CN102502716B - Technology for cooling ammonia mother liquor I in crystallizing working section during combined soda producing process - Google Patents
Technology for cooling ammonia mother liquor I in crystallizing working section during combined soda producing process Download PDFInfo
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- CN102502716B CN102502716B CN2011103547609A CN201110354760A CN102502716B CN 102502716 B CN102502716 B CN 102502716B CN 2011103547609 A CN2011103547609 A CN 2011103547609A CN 201110354760 A CN201110354760 A CN 201110354760A CN 102502716 B CN102502716 B CN 102502716B
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- mother liquor
- ammonia
- cold
- heat exchange
- crystallizer
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 197
- 239000012452 mother liquor Substances 0.000 title claims abstract description 107
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 98
- 238000000034 method Methods 0.000 title claims abstract description 34
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 title claims abstract description 24
- 238000001816 cooling Methods 0.000 title claims abstract description 14
- 238000005516 engineering process Methods 0.000 title abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000013078 crystal Substances 0.000 claims abstract description 6
- 238000002425 crystallisation Methods 0.000 claims description 25
- 230000008025 crystallization Effects 0.000 claims description 25
- 238000005185 salting out Methods 0.000 claims description 12
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 claims description 8
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 6
- 235000019270 ammonium chloride Nutrition 0.000 claims description 4
- 238000004458 analytical method Methods 0.000 claims description 4
- 239000002826 coolant Substances 0.000 claims description 4
- 238000001556 precipitation Methods 0.000 claims description 4
- 238000005086 pumping Methods 0.000 claims description 4
- 239000010413 mother solution Substances 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- 239000011780 sodium chloride Substances 0.000 claims description 3
- 238000007710 freezing Methods 0.000 abstract description 5
- 230000008014 freezing Effects 0.000 abstract description 5
- 150000003839 salts Chemical class 0.000 abstract description 3
- 239000002002 slurry Substances 0.000 abstract 2
- 239000002562 thickening agent Substances 0.000 abstract 2
- 235000017550 sodium carbonate Nutrition 0.000 description 6
- 229910000029 sodium carbonate Inorganic materials 0.000 description 6
- 239000003513 alkali Substances 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 235000021050 feed intake Nutrition 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
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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
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- Sorption Type Refrigeration Machines (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A technology for cooling ammonia mother liquor I in a crystallizing working section during a combined soda producing process is characterized by comprising the following steps that: hot ammonia mother liquor I is sent to a water cooler, the heat of the hot ammonia mother liquor I is exchanged and the temperature of the hot ammonia mother liquor I is reduced; the ammonia mother liquor I exchanges heat with mother liquor II through a mother liquor heat exchanger; the ammonia mother liquor I is sent to an ammonia mother liquor I crystallizer and an ammonia mother liquor I heat exchanger and exchanges heat with cold mother liquor II; the ammonia mother liquor I returns to an ammonia mother liquor I crystallizer through a collecting trough, overflows to a cold ammonia mother liquor I barrel, is sent to a cold separating crystallizer and to an external cooler, and exchanges heat with liquid ammonia; after the heat exchange, the ammonia mother liquor I returns to the cold separating crystallizer through the collecting trough; crystal slurry is sent to a cold separating thickener and a salt separating crystallizer; the separated crystal slurry is sent to a salt separating thickener; overflowing cold mother liquor II exchanges heat with the ammonia mother liquor I to obtain the mother liquor II; the obtained mother liquor II exchanges heat with the ammonia mother liquor I; and the mother liquor II after being subjected to the heat exchange is sent to an ammonia absorbing system. The technology for cooling the ammonia mother liquor I in the crystallizing working section during the combined soda producing process is a low-temperature AI cooling technology, which makes full use of high-quality low-temperature cold to reduce a freezing load of the system so as to fulfill an aim of saving energy; and the problem that the heat exchanger is easily blocked by crystallized AI because of too low temperature of the AI is solved.
Description
Technical field
The present invention relates to a kind of the present invention is the ammonia I of crystallization workshop section mother liquor process for cooling in a kind of the alkaline process soda ash production technique, particularly a kind of procedure of producing soda under joint alkaline process.
