CN104925809B - A kind of method and system that carbon dioxide is reclaimed from industrial waste gas - Google Patents
A kind of method and system that carbon dioxide is reclaimed from industrial waste gas Download PDFInfo
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- CN104925809B CN104925809B CN201510250717.6A CN201510250717A CN104925809B CN 104925809 B CN104925809 B CN 104925809B CN 201510250717 A CN201510250717 A CN 201510250717A CN 104925809 B CN104925809 B CN 104925809B
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- waste gas
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Abstract
The invention provides a kind of method that carbon dioxide is reclaimed from industrial waste gas, comprise the following steps：Step one：Acquisition ammonium bicarbonate aqueous solution and tail gas are contacted under 0.1 3.0MPa with ammoniacal liquor by industrial waste gas by desulfurization process and after being cooled to 20 30 DEG C, tail gas progress desalination water washing heel row is put；Step 2：The ammonium bicarbonate aqueous solution that step one is obtained be forced into after 1.7 3.0MPa be passed through it is middle pressure first ammonium converter contact with ammonia obtain in pressure first ammonium salt solution；Step 3：Medium pressure first ammonium salt solution is passed through urea plant, for producing urea.CO is reclaimed from industrial waste gas present invention also offers one kind2System.The method of the present invention and system are using industrial waste gas as raw material, using factory's deposed ammonia, by CO2Reclaim and be used for urea production.Without introducing raw material from the external world, effective recycling is carried out to waste gas, course of reaction is simple, easy to operate, reduces waste gas CO2Discharge, it is environment-friendly, and reached the actual benefit of urea with increased yield, have a good application prospect.
Description
Technical field
The present invention relates to industrial waste gas process field, and in particular to a kind of method that carbon dioxide is reclaimed from industrial waste gas
And system.
Background technology
Global warming has become the environmental problem of the maximum-norm of facing mankind, increasingly by countries in the world political affairs
Mansion and the concern of the people.At present, emission reduction and trapping greenhouse gases are one of most active brainstorm subjects of sciemtifec and technical sphere.CO2Separation
Trapping technique generally comprises solvent absorption, physisorphtion, membrane separation process, low temperature processing and O2/CO2Circulating combustion method etc..
CO in industrial discharged waste gas, boiler smoke2Concentration is low, about 5%~15%, CO2Trapping reclaims difficult, and cost is higher.
Existing CO2It is typically using to CO to flutter collection technology2Absorbability is strong, i.e. the big physically or chemically solvent of solubility,
The CO in carbon containing waste gas is absorbed under a certain pressure2, carbon containing waste liquid heating under reduced pressure parses CO2Gas, obtains regeneration gas.Regeneration gas
Can individually be pressurizeed production urea.But there is presently no convenient, energy-conservation the CO suitable for urea plant2Recovery method.
The content of the invention
It is an object of the invention to provide the general of a kind of course of reaction simplicity for being suitable for urea production factory application, energy-conservation
The method that carbon dioxide recovery in industrial waste gas is utilized.
Second object of the present invention is to provide a kind of industrial waste gas processing system.
To achieve the above objectives, the invention provides a kind of method that carbon dioxide is reclaimed from industrial waste gas, including with
Lower step：
Step one：Connect by industrial waste gas by desulfurization process and after being cooled to 20-30 DEG C with ammoniacal liquor under 0.1-3.0MPa
Touch and obtain ammonium bicarbonate aqueous solution and tail gas, tail gas progress desalination water washing heel row is put；
Step 2：The ammonium bicarbonate aqueous solution that step one is obtained, which is forced into after 1.7-3.0MPa, is passed through middle pressure first ammonium conversion
Device is contacted with ammonia presses first ammonium salt solution in acquisition；
Step 3：Medium pressure first ammonium salt solution is passed through urea plant, for producing urea.
Optionally, the industrial waste gas is the waste gas that produces in urea production process, wherein, the content of carbon dioxide is 5-
15%.
Optionally, ammonia described in step 2 is to be isolated from the process gas containing ammonia of rectifying column in urea production process.
The invention provides a kind of industrial waste gas processing system, including：
Carbon dioxide absorption tower (1), tail gas washer (2), carbon ammonium booster (3), hydrojet pump (4), middle pressure first ammonium
Converter (5).
