CN102303873A - Ammonia recovery process and equipment for non-ferrous metal metallurgical industry - Google Patents
Ammonia recovery process and equipment for non-ferrous metal metallurgical industry Download PDFInfo
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- CN102303873A CN102303873A CN201110210802A CN201110210802A CN102303873A CN 102303873 A CN102303873 A CN 102303873A CN 201110210802 A CN201110210802 A CN 201110210802A CN 201110210802 A CN201110210802 A CN 201110210802A CN 102303873 A CN102303873 A CN 102303873A
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Abstract
The invention discloses an ammonia recovery process and equipment for a non-ferrous metal metallurgical industry. The process comprises the following steps: mixing a base liquid with a raw material liquid in a pipeline and then feeding a mixed liquid to the upper part of an ammonia still, and carrying out steam stripping to remove ammonia in the raw material liquid; feeding a low-ammonia aqueous solution obtained at the bottom of the ammonia still to the next process; condensing gas-phase ammonia on the top of the ammonia still in an ammonia dephlegmator so as to obtain high-concentration ammonia gas; feeding the high-concentration ammonia gas into the bottom of an ammonia recovery tower to be absorbed by soft water; and recovering and recycling the high-mass-concentration ammonia water obtained at the bottom of the ammonia recovery tower, and evacuating trace fixed gas at the top of the ammonia recovery tower. The equipment is suitable for the ammonia recovery process disclosed by the invention and mainly comprises the ammonia still and the ammonia recovery tower, wherein the upper part of the ammonia still is in pipe connection with an alkali formulating tank through an alkali liquid pump and in pipe connection with a raw material liquid through a raw material pump; the ammonia dephlegmator is arranged inside the upper part of the ammonia still, and the lower part of the ammonia still is externally connected with a reboiler and is in pipe connection with the upper part of the ammonia still; and the kettle bottom of the ammonia recovery tower is in pipe connection with an ammonia water pump, the upper part of the ammonia recovery tower is in pipe connection with a soft water pipe, and the top of the ammonia recovery tower is provided with a discharge pipe.
Description
Technical field
The present invention relates to the recovering ammonia technique in the chemical industry, especially a kind of ammonia reclaiming process and equipment that is used for the Non-ferrous Metallurgy industry.
Background technology
Regular meeting produces the aqueous solution (abbreviation stock liquid) of the complex compound that contains solid particle polluter, volatilization ammonia, nonferrous metal ion, nonferrous metal ion and ammonia formation in a large number in the non-ferrous metal production process.This stock liquid need pass through the ammonia recycling; With wherein volatilization ammonia and with the ammonia removal of complexing of metal ion, the solution that obtains containing ammonia≤150ppm is delivered to subsequent processing, and the ammonia that is removed is processed the ammoniacal liquor of mass concentration>=20%; Return previous operation, recycling.
Existing ammonia reclaiming process is: stock liquid is sent in the bubble deck distillation tower of an atmospheric operation and distilled to remove ammonia, cat head is provided with condenser the ammonia vapour that distills out is condensed into ammoniacal liquor.Because the efficient of bubble deck is low, ammonia content is higher in the liquid phase at the bottom of the tower, seriously surpasses the environmental protection index requirement, thereby influences the normal running of back operation; It is not high that atmospheric operation is added the ammonia removal rate, makes the ammonia vapour of cat head through obtaining the ammoniacal liquor of mass concentration about 5% after the condenser condenses.On the one hand, this ammoniacal liquor can not be recycled because of concentration is too low, is that ammonia that all the other major parts are not condensed becomes non-condensable gas and effluxed on the other hand, has both caused the significant wastage of ammonia, makes ammonia recovery very low, has polluted environment again.In addition; The structure of bubble deck causes it to be stopped up by the solid particle polluter in the stock liquid easily; And in case stop up just necessary stop production to overhaul block clearing; Even the tower tray that more renews; Just can keep the distillatory normal running; What not only influence was produced normally carries out, and has reduced production efficiency, has also increased production cost.
Summary of the invention
To the deficiency of prior art, the technical problem that quasi-solution of the present invention is determined is that a kind of ammonia reclaiming process and equipment that is used for the Non-ferrous Metallurgy industry is provided; It is high that this technology and equipment remove ammonia efficient, and ammonia recovery is high, has both practiced thrift resource; Protect environment, also reduced production cost; This equipment is difficult for stopping up, and production efficiency is high.
