CN1124230A - Producing method for synthetic ammonia - Google Patents
Producing method for synthetic ammonia Download PDFInfo
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- CN1124230A CN1124230A CN 95112804 CN95112804A CN1124230A CN 1124230 A CN1124230 A CN 1124230A CN 95112804 CN95112804 CN 95112804 CN 95112804 A CN95112804 A CN 95112804A CN 1124230 A CN1124230 A CN 1124230A
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Abstract
The invented method makes the prepared mixed gas undergo the processes of sweetening, carbon monoxide transformation and deprivation of CO2, then refining to obtain H2 and N2, making synthetic ammonia and entering the liquid ammonia storage tank. The gas in the liquid ammonia storage tank is directly added to the procedure of making up ammonia of the absorption liquid of the refining process to separate and send out the residual gas. the absorption liquid firstly absorbs CO, CO2, and H2S and separates them, then conducts water cooling, it would be better to make the gas of liquid ammonia storage tank be fed in the water-cooled absorption liquid to make up ammonia, then the absorptionliquid is sent to absorption tower for circulation application after buffering, recooling by water, ammonia cooling and booster. The ammonia recovery rate of the liquid ammonia storage tank gas up to 96% odd.
Description
The present invention relates in a kind of production method of synthetic ammonia, particularly production of synthetic ammonia, refining procedure and anhydrous ammonia tank gas utilize improving one's methods of operation again.
The production method of existing synthetic ammonia, the mixed gas for preparing hydrogen and nitrogen earlier, then with its processing of carrying out desulfurization, carbon monodixe conversion, sloughing carbonic acid gas, absorb remaining carbon monoxide, carbonic acid gas and hydrogen sulfide through refining procedure again, the purified hydrogen that obtains and nitrogen synthesized make synthetic ammonia, enter anhydrous ammonia tank, the part ammonia that accompanies in the anhydrous ammonia tank gas of emitting when anhydrous ammonia tank gas recovery process reduces pressure anhydrous ammonia tank again reclaims, and isolates remaining gas and sends and make fuel.Wherein, it is that absorption liquid is after the refining absorption tower absorbs remaining carbon monoxide, carbonic acid gas and hydrogen sulfide reaction that the refining procedure absorption liquid recycles process, enter the regenerator column Reaction Separation of heating through decompression and go out carbon monoxide, carbonic acid gas, ammonia and aqueous vapor, cool off through water cooler again, in addition liquefied ammonia is transformed into ammonia through the metering of liquid ammonia bottle, charge in the absorption liquid in the water cooler, make the total ammonia content of absorption liquid remain on 7-11 moles every liter, pass through the cold cooling of ammonia again, be pressurized to 13-15 megapascal (MPa)s and enter the refining absorption tower and recycle.And anhydrous ammonia tank gas recovery process is the isobaric ammonia of inhaling of anhydrous ammonia tank gas water of emitting when anhydrous ammonia tank is reduced pressure, and isolated gas is sent and made fuel, with the ammoniacal liquor that obtains adopt the method for steam ammonia still process reclaim liquefied ammonia.The problem that prior art exists is: refining procedure must be transformed into ammonia with liquefied ammonia, ammoniated process is intermittent, it is unstable that ammonia reacts in non-pressurized water cooler, cause total ammonia content to be difficult to stablize, inhale the ammonia process and in water cooler, carry out, so water cooler damages easily, the consumption of product liquefied ammonia is big,, one ton of liquefied ammonia of every production, refining procedure will consume about 25 kilograms in liquefied ammonia.Moreover anhydrous ammonia tank gas recovery process reclaims the complex procedures of ammonia, the energy expenditure height, and one ton of liquefied ammonia of every recovery need consume seven tons of left and right sides steam, and the rate of recovery is low, has only about 60-80%.
The objective of the invention is at the deficiencies in the prior art, proposed a kind ofly can fully reclaim the ammonia that the anhydrous ammonia tank band of gas goes out, reduce the ammonia loss of refining procedure in the production of synthetic ammonia, solve the production method of the synthetic ammonia of perishable problem of water cooler and the total ammonia content of stable absorption liquid.