Optionally, floating filler (11), exhaust gas entrance (12), tail gas are provided with the carbon dioxide absorption tower (1) to go out
Mouth (13), ammoniacal liquor inlet (14), ammonium bicarbonate aqueous solution outlet (15), wherein, the floating filler (11) is nonmetallic sky
Bulbus cordis or medicine ball.
Optionally, the exhaust gas entrance (12) is arranged at the bottom of carbon dioxide absorption tower (1), and ammoniacal liquor inlet (14) is set
The top of carbon dioxide absorption tower (1) is placed in, offgas outlet (13) is arranged at the top of carbon dioxide absorption tower (1) and by pipe
Road is connected with being arranged at the gas inlet (21) of tail gas washer (2) bottom；Washing is additionally provided with the tail gas washer (2)
Water inlet (22), exhaust port (23) and valve plate (24).
Optionally, medium pressure first ammonium converter (5) top is provided with ammonium bicarbonate solution entrance (51), bottom and is provided with ammonia
Gas entrance (52), middle pressure first ammonium salt solution outlet (53).
Optionally, the ammonium bicarbonate aqueous solution outlet (15) is connected with carbon ammonium booster (3), the carbon ammonium booster
(3) the other end is connected by ammonium hydrogen carbonate pipeline (8) with ammonium hydrogen carbonate entrance (51).
Optionally, the system also includes exporting high pressure carbamate pump (6), the height that (53) are connected with middle pressure first ammonium salt solution
The other end of pressure first ammonium pump (6) is connected with Urea Conversion System.
Optionally, the ammonia entrance (52) is connected by ammonia pipeline (9) with urea rectifying column (7).
Method provided by the present invention is with containing 5%~15%CO2Industrial waste gas as initiation material, utilize factory to give up ammonia
Water, by CO2Reclaim and be used for urea production, it is to avoid CO present in existing recovery method2Seal problem up for safekeeping.This method without
Raw material need to be introduced from the external world, effective recycling has been carried out to waste gas.Course of reaction that the technique that the present invention is reclaimed is related to is simple,
It is easy to operate, reduce waste gas CO2Discharge, it is environment-friendly, and reached the actual benefit of urea with increased yield, should with good
Use prospect.
Brief description of the drawings
Accompanying drawing is, for providing a further understanding of the present invention, and to constitute a part for specification, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is the structural representation of system of the present invention；
Description of reference numerals：
1：Carbon dioxide absorption tower；11：Floating filler；12：Exhaust gas entrance；13：Offgas outlet；14：Ammoniacal liquor inlet；
15：Ammonium bicarbonate aqueous solution is exported；
2：Tail gas washer；21:Gas inlet；22：Washing water inlet；23：Exhaust port；24：Valve plate；25：
Ammoniacal liquor return pipeline；
3：Carbon ammonium booster；4：Hydrojet pump；
5：Middle pressure first ammonium converter；51：Ammonium hydrogencarbonate entrance；52：Ammonia entrance；
53：Middle pressure first ammonium salt solution outlet；54：Cooling system；55：Gaseous phase outlet；
6：High pressure carbamate pump；7：Urea rectifying column；
8：Ammonium hydrogen carbonate pipeline；81：Middle pressure carbon ammonium returns to injector；
9：Ammonia pipeline.
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that this place is retouched
The embodiment stated is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The invention provides a kind of method that carbon dioxide is reclaimed from industrial waste gas, comprise the following steps：
Step one：Connect by industrial waste gas by desulfurization process and after being cooled to 20-30 DEG C with ammoniacal liquor under 0.1-3.0MPa
Touch and obtain ammonium bicarbonate aqueous solution and tail gas, tail gas progress desalination water washing heel row is put；
Step 2：The ammonium bicarbonate aqueous solution that step one is obtained, which is forced into after 1.7-3.0MPa, is passed through middle pressure first ammonium conversion
Device is contacted with ammonia presses first ammonium salt solution in acquisition；
Step 3：Medium pressure first ammonium salt solution is passed through urea plant, for producing urea.
It is preferred that, the condition contacted in step one is 22-28 DEG C, 0.2-2.0MPa.
Wherein, in step one, the industrial waste gas relative to every cubic metre, the consumption of ammoniacal liquor is 1-5 liters.
In method provided by the present invention, the industrial waste gas is the industrial waste gas containing carbon dioxide, carbon dioxide
Content can be 5-15% (volumn concentration).It is preferred that in the case of, the industrial waste gas is production in urea production process
Raw waste gas, wherein, the content of carbon dioxide is 5-15% (volumn concentration).