Background technology
Crystallization Procedure is in traditional soda ash production process: the hot AI of self-priming ammonia send water-cooled and water coolant heat exchange in the future earlier, the AI temperature is down to 38 ~ 40 ℃ after the heat exchange, change (about 4 ~ 6) through one group of mother again, the AI temperature is down to 26 ~ 28 ℃ after the heat exchange, feed intake with cold AI and to be pumped to cool crystallizer, beat cold AI by propeller pump and go outer cooler and liquefied ammonia heat exchange, cold AI after the heat exchange returns cool crystallizer through aggregate groove, take out magma by the cool crystallizer middle part and send cold analysis stiff device, the cool crystallizer overflow precipitation and crystallization device that desalts, salting-out crystallizer is further separated out ammonium chloride crystals by utilizing common-ion effcet with salt, is taken out by the salting-out crystallizer middle part and send the stiff device of saltouing, salting-out crystallizer overflows back cold female II bucket, be pumped to mother with cold female II and change the heat exchange with AI, the female II bucket of the female II backheat after the heat exchange removes to inhale ammonia with hot female II pumping.There is following defective in this crystallization process for cooling: cold AI feed temperature is higher, certainly will increase the freezing load of system, can not utilize the low level cold effectively and reasonably, increases the ice maker load of refrigeration system, has strengthened facility investment and the maintenance expense of system; Owing to increased the freezing load of system, certainly will increase the mass consumption of working cost, the especially energy of system.Calculate with 300,000 tons/year soda ash throughput, needing increases by 3 500,000 Kcal/h ice makers, about 500,000 yuan, therefore increases by 1,500,000 yuan of costs of equipment with every expense; Calculate with 300,000 tons/year soda ash throughput, the system energy consumption increase is bigger, and soda ash ton alkali power consumption is higher, about 250KW.h/ ton alkali.
Summary of the invention
Technical problem to be solved by this invention is at the deficiencies in the prior art, and the ammonia I of crystallization workshop section mother liquor (AI) process for cooling in a kind of procedure of producing soda under joint alkaline process new, that can reduce system's freezing load, minimizing facility investment expense and energy consumption is provided.
Technical problem to be solved by this invention is to realize by following technical scheme.The present invention is the ammonia I of crystallization workshop section mother liquor process for cooling in a kind of procedure of producing soda under joint alkaline process, is characterized in that its step is as follows:
(1) the hot ammonia I mother liquor of elder generation's self-priming ammonia in future send water cooler and water coolant heat exchange, after ammonia I mother liquor temperature is down to 38 ~ 40 ℃, then through one group of mother liquor interchanger and mother liquor II heat exchange, ammonia I mother liquor temperature is down to 26 ~ 28 ℃, deliver to ammonia I mother liquor crystallization device again, by first propeller pump ammonia I mother liquor is squeezed into ammonia I mother liquor interchanger and cold female II heat exchange, the ammonia I mother liquor after the heat exchange returns through first aggregate groove and gets 23 ~ 24 ℃ cold ammonia I mother liquor in the ammonia I mother liquor crystallization device; Cold ammonia I mother liquor overflows to the cold ammonia I mother vat from ammonia I mother liquor crystallization device, with the cold ammonia I mother liquor pump that feeds intake cold ammonia I mother liquor is delivered to cool crystallizer, deliver to outer cooler and liquefied ammonia heat exchange by second propeller pump again, 9 ~ 11 ℃ of cold ammonia I mother liquors that obtain after the heat exchange return cool crystallizer through second aggregate groove;
(2) take out magma from the cool crystallizer middle part and send cold analysis stiff device, the cool crystallizer overflow precipitation and crystallization device that desalts, in salting-out crystallizer, add an amount of NaCl, utilize common-ion effcet, further separate out ammonium chloride crystals, take out magma from the salting-out crystallizer middle part and send the stiff device of saltouing, the salting-out crystallizer overflow is to cold female II bucket, with pump cold female II is delivered to ammonia I mother liquor interchanger, the 3rd propeller pump that connects on the ammonia I mother liquor interchanger is with cold female II and the heat exchange of ammonia I Recycling Mother Solution, reduce ammonia I mother liquor temperature, improve cold female II temperature simultaneously, the mother liquor II that obtains after the heat exchange delivers to mother liquor interchanger and the heat exchange of ammonia I mother liquor, and the mother liquor II after the heat exchange delivers to mother liquor II bucket, and mother liquor II goes to inhale ammonia system by pumping.
In the above-described procedure of producing soda under joint alkaline process in the ammonia I of the crystallization workshop section mother liquor process for cooling technical scheme: described one group of mother liquor interchanger is preferably connected to form by 3-5 interchanger, is most preferably connected to form by 4 interchanger.
Technology compares experiment according to the present invention, and save energy is calculated as follows: calculate with 300,000 tons/year soda ash throughput widely, technology on year-on-year basis, can reduce by 3 500,000 Kcal/h ice makers, therefore every expense reduces 1,500,000 yuan of costs of equipment about 500,000 yuan; The power of motor of 500,000 Kcal/h ice makers is 250KW, and with 0.6 yuan of calculating of every degree electricity, then three 500,000 Kcal/h ice makers can reduce 3,600,000 yuan of the electricity charge every year.
