CN101935056A - Ammonia separating process for ammonia synthesis - Google Patents
Ammonia separating process for ammonia synthesis Download PDFInfo
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- CN101935056A CN101935056A CN2010102863074A CN201010286307A CN101935056A CN 101935056 A CN101935056 A CN 101935056A CN 2010102863074 A CN2010102863074 A CN 2010102863074A CN 201010286307 A CN201010286307 A CN 201010286307A CN 101935056 A CN101935056 A CN 101935056A
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- ammonia
- absorption
- gas
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- refrigeration
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 415
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 210
- 238000000034 method Methods 0.000 title claims abstract description 48
- 230000008569 process Effects 0.000 title claims abstract description 37
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 21
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 21
- 238000010521 absorption reaction Methods 0.000 claims abstract description 46
- 238000005057 refrigeration Methods 0.000 claims abstract description 29
- 239000007789 gas Substances 0.000 claims description 52
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 18
- 238000005516 engineering process Methods 0.000 claims description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 239000001257 hydrogen Substances 0.000 claims description 9
- 229910052739 hydrogen Inorganic materials 0.000 claims description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 8
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 7
- 229910052708 sodium Inorganic materials 0.000 claims description 7
- 239000011734 sodium Substances 0.000 claims description 7
- 230000002745 absorbent Effects 0.000 claims description 5
- 239000002250 absorbent Substances 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 5
- 230000006835 compression Effects 0.000 claims description 4
- 238000007906 compression Methods 0.000 claims description 4
- 239000003507 refrigerant Substances 0.000 claims description 4
- 238000009834 vaporization Methods 0.000 claims description 4
- 230000008016 vaporization Effects 0.000 claims description 4
- 239000002925 low-level radioactive waste Substances 0.000 claims description 3
- 230000006837 decompression Effects 0.000 claims description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 4
- VGTPCRGMBIAPIM-UHFFFAOYSA-M sodium thiocyanate Chemical compound [Na+].[S-]C#N VGTPCRGMBIAPIM-UHFFFAOYSA-M 0.000 abstract description 3
- HAAFARYZKVVJHG-UHFFFAOYSA-M sodium azane thiocyanate Chemical compound N.[Na]SC#N HAAFARYZKVVJHG-UHFFFAOYSA-M 0.000 abstract 2
- 238000004134 energy conservation Methods 0.000 abstract 1
- 239000012808 vapor phase Substances 0.000 abstract 1
- 238000009833 condensation Methods 0.000 description 10
- 230000005494 condensation Effects 0.000 description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000003337 fertilizer Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- IIPYXGDZVMZOAP-UHFFFAOYSA-N lithium nitrate Chemical compound [Li+].[O-][N+]([O-])=O IIPYXGDZVMZOAP-UHFFFAOYSA-N 0.000 description 2
- 231100000572 poisoning Toxicity 0.000 description 2
- 230000000607 poisoning effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- ZVCDLGYNFYZZOK-UHFFFAOYSA-M sodium cyanate Chemical compound [Na]OC#N ZVCDLGYNFYZZOK-UHFFFAOYSA-M 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention relates to an ammonia separating process for ammonia synthesis, in particular to an absorption ammonia separating process. In the ammonia separating process, two units of absorption ammonia separating and absorption refrigeration are merged, wherein in the unit of the absorption ammonia separating, ammonia is absorbed and separated, and is desorbed and condensed to form liquid ammonia serving as a product; and in the unit of the absorption refrigeration, the refrigeration is performed by utilizing the absorption principle so as to provide refrigeration capacity for the absorption of the ammonia. The ammonia separating process is mainly characterized in that in the processes of the ammonia separating and the refrigeration, heat transfer and mass transfer are performed simultaneously, an absorption method is adopted, ammonia stilling equipment is shared, and absorption barren liquor is processed together; the heat of the ammonia stilling process is derived from low heat energy of ammonia synthesis gas; liquid ammonia serving as a cold source in the process of the refrigeration is one part of the liquid ammonia serving as the product, and an analyzer and a condenser are not needed to be arranged individually; and absorption working medium pairs adopted by the absorption ammonia separating and the absorption refrigeration are sodium thiocyanate-ammonia working medium pairs, sodium thiocyanate is not contained in a vapor phase, and ammonia is separated from sodium thiocyanate-ammonia solution easily. Compared with the conventional condensate ammonia separating, the ammonia separating process of the invention has the advantages that: the power dissipation of ice machines is replaced by the recovered low heat energy, and the effect of energy conservation is obvious.