Task of the present invention is to realize like this, the present invention is a kind of production method of synthetic ammonia, earlier the hydrogen of preparation and the mixed gas of nitrogen are carried out desulfurization, carbon monodixe conversion, slough the processing of carbonic acid gas, absorb remaining carbon monoxide through refining procedure again, carbonic acid gas and hydrogen sulfide, the purified hydrogen that obtains and nitrogen synthesized make synthetic ammonia, enter anhydrous ammonia tank, the part ammonia that accompanies in the anhydrous ammonia tank gas of emitting when again anhydrous ammonia tank being reduced pressure reclaims, isolating remaining gas sends and makes fuel, wherein, the absorption liquid of refining procedure makes its total ammonia content remain on 7-11 moles every liter by replenishing ammonia in recycling process, characteristics of the present invention are the anhydrous ammonia tank gas of emitting when anhydrous ammonia tank is reduced pressure adds the refining procedure absorption liquid by the device that can inhale ammonia the processes that recycle, directly replenish ammonia, isolate remaining gas and send and make fuel to absorption liquid.Like this, refining procedure need not consume liquefied ammonia, does not need liquefied ammonia is transformed into the device of ammonia yet, and ammoniated process is continual and steady, and ammonia is stable reaction in the device that can inhale ammonia, and total ammonia content is also stable in the absorption liquid, does not inhale ammonia react in the water cooler and is not easy to damage; Cancel the complicated procedures of forming of anhydrous ammonia tank gas recovery process recovery ammonia again, reduced energy expenditure, improved the liquefied ammonia rate of recovery of anhydrous ammonia tank gas.
The production method of described synthetic ammonia, it is to absorb remaining carbon monoxide with absorption liquid through the refining absorption tower that the refining procedure absorption liquid recycles process, after carbonic acid gas and the hydrogen sulfide reaction, enter the regenerator column Reaction Separation of heating through decompression and go out carbon monoxide, carbonic acid gas, ammonia and aqueous vapor, again through water-cooled cooling, replenish ammonia, again through the cold cooling of ammonia, be pressurized to 13-15 megapascal (MPa)s, entering the refining absorption tower recycles, must elimination precipitate before entering the refining absorption tower, after being characterized in being preferably in refining procedure absorption liquid water-cooled cooling, drawing the absorption liquid supercharging enters in the device that can inhale ammonia, the anhydrous ammonia tank gas of emitting when anhydrous ammonia tank is reduced pressure also feeds the device that can inhale ammonia absorption liquid is mended ammonia, mend absorption liquid behind the ammonia and carry out water-cooled cooling again send into the cold stage of ammonia after buffering, the isolated gas of device that can inhale ammonia is sent and is made fuel.Can reduce the energy waste in the Ammonia Production, make operation rationally simple again.
The production method of described synthetic ammonia is characterized in that the device that can inhale ammonia preferably adopts the pressure-bearing limit to be not less than the ammonia absorption tower of 1.5 megapascal (MPa)s.It is more abundant to make absorption liquid inhale ammonia, can improve the rate of recovery of ammonia in the anhydrous ammonia tank gas.
The present invention compared with prior art, owing to taked to replenish to absorption liquid at refining procedure the production method of the synthetic ammonia of ammonia with anhydrous ammonia tank gas, refining procedure need not consume liquefied ammonia, does not need liquefied ammonia is transformed into ammonia process and device yet, and ammoniated process is continual and steady, ammonia is stable reaction in the device that can inhale ammonia, total ammonia content is stable in the absorption liquid, and water cooler is not easy to damage, and the life-span prolongs, one ton of synthetic ammonia of every production, refining procedure are just saved about 25 kilograms in liquefied ammonia.Because of having cancelled the complicated procedures of forming of anhydrous ammonia tank gas recovery process recovery ammonia, reduced energy expenditure again, one ton of synthetic ammonia of every recovery can be saved about seven tons of steams, and the rate of recovery is brought up to more than 96%.Solved refining procedure ammonia consumption height in production of synthetic ammonia for a long time, the total ammonia content instability of absorption liquid, water cooler damages this technical barrier easily.Simplified whole production technology.