Compared with prior art, the present invention has the following advantages: the present invention adopts AI subcooling technology, takes full advantage of high-grade low temperature cold, accomplish the reasonable utilization of cold, reduction system freezing load reaches the purpose of save energy, has greatly saved industrial cost.Solve simultaneously cold AI temperature again and crossed the problem that interchanger is stopped up in low easy crystallization.
Description of drawings
Fig. 1 is a kind of structural representation of the present invention.
Embodiment
Following with reference to accompanying drawing, further describe concrete technical scheme of the present invention, so that those skilled in the art understands the present invention further, and do not constitute the restriction to its right.
Embodiment 1, with reference to Fig. 1, and the ammonia I of crystallization workshop section mother liquor process for cooling in a kind of procedure of producing soda under joint alkaline process, its step is as follows:
(1) the hot ammonia I mother liquor of elder generation's self-priming ammonia in future send water cooler 1 and water coolant heat exchange, after ammonia I mother liquor temperature is down to 38 ~ 40 ℃, then through one group of mother liquor interchanger 2 and mother liquor II heat exchange, ammonia I mother liquor temperature is down to 26 ~ 28 ℃, deliver to ammonia I mother liquor crystallization device 3 again, by first propeller pump 4 ammonia I mother liquor is squeezed into ammonia I mother liquor interchanger 5 and cold female II heat exchange, the ammonia I mother liquor after the heat exchange returns through first aggregate groove 6 and gets 23 ~ 24 ℃ cold ammonia I mother liquor in the ammonia I mother liquor crystallization device 3; Cold ammonia I mother liquor overflows to the cold ammonia I mother vat 7 from ammonia I mother liquor crystallization device 3, with the cold ammonia I mother liquor pump 8 that feeds intake cold ammonia I mother liquor is delivered to cool crystallizer 9, deliver to outer cooler 10 and liquefied ammonia heat exchange by second propeller pump 11 again, 9 ~ 11 ℃ of cold ammonia I mother liquors that obtain after the heat exchange return cool crystallizer 9 through second aggregate groove 12;
(2) take out magma from cool crystallizer 9 middle parts and send cold analysis stiff device, the cool crystallizer 9 overflows precipitation and crystallization device 13 that desalts, in salting-out crystallizer 13, add an amount of NaCl, utilize common-ion effcet, further separate out ammonium chloride crystals, take out magma from salting-out crystallizer 13 middle parts and send the stiff device of saltouing, salting-out crystallizer 13 overflows are to cold female II bucket 14, with pump cold female II is delivered to ammonia I mother liquor interchanger 5, the 3rd propeller pump 15 that connects on the ammonia I mother liquor interchanger 5 is with cold female II and the heat exchange of ammonia I Recycling Mother Solution, reduce ammonia I mother liquor temperature, improve cold female II temperature simultaneously, the mother liquor II that obtains after the heat exchange delivers to mother liquor interchanger 2 and the heat exchange of ammonia I mother liquor, and the mother liquor II after the heat exchange delivers to mother liquor II bucket 16, and mother liquor II goes to inhale ammonia system by pumping.
Claims (2)
1. the ammonia I of crystallization workshop section mother liquor process for cooling in the procedure of producing soda under joint alkaline process is characterized in that its step is as follows:
(1) the hot ammonia I mother liquor of elder generation's self-priming ammonia in future send water cooler (1) and water coolant heat exchange, after ammonia I mother liquor temperature is down to 38 ~ 40 ℃, then through one group of mother liquor interchanger (2) and mother liquor II heat exchange, ammonia I mother liquor temperature is down to 26 ~ 28 ℃, deliver to ammonia I mother liquor crystallization device (3) again, by first propeller pump (4) ammonia I mother liquor is squeezed into ammonia I mother liquor interchanger (5) and cold female II heat exchange, the ammonia I mother liquor after the heat exchange returns through first aggregate groove (6) and gets 23 ~ 24 ℃ cold ammonia I mother liquor in the ammonia I mother liquor crystallization device (3); Cold ammonia I mother liquor overflows to the cold ammonia I mother vat (7) from ammonia I mother liquor crystallization device (3), with the cold ammonia I mother liquor pump (8) that feeds intake cold ammonia I mother liquor is delivered to cool crystallizer (9), deliver to outer cooler (10) and liquefied ammonia heat exchange by second propeller pump (11) again, 9 ~ 11 ℃ of cold ammonia I mother liquors that obtain after the heat exchange return cool crystallizer (9) through second aggregate groove (12);
(2) take out magma from cool crystallizer (9) middle part and send cold analysis stiff device, cool crystallizer (9) the overflow precipitation and crystallization device (13) that desalts, in salting-out crystallizer (13), add an amount of NaCl, utilize common-ion effcet, further separate out ammonium chloride crystals, take out magma from salting-out crystallizer (13) middle part and send the stiff device of saltouing, salting-out crystallizer (13) overflow is to cold female II bucket (14), with pump cold female II is delivered to ammonia I mother liquor interchanger (5), the 3rd propeller pump (15) that connects on the ammonia I mother liquor interchanger (5) is with cold female II and the heat exchange of ammonia I Recycling Mother Solution, reduce ammonia I mother liquor temperature, improve cold female II temperature simultaneously, the mother liquor II that obtains after the heat exchange delivers to mother liquor interchanger (2) and the heat exchange of ammonia I mother liquor, and the mother liquor II after the heat exchange delivers to mother liquor II bucket (16), and mother liquor II goes to inhale ammonia system by pumping.
