CN103936030A - Aqua ammonia refining concentration method - Google Patents
Aqua ammonia refining concentration method Download PDFInfo
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- CN103936030A CN103936030A CN201310291219.7A CN201310291219A CN103936030A CN 103936030 A CN103936030 A CN 103936030A CN 201310291219 A CN201310291219 A CN 201310291219A CN 103936030 A CN103936030 A CN 103936030A
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- Prior art keywords
- aqua ammonia
- ammoniacal liquor
- ammonia
- refining
- concentration method
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Abstract
The invention discloses an aqua ammonia refining concentration method. Aqua ammonia is sent to an aqua ammonia refining tank pipeline, and then the aqua ammonia is sent to a semi-removal pipeline after the aqua ammonia concentration is improved. The method can be applied to the technical field of urea production. The aqua ammonia refining concentration method provided by the invention can reasonably utilize a conventional device, performs refining concentration operation on aqua ammonia to the largest degree, and can achieve maximization of resource utilization. The aqua ammonia refining concentration method provided by the invention can effectively reduce the semi-removal aqua ammonia amount, and is reasonable in operation steps and easy to implement.
Description
Technical field
The present invention relates to Technology for Urea Production field, especially a kind of ammoniacal liquor refining concentrating method.
Background technology
At present, along with scientific and technical development, in increasing technical field, be applied to this operation of ammoniacal liquor refining concentrate.In existing technology, main by realizing below the operation of ammoniacal liquor refining concentrate: according to ammonia different solubility at different pressures and temperature, will to divide the weak ammonia in post from film, use the means of rectifying, use steam heating weak ammonia, ammonia is overflowed, control temperature well, thus concentrate weak ammonia; Produce the qualified gas ammonia (ammonia content reaches more than 97%) for salt made from earth containing a comparatively high percentage of sodium chloride production, reclaim soft water simultaneously; Alleviate the too much difficulty of carbonization weak ammonia amount, reduce the discharge of weak ammonia, turn waste into wealth, improve the utilization ratio of ammonia.
The principle of work of existing ammoniacal liquor refining concentrate is as follows: level off to 0 according to ammonia solubleness under certain pressure and certain temperature, adopt the method for rectifying that ammonia is effectively separated with water, the content of Ammonia In Aqueous Solution reaches minimum, thereby produces the gas ammonia that purity is high.System pressure is at 0.28～0.30MPa, temperature is under 135～140 DEG C of conditions, ammonia and water become gaseous state, after each section of cooling and overhead condenser cooling through rectifying tower, make water vapor liquefy and ammonia still exists with gaseous form, and control condensator outlet temperature below 35 DEG C, make Ammonia solubility level off to 0, and ammonia is sent to the use of ammonium nitrate post with the form of gas ammonia.
The algorithm of existing ammoniacal liquor refining concentrate is as follows: the weak ammonia that film is assigned to is respectively from one of rectifying, two packing section tops enter, through sparger be uniformly distributed by after heat up for the first time by the ammonia on ripple packing and bottom and water vapor contact heat-exchanging, then arrive the liquid storing section of rectifying section, communicating pipe by rectifying tower and reboiler arrives reboiler, during by reboiler tubulation by outer steam heating to 135～140 DEG C of tubulation, ammonia and water enter the empty liquid Duan Shiyu weak ammonia heat exchange of rectifying section liquid storing section top with the form of gaseous state from the outlet of reboiler and cool to 86～90 DEG C, then enter one section of ripple packing bottom, rise process in one, the weak ammonia heat exchange of getting off in two sections of top is reduced to 53～55 DEG C, then enter two sections of ripple packing bottoms, in two sections of ripple packings, continuing heat exchange with weak ammonia cools to after 45～47 DEG C, enter in overhead condenser tubulation and be cooled to 30～35 DEG C by the outer cooling circulating water of pipe, finally enter gas-liquid separator, liquid return to rectifying tower as phegma.Gas ammonia is sent to ammonium nitrate post and is used from gas-liquid separator top.At the bottom of rectifying tower, still raffinate (ammonia content≤0.95%) goes synthetic workshop circulating water system to do its make up water use.Saturation steam enter between reboiler tubulation with pipe in weak ammonia heat exchange, water of condensation is to the steam condensate house steward in pressurization nitric acid post.From the recirculated water of supply mains on cold water pump recirculated water enter between overhead condenser tubulation with tubulation in ammonia and water vapor heat exchange, then get back to recirculated water return main.Existing ammoniacal liquor refining concentrate operation is comparatively complicated, can not effectively promote and apply.
