CN104726141A - Method for ammonia removal of coke oven gas - Google Patents
Method for ammonia removal of coke oven gas Download PDFInfo
- Publication number
- CN104726141A CN104726141A CN201510140324.XA CN201510140324A CN104726141A CN 104726141 A CN104726141 A CN 104726141A CN 201510140324 A CN201510140324 A CN 201510140324A CN 104726141 A CN104726141 A CN 104726141A
- Authority
- CN
- China
- Prior art keywords
- coke
- oven gas
- mother liquor
- ammonia
- saturex
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/103—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkali- or earth-alkali- or NH4 salts or inorganic acids derived from sulfur
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
- C01C1/242—Preparation from ammonia and sulfuric acid or sulfur trioxide
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
Abstract
The invention discloses a method for ammonia removal of a coke oven gas. According to the method, on the basis of the existing production process method, residual ammonia water is used for cooling ammonia distillation wastewater, which is generated by an ammonia still, to 55-65 DEG C in a first heat exchanger, and then the cooled ammonia distillation wastewater is used as new water delivered into a saturator to prepare a mother solution. Because the temperature of the added ammonia distillation wastewater is close to that of the mother solution in the saturator, the temperature of the mother solution cannot be greatly influenced after the ammonia distillation wastewater is added into the mother solution, and the temperature of the mother solution always fluctuates up and down in a reasonable range of set values, thereby ensuring the normal and stable production of an ammonia removal process of the coke oven gas; and the ammonia distillation wastewater is used for replacing middle-temperature water or low-temperature water and the like to serve as the new water supplemented into the mother solution, so that the new water consumption of the ammonia removal process is reduced, and the repeated utilization of the ammonia distillation wastewater is realized at the same time.
Description
Technical field
The present invention relates to fine purification technique for coke oven gas technical field, especially relate to a kind of coke-oven gas deamination method.
Background technology
Coke-oven gas, refers to and several bituminous coal is mixed with coking coal, and in pit kiln after high temperature carbonization, a kind of inflammable gas produced while the products such as output coke and tar is the byproduct of coking industry.The main component of coke-oven gas is the gases such as water vapour, hydrogen, methane, tar gas, benzene vapour, naphthalene steam, ammonia, carbon monoxide, carbonic acid gas, hydrogen sulfide, prussic acid.
Along with the raising of environmental requirement, need to carry out purifying treatment to the coke-oven gas of pit kiln output, remove the various impurity such as hydrogen sulfide wherein, prussic acid, ammonia, tar and naphthalene, make it to reach country or industry standard, supply industry or civilian users use; Meanwhile, above-mentioned impurity is recycled with the form of chemical by-product.
In process of coking, the most of the nitrogen in coal enters coke-oven gas with the form of ammonia; In desulfurization process, with ammonia as after alkali source desulfurization, excessive ammonia can enter subsequent handling with coke-oven gas.Because ammonia has certain toxicity, corrodibility and have the smell of pungency stench, needed the ammonia in coke-oven gas to remove before coke-oven gas supply industry or civilian users use.At present, in industrial production, coke-oven gas deamination technique many employings saturex method, in saturex, mother liquor and coke-oven gas move toward one another, utilize the sulfuric acid in mother liquor to be absorbed by the ammonia in coke-oven gas, generate ammonium sulfate.The ammonium sulfate generated is dissolved in mother liquor, and regular extracting part decomposition mother solution is sent to production ammonium sulfate.
In deamination process, mother liquor, owing to the reason such as to carry secretly by thermal evaporation, product, inevitably causes partial loss, cause mother liquor volume to reduce and acidity unstable, need the new water of regular replenishment and acid to maintain mother liquor volume and acidity is stable.At present, the middle warm water in new water many employings production system or water at low temperature.In production process, mother liquor temperature need maintain 45 DEG C ~ 55 DEG C, and middle warm water is about 30 DEG C, water at low temperature is about 18 DEG C, and the two temperature is all far below mother liquor temperature, mother liquor temperature is caused to decline by a big margin after adding mother liquor, reduce the specific absorption of mother liquor to ammonia in coal gas, reduce the percent crystallization in massecuite of ammonium sulfate, the normal table having had a strong impact on whole deamination operation is produced, the new water of at substantial, causes production cost higher simultaneously.
