CN101857246A - Process method for co-producing ammonium bicarbonate by using coking plant waste - Google Patents
Process method for co-producing ammonium bicarbonate by using coking plant waste Download PDFInfo
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- CN101857246A CN101857246A CN201010210311A CN201010210311A CN101857246A CN 101857246 A CN101857246 A CN 101857246A CN 201010210311 A CN201010210311 A CN 201010210311A CN 201010210311 A CN201010210311 A CN 201010210311A CN 101857246 A CN101857246 A CN 101857246A
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- 235000012538 ammonium bicarbonate Nutrition 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims abstract description 23
- 238000004939 coking Methods 0.000 title claims abstract description 13
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 title claims abstract description 9
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 title claims abstract description 9
- 239000001099 ammonium carbonate Substances 0.000 title claims abstract description 9
- 239000010908 plant waste Substances 0.000 title claims abstract description 8
- 239000007789 gas Substances 0.000 claims abstract description 37
- 239000002912 waste gas Substances 0.000 claims abstract description 14
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 13
- 239000000571 coke Substances 0.000 claims abstract description 10
- 239000003546 flue gas Substances 0.000 claims abstract description 7
- 238000005406 washing Methods 0.000 claims abstract description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 6
- 238000004821 distillation Methods 0.000 claims abstract description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 57
- 229910021529 ammonia Inorganic materials 0.000 claims description 27
- 239000012452 mother liquor Substances 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 13
- 239000000725 suspension Substances 0.000 claims description 10
- 239000002699 waste material Substances 0.000 claims description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 8
- 238000010521 absorption reaction Methods 0.000 claims description 7
- 238000004140 cleaning Methods 0.000 claims description 7
- 238000003672 processing method Methods 0.000 claims description 7
- 238000003860 storage Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 6
- 239000007787 solid Substances 0.000 claims description 6
- 239000002562 thickening agent Substances 0.000 claims description 5
- 241000282326 Felis catus Species 0.000 claims description 4
- 150000001718 carbodiimides Chemical class 0.000 claims description 4
- 238000003763 carbonization Methods 0.000 claims description 4
- 238000002203 pretreatment Methods 0.000 claims description 4
- 230000001839 systemic circulation Effects 0.000 claims description 4
- 235000011089 carbon dioxide Nutrition 0.000 claims description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 3
- 239000001569 carbon dioxide Substances 0.000 claims description 2
- 238000005119 centrifugation Methods 0.000 claims description 2
- 238000002425 crystallisation Methods 0.000 claims description 2
- 230000008025 crystallization Effects 0.000 claims description 2
- 239000010808 liquid waste Substances 0.000 claims description 2
- 238000012856 packing Methods 0.000 claims description 2
- 238000009656 pre-carbonization Methods 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- 238000010025 steaming Methods 0.000 claims description 2
- 239000012141 concentrate Substances 0.000 claims 1
- 239000002351 wastewater Substances 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 6
- 229910052799 carbon Inorganic materials 0.000 abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 25
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 8
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 8
- 235000011130 ammonium sulphate Nutrition 0.000 description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- 239000003337 fertilizer Substances 0.000 description 4
- HIVLDXAAFGCOFU-UHFFFAOYSA-N ammonium hydrosulfide Chemical compound [NH4+].[SH-] HIVLDXAAFGCOFU-UHFFFAOYSA-N 0.000 description 3
- 238000007689 inspection Methods 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 230000004087 circulation Effects 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 239000005696 Diammonium phosphate Substances 0.000 description 1
- JJEJDZONIFQNHG-UHFFFAOYSA-N [C+4].N Chemical compound [C+4].N JJEJDZONIFQNHG-UHFFFAOYSA-N 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 description 1
- 229910000388 diammonium phosphate Inorganic materials 0.000 description 1
- 235000019838 diammonium phosphate Nutrition 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000008234 soft water Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000003643 water by type Substances 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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- Industrial Gases (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a process method for co-producing ammonium bicarbonate by using coking plant waste, comprising the following steps: exchanging heat of flue gas in a coke oven flue channel to lower the temperature to 40-50 DEG C, absorbing and concentrating by a washing tower to obtain CO2 gas the volume concentration of which is 25%-28%, and lowering the temperature to below 35 DEG C; carrying out distillation pretreatment on coking plant waste ammonia water; and leading the pretreated strong ammonia water and CO2 gas into a synthetic tower to react to generate ammonium bicarbonate. In the invention, waste water and waste gas exhausted by coking industry are fully utilized to synthesize ammonium bicarbonate suitable for the growth of crops, the investment is low no matter a new factory is built or an old factory is transformed, the process is simple, convenient, mature and reliable, the cost is greatly reduced, and the method has higher economic yield. By the comprehensive utilization of waste gas and waste water, the pollution to atmosphere is significantly reduced, thus achieving the purposes of energy saving and emission reduction, being in line with the policy of developing low-carbon economy implemented by China currently, and having great social benefit.