Method provided by the present invention for by industrial waste gas carry out desulfurization process method do not require particularly, as long as
Sulfur content in waste gas can be taken off to below 5ppmv, for example, can use ferric oxide desulfurizer or active carbon desulfurization side
Method.
Wherein, the concentration of the ammoniacal liquor can be 5-25% (weight/mass percentage composition), preferably in the case of, in order to obtain more
Good trade waste processing utilizing status, the ammoniacal liquor can be ammonia-containing water, for example, can be collected from lignite (or cigarette
Coal) fixed bed pressured gasification discharge ammonia-containing water.
Wherein, the industrial waste gas relative to every cubic metre, the consumption of ammoniacal liquor is 1-5 liters.The speed that is passed through of industrial waste gas is regarded
Depending on the amount and ammonia density of the ammonia-containing water of recovery.
Wherein, ammonia level is less than 18mg/Nm in the tail gas3Reach atmospheric emission standard.
The concentration of the ammonium bicarbonate aqueous solution is 20-80 g/l.
Method provided by the present invention has no particular limits for the method cleaned to tail gas, for example, can use
Ferric oxide desulfurizer or active carbon desulfurization method.
Optionally, ammonia described in step 2 be urea production process in be isolated from rectifying column the process gas containing ammonia amount
Do not require, as long as so that the NH being passed through3After reacted, obtained methylamine solution concentration is up to standard.
The temperature conditionss contacted in step 2 are 20-30 DEG C.The speed that is passed through of ammonium hydrogen carbonate can be according to recovery containing ammonia
The amount and ammonia density of waste water are adjusted.
In step 3, middle pressure first ammonium salt solution, which is passed through in carbamide production system, is used for subsequent production urea, medium pressure
The concentration of first ammonium salt solution is 60-80% (weight/mass percentage composition).
As shown in figure 1, the industrial waste gas processing system of the present invention, including：
Carbon dioxide absorption tower 1, tail gas washer 2, carbon ammonium booster 3, hydrojet pump 4, middle pressure first ammonium converter 5.
Wherein, floating filler 11, exhaust gas entrance 12, offgas outlet 13, ammoniacal liquor are provided with the carbon dioxide absorption tower 1
Inlet 14, ammonium bicarbonate aqueous solution outlet 15, wherein, the floating filler 11 is Nonmetallic hollow sphere or medicine ball.
Wherein, the effect of the floating filler 11 is the ammoniacal liquor Action of Gravity Field and bottom of towe ascending air sprayed in tower top
Thrust under, constantly floated by filler internals, gas-liquid two-phase is more fully contacted, improve CO2Absorption efficiency is with removing
Dirt efficiency.
The exhaust gas entrance 12 is arranged at the bottom of carbon dioxide absorption tower 1, and ammoniacal liquor inlet 14 is arranged at carbon dioxide
The top on absorption tower 1, offgas outlet 13 is arranged at the top of carbon dioxide absorption tower 1 and cleaned by pipeline with being arranged at tail gas
The gas inlet 21 of the bottom of device 2 is connected.Washing water inlet 22, the and of exhaust port 23 are additionally provided with the tail gas washer 2
Valve plate 24, the quantity of valve plate has no particular limits, and can be individual layer, the structure of valve plate can be according to difference
Tolerance load is adjusted.
In one embodiment of the invention, the industrial waste gas after desulfurization by hydrojet pump 4 through exhaust gas entrance 12
Into carbon dioxide absorption tower 1, gas flows upwards through the effect of floating filler 11 and via the input of ammoniacal liquor inlet 14
Ammoniacal liquor counter current contacting, carries out mass transfer reaction, and tail gas enters tail gas washer with gas inlet 21 by the road by offgas outlet 13
2, ammonium bicarbonate aqueous solution is through the transport of ammonium bicarbonate aqueous solution outlet 15 to carbon ammonium booster 3.In tail gas washer, warp is utilized
The washings that washing water inlet 22 enters are cleaned to tail gas, and the tail gas after cleaning is discharged by exhaust port 23.Dioxy
Change and be also provided with ammoniacal liquor return pipeline 25 between carbon absorption tower 1 and tail gas washer 2, it is de- for that will be passed through in washer 2
The ammoniacal liquor obtained after salt solution cleaning returns to carbon dioxide absorption tower 1 and recycled.
