CN1168852C - Method for producing liquir nitrogen by using electrolysis process - Google Patents
Method for producing liquir nitrogen by using electrolysis process Download PDFInfo
- Publication number
- CN1168852C CN1168852C CNB011082798A CN01108279A CN1168852C CN 1168852 C CN1168852 C CN 1168852C CN B011082798 A CNB011082798 A CN B011082798A CN 01108279 A CN01108279 A CN 01108279A CN 1168852 C CN1168852 C CN 1168852C
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- CN
- China
- Prior art keywords
- chlorine
- ammonia
- hydrogen
- liquid
- electrolytic solution
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 238000000034 method Methods 0.000 title claims abstract description 30
- 238000005868 electrolysis reaction Methods 0.000 title claims abstract description 21
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims description 16
- 229910052757 nitrogen Inorganic materials 0.000 title claims description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 82
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 claims abstract description 44
- 239000001257 hydrogen Substances 0.000 claims abstract description 36
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 36
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 28
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000000460 chlorine Substances 0.000 claims abstract description 27
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 27
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims abstract description 22
- 235000019270 ammonium chloride Nutrition 0.000 claims abstract description 22
- 229910021529 ammonia Inorganic materials 0.000 claims description 39
- 238000001816 cooling Methods 0.000 claims description 22
- 239000007788 liquid Substances 0.000 claims description 19
- 239000008151 electrolyte solution Substances 0.000 claims description 17
- 239000000243 solution Substances 0.000 claims description 16
- 238000007906 compression Methods 0.000 claims description 8
- 230000006835 compression Effects 0.000 claims description 8
- 150000002431 hydrogen Chemical class 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 10
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 abstract description 3
- 239000011780 sodium chloride Substances 0.000 abstract description 2
- 230000005611 electricity Effects 0.000 abstract 1
- 235000002639 sodium chloride Nutrition 0.000 abstract 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 238000010025 steaming Methods 0.000 description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The present invention discloses a method for producing liquid chlorine by electrolyzing ammonium chloride solution. The method electrolyzes 25 to 40% of ammonium chloride solution under the direct-current power supply of 2.5 to 3V, liquid chlorine is produced, and meanwhile, hydrogen and liquid ammonia are produced. For producing 1 ton chlorine, compared with original traditional electrolysis common salt water method, the present invention saves electricity by 10 to 15%, and the production capacity of a single electrolytic tank can be improved by 10 to 20%.
Description
The present invention relates to the method for a kind of production method of liquid chlorine, particularly a kind of producing liquir nitrogen by using electrolysis process.
The technology of tradition producing liquir nitrogen by using electrolysis process is electrolytic saltwater.This technology is to adopt the direct supply of 3V, makes the salt solution electrolysis under bigger electric current.Collect chlorine at anode, collect hydrogen at negative electrode, the liquid of staying in the electrolyzer can be used to produce sodium hydroxide.Mainly there is following point aborning in this technology:
(1) electrolysis makes power consumption higher.Produce 1 ton of liquid chlorine current consumption and be approximately 2350 kilowatt-hours;
(2) it is lower to enter the sodium chloride concentration of electrolyzer, has only about 24%, causes the throughput of single electrolyzer lower like this;
The objective of the invention is at the deficiencies in the prior art, the producing liquir nitrogen by using electrolysis process that a kind of energy consumption is low and throughput is high novel process is provided.Be to adopt ammonium chloride solution to utilize the method for producing liquir nitrogen by using electrolysis process and by-product liquid hydrogen, liquefied ammonia as electrolytic solution,
Purpose of the present invention is reached by following technical scheme, the present invention is a kind of method of producing liquir nitrogen by using electrolysis process, two electrodes are set in electrolytic solution, feed direct supply, collect the chlorine of anode generation, the hydrogen that negative electrode produces, make liquid chlorine, liquid hydrogen after compressed respectively, the condensation, be characterized in that electrolytic solution is the ammonium chloride solution of weight concentration 25-40%, power supply adopts the 2.5-3V direct supply.
For making the present invention obtain better effect, the present invention also can be by further realizing with the below: the method for above-mentioned production liquid chlorine is characterized in obtaining ammonia, its cooling, compression, condensation being made liquefied ammonia being heated to 85-100 ℃ of evaporation under the remaining electrolytic solution normal pressure in the electrolyzer.
For making the present invention obtain better effect, the present invention also can further realize by following scheme: the method for above-mentioned production liquid chlorine is characterized in chlorine, hydrogen, ammonia compressed respectively and is cooled to that used cooling backwater is used for disposing ammonium chloride electrolytic solution in liquid chlorine, liquid hydrogen, the liquefied ammonia process.To reclaim the heat that reaction process produces.