Therefore, how to provide with the new water of its temperature close and the usage quantity reducing new water is the technical problem that current those skilled in the art need solution badly to mother liquor.
Summary of the invention
In view of this, the object of this invention is to provide a kind of coke-oven gas deamination method, the present invention can provide the new water with its temperature close to mother liquor, and the usage quantity of new water can be reduced, thus avoid deamination operation normal table being produced to the impact caused because new water temp is lower, save a large amount of new water simultaneously, reduce production cost.
For solving above-mentioned technical problem, technical scheme provided by the invention is:
A kind of coke-oven gas deamination method, comprises the following steps:
1) by Recycling Mother Solution pump, the mother liquor bottom saturex is delivered to saturex top, from up to down sprays;
2) coke-oven gas enters saturex by the entrance on saturex sidewall, bottom-up motion;
3) coke-oven gas and mother liquor move toward one another, fully contact, and the sulfuric acid in mother liquor is by the NH in coke-oven gas
3absorb, generate ammonium sulfate, the coke-oven gas after deamination is discharged from saturex top, and enter follow-up final cooling process, mother liquor flows back to bottom saturex;
4) remained ammonia is sent to ammonia still ammonia still process, output distilled ammonia wastewater after First Heat Exchanger heats up;
5) by step 4) distilled ammonia wastewater of output toward First Heat Exchanger, utilizes remained ammonia distilled ammonia wastewater to be cooled to 55 DEG C ~ 65 DEG C by distilled ammonia wastewater pumping in First Heat Exchanger;
6) using step 5) cooled distilled ammonia wastewater as new water deliver to saturex preparation mother liquor;
7) production ammonium sulfate is sent to by crystallization pump extracting part decomposition mother solution.
Preferably, described step 1) in the temperature of mother liquor bottom saturex be 45 DEG C ~ 55 DEG C.
Preferably, described step 1) in the liquid-gas ratio of mother liquor bottom saturex be 15L/m
3~ 30L/m
3.
Preferably, described step 1) in the acidity of mother liquor bottom saturex be 5% ~ 6%.
Preferably, the temperature that enters of described coke-oven gas is 50 DEG C ~ 65 DEG C, and outflow temperature is 45 DEG C ~ 55 DEG C, and ammonia quantity is 40mg/m
3~ 60mg/m
3.
Preferably, described step 6) in the distilled ammonia wastewater amount filled in mother liquor be 10m
3/ time ~ 15m
3/ time, flow is 0.3m
3/ h ~ 0.5m
3/ h.
Preferably, by described step 6) in remaining distilled ammonia wastewater through second interchanger cooling after be sent to biological phenol removal process, the temperature of described second heat exchanger exit distilled ammonia wastewater is 25 DEG C ~ 40 DEG C.
Preferably, described First Heat Exchanger and the second interchanger are plate-type heat exchanger.
Compared with prior art, the present invention has following Advantageous Effects:
(1). utilize remained ammonia in First Heat Exchanger, distilled ammonia wastewater is cooled to saturex bottom the close temperature of mother liquor, then cooled distilled ammonia wastewater is delivered to saturex preparation mother liquor as new water, because in the temperature of added distilled ammonia wastewater and saturex, the temperature of mother liquor is close, can not affect greatly mother liquor temperature after being added to mother liquor, mother liquor temperature is fluctuated in the zone of reasonableness of set(ting)value, thus ensure that coke-oven gas deamination operation normal table is produced.
(2). in replacing with distilled ammonia wastewater, warm water or water at low temperature etc. fill in mother liquor as new water, decrease the new water consumption of deamination operation, achieve the recycling of distilled ammonia wastewater simultaneously.
(3). part distilled ammonia wastewater is filled into mother liquor, decreases the distilled ammonia wastewater amount being sent to biological phenol removal process, reduce the running cost of biological phenol removal process.
(4). distilled ammonia wastewater fills into mother liquor after being through First Heat Exchanger cooling, thus ensure that with the distilled ammonia wastewater amount of remained ammonia heat exchange constant, make remained ammonia enter ammonia still temperature not by the impact that the distilled ammonia wastewater amount filling into mother liquor is how many, ensure that the normal production of ammonia still.