Description
Technical field
The present invention relates to a kind of ammonia separating technology of ammonia synthesis, relate in particular to a kind of absorption minute ammonia process.
Background technology
By nitrogen hydrogen synthetic ammonia, owing to ammonia content in the gas after the building-up reactions is not high, generally have only 12%～22%, so need (mainly be nitrogen, hydrogen, ammonia from going out the tower synthetic gas, be called product gas at this) in ammonia is separated (normal be called for short " branch ammonia "), remaining nitrogen hydrogen (being called circulation gas) returns and recycles.Divide the method for ammonia to mainly contain condensation method and absorption process, all adopt condensation method at present basically.On the synthetic ammonia development history, once adopted absorption process, but because the absorption agent that is adopted is a water, be entrained with water in the circulation gas behind the branch ammonia, the poisoning of catalyst that can cause ammonia synthesis, and nitrogen and hydrogen can be soluble in water under the high pressure, cause the loss of nitrogen and hydrogen thus, therefore in large-scale ammonia synthesizing industry, absorb and divide the ammonia flow process to be eliminated, only be used for the little chemical fertilizer technology that some produce ammoniacal liquor.Though condensation divides ammonia to overcome problems such as poisoning of catalyst, must synthetic gas fully be lowered the temperature, need be in a large amount of refrigeration merit of the cold link consumption of ammonia.If working pressure reduces, condensation divides the difficulty of ammonia further to increase.Divide ammonia can be issued to separating effect preferably and absorb at lower pressure.
People such as Yang Jingchang are published in " chemical fertilizer industry " the 34th volume the 4th phase paper of 24～29 pages " the synthetic ammonia absorption extraction that low temperature exhaust heat drives and with the comparison of condensation separation " and have proposed to utilize the lithium nitrate absorption process to divide ammonia, from ammonia separating effect aspect and condensation method contrast, when working pressure is higher, two kinds of methods are suitable substantially, but when working pressure is reduced to 10MPa, the advantage of absorption process is very obvious, if working pressure further is reduced to 6Mpa, it is very difficult that condensation method becomes, and still realizes easily and absorb rule.From energy consumption, what condensation method consumed mainly is refrigeration merit, i.e. high-grade energy, and absorption process consumption mainly is low temperature heat energy, and this is very abundant in ammonia synthesis technology, and promptly absorption process has obvious power savings advantages, and along with the reduction of working pressure, its advantage is more outstanding.
Summary of the invention
The objective of the invention is to, a kind of absorption refrigeration is proposed and absorption minute ammonia bonded divides ammonia process, make full use of the waste heat of ammonia synthesis gas, performance absorb to divide outstanding advantage and the absorption refrigeration advantage of saving the high-quality energy of ammonia in low voltage operated, farthest realizes energy-saving and cost-reducing.