For making the present invention obtain better effect, the present invention also can further realize by following scheme: the method for above-mentioned production liquid chlorine is characterized in the residue weak ammonia that residue electrolytic solution evaporation in the electrolyzer is produced in the liquefied ammonia process is reclaimed as configuration ammonium chloride electrolytic solution.To reclaim wherein contained ammonia.
Use ammonium chloride solution as electrolytic solution electrolysis production liquid chlorine coproduction liquid hydrogen and liquefied ammonia, produce 1 ton of liquid chlorine current consumption and be about 2100 kilowatt-hours, more former method unit consumption decline 10-15%; Single electrolyzer throughput improves 10-20%.And this method has made full use of reaction heat energy, three-waste free discharge, obvious social benefit.
Following examples describe the present invention in detail:
Embodiment one.With the ammonium chloride solution input electrolyzer of the weight concentration 40% that configures, the instantaneous throughput of this design of electrolysis cells liquid chlorine is 10,000 tons/year, passes to the 3V direct current, and ammonium chloride solution is carried out electrolysis; Collect the chlorine that anode produces by gas trap, the hydrogen that negative electrode produces is introduced into chlorine treatment system and hydrogen treat system respectively, and the remained ammonia in the electrolyzer is introduced ammonia disposal system.
In chlorine treatment system and hydrogen treat system, use earlier water cooling chlorine and hydrogen respectively, to the sensible heat of chlorine and hydrogen, configuration makes water as ammonium chloride solution with backwater in cooling during with the recovery electrolysis.Chlorine and hydrogen change liquid chlorine and liquid hydrogen into after distinguishing drying, compression, cooling again, are delivered to storage tank respectively.
To inject ammonia steaming system from the ammoniacal liquor that electrolyzer is drawn, use is steam heated to 100 ℃ and steams ammonia, and through cooling, gas-liquid separation, compression and cooling, it is standby to be transformed into liquid ammonia.The ammoniacal liquor that gas-liquid separation goes out enters ammonia steaming system again, uses as the ammonia still process stock liquid.Through ammonia still process weak ammonia later return the electrolytic solution preparation system and from chlorine, hydrogen cooling with backwater together as the configuration water of ammonium chloride solution.Unit consumption of energy: 2190 kilowatt-hour/tons, single electrolyzer throughput: 1.266 tons/hour.
Embodiment two.With the ammonium chloride solution input electrolyzer of the weight concentration 30% that configures, the instantaneous throughput of this design of electrolysis cells liquid chlorine is 10,000 tons/year, passes to the 2.5V direct current, and ammonium chloride solution is carried out electrolysis; Collect the chlorine that anode produces by gas trap, the hydrogen that negative electrode produces, and be introduced into chlorine treatment system and hydrogen treat system, the remained ammonia in the electrolyzer is introduced ammonia disposal system.
In chlorine treatment system and hydrogen treat system, use earlier water cooling chlorine and hydrogen respectively, to the sensible heat of chlorine and hydrogen, configuration makes water as ammonium chloride solution with backwater in cooling during with the recovery electrolysis.Chlorine and hydrogen change liquid chlorine and liquid hydrogen into after distinguishing drying, compression, cooling again, are delivered to storage tank respectively.
To inject ammonia steaming system from the ammoniacal liquor that electrolyzer is drawn, use is steam heated to 90 ℃ and steams ammonia, and through cooling, gas-liquid separation, compression and cooling, it is standby to be transformed into liquid ammonia.The ammoniacal liquor that gas-liquid separation goes out enters ammonia steaming system again, uses as the ammonia still process stock liquid.Through ammonia still process weak ammonia later return the electrolytic solution preparation system and from chlorine, hydrogen cooling with backwater together as the configuration water of ammonium chloride solution.Unit consumption of energy: 2089 kilowatt-hour/tons, single electrolyzer throughput: 1.14 tons/hour.
Embodiment three.With the ammonium chloride solution input electrolyzer of the weight concentration 25% that configures, the instantaneous throughput of this design of electrolysis cells liquid chlorine is 10,000 tons/year, passes to the 2.8V direct current, and ammonium chloride solution is carried out electrolysis; Collect the chlorine that anode produces by gas trap, the hydrogen that negative electrode produces, and be introduced into chlorine treatment system and hydrogen treat system, the remained ammonia in the electrolyzer is introduced ammonia disposal system.
In chlorine treatment system and hydrogen treat system, use earlier water cooling chlorine and hydrogen respectively, to the sensible heat of chlorine and hydrogen, configuration makes water as ammonium chloride solution with backwater in cooling during with the recovery electrolysis.Chlorine and hydrogen change liquid chlorine and liquid hydrogen into after distinguishing drying, compression, cooling again, are delivered to storage tank respectively.