The technical scheme that the present invention solves said Technology problem is; Design a kind of ammonia reclaiming process that is used for the Non-ferrous Metallurgy industry; Its technical process is: the alkali lye that comes autogamy alkali groove; After the lye pump supercharging; After in pipeline, mixing through the stock liquid after the feedstock pump supercharging; Send into the top of ammonia still, the steam that the ammonia in the stock liquid is provided by reboiler carries out stripping and removes; The aqueous solution of ammonia content≤150ppm that the ammonia still bottom obtains is delivered to subsequent processing; The ammonia at ammonia still top is after the condensation of ammonia dephlegmator; Obtain the high strength ammonia pneumatic transmission and go into the bottom of ammonia recovery tower; And absorb by the soft water that adds from ammonia recovery tower top; The ammoniacal liquor that obtains mass concentration>=20% in ammonia recovery tower bottom returns previous operation; Recycling, ammonia recovery tower top contain the trace non-condensable gas emptying of ammonia≤10ppm; Said alkali lye is the NaOH aqueous solution of mass concentration 10～40%, and the add-on of alkali lye is 0.25-1 ton/ton stock liquid; The operating pressure of said ammonia still is 0.3～0.7MPa; The operating pressure of said ammonia recovery tower is 0.15～0.55MPa; Said soft temperature≤30 ℃.
The technical scheme that the present invention solves said equipment and technology problem is; Design a kind of ammonia recovery system that is used for the Non-ferrous Metallurgy industry; Mainly comprise an ammonia still and an ammonia recovery tower; The top of ammonia still through lye pump with join the alkali barrel and connect; The top of ammonia still connects through feedstock pump and stock liquid pipe simultaneously; And before the top that gets into ammonia still, said stock liquid and alkali lye are incorporated in the mixed pipe line; The ammonia dephlegmator is installed in the top of said ammonia still, and the bottom of ammonia still is circumscribed with reboiler; The bottom of said ammonia recovery tower and the upper tube of ammonia still connect, and the still bottom tube of ammonia recovery tower connects aqua ammonia pump, and the upper tube of ammonia recovery tower connects hose, and the top is provided with vapor pipe; By-pass valve control and measuring instrument are installed in the said connecting pipeline.
Compared with prior art, Processes and apparatus of the present invention has the following advantages:
1. efficient is high, ammoniated decreasing ratio >=99.9% in the stock liquid.Ammonia still in the technology has adopted efficiently tower tray-radial side to lead jet tray CJST, and distillation efficiency improves greatly, and ammonia still tower bottoms phase (stock liquid after promptly handling) contains ammonia≤150ppm, can directly deliver to subsequent processing.
2. tower tray is difficult for blockedly, makes production efficiency improve, and production cost reduces.High-efficient tower plate-radial side that ammonia still adopted is led jet tray CJST; Have self-stip ability and good performance of anti-blockage, be difficult for being stopped up, do not need stop production to overhaul block clearing continually by the solid particle polluter in the stock liquid; Reduce production cost, improved production efficiency and economic benefit.
3. ammonia recovery is high, can reach more than 99.5%, only has the gas that contains ammonia≤10ppm to efflux, and is free from environmental pollution.The operating pressure of ammonia still in the technology and ammonia recovery tower is higher than normal pressure, makes that ammonia is easier to absorbed by soft water; Ammonia reclaims the setting of spiral coil cooling tube on Tata still heat-exchanging water tank and the compound absorption tray; The big calorimetric that produces when all in time ammonia being absorbed by soft water is shifted out outside the tower; Guaranteed that soft water absorbs efficiently carrying out smoothly of ammonia; Tower bottom just is able to obtain the ammoniacal liquor of mass concentration >=20%; Return previous operation recycling; What the minute quantity of having only top of tower satisfied environmental requirement contains ammonia gas emptying (almost reaching the zero release of ammonia), has good economy and environmental benefit.
Description of drawings
Fig. 1 is applied to the ammonia recovery novel process of Non-ferrous Metallurgy industry and technical process and the device structure synoptic diagram of a kind of embodiment of equipment for the present invention.