The technical scheme of the ammonia separating technology of ammonia synthesis of the present invention is: divide ammonia and two technique units of absorption refrigeration to merge into a unit flow process traditional absorption; Carry out entering ammonia still (1) heating working medium of this technology to rich solution after product gas after the ammonia synthesis reclaims through high-temperature residual heat, rich solution is heated back ammonia and flashes to gaseous ammonia and enter condenser (2) and be condensed into liquefied ammonia, a liquefied ammonia part is preserved as product, another part becomes gas ammonia to enter ammonia cooler (9) output cold as refrigerant through throttling valve (3) reduction vaporization, then enter resorber (5) and by working medium lean solution is absorbed, the working medium behind the absorption ammonia is delivered to ammonia still (1) heating ammonia still process to rich solution by recycle pump (6); The product gas that comes out from ammonia still (1) enters branch ammonia tower (4) and by working medium lean solution is absorbed wherein ammonia, and non-absorbent gas (mainly be nitrogen, hydrogen, be called circulation gas) enters loop compression workshop section to be continued to use; Cooling reduces temperature through ammonia cooler (10) to lean solution to be heated the working medium of having evaporated ammonia in ammonia still (1), a part is delivered to resorber (5) through variable valve (8) decompression and is absorbed gas ammonia from ammonia cooler (9), and another part is delivered to branch ammonia tower (4) by lean pump (7) and absorbed gas ammonia in the product gas;
The working pressure of described ammonia still, branch ammonia tower and resorber is respectively 1.5～3.5Mpa, 1.6～4.2Mpa and 0.2～0.8Mpa; The product atmospheric pressure that enters ammonia still is 1.7～4.3MPa, and temperature is 120～250 ℃, and tower exit temperature is 80～200 ℃, enters water cooler and reduces to 25～60 ℃.The lean solution temperature that goes out ammonia still is 60～150 ℃, is cooled to 25～60 ℃ through water cooler, is cooled to one 5～15 ℃ through ammonia cooler again.
The heat that consumes in absorption branch ammonia and the absorption refrigeration technology is from the low level waste heat of ammonia synthesis gas.
It is right to being Sodium Thiocyanate 99 one ammonia working medium to absorb the working medium of dividing ammonia and absorption refrigeration to adopt.
Low-temperature receiver liquefied ammonia in the process of refrigeration is taken from product liquefied ammonia.
The present invention divides ammonia and two technique unit flow processs of absorption refrigeration to merge into a unit flow process traditional absorption, provide required cold by absorption refrigeration for minute ammonia system, divide ammonia and the shared ammonia still of refrigeration, both there had been heat transfer process in the two, and mass transfer process is arranged again.Make full use of a large amount of technology tow taste heats simultaneously, this part heat is recycled water coolant with the form of used heat and takes away in traditional process, be dissipated in the environment.Idiographic flow is: carry out entering the ammonia still heating working medium to rich solution after process gas (product gas) after the ammonia synthesis reclaims through high-temperature residual heat, ammonia flashed to gaseous ammonia and enters condenser after rich solution was heated, gaseous ammonia promptly is condensed into liquefied ammonia, a liquefied ammonia part is preserved as product, another part becomes gas ammonia to enter ammonia cooler output cold as refrigerant through the throttling valve reduction vaporization, then enter resorber and by working medium lean solution is absorbed, the working medium behind the absorption ammonia is delivered to ammonia still heating ammonia still process to rich solution by recycle pump; The product gas that comes out from ammonia still enters branch ammonia tower and by working medium lean solution is absorbed wherein ammonia, and non-absorbent gas (circulation gas) enters loop compression workshop section to be continued to use; Cooling reduces temperature through ammonia cooler to lean solution to be heated the working medium of having evaporated ammonia in ammonia still, delivers to branch ammonia tower by lean pump and absorbs ammonia in the product gas, delivers to resorber and absorb and be used for cooled gas ammonia.
Absorb to divide the heat that consumes in ammonia and the absorption refrigeration all from the low level waste heat of ammonia synthesis gas in this technology.It is right to being sodium rhodanate-ammonia working medium to absorb the working medium of dividing ammonia and absorption refrigeration to adopt, this working medium centering Sodium Thiocyanate 99 is as solid solute, can not appear in the steam of solution, make the separation of ammonia more or less freely, be easier to avoid the Working medium pollution process gas that ammonia synthesis catalyst is poisoned yet.In addition, ammonia also as refrigeration agent, makes technological process obtain simplifying both as the product that divides ammonia.