Description
Technical field
The present invention relates to chemical field, relate in particular to the waste gas in the coking industry, the processing method of the solid-state bicarbonate of ammonia of waste water reclamation coproduction.
Background technology
In coke-oven plant's production process, discharge a large amount of waste gas more than 260 ℃ from coke oven flue, discharge a large amount of deposed ammonias in the ammonia still process process, wherein contain ammonia 10 grams in every cubic metre the deposed ammonia, containing volumetric concentration in the waste gas is the CO2 gas of 6-10%, and the environmental protection treatment of these deposed ammonias and waste gas is to hinder the bottleneck of coking industry development always.Deposed ammonia during the most of coke-oven plant of China produces and the CO in the coke-oven gas
2, gas such as N, directly be discharged in the atmosphere, do not reclaim, atmosphere and river are caused serious pollution.
For waste gas and the waste water of administering the coke-oven plant, domestic 95% above coke-oven plant adopts ammonium sulfate process, forms ammonium sulfate with the ammonia in the sulfuric acid absorption coal gas, adopts this technology to have following problem:
The one,, after synthetic production concentrated fertilizer occurred, the ammonium sulfate fertilizer efficiency that the coke-oven plant produces was low, of poor quality, seems inessential as agricultural fertilizer, and selling price is low, and product is at a discount substantially.
The 2nd,, ammonium sulfate production cost height, price is low, loses more than gain.To produce 600000 tons of coke per year is example, and the sulfuric acid consumption is 5153 tons/year, buys 650 yuan of sulfuric acid needs per ton, one ton of ammonium sulfate of every sale then about 500 yuan, the consumption of water power vapour, equipment amortization, productive expense in addition.Annual loss is counted roughly 3,000,000 yuan.
The 3rd,, the ammonium sulfate process investment in fixed assets is big, and only construction investment needs 3,000,000 yuan, and facility investment amounts to 1,300 ten thousand yuan in addition, gives the heavy fund obligation of enterprise's back.
Handle the disadvantage that coking plant waste brings in order to overcome ammonium sulfate process, a kind of anhydrous ammonia novel process has appearred, it is to generate diammonium phosphate with the ammonia that phosphoric acid absorbs in the coal gas, heat then absorbed ammonia is discharged, obtain the higher anhydrous ammonia of purity, the problem that this technology exists in popularization is a lot, mainly shows following several respects.
The one,, the general coke-oven plant of the liquid ammonia of being produced can not autodigestion, need be transported to fertilizer industry, dull sale.
The 2nd,, the distillation plant of production anhydrous ammonia, admission at the bottom of rectifying tower and the desorption tower requirement tower, pressure higher (more than the 1.8Mpa), general coke-oven plant existence conditions does not possess.
The 3rd,, though facility investment is lower than sulphur ammonium, production cost is higher, can only small profits production.
Summary of the invention
For solve the above-mentioned technical problem that existing coke-oven plant utilizes ammonium sulfate process and anhydrous ammonia technology to exist in handling the waste process, the invention provides a kind of waste gas in the coking industry and processing method of the solid-state bicarbonate of ammonia of waste water coproduction utilized.