The effect of carbon ammonium booster 3 is that the ammonium bicarbonate aqueous solution for generating carbon dioxide absorption tower 1 boosts to 1.7-
First ammonium converter is pressed in entering after 3.0Mpa through ammonium hydrogen carbonate pipeline 8.The ammonium hydrogen carbonate pipeline 8 can also pass through middle pressure carbon ammonium
Return to injector 81 to be connected with hydrojet pump 4, for providing the power resources that flue gas enters absorption tower.
Wherein, the top of medium pressure first ammonium converter 5 is provided with ammonium hydrogen carbonate entrance 51, bottom and is provided with ammonia entrance
52nd, middle pressure first ammonium salt solution outlet 53.The ammonium bicarbonate aqueous solution outlet 15 is connected with carbon ammonium booster 3, the carbon ammonium boosting
The other end of pump 3 is connected by ammonium hydrogen carbonate pipeline 8 with ammonium hydrogen carbonate entrance 51.It is additionally provided with middle pressure first ammonium converter 5 cold
But system 54.
In one embodiment of the invention, passed through after the carbon ammonium booster pressurizes ammonium bicarbonate aqueous solution by carbonic acid
Pressure first ammonium converter 5 is contacted with ammonia during hydrogen ammonium pipeline 8 enters, and the middle pressure first ammonium salt solution obtained after contact is molten by middle pressure first ammonium
Liquid outlet 53 is discharged, and the residual gas in middle pressure first ammonium converter 5 is discharged by gaseous phase outlet 55, and the residual gas of discharge goes low
Pressure absorption system is absorbed, and the low pressure absorption system comes from urea rectifying column to be used to recycle in field of urea production
Gas device, be the conventional equipment of field of urea production.
In one embodiment of the invention, the system also includes the high pressure being connected with middle pressure first ammonium salt solution outlet 53
First ammonium pump 6, the other end of the high pressure carbamate pump 6 are connected with Urea Conversion System, and middle pressure first ammonium salt solution passes through high pressure carbamate pump 6
Urea Conversion System is gone after pressurization is used for urea production.
In one embodiment of the invention, the ammonia entrance 52 is connected by ammonia pipeline 9 with urea rectifying column 7
Connect, for first ammonium converter 5 will to be pressed in the input of the ammonia of urea rectifying column 7.
Below will the present invention is described in detail by embodiment.It will be appreciated that following examples are given
Go out merely to play descriptive purpose, be not used to limit the scope of the present invention.Those skilled in the art exists
In the case of without departing substantially from spirit of the invention and spirit, various modifications and replacement can be carried out to the present invention.
Embodiment 1
Power boiler flue gas (CO in urea plant after active carbon method desulfurization210%) it, is 25 in temperature that content is
DEG C, pressure is enters carbon dioxide absorption tower 1 under 0.15MPa through hydrojet pump 4 and exhaust gas entrance 12, and gas flows up logical
(ammonia concn is with the deposed ammonia that is inputted via ammoniacal liquor inlet 14 for the effect for crossing floating filler 11 (polypropylene hollow ball)
15%, the power boiler flue gas relative to every cubic metre, the consumption of deposed ammonia is 2.5 liters) counter current contacting, mass transfer reaction is carried out,
Tail gas enters tail gas washer 2 with gas inlet 21 by the road by offgas outlet 13, and (concentration is 80g/ to ammonium bicarbonate aqueous solution
L) through the transport of ammonium bicarbonate aqueous solution outlet 15 to carbon ammonium booster 3.
In tail gas washer, the washings (desalted water) entered using scrubbed water inlet 22 are cleaned to tail gas,
Tail gas after cleaning is discharged into air by exhaust port 23, NH in the tail gas after cleaning3Content is less than 18mg/Nm3, CO2
Content is less than 2%.
The ammonium bicarbonate aqueous solution of carbon dioxide absorption tower generation boosts to 2.0MPa, via carbonic acid through carbon ammonium booster 3
Hydrogen ammonium pipeline 8 presses first ammonium converter 5 in entering, with (the gaseous mixture containing ammonia of gaseous mixture containing ammonia from urea rectifying column 7 at 25 DEG C
Pressure first ammonium converter in being entered by ammonia pipeline 9 and ammonia entrance 52) contact conversion reaction is carried out, press first ammonium molten in generation
Liquid；Then first ammonium salt solution will be pressed therefrom to press first ammonium salt solution to export 53 outputs in gained to pressurize through urea plant mesohigh first ammonium pump 6,
Urea Conversion System generation urea is returned, processing procedure is completed.
