CN202279792U - Device by utilizing methanol purge gas to jointly produce methanol and synthetic ammonia - Google Patents
Device by utilizing methanol purge gas to jointly produce methanol and synthetic ammonia Download PDFInfo
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- CN202279792U CN202279792U CN2011201015364U CN201120101536U CN202279792U CN 202279792 U CN202279792 U CN 202279792U CN 2011201015364 U CN2011201015364 U CN 2011201015364U CN 201120101536 U CN201120101536 U CN 201120101536U CN 202279792 U CN202279792 U CN 202279792U
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Abstract
The utility model relates to a device by utilizing methanol purge gas to jointly produce methanol and synthetic ammonia, which comprises a carbon dioxide adsorption tower, a methanol synthesizing tower, a methanol cooler, a methanol separation device, a methane synthesizing tower, an ammonia synthesizing tower, an ammonia gas cooling device, an ammonia gas separation tower and a flash drum, wherein devices of the carbon dioxide adsorption tower, the methanol synthesizing tower, the methanol cooler, the methanol separation device, the methane synthesizing tower, the ammonia synthesizing tower, the ammonia gas cooling device, the ammonia separation tower and the flash drum are sequentially connected with one another through pipelines, a liquid ammonia collector is arranged at a liquid ammonia outlet of the flash drum, and a liquid ammonia collector goes to a liquid ammonia outlet of the flash drum The device has advantages that: an industrial chain of coke, oven gas, methanol production and synthetic ammonia production is formed, a circulating economic route capable of adequately utilizing the resource is provided, not only can the pollution problem of a coking enterprise be fundamentally solved, but also the waste gas is converted into liquid ammonia, the additional value of a product can be effectively improved, and the enterprise economic benefit can be enhanced.
Description
Technical field
The utility model relates to a kind of methyl alcohol speed to exit device of combination producing methyl alcohol and synthetic ammonia that utilizes.
Background technology
The coke output of China is very big, and China reaches 2.5 hundred million tons at coke output in 2010, and Chinese coke output ranks first in the world continuously in year, accounts for world's coke ultimate production 46%.The coke of China is mainly used Iron And Steel Industry at home.The coking industry that high speed development gets up along with the great demand of Iron And Steel Industry STRENGTH ON COKE; When coke output increased substantially, the coke-oven gas of a large amount of by-products was not rationally utilized, and has caused the environment rapid deterioration in coke producing region; The independent coal chemical enterprise of many single coking " Jiao does not change "; Take a mode of sky lamp to burn in a large amount of coke-oven gas and diffuse, both serious environment pollution caused the wasting of resources again.For the pollution problem that solves coking industry and improve the competitive power of coke industry, the comprehensive utilization of coke(oven)gas more and more obtains designing the attention with production unit, and begins to develop the process exploitation of coke(oven)gas system synthetic ammonia and methyl alcohol.2004 the end of the year China first cover coke(oven)gas system methanol device go into operation successfully in the Qujing, Yunnan, the exploitation of this technology has improved the utility value of coke(oven)gas greatly, the cost of coke descends significantly, for head has been held in the utilization of coke(oven)gas successfully.At present domestic existing nearly 10 cover coke-oven gas system methanol devices are put into commercial operation, and mostly single covering device design scale is 10～200,000 t/a.Because protium is generally more than 70% in the coke(oven)gas, carbon is below 15%, and the chemical reaction hydrogen-carbon ratio of synthesizing methanol is 2: 1; Carbon is not enough when therefore causing the methyl alcohol building-up reactions, and it is unrealistic to go up gas maked coal benefit carbon, so domestic majority coke(oven)gas system methanol technics does not have carbon compensator at present; Cause the hydrogen-carbon ratio in the synthetic gas high; Excessive hydrogen can cause the methanol synthesis loop circulating flow rate to increase in the building-up reactions, increases the quantity discharged of synthesis cycle consumption of compressor and off-gas, makes the clean hydrogen of producing through a plurality of operations such as purification, conversions get into fuel system as off-gas and burns; Wasted resource, increased and produced consumption.