For achieving the above object, processing method of the present invention is:
The first step: the flue gas pre-treatment in the coke oven chimney
260 ℃ of left and right sides flue gases in the coke oven flue are cooled to 40-50 ℃ with other with hot equipment heat exchange earlier, absorb, concentratedly obtain the CO that volumetric concentration is 25%-28% through washing tower again
2Gas, and be cooled to again below 35 ℃.
Second step: coke-oven plant's deposed ammonia is carried out pre-treatment
The deposed ammonia of coke-oven plant is obtained the strong aqua that volumetric concentration is 16-20% through distillation, and introducing synthetic tower top is stand-by.
The 3rd step: the CO that the strong aqua that utilized for second step obtained obtains the first step
2Gas absorbs
With the CO after the first step processing
2Gas is sent into synthetic tower from the bottom, in synthetic tower, be lower than under 35 ℃ of pressure conditions with 0.25-0.4Mpa from bottom to top fully to contact and generate the bicarbonate of ammonia solids suspension with strong aqua that second step obtained, suspension takes out from the tower bottom, through crystallization, centrifugation, obtain pure bicarbonate of ammonia finished product, isolated residue mother liquor enters next step and recycles, and the waste liquid after the carbonization enters next step recycling after discharging at the bottom of the tower;
The 4th step: the recovery of residue mother liquor and waste liquid
The waste liquid of discharging at the bottom of the tower enters ammonia-cleaning tower washing back ammoniacal liquor and enters systemic circulation again and use, and tail gas enters atmosphere; The residue mother liquor enters strong aqua that the synthetic tower in the 3rd step comes with cat head by pipeline and enters synthetic tower once more and circulate.
In order to improve ammoniacal liquor and CO
2Reaction efficiency in synthetic tower, the two-stage synthetic tower that described synthetic tower of the 3rd step forms for series connection, CO
2The concrete technical process of gas in the two-stage synthetic tower is:
The CO that the first step obtains
2Gas enters first step synthetic tower and second stage synthetic tower bottom, CO in first step synthetic tower respectively
2Gas fully contacts with the strong aqua that second step of coming from cat head obtains, the strong aqua absorbing carbon dioxide, formed pre-carbodiimide solution by pre-carbonization, discharge pre-carbodiimide solution from first step synthetic tower bottom, after the discharge again by being pumped into synthetic tower top, the second stage, further the carbonic acid gas in the absorption tower generates the bicarbonate of ammonia solids suspension.
Advantage of the present invention is:
1, the present invention utilizes the waste gas that is discharged in the atmosphere in the coke oven chimney that deposed ammonia is reclaimed, and has promptly utilized charking deposed ammonia, prevents the pollution to underground water and river, has reclaimed the CO that is discharged in the chimney in the atmosphere again
2, with CO
2Further utilize as raw material, prevented CO
2Discharging has reached the circulation comprehensive utilization to atmospheric pollution, and tangible economic benefit and social benefit are arranged.To produce 900000 tons coke-oven plant per year is example, owing to utilized waste gas, waste water co-producing ammonium bicarbonate, annual CO
2Reduction of discharging be 5000 ten thousand steres, amount to the pure CO of concentration more than 99%
2400 ten thousand steres (5570 tons).
2, adopt the technology of the present invention, less investment only accounts for ordinary method and produces 1/2 of sulphur ammonium investment, and technical process is simple, mature and reliable, and floor space is little, and benefit is obvious.For example: produce 1000000 tons of coke-oven plants per year, can 10000 tons of carbon ammoniums of supporting coproduction, 2,800,000 yuan (produce one ton of bicarbonate of ammonia and can have a net gain 280 yuan) of the profit of can making a profit.Produce 10000 tons per year and produce the sulphur ammonium, 3,300,000 yuan of year losss.
3, the CO of coke oven chimney
2Gas not only can be recycled, and the waste heat of coke oven flue gas can effectively utilize equally.According to thermodynamic (al) the 3rd law, to utilize the heat energy potential difference that about 260 ℃ flue gas is reclaimed by heat exchange and latent heat and can be used as ammonia still and other needed steam sources, basic substituting given birth to steam and saved energy consumption greatly, reduced cost.