(5). when in use, warm water or water at low temperature fill into mother liquor as new water, because the usage quantity of warm water or water at low temperature in other production process is larger with seasonal variation fluctuation, cannot ensure that the new water yield filling into mother liquor is stable and sufficient, and the pressure of middle warm water or water at low temperature is often on the low side, be unfavorable for conveying and add, and the distilled ammonia wastewater not only stable abundance of the scale of construction, and pressure is higher, be more suitable for filling into mother liquor as new water, ensure that the normal table of deamination operation is produced.
Accompanying drawing explanation
The principle of work schematic diagram of a kind of coke-oven gas deamination method that Fig. 1 provides for the embodiment of the present invention.
In figure, 1 ammonia still, 2 distilled ammonia wastewater pumps, 3 First Heat Exchangers, 4 second interchanger, 5 saturexs, 6 Recycling Mother Solution pumps, 7 crystallization pumps.
Embodiment
For making the object of the embodiment of the present invention, technical scheme and advantage clearly, below in conjunction with the accompanying drawing in the embodiment of the present invention, technical scheme in the embodiment of the present invention is clearly and completely described, obviously, described embodiment is a part of embodiment of the present invention, instead of whole embodiments.Based on the embodiment in the present invention, the every other embodiment that those of ordinary skill in the art obtain under the prerequisite not making creative work, all belongs to the scope of protection of the invention.
With reference to the principle of work schematic diagram of a kind of coke-oven gas deamination method that figure 1, Fig. 1 provides for the embodiment of the present invention.
The invention provides a kind of coke-oven gas deamination method, comprise the following steps:
1) by Recycling Mother Solution pump 6, the mother liquor bottom saturex 5 is delivered to saturex 5 top, from up to down sprays.
In one embodiment of the invention, the temperature of mother liquor is preferably 45 DEG C ~ 55 DEG C; The liquid-gas ratio of mother liquor is preferably 15L/m
3~ 30L/m
3; The acidity of mother liquor is preferably 5% ~ 6%.
2) coke-oven gas enters saturex 5 by the entrance on saturex 5 sidewall, bottom-up motion.In one embodiment of the invention, the temperature that enters of coke-oven gas is preferably 50 DEG C ~ 65 DEG C, and outflow temperature is preferably 45 DEG C ~ 55 DEG C, and ammonia quantity is preferably 40mg/m
3~ 60mg/m
3.
3) coke-oven gas and mother liquor move toward one another, fully contact, and the sulfuric acid in mother liquor is by the NH in coke-oven gas
3absorb, generate ammonium sulfate, the coke-oven gas after deamination is discharged from saturex 5 top, and enter follow-up final cooling process, mother liquor flows back to bottom saturex 5;
4) remained ammonia is sent to ammonia still 1 ammonia still process after First Heat Exchanger 3 heats up, output distilled ammonia wastewater;
5) by step 4) distilled ammonia wastewater of output is sent to First Heat Exchanger 3 by distilled ammonia wastewater pump 2, utilizes remained ammonia distilled ammonia wastewater to be cooled to 55 DEG C ~ 65 DEG C in First Heat Exchanger 3.Not necessarily consistent with the mother liquor temperature bottom saturex 5 through First Heat Exchanger 3 cooled distilled ammonia wastewater temperature, according to actual needs, the temperature of distilled ammonia wastewater can suitably higher than mother liquor temperature, also can suitably lower than mother liquor temperature, to regulate mother liquor temperature together with other annex solution, mother liquor temperature is finally made to begin to fluctuate at set(ting)value zone of reasonableness.The temperature that concrete First Heat Exchanger 3 exports distilled ammonia wastewater is determined by the temperature of the temperature of mother liquor and volume, other annex solution and volume and the distilled ammonia wastewater amount of filling into as new water.Utilize remained ammonia in First Heat Exchanger 3, distilled ammonia wastewater is cooled to saturex 5 bottom the close temperature of mother liquor, then cooled distilled ammonia wastewater is delivered to saturex 5 as new water and prepare mother liquor, because in the temperature of added distilled ammonia wastewater and saturex 5, the temperature of mother liquor is close, can not affect greatly mother liquor temperature after being added to mother liquor, mother liquor temperature is fluctuated in the zone of reasonableness of set(ting)value, thus ensure that coke-oven gas deamination operation normal table is produced.