The utility model content
The utility model technical problem to be solved is that a kind of methyl alcohol speed to exit device of combination producing methyl alcohol and synthetic ammonia that utilizes is provided to above-mentioned prior art present situation; This device utilizes the venting of speeding of discharging in the coke(oven)gas system methanol process; After decarburization, mending nitrogen, pure alkylation process; The syngas for synthetic ammonia that obtains rational proportion is produced synthetic ammonia, thereby has well solved the problem of utilizing that methyl alcohol speeds to exit.
The utility model solves the problems of the technologies described above the technical scheme that is adopted: this utilizes methyl alcohol speed the to exit device of combination producing methyl alcohol and synthetic ammonia; It is characterized in that: said device includes carbonic acid gas adsorption tower, methyl alcohol synthetic reactor, methyl alcohol water cooler, methanol separator, methane synthetic tower, ammonia synthesis converter, ammonia refrigerating unit, ammonia knockout tower, flash drum; The bottom inlet of said carbonic acid gas adsorption tower is connected with the pipeline that methyl alcohol speeds to exit; Carbonic acid gas adsorption tower top exit; Through pipeline with join mutually from the nitrogen pipeline in the air-seperation system after be connected with the inlet mouth of first gas compressor in the lump; The air outlet of first gas compressor is connected with the inlet mouth of methyl alcohol synthetic reactor through pipeline; The outlet of methyl alcohol synthetic reactor is connected through the inlet mouth of pipeline with the methyl alcohol water cooler; And the gas liquid outlet of methyl alcohol water cooler is connected with the import of methanol separator through pipeline; And the outlet of the methanol liquid of methanol separator is led to the methyl alcohol scoop through pipeline from the bottom of methanol separator, and the outlet of the top gas of methanol separator is connected through the inlet mouth of pipeline with the methane synthetic tower, and the air outlet of methane synthetic tower is connected through the inlet mouth of pipeline with second gas compressor; And the pneumatic outlet of second gas compressor is connected with the inlet mouth of ammonia synthesis converter through pipeline; And the air outlet of ammonia synthesis converter is connected through the inlet mouth of pipeline with the ammonia refrigerating unit, and the outlet of ammonia refrigerating unit is connected through the import of pipeline with the ammonia knockout tower, and the outlet of the top gas of ammonia knockout tower is connected through the import of pipeline with the 3rd gas compressor; And the air outlet of the 3rd gas compressor through the pipeline and the pneumatic outlet pipeline of second gas compressor meet close the back be connected with the inlet mouth of ammonia synthesis converter; The bottom liquid outlet of ammonia knockout tower is connected with the import of flash drum through pipeline, and the outlet of the liquefied ammonia of flash drum is removed the liquefied ammonia scoop through pipeline, and the pneumatic outlet at flash drum top is through pipeline deammoniation recovery system.
As improvement; Also can be provided with heat recoverer between said ammonia synthesis converter and the ammonia refrigerating unit; The air outlet of said ammonia synthesis converter is connected with the inlet mouth of heat recoverer through pipeline, and the air outlet of heat recoverer is connected through the inlet mouth of pipeline with the ammonia refrigerating unit.
Improve again; Said ammonia refrigerating unit includes the ammonia cooler of cooling water cooler and ammonia refrigerant; The air outlet of said heat recoverer is connected with the inlet mouth of cooling water cooler through pipeline; And the air outlet of cooling water cooler is connected with the bottom air inlet of ammonia cooler through pipeline, and the outlet that is positioned at ammonia cooler top is connected through the import of pipeline with the ammonia knockout tower.
Improve, the waste gas in the said ammonia recovery system goes boiler combustion through pipeline again.
Improve, the carbonic acid gas that absorbs in the said carbonic acid gas adsorption tower goes methyl alcohol to synthesize portion through pipeline again.