Embodiment 2
Power boiler flue gas (CO in urea plant after active carbon method desulfurization215%) it, is 30 in temperature that content is
DEG C, pressure is enters carbon dioxide absorption tower 1 under 3MPa through hydrojet pump 4 and exhaust gas entrance 12, and gas is flowed upwards through
Floating filler 11 (polypropylene hollow ball) effect with via ammoniacal liquor inlet 14 input deposed ammonia (ammonia concn is 25%,
Relative to every cubic metre power boiler flue gas, the consumption of deposed ammonia is 1 liter) counter current contacting, mass transfer reaction is carried out, tail gas passes through tail
Gas outlet 13 enters tail gas washer 2 with gas inlet 21 by the road, and ammonium bicarbonate aqueous solution (concentration is 20g/L) is through bicarbonate
Transport to carbon ammonium booster 3 aqueous ammonium outlet 15.
In tail gas washer, the washings (desalted water) entered using scrubbed water inlet 22 are cleaned to tail gas,
Tail gas after cleaning is discharged into air by exhaust port 23, NH in the tail gas after cleaning3Content is less than 18mg/Nm3, CO2
Content is less than 3%.
The ammonium bicarbonate aqueous solution of carbon dioxide absorption tower generation boosts to 3.0MPa, via carbonic acid through carbon ammonium booster 3
Hydrogen ammonium pipeline 8 presses first ammonium converter 5 in entering, with (the gaseous mixture containing ammonia of gaseous mixture containing ammonia from urea rectifying column 7 at 25 DEG C
Pressure first ammonium converter in being entered by ammonia pipeline 9 and ammonia entrance 52) contact conversion reaction is carried out, press first ammonium molten in generation
Liquid；Then first ammonium salt solution will be pressed therefrom to press first ammonium salt solution to export 53 outputs in gained to pressurize through urea plant mesohigh first ammonium pump 6,
Urea Conversion System generation urea is returned, processing procedure is completed.
Embodiment 3
Power boiler flue gas (CO in urea plant after active carbon method desulfurization25%) it, is 20 in temperature that content is
DEG C, pressure is enters carbon dioxide absorption tower 1 under 1.5MPa through hydrojet pump 4 and exhaust gas entrance 12, and gas flows up logical
Cross floating filler 11 (polypropylene hollow ball) effect with via ammoniacal liquor inlet 14 input deposed ammonia (ammonia concn is 5%,
Relative to every cubic metre power boiler flue gas, the consumption of deposed ammonia is 5 liters) counter current contacting, mass transfer reaction is carried out, tail gas passes through tail
Gas outlet 13 enters tail gas washer 2 with gas inlet 21 by the road, and ammonium bicarbonate aqueous solution (concentration is 40g/L) is through bicarbonate
Transport to carbon ammonium booster 3 aqueous ammonium outlet 15.
In tail gas washer, the washings (desalted water) entered using scrubbed water inlet 22 are cleaned to tail gas,
Tail gas after cleaning is discharged into air by exhaust port 23, NH in the tail gas after cleaning3Content is less than 18mg/Nm3, CO2
Content is less than 3%.
The ammonium bicarbonate aqueous solution of carbon dioxide absorption tower generation boosts to 1.7MPa, via carbonic acid through carbon ammonium booster 3
Hydrogen ammonium pipeline 8 presses first ammonium converter 5 in entering, with (the gaseous mixture containing ammonia of gaseous mixture containing ammonia from urea rectifying column 7 at 25 DEG C
Pressure first ammonium converter in being entered by ammonia pipeline 9 and ammonia entrance 52) contact conversion reaction is carried out, press first ammonium molten in generation
Liquid；Then first ammonium salt solution will be pressed therefrom to press first ammonium salt solution to export 53 outputs in gained to pressurize through urea plant mesohigh first ammonium pump 6,
Urea Conversion System generation urea is returned, processing procedure is completed.
Although above the present invention is described in detail with a general description of the specific embodiments,
On the basis of the present invention, it can be made some modifications or improvements, this will be apparent to those skilled in the art.Cause
This, these modifications or improvements, belong to the scope of protection of present invention without departing from theon the basis of the spirit of the present invention.