Fig. 1 is a process flow diagram of the present invention.
Fig. 2 is for replenishing the process schematic representation of ammonia to the absorption liquid that recycles in the refining procedure of prior art.
Fig. 3 replenishes the process schematic representation of ammonia to the absorption liquid that recycles at refining procedure with anhydrous ammonia tank gas for the present invention.
Among Fig. 2, it is that absorption liquid absorbs remaining carbon monoxide through the refining absorption tower that the refining procedure absorption liquid recycles process, after carbonic acid gas and the hydrogen sulfide reaction, decompression enters the regenerator column Reaction Separation of heating and goes out carbon monoxide, carbonic acid gas, ammonia and aqueous vapor, cool off through water cooler again, with liquefied ammonia after the metering of liquid ammonia bottle flashes to ammonia, in 0.08 megapascal (MPa), under 40-45 ℃ the processing condition, charge into the water cooler middle part successively and replenish ammonia to absorption liquid, make the total ammonia content of absorption liquid remain on every liter of 7-11 mole, it is cold to pass through ammonia again, is pressed into the refining absorption tower with topping-up pump, advances elimination precipitation before the refining absorption tower.Inhale ammonia process discontinuous carrying out in water cooler, reaction is unstable, is easy to damage water cooler, and total ammonia content of absorption liquid is also unstable.
Contrast Fig. 1, Fig. 3 below and further describe technology contents of the present invention.Fig. 1, Fig. 3 are used to produce per year the embodiment of 30,000 tons of ammonia synthesis process flow processs for the production method of synthetic ammonia of the present invention.The mixed gas for preparing hydrogen and nitrogen earlier, then with its processing of carrying out desulfurization, carbon monodixe conversion, sloughing carbonic acid gas, do the absorption liquid reaction at refining procedure with cuprammonia again and remove remaining carbon monoxide, carbonic acid gas and hydrogen sulfide, purified hydrogen that obtains and nitrogen, synthesize and make synthetic ammonia, enter anhydrous ammonia tank, the content of ammonia is higher in the anhydrous ammonia tank gas of emitting during the anhydrous ammonia tank decompression, and its composition is: hydrogen: 22-25%; Nitrogen: 8-12%; Methane: 10-14%; Ammonia: 45-51%; Argon gas: 1.5-2.5%.One ton of synthetic ammonia of every production will produce anhydrous ammonia tank gas 65-70 standard cubic meter, amount to and take 25.8 kilograms in liquefied ammonia out of, and this ammonia is reclaimed, and can satisfy the requirement of cuprammonia ammonification.The absorption liquid of refining procedure is a cuprammonia, it is to enter the remaining carbon monoxide of absorption in the refining absorption tower after cuprammonia is forced into 13-15 megapascal (MPa)s with topping-up pump that cuprammonia recycles process, carbonic acid gas and hydrogen sulfide, after the reaction, enter the regenerator column Reaction Separation of heating through decompression and go out carbon monoxide, carbonic acid gas, ammonia and aqueous vapor, cool off through water cooler again, by replenishing ammonia its total ammonia content is remained in 7-11 moles every liter the scope in the water cooler stage, pass through the cold cooling of ammonia again, be forced into topping-up pump and enter the refining absorption tower after 13-15 megapascal (MPa)s and recycle.Advance before the refining absorption tower, must remove copper sulfide precipitation.The pressure-bearing limit on refining absorption tower is not less than 15 megapascal (MPa)s.In the present embodiment, drawing temperature in water cooler outlet is 40-45 ℃ cuprammonia, flow is per hour 4.6 cubic metres, account for 1/4th of global cycle amount, be pressurized to 1.9-2.0 megapascal (MPa)s through topping-up pump and send into top, ammonia absorption tower, flow from the top down, the anhydrous ammonia tank gas of emitting when anhydrous ammonia tank is reduced pressure feeds the ammonia absorption tower, the anhydrous ammonia tank airshed is 280 standard cubic meter per hour, and pressure is about 1.5 megapascal (MPa)s, and ammonia absorption