Compared with prior art; The advantage of the utility model is to have formed " coke-coke(oven)gas-production methyl alcohol-production synthetic ammonia " industrial chain; The recycling economy route that provides a resource to make full use of, the pollution problem that has not only fundamentally solved coal chemical enterprise, and waste gas is converted into liquefied ammonia; Effectively improve value-added content of product, promoted the business economic benefit.
Description of drawings
Fig. 1 is the structural representation of the utility model embodiment.
Embodiment
Embodiment describes in further detail the utility model below in conjunction with accompanying drawing.
As shown in Figure 1; Methyl alcohol speed the to exit device of combination producing methyl alcohol and synthetic ammonia that utilizes of present embodiment includes carbonic acid gas adsorption tower 1, methyl alcohol synthetic reactor 2, methyl alcohol water cooler 21, methanol separator 3, methane synthetic tower 4, ammonia synthesis converter 5, ammonia refrigerating unit, ammonia knockout tower 8, flash drum 9; The bottom inlet of said carbonic acid gas adsorption tower 1 is connected with the pipeline that methyl alcohol speeds to exit; Carbonic acid gas adsorption tower 1 top exit; Through pipeline with join mutually from the nitrogen pipeline in the air-seperation system 12 after be connected with the inlet mouth of first gas compressor 13 in the lump; The air outlet of first gas compressor 13 is connected through the inlet mouth of pipeline with methyl alcohol synthetic reactor 2; The outlet of methyl alcohol synthetic reactor 2 is connected through the inlet mouth of pipeline with methyl alcohol water cooler 21; And the gas liquid outlet of methyl alcohol water cooler 21 is connected through the import of pipeline with methanol separator 3; And the outlet of the methanol liquid of methanol separator 3 is led to the methyl alcohol scoop through pipeline from the bottom of methanol separator 3; And the outlet of the top gas of methanol separator 3 is connected through the inlet mouth of pipeline with methane synthetic tower 4, and the air outlet of methane synthetic tower 4 is connected through the inlet mouth of pipeline with second gas compressor 41, and the pneumatic outlet of second gas compressor 41 is connected through the inlet mouth of pipeline with ammonia synthesis converter 5; And the air outlet of ammonia synthesis converter 5 is connected through the inlet mouth of pipeline with the ammonia refrigerating unit; And the outlet of ammonia refrigerating unit is connected through the import of pipeline with ammonia knockout tower 8, and the top gas of ammonia knockout tower 8 outlet is connected through the import of pipeline with the 3rd gas compressor 81, and meets to close through the pipeline and the pneumatic outlet pipeline of second gas compressor 41 and then be connected with the inlet mouth of ammonia synthesis converter 5 in the air outlet of the 3rd gas compressor 81; The bottom liquid outlet of ammonia knockout tower 8 is connected through the import of pipeline with flash drum 9; And the outlet of the liquefied ammonia of flash drum 9 is removed the liquefied ammonia scoop through pipeline, and the pneumatic outlet at flash drum 9 tops passes through pipeline deammoniation recovery system 91, and the waste gas in the ammonia recovery system 91 goes boiler combustion through pipeline.The carbonic acid gas that absorbs in the above-mentioned carbonic acid gas adsorption tower 1 goes methyl alcohol to synthesize portion 10 through pipeline.
As shown in Figure 1; Be provided with heat recoverer 6 between above-mentioned ammonia synthesis converter 5 and the ammonia refrigerating unit; And the ammonia refrigerating unit includes the ammonia cooler 7 of cooling water cooler 71 and ammonia refrigerant; The air outlet of ammonia synthesis converter 5 is connected through the inlet mouth of pipeline with heat recoverer 6; And the air outlet of heat recoverer is connected through the inlet mouth of pipeline with cooling water cooler 71, and the air outlet of cooling water cooler is connected through the bottom air inlet of pipeline with ammonia cooler 7, and the outlet that is positioned at ammonia cooler 7 tops is connected through the import of pipeline with ammonia knockout tower 8.
The advantage of the utility model device is:
1, with the synthetic venting of speeding of methyl alcohol as virgin gas, production application is synthetic ammonia very widely, avoided a large amount of valuable gases act as a fuel gas firing or directly emptying burn the wasting of resources and the environmental pollution that is caused.