In a word, the present invention makes full use of waste water and the synthetic carbon ammonium that is fit to crop growth of waste gas that coking industry is discharged, no matter build new factory or the transformation of old factory, investment is all lacked, and the easy mature and reliable of technology greatly reduces cost, has higher economic income rate.By comprehensive utilization to waste gas and waste water, less greatly to atmospheric pollution, reach the purpose of energy-saving and emission-reduction, meet current country-driven development low-carbon economy policy, have very big social benefit.
Description of drawings
Fig. 1 is a process flow sheet of the present invention.
Among the figure: 1,2-interchanger, 3-blower fan, 4-absorption tower, 5-thickener, the 6-gas storage holder, 7-compressor, 8, the 9-water circulating pump, 10,11, the 20-water cooling tower, 12,13-cold water pump, 14, the 15-synthetic tower, 16,17-examines tank, 18,19-refrigeration cycle water pump, 21,22-ammonia vessel, 23-water leg, 24, the 25-aqua ammonia pump, 26,27-mother liquor pump, the 28-ammonia-cleaning tower, 29-examines tank, 30-stiff device, 31-whizzer, the 32-hopper, 33-mother liquor tank, 34, the softening water pump of 35-, 36-demineralized water tank.
Embodiment
Further specify technical scheme of the present invention according to process flow sheet shown in Figure 1 below.
As can be seen from Figure 1:
The first step: about 260 ℃ waste gas process interchanger 1 and 2 from chimney heat exchange step by step is divided into two-way after being cooled to 40-50 ℃, one the tunnel directly enters gas storage holder 6 through blower fan 3, another road enters absorption tower 4 and washes attachedly, utilizes the natural pressure potential difference to enter thickener 5 heated and stirred, to promote CO
2Concentration, the high concentration CO that comes out from thickener 5
2Gas enters gas storage holder 6 and lower concentration CO
2Gas mixes stand-by;
Second step: liquid waste disposal process
Advancing distillation by the deposed ammonia of ammonia steaming system enters in ammonia vessel 21 and 22 stand-by;
The 3rd step: the CO in the gas storage holder 6
2Gas is introduced synthetic tower 14 and 15 bottoms by compressor 7, and the ammoniacal liquor in the ammonia vessel 21 and 22 is incorporated into synthetic tower 14 and 15 synthetic tower tops respectively by aqua ammonia pump 24 and 25, and as required, synthetic tower 14 and 15 can be realized parallel connection or series connection by valve; In synthetic tower, deposed ammonia and CO
2Gas fully contacts, generate the bicarbonate of ammonia solids suspension, suspension takes out from synthetic tower 14 and 15 bottoms, pump into high-order stiff device 30, utilize the nature potential difference to enter whizzer 31 and carry out solid-liquid separation, isolating xln be pure bicarbonate of ammonia finished product, the bicarbonate of ammonia finished product enters the outbounds of hopper 32 packing;
The 4th step: the thin liquid that parting liquid and stiff device overflow enters mother liquor tank 33, is delivered to synthetic tower top and the utilization of strong aqua mixed cycle by mother liquor pump 26 and 27.Waste liquid after the carbonization is discharged from synthetic tower 14 and 15 bottoms, enters water leg 23, and ammoniacal liquor enters the systemic circulation use again after ammonia-cleaning tower 28 washings, and tail gas enters atmosphere.
From figure, also can find out, interchanger 1 and 2 recirculated water by water circulating pump 8 and 9 and water cooling tower 10 supply with; The recirculated water on absorption tower 4 by cold water pump 12 and 13 and water cooling tower 11 supply with; Ammonia vessel 21 and 22 ammoniacal liquor pump into the synthetic tower top by aqua ammonia pump 24 and 25; Mother liquor in the mother liquor tank 33 pumps into synthetic tower with the deposed ammonia recycle by mother liquor pump 26 and 27; The recirculated water of ammonia-cleaning tower 28 and synthetic tower by refrigeration cycle water pump 18 and 19 and water cooling tower 20 supply with; All recirculated waters pump into circulating water system from demineralized water tank 36 by soft water water pump 34 and 35.Be respectively equipped with inspection tank 16 and 17 on the synthetic tower 14 and the 15 circulation mouths of a river, ammonia-cleaning tower 28 circulating water outlets are provided with inspection tank 29, and the purpose that the inspection tank is set is to detect water temperature and leak source, enter water cooling tower after the condensation water outlet is concentrated.