This technology will absorb branch ammonia and combine with absorption refrigeration, and refrigeration and branch ammonia are the low temperature exhaust heat of consumable products gas except that the certain electric energy of pump consumption, and energy-saving effect is very outstanding.In addition, compare condensation and divide ammonia, ammonia still overhead condenser refrigerative is pure ammonia rather than circulation gas in the absorption branch ammonia flow process, and ammonia very easily liquefies, and condenser only need use recirculated water as low-temperature receiver, does not need the more low-temperature receiver of low temperature.The nitrogen hydrogen that accounts for product gas 78% no longer resembles condensation and divides in the ammonia process and together be cooled to-10 ℃ with ammonia, but is absorbed wherein gas ammonia by liquid scrubbing in the absorption tower, has saved a large amount of nitrogen hydrogen and has been cooled to-10 ℃ of required colds.
Description of drawings
Fig. 1 is that the embodiment of the invention absorbs branch ammonia and refrigerating schema.
Fig. 1 get the bid the note be respectively: the 1-ammonia still, the 2-condenser, 3-throttling valve, 4-divide the ammonia tower, 5-resorber, 6-recycle pump, 7-lean pump, 8-variable valve, 9-ammonia cooler, 10-water cooler, 11-water cooler.
Embodiment
The invention will be further described below in conjunction with embodiment.
Carry out process gas (product gas) after the ammonia synthesis through overexpansion acting, waste heat recovery, temperature is 180 ℃, pressure is 2.9Mpa, ammonia still 1 heating working medium that enters this technology is to rich solution, after rich solution is heated wherein ammonia flash to gas ammonia and enter condenser 2 and be condensed into liquefied ammonia, a liquefied ammonia part is preserved as product, and another part becomes gas ammonia to enter ammonia cooler 9 output colds as refrigerant through throttling valve 3 reduction vaporizations, cooling from the working medium of ammonia still to lean solution.Then gas ammonia enters resorber 5 and by working medium lean solution is absorbed, and the working medium that absorbs behind the ammonia is delivered to ammonia still 1 heating ammonia still process to rich solution by recycle pump 6.The product gas that comes out from ammonia still 1 at first enters water cooler 11 and reduces temperature, enters branch ammonia tower 4 again and by working medium lean solution is absorbed wherein ammonia, and non-absorbent gas (circulation gas) enters loop compression workshop section to be continued to use.In ammonia still 1, be heated the working medium of having evaporated ammonia lean solution is reduced temperature through water cooler 10, ammonia cooler 9 coolings, a part reduces pressure through variable valve 8 and delivers to the gas ammonia that resorber 5 absorbs from ammonia cooler 9, and another part is delivered to the gas ammonia that branch ammonia tower 4 absorbs in the product gas by lean pump 7.
The working pressure of above-mentioned ammonia still, branch ammonia tower and resorber is respectively 1.5～3.5Mpa, 1.6～4.2Mpa and 0.2～0.8Mpa; The product atmospheric pressure that enters ammonia still is 1.7～4.3MPa, and temperature is 120～250 ℃, and tower exit temperature is 80～200 ℃, enters water cooler and reduces to 25～60 ℃.The lean solution temperature that goes out ammonia still is 60～150 ℃, is cooled to 25～60 ℃ through water cooler, is cooled to-5～15 ℃ through ammonia cooler again.