Embodiment
Further describe the present invention below in conjunction with embodiment and accompanying drawing thereof.
The ammonia reclaiming process that is used for the Non-ferrous Metallurgy industry of the present invention's design (is called for short technology; Referring to Fig. 1); Its technical process is: the alkali lye that comes autogamy alkali groove 3; After lye pump 6 superchargings; After in pipeline, mixing through the stock liquid after feedstock pump 7 superchargings; Send into the top of ammonia still 1, the steam that the ammonia in the stock liquid is provided by reboiler 5 carries out stripping and removes; The aqueous solution of ammonia content≤150ppm that ammonia still 1 bottom obtains is delivered to subsequent processing; The ammonia at ammonia still 1 top is after 4 condensations of ammonia dephlegmator; Obtain the bottom that the high density ammonia gets into ammonia recovery tower 2; And absorb by the soft water that adds from ammonia recovery tower 2 tops; The ammoniacal liquor that obtains mass concentration>=20% in ammonia recovery tower 2 bottoms returns previous operation; Recycling, ammonia recovery tower 2 tops contain the trace non-condensable gas emptying of ammonia≤10ppm; Said alkali lye is the NaOH aqueous solution of mass concentration 10～40%, and the add-on of alkali lye is 0.25-1 ton/ton stock liquid; The operating pressure of said ammonia still 1 is 0.3～0.7MPa; The operating pressure of said ammonia recovery tower 2 is 0.15～0.55MPa; Said soft temperature≤30 ℃.
It is for the complex compound hydrolysis that makes nonferrous metal ion and ammonia formation in the stock liquid changes into volatilization ammonia that technology of the present invention adds alkali lye (the NaOH aqueous solution of mass concentration 10～40%), thereby is convenient in ammonia still, remove.Technology of the present invention is not got rid of the alkali lye that uses other to be suitable for.
The present invention has designed a kind of ammonia recovery system that is used for the Non-ferrous Metallurgy industry simultaneously (referring to Fig. 1; Abbreviation equipment); This equipment is applicable to the ammonia reclaiming process that is used for the Non-ferrous Metallurgy industry of the present invention; Mainly comprise an ammonia still 1 and an ammonia recovery tower 2; The top of ammonia still 1 through lye pump 6 with join alkali groove 3 pipes and connect; The top of ammonia still 1 connects through feedstock pump 7 and stock liquid pipe simultaneously; And before the top that gets into ammonia still 1, said stock liquid and alkali lye are incorporated in the mixed pipe line; Ammonia dephlegmator 4 is installed in the top of said ammonia still 1, and the bottom of ammonia still 1 is circumscribed with reboiler 5; The upper tube of the bottom of said ammonia recovery tower 2 and ammonia still 1 connects, and the still bottom tube of ammonia recovery tower 2 connects aqua ammonia pump 8, and the upper tube of ammonia recovery tower 2 connects hose, and the top is provided with vapor pipe; By-pass valve control and measuring instrument are installed in the described connecting pipeline.
Component itself such as the described ammonia dephlegmator of present device 4, reboiler 5, lye pump 6, feedstock pump 7 and aqua ammonia pump 8 are prior art products.By-pass valve control of installing in the described connecting pipeline and measuring instrument (not marking among Fig. 1) are prior art.
One of core of present device is ammonia still 1 (referring to Fig. 1).The tower diameter of ammonia still 1 is decided according to stock liquid different treatment amount.Be provided with 15～35 layers of radial side in the tower and lead jet tray; This tower tray CJST is applicant's a patent formerly; I.e. " a kind of radial side is led jet tray " (patent No. ZL200620025314.8) (this patented technology is considered as being referred in the content of the present invention), operating pressure 0.3～0.7MPa (gauge pressure) of limiting.Type of heating at the bottom of ammonia still 1 tower can be conventional open steam heating, reboiler indirect heating or tube furnace heating.If during the reboiler indirect heating, the heating thermal source of reboiler can be steam or thermal oil.The ammonia dephlegmator 4 of described ammonia still 1 cat head can be fixed tube sheet heat exchanger or spiral-plate exchanger; Described ammonia dephlegmator 4 can select directly to place the internal reflux formula that is connected with the cat head flange on the cat head with the mode of connection of ammonia still 1, or places outside the tower and the external reflux type of separate connection.Described heat exchanger structure is originally as prior art.Described ammonia dephlegmator 4 also is a prior art with the mode of connection of ammonia still 1 itself.