2, the synthetic carbonic acid gas that decarburization produced of speeding to exit of methyl alcohol returns methanol synthesizer again, has optimized the hydrogen-carbon ratio of methyl methanol syngas, has improved methyl alcohol synthetic efficient, has reduced methyl methanol syngas consumption.
3, realized the reasonable disposition of each production factors, the cost of coke, coke(oven)gas, methyl alcohol, synthetic ammonia is all decreased.
4, present technique adopts advanced variable pressure gas adsorption and purification technology, pure alkanisation technology and low pressure ammonia synthesis technology.
5, the water cooler in the ammonia synthesizer adopts evaporative type cooler, reduces cooling water amount, saves floor occupying area.
But 6, synthetic tower outlet high-temperature gas by-product MP steam.
Embodiment one
Certain factory's coke output is 1,500,000 tons/year, and the coke(oven)gas that produces in the production process can be produced 200,000 tons/year of methyl alcohol.Because hydrogen-carbon ratio is high in the methyl methanol syngas, the venting of speeding that in methanol production process, produces is big, and except that being used for coking fuel on a small quantity, most of emptying is burnt.New supporting 80,000 tons of synthetic ammonia installations of a cover that start, methyl alcohol 33000Nm that exits that speeds
3/ h, gaseous fraction is H
276.74%CH
41.18%N
29.75% CO6.59%CO
25.59% CmHn 2.1%, pressure 4.5MPa, 35 ℃ of temperature reduce pressure to getting into decarburization workshop section behind the 2.1MPa, and the dioxide gas that decarburization produces returns methanol synthesizer after pressurizeing.Mainly contain hydrogen, nitrogen and a small amount of carbon monoxide, carbonic acid gas and methane through the gas after the decarburization.For guaranteeing of the requirement of Ammonia Production hydrogen nitrogen, after decarburization workshop section, replenish high pure nitrogen (nitrogen is from space division system 99.99%) 3400Nm than 3: 1
3/ h makes composition in the gas satisfy the needed hydrogen nitrogen ratio of synthetic ammonia and requires.Allotment back gaseous tension 2.1MPa, 35 ℃ of temperature.This gas successively gets into methanolizing and methanation workshop section through compressor pressurizes to 10MPa, with CO+CO
2Be reduced to below the 20PPM, further be forced into then and get into ammonia synthesis workshop section behind the 25MPa,, produce finished product synthetic ammonia 10t/h through steps such as preheating, reaction, cooling, ammonia separation.
Embodiment two
Certain factory's coke output is 1,200,000 tons/year, and the coke(oven)gas that produces in the production process is produced 150,000 tons/year of methyl alcohol, supporting 60,000 tons of synthetic ammonia installations and 30,000 tons of food carbon dioxide plants.The methyl alcohol 26000Nm that exits that speeds
3/ h, gaseous fraction is H
273.25%CH
41.38%N29.25%CO6.28%CO
25.86%CmHn 2.1%, gaseous tension 4.2MPa, and 35 ℃ of temperature reduce pressure to getting into pressure swing adsorption decarbonization workshop section behind the 2.0MPa, and the dioxide gas that decarburization produces is produced 30,000 tons of/year food-grade carbon-dioxides through the pressurization back.Gaseous constituent through after the decarburization is: hydrogen 76.85%, nitrogen 9.73% also have a small amount of carbon monoxide, carbonic acid gas and methane.For guaranteeing of the requirement of Ammonia Production hydrogen nitrogen, after decarburization workshop section, replenish high pure nitrogen (nitrogen is from space division system 99.99%) 2700Nm than 3: 1
3/ h makes composition in the gas satisfy the needed hydrogen nitrogen ratio of synthetic ammonia and requires.Allotment back gaseous tension 2.1MPa, 35 ℃ of temperature.This gas successively gets into methanolizing and methanation workshop section through compressor pressurizes to 10MPa, with CO+CO
2Be reduced to below the 20PPM, further be forced into then and get into ammonia synthesis workshop section behind the 25MPa,, produce finished product synthetic ammonia 8t/h through steps such as preheating, reaction, cooling, ammonia separation.