Absorb and divide ammonia and absorption refrigeration all to adopt sodium rhodanate-ammonia working medium right.Sodium rhodanate-ammonia solution is dissolved in the liquefied ammonia by the solid sulfur Zassol and gets.Under identical temperature, the vapour pressure of sodium rhodanate-ammonia solution is lower, when temperature is 20 ℃, the molar content of ammonia is 71.3% o'clock in the solution, the vapour pressure of solution only is 86.13KPa, and the vapour pressure of pure ammonia is 858.79KPa then under uniform temp, differs about ten times, this shows that ammonia is absorbed agent sodium rhodanate-ammonia solution absorption easily, also embodies the refrigeration characteristic of sodium rhodanate-ammonia working medium to excellence.Because the crystallization concentration (the quality percentage composition of ammonia) of this solution is 32% under the normal temperature, so the starting point concentration of the absorbent solution that adopts is 35%～50%.
The main technologic parameters of present embodiment is as follows: the working pressure of ammonia still, branch ammonia tower and resorber is respectively 2.1Mpa, 2.8Mpa and 0.3Mpa.The product atmospheric pressure that enters ammonia still is 2.8MPa, and temperature is 180 ℃, and tower exit temperature is 90 ℃, enters water cooler and reduces to 40 ℃.The lean solution temperature that goes out ammonia still is 80 ℃, is cooled to 40 ℃ through water cooler, is cooled to 0 ℃ through ammonia cooler again.Ammonia content is 22.3% in the product gas, and ammonia content is 2.0% in the circulation gas after minute ammonia tower absorbs.
Claims (4)
1. the ammonia separating technology of an ammonia synthesis is characterized in that: divide ammonia and two technique units of absorption refrigeration to merge into a unit flow process traditional absorption; Carry out entering ammonia still (1) heating working medium of this technology to rich solution after product gas after the ammonia synthesis reclaims through high-temperature residual heat, rich solution is heated back ammonia and flashes to gaseous ammonia and enter condenser (2) and be condensed into liquefied ammonia, a liquefied ammonia part is preserved as product, another part becomes gas ammonia to enter ammonia cooler (9) output cold as refrigerant through throttling valve (3) reduction vaporization, then enter resorber (5) and by working medium lean solution is absorbed, the working medium behind the absorption ammonia is delivered to ammonia still (1) heating ammonia still process to rich solution by recycle pump (6); The product gas that comes out from ammonia still (1) enters branch ammonia tower (4) and by working medium lean solution is absorbed wherein ammonia, and non-absorbent gas (mainly be nitrogen, hydrogen, be called circulation gas) enters loop compression workshop section to be continued to use; Cooling reduces temperature through ammonia cooler (10) to lean solution to be heated the working medium of having evaporated ammonia in ammonia still (1), a part is delivered to resorber (5) through variable valve (8) decompression and is absorbed gas ammonia from ammonia cooler (9), and another part is delivered to branch ammonia tower (4) by lean pump (7) and absorbed gas ammonia in the product gas;
The working pressure of described ammonia still, branch ammonia tower and resorber is respectively 1.5～3.5Mpa, 1.6～4.2Mpa and 0.2～0.8Mpa; The product atmospheric pressure that enters ammonia still is 1.7～4.3MPa, and temperature is 120～250 ℃, and tower exit temperature is 80～200 ℃, enters water cooler and reduces to 25～60 ℃.The lean solution temperature that goes out ammonia still is 60～150 ℃, is cooled to 25～60 ℃ through water cooler, is cooled to-5～15 ℃ through ammonia cooler again.
2. the ammonia separating technology of ammonia synthesis according to claim 1 is characterized in that: absorb and divide the heat that consumes in ammonia and the absorption refrigeration technology low level waste heat from ammonia synthesis gas.
3. the ammonia separating technology of ammonia synthesis according to claim 1 is characterized in that: absorb and divide the working medium of ammonia and absorption refrigeration employing right to being sodium rhodanate-ammonia working medium.