Claims (3)
1. processing method of utilizing the coking plant waste co-producing ammonium bicarbonate is characterized in that processing step is as follows:
The first step: the flue gas pre-treatment in the coke oven chimney
Flue gas heat exchange in the coke oven flue is cooled to 40-50 ℃, absorbs, concentrate that to obtain volumetric concentration be 25%28% CO again through washing tower
2Gas, and be cooled to again below 35 ℃;
Second step: coke-oven plant's deposed ammonia is carried out pre-treatment
The deposed ammonia of coke-oven plant is obtained the strong aqua that volumetric concentration is 16-20% through distillation, and introducing synthetic tower top is stand-by;
The 3rd step: the CO that the strong aqua that utilized for second step obtained obtains the first step
2Gas absorbs
With the CO after the first step processing
2Gas is sent into synthetic tower from the bottom, in synthetic tower, be lower than under 35 ℃ of pressure conditions with 0.25-0.4Mpa from bottom to top fully to contact and generate the bicarbonate of ammonia solids suspension with strong aqua that second step obtained, suspension takes out from the tower bottom, through crystallization, centrifugation, obtain pure bicarbonate of ammonia finished product, isolated residue mother liquor enters next step and recycles, and the waste liquid after the carbonization enters next step recycling after discharging at the bottom of the tower;
The 4th step: the recovery of residue mother liquor and waste liquid
The waste liquid of discharging at the bottom of the tower enters ammonia-cleaning tower washing back ammoniacal liquor and enters systemic circulation again and use, and tail gas enters atmosphere; The residue mother liquor enters strong aqua that the synthetic tower in the 3rd step comes with cat head by pipeline and enters synthetic tower once more and circulate.
2. the processing method of utilizing the coking plant waste co-producing ammonium bicarbonate as claimed in claim 1 is characterized in that, the two-stage synthetic tower that described synthetic tower of the 3rd step forms for series connection, CO
2The concrete technical process of gas in the two-stage synthetic tower is:
The CO that the first step obtains
2Gas enters first step synthetic tower and second stage synthetic tower bottom, CO in first step synthetic tower respectively
2Gas fully contacts with the strong aqua that second step of coming from cat head obtains, the strong aqua absorbing carbon dioxide, formed pre-carbodiimide solution by pre-carbonization, discharge pre-carbodiimide solution from first step synthetic tower bottom, after the discharge again by being pumped into synthetic tower top, the second stage, further the carbonic acid gas in the absorption tower generates the bicarbonate of ammonia solids suspension.
3. the processing method of utilizing the coking plant waste co-producing ammonium bicarbonate as claimed in claim 1 is characterized in that processing step is as follows:
The first step: from chimney come waste gas through interchanger step by step heat exchange be divided into two-way after being cooled to 40-50 ℃, the one tunnel directly enters gas storage holder through blower fan, another road enters the absorption tower and washes attachedly, utilizes the natural pressure potential difference to enter the thickener heated and stirred, to promote CO
2Concentration, the high concentration CO that comes out from thickener
2Gas enters gas storage holder and lower concentration CO
2Gas mixes stand-by;
Second step: liquid waste disposal process
Advancing distillation by the deposed ammonia of ammonia steaming system enters in the ammonia vessel stand-by;
The 3rd step: the CO in the gas storage holder 6
2Gas is introduced the synthetic tower bottom by compressor, and the ammoniacal liquor in the ammonia vessel is incorporated into synthetic tower synthetic tower top respectively by aqua ammonia pump; In synthetic tower, deposed ammonia and CO