Another core of present device is ammonia recovery tower 2 (referring to Fig. 1).The tower diameter of ammonia recovery tower 2 is decided according to the different tolerance of the high strength ammonia vapour of ammonia still cat head, and operating pressure is 0.15～0.55MPa (gauge pressure).Be soaked with in the liquid phase of ammonia recovery tower 2 tower stills >=1 layer and every layer conventional heat-exchanging water tank that has 1～4, the big calorimetric that produces in the time of ammonia vapour can being absorbed by soft water is shifted out outside the tower, to guarantee that ammonia vapour is by the stable operation of carrying out smoothly of absorbing of soft water and tower; Top in the ammonia recovery tower 2 is provided with 10～20 layers of compound absorption tray; This tower tray is applicant's a patent formerly; Promptly " a kind of compound absorption tray " (ZL200410072726.2) limits (this tower tray patented technology is considered as being referred in the technology contents of the present invention), shifts out outside the tower with the ammonia vapour that will be not do not absorbed mutually by the tower bottoms absorption heat with the generation of the liquid phase effect on the tower tray.Heat-exchanging water tank and spiral coil cooling tube all use recirculated cooling water (send water temp≤32 ℃) as heat-eliminating medium; Soft water temperature≤30 that add from ammonia recovery tower 2 tops ℃.
The present invention does not address part and is applicable to prior art.
Provide specific embodiment of the present invention below.
Embodiment 1
0.25 ton of/ton stock liquid of the alkali lye of autogamy alkali groove 3; Alkali lye is the NaOH aqueous solution of mass concentration 40%; After lye pump 6 superchargings; With 4 tons/hour of stock liquids (total ammonia content of mass concentration 25%) after feedstock pump 7 superchargings; After the two mixes in pipeline; Be admitted to ammonia still 1 (operating pressure 0.3MPa gauge pressure; 15 layers of the tower tray numbers of plies) top; The steam that ammonia in the stock liquid is provided by reboiler 5 carries out stripping and removes; Obtain the solution that ammonia content is 150ppm at the bottom of the tower of ammonia still 1, deliver to subsequent processing; The ammonia of the cat head of ammonia still 1 obtains high strength ammonia vapour (mass concentration 70%) and gets into ammonia recovery tower 2 (operating pressure 0.15MPa gauge pressures after 4 condensations of ammonia dephlegmator; 10 layers of the tower tray numbers of plies; 4 layers, every layer 3 in water tank) bottom; The soft water (30 ℃ of temperature) that adds from ammonia recovery tower 2 tops absorbs; The ammoniacal liquor that ammonia recovery tower 2 bottoms obtain mass concentration 20% returns previous operation; The gas that ammonia recovery tower 2 tops contain ammonia 10ppm effluxes emptying.
Embodiment 2
0.5 ton of/ton stock liquid of the NaOH aqueous solution of the mass concentration 20% of autogamy alkali groove 3; After lye pump 6 superchargings; With 4 tons/hour of stock liquids (total ammonia content of mass concentration 25%) after feedstock pump 7 superchargings; After the two mixes in pipeline; Be admitted to the top of ammonia still 1 (operating pressure 0.5MPa gauge pressure, 20 layers of the tower tray numbers of plies), the steam that the ammonia in the stock liquid is provided by reboiler 5 carries out stripping and removes; Obtain the solution that ammonia content is 120ppm at the bottom of the tower of ammonia still 1, deliver to subsequent processing; The ammonia of the cat head of ammonia still 1 obtains high strength ammonia vapour (mass concentration 70%) and gets into ammonia recovery tower 2 (operating pressure 0.35MPa gauge pressures after 4 condensations of ammonia dephlegmator; 15 layers of the tower tray numbers of plies; 4 layers, every layer 3 in water tank) bottom; The soft water (26 ℃ of temperature) that adds from ammonia recovery tower 2 tops absorbs; The ammoniacal liquor that ammonia recovery tower 2 bottoms obtain mass concentration 25% returns previous operation; The gas that ammonia recovery tower 2 tops contain ammonia 8ppm effluxes emptying.