To inject ammonia steaming system from the ammoniacal liquor that electrolyzer is drawn, use is steam heated to 80 ℃ and steams ammonia, and through cooling, gas-liquid separation, compression and cooling, it is standby to be transformed into liquid ammonia.The ammoniacal liquor that gas-liquid separation goes out enters ammonia steaming system again, uses as the ammonia still process stock liquid.Through ammonia still process weak ammonia later return the electrolytic solution preparation system and from chlorine, hydrogen cooling with backwater together as the configuration water of ammonium chloride solution.Unit consumption of energy: 2095 kilowatt-hour/tons, single electrolyzer throughput: 1.206 tons/hour.
Claims (4)
1, a kind of method of producing liquir nitrogen by using electrolysis process, two electrodes are set in electrolytic solution, feed direct supply, collect the chlorine of anode generation, the hydrogen that negative electrode produces, make liquid chlorine, liquid hydrogen after compressed respectively, the condensation, it is characterized in that electrolytic solution is the ammonium chloride solution of weight concentration 25-40%, power supply adopts the 2.5-3V direct supply.
2, the method for production liquid chlorine according to claim 1 is characterized in that obtaining ammonia, its cooling, compression, condensation being made liquefied ammonia being heated to 85-100 ℃ of evaporation under the remaining electrolytic solution normal pressure in the electrolyzer.
3, the method for production liquid chlorine according to claim 1 and 2 is characterized in that chlorine, hydrogen, ammonia compressed respectively and is cooled to that used cooling backwater is used for disposing ammonium chloride electrolytic solution in liquid chlorine, liquid hydrogen, the liquefied ammonia process.
4, the method for production liquid chlorine according to claim 1 and 2 is characterized in that the residue weak ammonia that residue electrolytic solution evaporation in the electrolyzer is produced in the liquefied ammonia process is reclaimed as configuration ammonium chloride electrolytic solution.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011082798A CN1168852C (en) | 2001-02-28 | 2001-02-28 | Method for producing liquir nitrogen by using electrolysis process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011082798A CN1168852C (en) | 2001-02-28 | 2001-02-28 | Method for producing liquir nitrogen by using electrolysis process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1321796A CN1321796A (en) | 2001-11-14 |
| CN1168852C true CN1168852C (en) | 2004-09-29 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011082798A Expired - Lifetime CN1168852C (en) | 2001-02-28 | 2001-02-28 | Method for producing liquir nitrogen by using electrolysis process |
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| Country | Link |
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| CN (1) | CN1168852C (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107201531B (en) * | 2017-04-27 | 2020-10-30 | 新疆中泰化学阜康能源有限公司 | Strong acid light salt water recycling device after chlorate decomposer decomposes in electrolysis process |
| CN109609971B (en) * | 2019-01-04 | 2019-12-31 | 北京神州瑞霖环境技术研究院有限公司 | Cation diaphragm electrolytic cell series device for removing carbon after electrolysis and application thereof |
| CN109468656B (en) * | 2019-01-04 | 2020-05-05 | 北京神州瑞霖环境技术研究院有限公司 | Cation diaphragm electrolytic cell series device for removing carbon before electrolysis and application thereof |
| CN111378984B (en) * | 2020-02-17 | 2021-08-20 | 北京科技大学 | Device and method for preparing chlorine and sodium hypochlorite by electrolyzing ammonium chloride wastewater |
-
2001
- 2001-02-28 CN CNB011082798A patent/CN1168852C/en not_active Expired - Lifetime
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| Publication number | Publication date |
|---|---|
| CN1321796A (en) | 2001-11-14 |
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Owner name: LIU XIAOXIANG Effective date: 20050812 Owner name: ZHAO XIANGHAI Free format text: FORMER OWNER: DEBANG CHEMICAL INDUSTRY GROUP CO. LTD., JIANGSU |
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Effective date of registration: 20050812 Address after: Room 2, unit 21, building 6, 401, neat Road, Sinpo District, Jiangsu, Lianyungang, 222001 Co-patentee after: Liu Xiaoxiang Patentee after: Zhao Xianghai Address before: 222023 No. 51, South South Road, Haizhou District, Jiangsu, Lianyungang Patentee before: Debang Chemical Industry Group Co., Ltd., Jiangsu |
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Free format text: FORMER OWNER: LIU XIAOXIANG Effective date: 20141020 Owner name: DEBANG CHEMICAL INDUSTRY GROUP CO. LTD., JIANGSU Free format text: FORMER OWNER: ZHAO XIANGHAI Effective date: 20141020 |
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Free format text: CORRECT: ADDRESS; FROM: 222001 LIANYUNGANG, JIANGSU PROVINCE TO: 222000 LIANYUNGANG, JIANGSU PROVINCE |
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Effective date of registration: 20141020 Address after: 222000 No. 51, South South Road, Haizhou District, Jiangsu, Lianyungang Patentee after: Debang Chemical Industry Group Co., Ltd., Jiangsu Address before: Room 2, unit 21, building 6, 401, neat Road, Sinpo District, Jiangsu, Lianyungang, 222001 Patentee before: Zhao Xianghai Patentee before: Liu Xiaoxiang |
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