The idiographic flow explanation:
One, transformation adsorption process:
Pressure-swing absorption apparatus (promptly referring to the carbonic acid gas adsorption tower, down together) is made up of the adsorption tower and the special-purpose sequencing valve of Duo Tai of a plurality of parallel connections.The bottom of speeding to exit from adsorption tower from the methyl alcohol of the next carbonated 6～10% of methanol synthesizer gets into adsorbent bed; Select at sorbent material under the condition of absorption; Carbonic acid gas during methyl alcohol speeded to exit absorbs, and the hydrogen and nitrogen gas that is not adsorbed gets into the compression section of first gas compressor.
Two, pure alkanisation flow process:
Through containing CO, the CO of small portion of residual in the virgin gas behind the pressure swing adsorption decarbonization
2, O
2Deng obnoxious flavour, in order to prevent their murders by poisoning to ammonia synthesis catalyst, virgin gas must purify before sending into ammonia synthesis converter.The hydrogen and nitrogen gas that pressure-swing absorption apparatus comes is sent into the methyl alcohol synthesizing section by compressor pressurizes to 10MPa, and under the effect of catalyzer, the carbon monoxide in the gas, carbonic acid gas and hydrogen are in methyl alcohol synthetic reactor, and reaction generates methyl alcohol in the presence of catalyzer,
The alcoholization reaction equation is: CO+2H
2→ CH
3OH
CO
2+3H
2→CH
3OH+H
2O
The pure gasification that is come out by the methyl alcohol synthesizing section (contains CO+CO
2=0.7%), gets into methanator (being nail alkane synthetic tower), under the methanation catalyst effect, accomplish methanation reaction, make methane gasification CO+CO through after the heat exchange
2=20ppm.Qualified methanation pneumatic transmission to the second gas compressor and get into and be sent to ammonia synthesis workshop section after compression section further is forced into 20MPa.
The alkylation reaction equation:
nCO+2nH
2→CnH
2n+2+(n-1)H
2O
nCO+(2n+1)H
2→CnH
2n+2+nH
2O
nCO
2+(3n+1)H
2→CnH
2n+2+2nH
2O
Synthetic ammonia process:
Come the qualified methane gasification of 20MPa from compressor, get into ammonia synthesis converter through the heating back, under the effect of catalyzer; Hydrogen and nitrogen reaction generate synthetic ammonia; The gas that goes out synthetic tower is through waste heat boiler (promptly referring to heat recoverer) by-product MP steam, and through cooling water cooler and the cooling of ammonia cooler two-stage, gas ammonia is condensed into liquefied ammonia to be separated from gas then; Obtain the liquefied ammonia product, water cooler adopts high-efficiency evaporation type radiator.The liquefied ammonia decompression back that separates gets into flash drum, and flash drum discharges liquefied ammonia dissolved available gas in high-pressure system and forms the venting of speeding, the deammoniation recovery system of speeding to exit, and the gas that ammonia reclaims out is sent to the through exhaust gas boiler burning, to reclaim its waste heat.Ammonia synthesis pressure: 20Mpa, ammonia synthesis temperature: 450-550 ℃, the ammonia synthesis reaction equation is: N
2+ 3H
2→ 2NH
3
Claims (5)