tower tower diameter is 0.6 meter, highly be 15.1 meters, in adorn 10 meters high polypropylene Pall ring fillers, ammonia basin atmospheric pressure is near 1.5 megapascal (MPa)s in the tower, the pressure-bearing limit on this ammonia absorption tower is not less than 2 megapascal (MPa)s.Cuprammonia is after packing layer and the anhydrous ammonia tank circulation of vital energy in the wrong direction stream contact absorption ammonia, the CAA liquid temp is elevated to 65-70 ℃, total ammonia content rises to 11.3 moles every liter from 8.2 moles every liter, enter surge tank under the effect of the cuprammonia 1.5 megapascal (MPa) left and right sides pressure in the ammonia absorption tower behind the benefit ammonia, after buffering, entering water cooler from the water cooler inlet again under the effect of liquid level difference cools off, enter the cold process of ammonia again, ammonia is inhaled in part recirculation, and total ammonia content of cuprammonia can remain in 8-9 moles every liter the scope like this.After anhydrous ammonia tank gas cuprammonia in the ammonia absorption tower is inhaled ammonia, separated sending, ammonia content is reduced to about 1.5-2% from 50.03-50.1% in the gas of sending.Is about 1.5 megapascal (MPa)s because of inhaling the ammonia process at air pressure, and temperature is to carry out under 40-70 ℃ the processing condition, and the ammonia dividing potential drop is 0.7-0.8 megapascal (MPa), the specific absorption height of ammonia, total ammonia content is stable, and the ammonia absorption tower reaction outside water cooler can not damage water cooler.In the present embodiment, the rate of recovery of ammonia reaches 97.4%, per hour reclaims 104 kilograms of synthetic ammonia.In 1 year, refining procedure is saved 750 tons in liquefied ammonia, amounts to 1,500,000 yuan of Renminbi.
Claims (3)
1, a kind of production method of synthetic ammonia, earlier the hydrogen of preparation and the mixed gas of nitrogen are carried out desulfurization, carbon monodixe conversion, slough the processing of carbonic acid gas, absorb remaining carbon monoxide through refining procedure again, carbonic acid gas and hydrogen sulfide, the purified hydrogen that obtains and nitrogen synthesized make synthetic ammonia, enter anhydrous ammonia tank, the part ammonia that accompanies in the anhydrous ammonia tank gas of emitting when again anhydrous ammonia tank being reduced pressure reclaims, isolating remaining gas sends and makes fuel, wherein, the absorption liquid of refining procedure makes its total ammonia content remain on 7-11 moles every liter by replenishing ammonia in recycling process, the invention is characterized in that the anhydrous ammonia tank gas of emitting when anhydrous ammonia tank reduced pressure adds the process that recycles of refining procedure absorption liquid by the device that can inhale ammonia, directly replenish ammonia, isolate remaining gas and send and make fuel to absorption liquid.
2, the production method of synthetic ammonia according to claim 1, it is to absorb remaining carbon monoxide with absorption liquid through the refining absorption tower that the refining procedure absorption liquid recycles process, after carbonic acid gas and the hydrogen sulfide reaction, enter the regenerator column Reaction Separation of heating through decompression and go out carbon monoxide, carbonic acid gas, ammonia and aqueous vapor, again through water-cooled cooling, replenish ammonia, again through the cold cooling of ammonia, be pressurized to 13-15 megapascal (MPa)s, entering the refining absorption tower recycles, must elimination precipitate before entering the refining absorption tower, after it is characterized in that being preferably in refining procedure absorption liquid water-cooled cooling, drawing the absorption liquid supercharging enters in the device that can inhale ammonia, the anhydrous ammonia tank gas of emitting when anhydrous ammonia tank is reduced pressure also feeds the device that can inhale ammonia absorption liquid is mended ammonia, the absorption liquid of mending behind the ammonia is sent into the cold stage of ammonia from carrying out water-cooled cooling again after cushioning, the isolated gas of device that can inhale ammonia is sent and made fuel.