Embodiment 3
1 ton of/ton stock liquid of the NaOH aqueous solution of the mass concentration 10% of autogamy alkali groove 3; After lye pump 6 superchargings; With 4 tons/hour of stock liquids (total ammonia content of mass concentration 25%) after feedstock pump 7 superchargings; After the two mixes in pipeline; Be admitted to the top of ammonia still 1 (operating pressure 0.7MPa gauge pressure, 35 layers of the tower tray numbers of plies), the steam that the ammonia in the stock liquid is provided by reboiler 5 carries out stripping and removes; Obtain the solution that ammonia content is 100ppm at the bottom of the tower of ammonia still 1, deliver to subsequent processing; The ammonia of the cat head of ammonia still 1 obtains high strength ammonia vapour (mass concentration 70%) and gets into ammonia recovery tower 2 (operating pressure 0.55MPa gauge pressures after 4 condensations of ammonia dephlegmator; 20 layers of the tower tray numbers of plies; 4 layers, every layer 3 in water tank) bottom; The soft water (20 ℃ of temperature) that adds from ammonia recovery tower 2 tops absorbs, and the ammoniacal liquor that ammonia recovery tower 2 bottoms obtain mass concentration 30% returns previous operation; The gas that ammonia recovery tower 2 tops contain ammonia 6ppm effluxes emptying.
The operation result of practical application example shows; Ammonia of the present invention reclaims novel process and equipment and has, advantages such as ammonia recovery high, production efficiency high, production cost low, free from environmental pollution, simple to operate easy control effective to the ammonia removal in the stock liquid; Not only be adapted at promoting the use of in the Non-ferrous Metallurgy industry, and be applicable to that the ammonia of other industry of chemical industry of similar operating mode reclaims.
Claims (4)
1. ammonia reclaiming process that is used for the Non-ferrous Metallurgy industry; Its technical process is: the alkali lye that comes autogamy alkali groove; After the lye pump supercharging; After in pipeline, mixing through the stock liquid after the feedstock pump supercharging; Send into the top of ammonia still, the steam that the ammonia in the stock liquid is provided by reboiler carries out stripping and removes; The aqueous solution of ammonia content≤150ppm that the ammonia still bottom obtains is delivered to subsequent processing; The ammonia at ammonia still top is after the condensation of ammonia dephlegmator; Obtain the high strength ammonia pneumatic transmission and go into the bottom of ammonia recovery tower; And absorb by the soft water that adds from ammonia recovery tower top; The ammoniacal liquor that obtains mass concentration>=20% in ammonia recovery tower bottom returns previous operation; Recycling, ammonia recovery tower top contain the trace non-condensable gas emptying of ammonia≤10ppm; Said alkali lye is the NaOH aqueous solution of mass concentration 10～40%, and the add-on of alkali lye is 0.25-1 ton/ton stock liquid; The operating pressure of said ammonia still is 0.3～0.7MPa; The operating pressure of said ammonia recovery tower is 0.15～0.55MPa; Said soft temperature≤30 ℃.
2. ammonia recovery system that is used for the Non-ferrous Metallurgy industry; This equipment is applicable to the said ammonia reclaiming process that is used for the Non-ferrous Metallurgy industry of claim 1; Mainly comprise an ammonia still and an ammonia recovery tower; The top of ammonia still through lye pump with join the alkali barrel and connect; The top of ammonia still connects through feedstock pump and stock liquid pipe simultaneously; And before the top that gets into ammonia still, said stock liquid and alkali lye are incorporated in the mixed pipe line; The ammonia dephlegmator is installed in the top of said ammonia still, and the bottom of ammonia still is circumscribed with reboiler; The bottom of said ammonia recovery tower and the upper tube of ammonia still connect, and the still bottom tube of ammonia recovery tower connects aqua ammonia pump, and the upper tube of ammonia recovery tower connects hose, and the top is provided with vapor pipe; By-pass valve control and measuring instrument are installed in the said connecting pipeline.