1. one kind is utilized methyl alcohol speed the to exit device of combination producing methyl alcohol and synthetic ammonia; It is characterized in that: said device includes carbonic acid gas adsorption tower (1), methyl alcohol synthetic reactor (2), methyl alcohol water cooler (21), methanol separator (3), methane synthetic tower (4), ammonia synthesis converter (5), ammonia refrigerating unit, ammonia knockout tower (8), flash drum (9); The bottom inlet of said carbonic acid gas adsorption tower (1) is connected with the pipeline that methyl alcohol speeds to exit; Carbonic acid gas adsorption tower (1) top exit; Through pipeline with join mutually from the nitrogen pipeline in the air-seperation system (12) after be connected with the inlet mouth of first gas compressor (13) in the lump; The air outlet of first gas compressor (13) is connected through the inlet mouth of pipeline with methyl alcohol synthetic reactor (2); The outlet of methyl alcohol synthetic reactor (2) is connected through the inlet mouth of pipeline with methyl alcohol water cooler (21); And the gas liquid outlet of methyl alcohol water cooler (21) is connected through the import of pipeline with methanol separator (3); And the outlet of the methanol liquid of methanol separator (3) is led to the methyl alcohol scoop through pipeline from the bottom of methanol separator (3); And the outlet of the top gas of methanol separator (3) is connected through the inlet mouth of pipeline with methane synthetic tower (4); And the air outlet of methane synthetic tower (4) is connected through the inlet mouth of pipeline with second gas compressor (41), and the pneumatic outlet of second gas compressor (41) is connected through the inlet mouth of pipeline with ammonia synthesis converter (5), and the air outlet of ammonia synthesis converter (5) is connected through the inlet mouth of pipeline with the ammonia refrigerating unit; And the outlet of ammonia refrigerating unit is connected through the import of pipeline with ammonia knockout tower (8); And the top gas of ammonia knockout tower (8) outlet is connected through the import of pipeline with the 3rd gas compressor (81), and meets to close through the pipeline and the pneumatic outlet pipeline of second gas compressor (41) and then be connected with the inlet mouth of ammonia synthesis converter (5) in the air outlet of the 3rd gas compressor (81), and the bottom liquid of ammonia knockout tower (8) exports and is connected through the import of pipeline with flash drum (9); And the outlet of the liquefied ammonia of flash drum (9) is removed the liquefied ammonia scoop through pipeline, and the pneumatic outlet at flash drum (9) top is through pipeline deammoniation recovery system (91).
2. device according to claim 1; It is characterized in that: be provided with heat recoverer (6) between said ammonia synthesis converter (5) and the ammonia refrigerating unit; The air outlet of said ammonia synthesis converter (5) is connected through the inlet mouth of pipeline with heat recoverer (6), and the air outlet of heat recoverer (6) is connected through the inlet mouth of pipeline with the ammonia refrigerating unit.
3. device according to claim 2; It is characterized in that: said ammonia refrigerating unit includes the ammonia cooler (7) of cooling water cooler (71) and ammonia refrigerant; The air outlet of said heat recoverer is connected with the inlet mouth of cooling water cooler through pipeline; And the air outlet of cooling water cooler (71) is connected through the bottom air inlet of pipeline with ammonia cooler (7), and the outlet that is positioned at ammonia cooler (7) top is connected through the import of pipeline with ammonia knockout tower (8).
4. according to arbitrary described device in the claim 1 to 3, it is characterized in that: the waste gas in the said ammonia recovery system (91) goes boiler combustion through pipeline.