2Gas fully contacts, and generates the bicarbonate of ammonia solids suspension, and suspension takes out from the synthetic tower bottom, pump into high-order stiff device, utilize the nature potential difference to enter whizzer and carry out solid-liquid separation, isolating xln be pure bicarbonate of ammonia finished product, the bicarbonate of ammonia finished product enters the outbound of hopper packing;
The 4th step: the thin liquid that mother liquor of separating and stiff device overflow enters mother liquor tank, is utilized by mother liquor pump delivery to synthetic tower top and strong aqua mixed cycle; Waste liquid after the carbonization is discharged from the synthetic tower bottom, and ammoniacal liquor enters the systemic circulation use again after the ammonia-cleaning tower washing, and tail gas enters atmosphere.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102502706A (en) * | 2011-11-03 | 2012-06-20 | 兖州煤业榆林能化有限公司 | Method for reclaiming ammonium hydrogen carbonate from non-condensable gas of stripping tower |
| CN102602960A (en) * | 2012-03-23 | 2012-07-25 | 济南冶金化工设备有限公司 | Method for stilling ammonia by aid of waste heat of flue gas of coke oven and equipment |
| CN105905923A (en) * | 2016-04-19 | 2016-08-31 | 成都成钢梅塞尔气体产品有限公司 | A method of producing ammonium bicarbonate by adopting carbon dioxide in boiler tail gas |
| CN105944526A (en) * | 2016-06-12 | 2016-09-21 | 晏廷书 | Low-temperature desulfurization, decarburization and denitration technique achieved by means of residual ammonia liquid and compound solution |
| CN107200607A (en) * | 2017-06-20 | 2017-09-26 | 山东金沂蒙生态肥业有限公司 | A kind of production method of the poly- member fertilizer of carbon sequestration fixed nitrogen nanometer |
| CN108128787A (en) * | 2018-01-13 | 2018-06-08 | 安徽金禾实业股份有限公司 | A kind of ammonium hydrogen carbonate recrystallization production method |
| CN113461029A (en) * | 2021-08-09 | 2021-10-01 | 山西长林能源科技有限公司 | Method and equipment for preparing ammonium bicarbonate by using flue waste gas and coke oven gas |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102502706A (en) * | 2011-11-03 | 2012-06-20 | 兖州煤业榆林能化有限公司 | Method for reclaiming ammonium hydrogen carbonate from non-condensable gas of stripping tower |
| CN102602960A (en) * | 2012-03-23 | 2012-07-25 | 济南冶金化工设备有限公司 | Method for stilling ammonia by aid of waste heat of flue gas of coke oven and equipment |
| CN102602960B (en) * | 2012-03-23 | 2014-03-19 | 济南冶金化工设备有限公司 | Method for stilling ammonia by aid of waste heat of flue gas of coke oven and equipment |
| CN105905923A (en) * | 2016-04-19 | 2016-08-31 | 成都成钢梅塞尔气体产品有限公司 | A method of producing ammonium bicarbonate by adopting carbon dioxide in boiler tail gas |
| CN105905923B (en) * | 2016-04-19 | 2018-03-27 | 四川梅塞尔气体产品有限公司 | Using the method for the carbon dioxide production ammonium hydrogencarbonate in boiler exhaust gas |
| CN105944526A (en) * | 2016-06-12 | 2016-09-21 | 晏廷书 | Low-temperature desulfurization, decarburization and denitration technique achieved by means of residual ammonia liquid and compound solution |
| CN107200607A (en) * | 2017-06-20 | 2017-09-26 | 山东金沂蒙生态肥业有限公司 | A kind of production method of the poly- member fertilizer of carbon sequestration fixed nitrogen nanometer |
| CN108128787A (en) * | 2018-01-13 | 2018-06-08 | 安徽金禾实业股份有限公司 | A kind of ammonium hydrogen carbonate recrystallization production method |
| CN108128787B (en) * | 2018-01-13 | 2021-04-23 | 安徽金禾实业股份有限公司 | Ammonium bicarbonate recrystallization production method |
| CN113461029A (en) * | 2021-08-09 | 2021-10-01 | 山西长林能源科技有限公司 | Method and equipment for preparing ammonium bicarbonate by using flue waste gas and coke oven gas |
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| CN101857246B (en) | 2012-09-05 |
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