3. the ammonia recovery system that is used for the Non-ferrous Metallurgy industry according to claim 2 is characterized in that being provided with in the described ammonia still 15～35 layers of radial side and leads jet tray; Type of heating at the bottom of the ammonia still process Tata is conventional open steam heating, reboiler indirect heating or tube furnace heating; Described ammonia dephlegmator is fixed tube sheet heat exchanger or spiral-plate exchanger; Described ammonia dephlegmator is directly to place the internal reflux formula that is connected with the cat head flange on the cat head with the mode of connection of ammonia still, or places outside the tower and the external reflux type of separate connection.
4. the ammonia recovery system that is used for the Non-ferrous Metallurgy industry according to claim 2 is characterized in that said ammonia reclaims in the liquid phase of Tata still to be soaked with >=1 layer and every layer conventional heat-exchanging water tank that has 1～4; Top in the ammonia recovery tower is provided with 10～20 layers of compound absorption tray.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201110210802A CN102303873A (en) | 2011-07-27 | 2011-07-27 | Ammonia recovery process and equipment for non-ferrous metal metallurgical industry |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201110210802A CN102303873A (en) | 2011-07-27 | 2011-07-27 | Ammonia recovery process and equipment for non-ferrous metal metallurgical industry |
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| CN102303873A true CN102303873A (en) | 2012-01-04 |
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| CN201110210802A Pending CN102303873A (en) | 2011-07-27 | 2011-07-27 | Ammonia recovery process and equipment for non-ferrous metal metallurgical industry |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104355343A (en) * | 2014-11-04 | 2015-02-18 | 赛鼎工程有限公司 | Purification technology for ammonia recycled from wastewater from coal gasification |
| CN105884106A (en) * | 2016-04-22 | 2016-08-24 | 唐山旭阳化工有限公司 | Benzene hydrogenation wastewater desulfurization and deamination treatment method aiming at improving deamination and treatment device applying same |
| CN106927485A (en) * | 2017-04-01 | 2017-07-07 | 中冶焦耐(大连)工程技术有限公司 | A kind of method with remained ammonia as waste high purity ammonia |
| CN112299444A (en) * | 2020-10-14 | 2021-02-02 | 营口正源电力配套设备有限公司 | Mobile liquid ammonia recovery ammonia tank replacement equipment and method |
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| CN1631491A (en) * | 2004-11-16 | 2005-06-29 | 天津市创举科技有限公司 | Compound absorption tray |
| CN2915212Y (en) * | 2006-02-08 | 2007-06-27 | 天津市创举科技有限公司 | A radial side pilot jet tray |
| CN101941720A (en) * | 2010-08-23 | 2011-01-12 | 天津市创举科技有限公司 | Tube furnace ammonia evaporation process and equipment |
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2011
- 2011-07-27 CN CN201110210802A patent/CN102303873A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1631491A (en) * | 2004-11-16 | 2005-06-29 | 天津市创举科技有限公司 | Compound absorption tray |
| CN2915212Y (en) * | 2006-02-08 | 2007-06-27 | 天津市创举科技有限公司 | A radial side pilot jet tray |
| CN101941720A (en) * | 2010-08-23 | 2011-01-12 | 天津市创举科技有限公司 | Tube furnace ammonia evaporation process and equipment |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104355343A (en) * | 2014-11-04 | 2015-02-18 | 赛鼎工程有限公司 | Purification technology for ammonia recycled from wastewater from coal gasification |
| CN104355343B (en) * | 2014-11-04 | 2015-11-18 | 赛鼎工程有限公司 | A kind of purification process for reclaiming ammonia in coal gasification waste water |
| CN105884106A (en) * | 2016-04-22 | 2016-08-24 | 唐山旭阳化工有限公司 | Benzene hydrogenation wastewater desulfurization and deamination treatment method aiming at improving deamination and treatment device applying same |
| CN106927485A (en) * | 2017-04-01 | 2017-07-07 | 中冶焦耐(大连)工程技术有限公司 | A kind of method with remained ammonia as waste high purity ammonia |
| CN106927485B (en) * | 2017-04-01 | 2023-05-16 | 中冶焦耐(大连)工程技术有限公司 | Method for preparing high-purity ammonia by taking residual ammonia water as raw material |
| CN112299444A (en) * | 2020-10-14 | 2021-02-02 | 营口正源电力配套设备有限公司 | Mobile liquid ammonia recovery ammonia tank replacement equipment and method |
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Application publication date: 20120104 |