12-20 | 2017-05-31 | 杨皓 | The technique that a kind of conversion gas pressure-variable adsorption combines decarburization with ammoniacal liquor after-purification |
| CN107235473A (en) * | 2017-06-09 | 2017-10-10 | 杨皓 | A kind of carbon black tail gas and coke oven tail gas combined production of ammonia alcohol synthesis gas process |
Citations (4)
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|---|---|---|---|---|
| CN1069708A (en) * | 1991-08-24 | 1993-03-10 | 化学工业部西南化工研究院 | Pressure swing adsorption process for removing carbon dioxide from ammonia plant shift gas |
| 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 |
| CN101095996A (en) * | 2006-06-30 | 2008-01-02 | 山东联合化工股份有限公司 | Transformed gas recycling technics through pressure swing adsorption process |
| CN101664629A (en) * | 2009-09-27 | 2010-03-10 | 杨皓 | Pressure swing absorption process for improving recovery rate with two groups running simultaneously |
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2016
- 2016-05-10 CN CN201610300798.0A patent/CN105967184B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1069708A (en) * | 1991-08-24 | 1993-03-10 | 化学工业部西南化工研究院 | Pressure swing adsorption process for removing carbon dioxide from ammonia plant shift gas |
| 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 |
| CN101095996A (en) * | 2006-06-30 | 2008-01-02 | 山东联合化工股份有限公司 | Transformed gas recycling technics through pressure swing adsorption process |
| CN101664629A (en) * | 2009-09-27 | 2010-03-10 | 杨皓 | Pressure swing absorption process for improving recovery rate with two groups running simultaneously |
Non-Patent Citations (1)
| Title |
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| 碳铵小厂改为变换气联碱的合理性探讨--解决我国纯碱生产途径之一;李琼玖;《化工设计通讯》;19831231;第1-11页，第23页 * |
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