Summary of the invention
The technical problem that the present invention solves is to provide a kind of ammoniacal liquor refining concentrating method, can reasonably utilize existing apparatus, to carrying out the operation of ammoniacal liquor refining concentrate, can realize the utilization of resources and maximize to greatest extent.
For solving the problems of the technologies described above, the invention provides a kind of ammoniacal liquor refining concentrating method, it is characterized in that, first ammoniacal liquor is delivered to refined ammonia barrel road, provide and deliver to half de-pipeline after ammonia concn.
Above-mentioned a kind of ammoniacal liquor refining concentrating method also can have following features: described ammoniacal liquor is delivered to and connected film after described half de-pipeline and carry hydrogen production device.
Above-mentioned a kind of ammoniacal liquor refining concentrating method also can have following features: described ammoniacal liquor is ice maker ammoniacal liquor.
Such scheme of the present invention has following beneficial effect:
1, a kind of ammoniacal liquor refining concentrating method provided by the invention, can reasonably utilize existing apparatus, to carrying out the operation of ammoniacal liquor refining concentrate, can realize the utilization of resources and maximize to greatest extent.
2, a kind of ammoniacal liquor refining concentrating method provided by the invention, can effectively reduce by the half deamination water yield, and operation steps is reasonable, easy to implement.
Embodiment
For the ease of setting forth the present invention, below with reference to specific embodiment, the enforcement of technical solution of the present invention is described in further detail.
The embodiment of the present invention provides a kind of ammoniacal liquor refining concentrating method, it is characterized in that, first ammoniacal liquor is delivered to refined ammonia barrel road, provides and delivers to half de-pipeline after ammonia concn.
Preferably, the embodiment of the present invention also can have following features: ammoniacal liquor is delivered to and connected film after half de-pipeline and carry hydrogen production device.
Preferably, the embodiment of the present invention also can have following features: ammoniacal liquor is ice maker ammoniacal liquor.
Although the disclosed embodiment of the present invention as above, the embodiment that described content just adopts for the ease of understanding the present invention, not in order to limit the present invention.Any those skilled in the art of the present invention; under the prerequisite of scope that does not depart from the disclosed spirit of the present invention; can make any modifications and variations what implement in form and in details; but scope of patent protection of the present invention, still must be as the criterion with the scope that appending claims was defined.
Claims (3)
1. an ammoniacal liquor refining concentrating method, is characterized in that, first ammoniacal liquor is delivered to refined ammonia barrel road, provides and delivers to half de-pipeline after ammonia concn.
2. ammoniacal liquor refining concentrating method as claimed in claim 1, is characterized in that, described ammoniacal liquor is delivered to and connected film after described half de-pipeline and carry hydrogen production device.
3. ammoniacal liquor refining concentrating method as claimed in claim 1 or 2, is characterized in that, described ammoniacal liquor is ice maker ammoniacal liquor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310291219.7A CN103936030A (en) | 2013-07-12 | 2013-07-12 | Aqua ammonia refining concentration method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310291219.7A CN103936030A (en) | 2013-07-12 | 2013-07-12 | Aqua ammonia refining concentration method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103936030A true CN103936030A (en) | 2014-07-23 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310291219.7A Pending CN103936030A (en) | 2013-07-12 | 2013-07-12 | Aqua ammonia refining concentration method |
Country Status (1)
| Country | Link |
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| CN (1) | CN103936030A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104591222A (en) * | 2015-01-13 | 2015-05-06 | 四川美丰化工股份有限公司 | Synthetic ammonia device ammonia hydroxide concentrating method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102153107A (en) * | 2010-11-29 | 2011-08-17 | 山东三和化工有限公司 | Process method for thickening thin ammonia water |
| CN202229520U (en) * | 2011-08-16 | 2012-05-23 | 贵州兴化化工股份有限公司 | Device used for cooling circulation system of ice maker |
| CN202912688U (en) * | 2012-11-19 | 2013-05-01 | 河南骏化发展股份有限公司 | Synthetic ammonia purge gas treatment system |
-
2013
- 2013-07-12 CN CN201310291219.7A patent/CN103936030A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102153107A (en) * | 2010-11-29 | 2011-08-17 | 山东三和化工有限公司 | Process method for thickening thin ammonia water |
| CN202229520U (en) * | 2011-08-16 | 2012-05-23 | 贵州兴化化工股份有限公司 | Device used for cooling circulation system of ice maker |
| CN202912688U (en) * | 2012-11-19 | 2013-05-01 | 河南骏化发展股份有限公司 | Synthetic ammonia purge gas treatment system |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104591222A (en) * | 2015-01-13 | 2015-05-06 | 四川美丰化工股份有限公司 | Synthetic ammonia device ammonia hydroxide concentrating method |
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| PB01 | Publication | ||
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| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20140723 |