5. according to arbitrary described device in the claim 1 to 3, it is characterized in that: the carbonic acid gas that absorbs in the said carbonic acid gas adsorption tower (1) goes methyl alcohol to synthesize portion (10) through pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201015364U CN202279792U (en) | 2011-04-05 | 2011-04-05 | Device by utilizing methanol purge gas to jointly produce methanol and synthetic ammonia |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201015364U CN202279792U (en) | 2011-04-05 | 2011-04-05 | Device by utilizing methanol purge gas to jointly produce methanol and synthetic ammonia |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202279792U true CN202279792U (en) | 2012-06-20 |
Family
ID=46225967
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011201015364U Expired - Lifetime CN202279792U (en) | 2011-04-05 | 2011-04-05 | Device by utilizing methanol purge gas to jointly produce methanol and synthetic ammonia |
Country Status (1)
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|---|---|
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102746112A (en) * | 2012-07-19 | 2012-10-24 | 新乡市金鑫化工设备有限责任公司 | Device for recycling methanol from methanol purge gas |
| CN103058139A (en) * | 2012-12-31 | 2013-04-24 | 营口三征有机化工股份有限公司 | Method for reproducing medium pressure steam by flare gas generated in synthesis ammonia production process |
| CN113860992A (en) * | 2021-11-10 | 2021-12-31 | 新乡广硕化工有限公司 | Method for comprehensively producing methanol, CNG (compressed natural gas) and liquid ammonia by using purge gas of methanol |
-
2011
- 2011-04-05 CN CN2011201015364U patent/CN202279792U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102746112A (en) * | 2012-07-19 | 2012-10-24 | 新乡市金鑫化工设备有限责任公司 | Device for recycling methanol from methanol purge gas |
| CN103058139A (en) * | 2012-12-31 | 2013-04-24 | 营口三征有机化工股份有限公司 | Method for reproducing medium pressure steam by flare gas generated in synthesis ammonia production process |
| CN103058139B (en) * | 2012-12-31 | 2014-07-16 | 营口三征有机化工股份有限公司 | Method for reproducing medium pressure steam by flare gas generated in synthesis ammonia production process |
| CN113860992A (en) * | 2021-11-10 | 2021-12-31 | 新乡广硕化工有限公司 | Method for comprehensively producing methanol, CNG (compressed natural gas) and liquid ammonia by using purge gas of methanol |
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Owner name: NINGBO YUANDONG INDUSTRY TECHNOLOGY CO., LTD. Effective date: 20140128 Owner name: SHANDONG HENGCHANG JUCAI CHEMICAL TECHNOLOGY CO., Free format text: FORMER OWNER: NINGBO YUANDONG INDUSTRY TECHNOLOGY CO., LTD. Effective date: 20140128 |
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Free format text: CORRECT: ADDRESS; FROM: 315010 NINGBO, ZHEJIANG PROVINCE TO: 276132 LINYI, SHANDONG PROVINCE |
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| TR01 | Transfer of patent right |
Effective date of registration: 20140128 Address after: No. 1 Chu Dun Zhen Road 276132 Shandong city of Linyi Province Hengchang Luozhuang District Patentee after: SHANDONG HENGCHANG POLYMER MATERIAL CHEMICAL INDUSTRY TECHNOLOGY CO., LTD. Patentee after: Ningbo Yuandong Industry Technology Co., Ltd. Address before: 315010 A, block 12D, 168 Zhangs Road, Ningbo, Zhejiang Patentee before: Ningbo Yuandong Industry Technology Co., Ltd. |
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| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: No. 1 Chu Dun Zhen Road 276132 Shandong city of Linyi Province Hengchang Luozhuang District Patentee after: SHANDONG HENGCHANG POLYMER MATERIAL CHEMICAL INDUSTRY TECHNOLOGY CO., LTD. Patentee after: Ningbo Jinyuandong Petrochemical Engineering Technology Co., Ltd. Address before: No. 1 Chu Dun Zhen Road 276132 Shandong city of Linyi Province Hengchang Luozhuang District Patentee before: SHANDONG HENGCHANG POLYMER MATERIAL CHEMICAL INDUSTRY TECHNOLOGY CO., LTD. Patentee before: Ningbo Yuandong Industry Technology Co., Ltd. |
|
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: No. 1 Chu Dun Zhen Road 276132 Shandong city of Linyi Province Hengchang Luozhuang District Patentee after: SHANDONG HENGCHANG POLYMER MATERIAL CHEMICAL INDUSTRY TECHNOLOGY CO., LTD. Patentee after: Ningbo Zhongke Far East catalytic Engineering Technology Co Ltd Address before: No. 1 Chu Dun Zhen Road 276132 Shandong city of Linyi Province Hengchang Luozhuang District Patentee before: SHANDONG HENGCHANG POLYMER MATERIAL CHEMICAL INDUSTRY TECHNOLOGY CO., LTD. Patentee before: Ningbo Jinyuandong Petrochemical Engineering Technology Co., Ltd. |
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Granted publication date: 20120620 |