Claims (2)
1. a kind of industrial waste gas processing system, it is characterised in that including：
Carbon dioxide absorption tower (1), tail gas washer (2), carbon ammonium booster (3), hydrojet pump (4), middle pressure first ammonium conversion
Device (5)；
Wherein, be provided with the carbon dioxide absorption tower (1) floating filler (11), exhaust gas entrance (12), offgas outlet (13),
Ammoniacal liquor inlet (14), ammonium bicarbonate aqueous solution outlet (15), wherein, the floating filler (11) is Nonmetallic hollow sphere or reality
Bulbus cordis；
The exhaust gas entrance (12) is arranged at the bottom of carbon dioxide absorption tower (1), and ammoniacal liquor inlet (14) is arranged at titanium dioxide
The top of carbon absorption tower (1), offgas outlet (13) is arranged at the top of carbon dioxide absorption tower (1) and by pipeline with being arranged at
Gas inlet (21) connection of tail gas washer (2) bottom；Washing water inlet is additionally provided with the tail gas washer (2)
(22), exhaust port (23) and valve plate (24)；
Medium pressure first ammonium converter (5) top be provided with ammonium hydrogen carbonate entrance (51), bottom be provided with ammonia entrance (52), in
Press first ammonium salt solution outlet (53)；
The ammonium bicarbonate aqueous solution outlet (15) is connected with carbon ammonium booster (3), and the other end of the carbon ammonium booster (3) leads to
Percarbonic acid hydrogen ammonium pipeline (8) is connected with ammonium hydrogen carbonate entrance (51)；
The system also includes high pressure carbamate pump (6), the high pressure carbamate pump (6) being connected with middle pressure first ammonium salt solution outlet (53)
The other end be connected with Urea Conversion System.
2. system according to claim 1, it is characterised in that the ammonia entrance (52) passes through ammonia pipeline (9) and urine
Plain rectifying column (7) connection.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201510250717.6A CN104925809B (en) | 2015-05-15 | 2015-05-15 | A kind of method and system that carbon dioxide is reclaimed from industrial waste gas |
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| CN201510250717.6A CN104925809B (en) | 2015-05-15 | 2015-05-15 | A kind of method and system that carbon dioxide is reclaimed from industrial waste gas |
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| CN104925809A CN104925809A (en) | 2015-09-23 |
| CN104925809B true CN104925809B (en) | 2017-07-11 |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108821288B (en) * | 2018-07-03 | 2020-08-07 | 杭州快凯高效节能新技术有限公司 | Preparation device and preparation process for producing high-quality liquid carbon dioxide |
| CN109665976B (en) * | 2018-11-15 | 2021-10-19 | 锦西天然气化工有限责任公司 | Ammonia process for recovering CO in flue gas2Process for combined production with urea |
| CN114984733A (en) * | 2022-05-10 | 2022-09-02 | 成都虹波钼业有限责任公司 | Method for treating mixed gas containing carbon dioxide and ammonia |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1061591A (en) * | 1990-11-22 | 1992-06-03 | 李雪波 | Process for producing urea |
| CN201168539Y (en) * | 2008-03-31 | 2008-12-24 | 郑州大学 | Carbon dioxide gas separating and gathering apparatus |
| CN101624355A (en) * | 2009-08-10 | 2010-01-13 | 四川金圣赛瑞化工有限责任公司 | Medium-pressure recovery process of low steam/carbon ratio-three-section adsorption-evaporative ammonia-cooling carbamide production |
| CN101830483A (en) * | 2010-03-10 | 2010-09-15 | 厦门市威士邦膜科技有限公司 | Production method for synthesizing ammonium bicarbonate fertilizer by using CO2 waste gas |
-
2015
- 2015-05-15 CN CN201510250717.6A patent/CN104925809B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1061591A (en) * | 1990-11-22 | 1992-06-03 | 李雪波 | Process for producing urea |
| CN201168539Y (en) * | 2008-03-31 | 2008-12-24 | 郑州大学 | Carbon dioxide gas separating and gathering apparatus |
| CN101624355A (en) * | 2009-08-10 | 2010-01-13 | 四川金圣赛瑞化工有限责任公司 | Medium-pressure recovery process of low steam/carbon ratio-three-section adsorption-evaporative ammonia-cooling carbamide production |
| CN101830483A (en) * | 2010-03-10 | 2010-09-15 | 厦门市威士邦膜科技有限公司 | Production method for synthesizing ammonium bicarbonate fertilizer by using CO2 waste gas |
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