2. the ammonia I of crystallization workshop section mother liquor process for cooling in the procedure of producing soda under joint alkaline process according to claim 1, it is characterized in that: described one group of mother liquor interchanger (2) is connected to form by 3-5 interchanger.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011103547609A CN102502716B (en) | 2011-11-10 | 2011-11-10 | Technology for cooling ammonia mother liquor I in crystallizing working section during combined soda producing process |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011103547609A CN102502716B (en) | 2011-11-10 | 2011-11-10 | Technology for cooling ammonia mother liquor I in crystallizing working section during combined soda producing process |
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| CN102502716A CN102502716A (en) | 2012-06-20 |
| CN102502716B true CN102502716B (en) | 2013-08-07 |
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Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102942195A (en) * | 2012-11-23 | 2013-02-27 | 湖北双环科技股份有限公司 | Method for improving production capacity of crystallizer for co-production of ammonium chloride and soda ash |
| CN105698427B (en) * | 2016-02-15 | 2017-12-08 | 赵祥海 | Workshop section's lithium bromide refrigerating cooling and the hot ammonia I mother liquors cleaning device of Outer Cooler and method are crystallized in procedure of producing soda under joint alkaline process |
| CN106276982A (en) * | 2016-10-19 | 2017-01-04 | 中盐昆山有限公司 | Soda and sociation center novel environment friendly circulation technology system and method |
| CN107585778A (en) * | 2017-10-15 | 2018-01-16 | 赵祥海 | Salting-out crystallizer outer loop cool-down method in procedure of producing soda under joint alkaline process |
| CN108147434B (en) * | 2017-12-07 | 2019-11-15 | 新奥泛能网络科技股份有限公司 | Join alkali system |
| CN108584990A (en) * | 2018-06-09 | 2018-09-28 | 连云港市擎天德邦科技发展有限公司 | Crystal external condensation device circulator and method in procedure of producing soda under joint alkaline process |
| CN110921685A (en) * | 2019-11-26 | 2020-03-27 | 连云港市福源德邦科技发展有限公司 | Crystallization reverse material flow device and method in combined-soda-process soda ash production process |
| CN111481959A (en) * | 2020-05-29 | 2020-08-04 | 连云港市福源德邦科技发展有限公司 | Crystallization external cooler circulating device and method in combined soda production process |
| CN116332204A (en) * | 2023-04-17 | 2023-06-27 | 重庆和友实业股份有限公司 | Improved method for producing sodium carbonate |
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| CN100404421C (en) * | 2006-06-27 | 2008-07-23 | 山东联合化工股份有限公司 | Process for combined production of melamine, sodium carbonate, and ammonium chloride |
| CN100590073C (en) * | 2008-04-30 | 2010-02-17 | 何淼 | 'Non-combined-soda process' production process for producing soda, ammonium chloride with melamine tail gas |
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Effective date of registration: 20180713 Address after: 222000 108, Tongguan South Road, Haizhou District, Lianyungang, Jiangsu. Patentee after: Lianyungang prime state science and Technology Development Co., Ltd. Address before: 222000 Zhu Aimin, Haizhou relocation Technology Department, No. 51 Jianghua North Road, Haizhou District, Lianyungang. Co-patentee before: Zhu Aimin Patentee before: Zhao Xianghai |
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Address after: 222000 108, Tongguan South Road, Haizhou District, Lianyungang, Jiangsu. Patentee after: Lianyungang Fuyuan Debon Technology Development Co., Ltd. Address before: 222000 108, Tongguan South Road, Haizhou District, Lianyungang, Jiangsu. Patentee before: Lianyungang prime state science and Technology Development Co., Ltd. |
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