3,, it is characterized in that the device that can inhale ammonia preferably adopts the pressure-bearing limit to be not less than the ammonia absorption tower of 1.5 megapascal (MPa)s according to the production method of claim 1 and 2 described synthetic ammonia.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95112804A CN1039700C (en) | 1995-12-05 | 1995-12-05 | Producing method for synthetic ammonia |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95112804A CN1039700C (en) | 1995-12-05 | 1995-12-05 | Producing method for synthetic ammonia |
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| Publication Number | Publication Date |
|---|---|
| CN1124230A true CN1124230A (en) | 1996-06-12 |
| CN1039700C CN1039700C (en) | 1998-09-09 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN95112804A Expired - Lifetime CN1039700C (en) | 1995-12-05 | 1995-12-05 | Producing method for synthetic ammonia |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1084297C (en) * | 1996-11-22 | 2002-05-08 | 湖南安淳节能技术有限公司 | Flow dividing process for ammonia or alcohol synthesis reaction system |
| WO2008022529A1 (en) * | 2006-08-16 | 2008-02-28 | Wuhan Hc Semitek Co., Ltd. | Synthesis method of high purity ammonia |
| CN100465094C (en) * | 2007-01-27 | 2009-03-04 | 营口三征有机化工股份有限公司 | Method of synthesizing ammonia by hydrogen gas purified by tail gas of sodium cyanide and alkali-chloride production |
| CN102101643A (en) * | 2010-12-20 | 2011-06-22 | 昆明理工大学 | Method for preparing ammonia synthesis gas from oxygen-enriched blast furnace gas |
| CN102593824A (en) * | 2012-02-17 | 2012-07-18 | 贵州兴化化工股份有限公司 | Power control system |
| CN103501877A (en) * | 2011-03-29 | 2014-01-08 | 赫多特普索化工设备公司 | Method for the purification of raw gas |
-
1995
- 1995-12-05 CN CN95112804A patent/CN1039700C/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1084297C (en) * | 1996-11-22 | 2002-05-08 | 湖南安淳节能技术有限公司 | Flow dividing process for ammonia or alcohol synthesis reaction system |
| WO2008022529A1 (en) * | 2006-08-16 | 2008-02-28 | Wuhan Hc Semitek Co., Ltd. | Synthesis method of high purity ammonia |
| CN100465094C (en) * | 2007-01-27 | 2009-03-04 | 营口三征有机化工股份有限公司 | Method of synthesizing ammonia by hydrogen gas purified by tail gas of sodium cyanide and alkali-chloride production |
| CN102101643A (en) * | 2010-12-20 | 2011-06-22 | 昆明理工大学 | Method for preparing ammonia synthesis gas from oxygen-enriched blast furnace gas |
| CN102101643B (en) * | 2010-12-20 | 2013-11-27 | 昆明理工大学 | Method for preparing ammonia synthesis gas from oxygen-enriched blast furnace gas |
| CN103501877A (en) * | 2011-03-29 | 2014-01-08 | 赫多特普索化工设备公司 | Method for the purification of raw gas |
| CN102593824A (en) * | 2012-02-17 | 2012-07-18 | 贵州兴化化工股份有限公司 | Power control system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1039700C (en) | 1998-09-09 |
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Owner name: DEBANG CHEMICAL INDUSTRY GROUP CO. LTD., JIANGSU Free format text: FORMER NAME OR ADDRESS: LIANYUNGANG CHEMICAL FERTILIZER FACTORY |
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Address after: Jiangsu city of Lianyungang province Haizhou Jiang Hua Lu Patentee after: Debang Chemical Industry Group Co., Ltd., Jiangsu Address before: East Gate, Haizhou, Lianyungang, Jiangsu Patentee before: Lianyungang Chemical Fertilizer Factory |
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Granted publication date: 19980909 |
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