4. the ammonia separating technology of ammonia synthesis according to claim 1, it is characterized in that: the low-temperature receiver liquefied ammonia in the process of refrigeration is taken from product liquefied ammonia.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102863074A CN101935056B (en) | 2010-09-19 | 2010-09-19 | Ammonia separating process for ammonia synthesis |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2010102863074A CN101935056B (en) | 2010-09-19 | 2010-09-19 | Ammonia separating process for ammonia synthesis |
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| Publication Number | Publication Date |
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| CN101935056A true CN101935056A (en) | 2011-01-05 |
| CN101935056B CN101935056B (en) | 2012-07-04 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102923733A (en) * | 2012-11-27 | 2013-02-13 | 天津衡创工大现代塔器技术有限公司 | Ammonia separation device and method |
| CN106766351A (en) * | 2017-01-18 | 2017-05-31 | 文安县天澜新能源有限公司 | A kind of method and apparatus for eliminating synthesis ammonia freezing post liquid ammonia storage tank emptying |
| CN109297255A (en) * | 2018-10-16 | 2019-02-01 | 安徽沃特普尔节能科技有限公司 | A kind of energy-saving gas ammonia compression process |
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|---|---|---|---|---|
| US4149857A (en) * | 1976-09-16 | 1979-04-17 | Veb Leuna-Werke "Walter Ulbricht" | Process for the two-stage separation of ammonia |
| CN1197763A (en) * | 1998-04-10 | 1998-11-04 | 刘金成 | Carbon dioxide eliminating technology used in ammonia synthesis and hydrogen production processes |
| JP2003251134A (en) * | 2002-03-06 | 2003-09-09 | Chubu Chemical Kk | Ammonia absorption apparatus and ammonia absorption method used for the same |
| CN1621763A (en) * | 2003-11-26 | 2005-06-01 | 吉林长山化肥集团长达有限公司机械厂 | Application of ammonia absorbing refrigeration in selexol decarbonization technique |
| CN1745037A (en) * | 2003-01-30 | 2006-03-08 | 帝斯曼知识产权资产管理有限公司 | From containing NH 3, CO 2And H 2Separate NH in the mixture of O 3, and separation of C O alternatively 2And H 2The method of O |
| CN1891628A (en) * | 2005-07-06 | 2007-01-10 | 窦和轩 | Method for recovering ammonia from purge gas |
-
2010
- 2010-09-19 CN CN2010102863074A patent/CN101935056B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4149857A (en) * | 1976-09-16 | 1979-04-17 | Veb Leuna-Werke "Walter Ulbricht" | Process for the two-stage separation of ammonia |
| CN1197763A (en) * | 1998-04-10 | 1998-11-04 | 刘金成 | Carbon dioxide eliminating technology used in ammonia synthesis and hydrogen production processes |
| JP2003251134A (en) * | 2002-03-06 | 2003-09-09 | Chubu Chemical Kk | Ammonia absorption apparatus and ammonia absorption method used for the same |
| CN1745037A (en) * | 2003-01-30 | 2006-03-08 | 帝斯曼知识产权资产管理有限公司 | From containing NH 3, CO 2And H 2Separate NH in the mixture of O 3, and separation of C O alternatively 2And H 2The method of O |
| CN1621763A (en) * | 2003-11-26 | 2005-06-01 | 吉林长山化肥集团长达有限公司机械厂 | Application of ammonia absorbing refrigeration in selexol decarbonization technique |
| CN1891628A (en) * | 2005-07-06 | 2007-01-10 | 窦和轩 | Method for recovering ammonia from purge gas |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102923733A (en) * | 2012-11-27 | 2013-02-13 | 天津衡创工大现代塔器技术有限公司 | Ammonia separation device and method |
| CN106766351A (en) * | 2017-01-18 | 2017-05-31 | 文安县天澜新能源有限公司 | A kind of method and apparatus for eliminating synthesis ammonia freezing post liquid ammonia storage tank emptying |
| CN109297255A (en) * | 2018-10-16 | 2019-02-01 | 安徽沃特普尔节能科技有限公司 | A kind of energy-saving gas ammonia compression process |
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|---|---|
| CN101935056B (en) | 2012-07-04 |
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