6) using step 5) cooled distilled ammonia wastewater delivers to saturex 5 as new water and prepares mother liquor.When using middle warm water or water at low temperature to fill into mother liquor as new water, because the usage quantity of warm water or water at low temperature in other production process is larger with seasonal variation fluctuation, cannot ensure that the new water yield filling into mother liquor is stable and sufficient, and the pressure of middle warm water or water at low temperature is often on the low side, be unfavorable for conveying and add, and the distilled ammonia wastewater not only stable abundance of the scale of construction, and pressure is higher, be more suitable for filling into mother liquor as new water, ensure that the normal table of deamination operation is produced; In replacing with distilled ammonia wastewater, warm water or water at low temperature etc. fill in mother liquor as new water, decrease the new water consumption of deamination operation, achieve the recycling of distilled ammonia wastewater simultaneously; And distilled ammonia wastewater fills into mother liquor after being through First Heat Exchanger 3 cooling, thus ensure that with the distilled ammonia wastewater amount of remained ammonia heat exchange constant, make remained ammonia enter ammonia still 1 temperature not by the impact that the distilled ammonia wastewater amount filling into mother liquor is how many, ensure that the normal production of ammonia still 1.
7) production ammonium sulfate is sent to by crystallization pump 7 extracting part decomposition mother solution.
In one embodiment of the invention, by step 6) in remaining distilled ammonia wastewater through second interchanger 4 cool after be sent to biological phenol removal process, the temperature that the second interchanger 4 exports distilled ammonia wastewater is 25 DEG C ~ 40 DEG C.Part distilled ammonia wastewater is filled into mother liquor, decreases the distilled ammonia wastewater amount being sent to biological phenol removal process, reduce the running cost of biological phenol removal process.
In one embodiment of the invention, First Heat Exchanger 3 and the second interchanger 4 are plate-type heat exchanger.
Above a kind of coke-oven gas deamination method provided by the present invention is described in detail.Apply specific embodiment herein to set forth principle of the present invention and embodiment, the explanation of above embodiment just understands method of the present invention and core concept thereof for helping.It should be pointed out that for those skilled in the art, under the premise without departing from the principles of the invention, can also carry out some improvement and modification to the present invention, these improve and modify and also fall in the protection domain of the claims in the present invention.
Claims (8)
1. a coke-oven gas deamination method, is characterized in that, comprises the following steps:
1) by Recycling Mother Solution pump, the mother liquor bottom saturex is delivered to saturex top, from up to down sprays;
2) coke-oven gas enters saturex by the entrance on saturex sidewall, bottom-up motion;
3) coke-oven gas and mother liquor move toward one another, fully contact, and the sulfuric acid in mother liquor is by the NH in coke-oven gas
3absorb, generate ammonium sulfate, the coke-oven gas after deamination is discharged from saturex top, and enter follow-up final cooling process, mother liquor flows back to bottom saturex;
4) remained ammonia is sent to ammonia still ammonia still process, output distilled ammonia wastewater after First Heat Exchanger heats up;
5) by step 4) distilled ammonia wastewater of output toward First Heat Exchanger, utilizes remained ammonia distilled ammonia wastewater to be cooled to 55 DEG C ~ 65 DEG C by distilled ammonia wastewater pumping in First Heat Exchanger;
6) using step 5) cooled distilled ammonia wastewater as new water deliver to saturex preparation mother liquor;
7) production ammonium sulfate is sent to by crystallization pump extracting part decomposition mother solution.
2. coke-oven gas deamination method according to claim 1, is characterized in that, described step 1) in the temperature of mother liquor bottom saturex be 45 DEG C ~ 55 DEG C.
3. coke-oven gas deamination method according to claim 1, is characterized in that, described step 1) in the liquid-gas ratio of mother liquor bottom saturex be 15L/m
3~ 30L/m
3.
4. coke-oven gas deamination method according to claim 1, is characterized in that, described step 1) in the acidity of mother liquor bottom saturex be 5% ~ 6%.
5. coke-oven gas deamination method according to claim 1, is characterized in that, the temperature that enters of described coke-oven gas is 50 DEG C ~ 65 DEG C, and outflow temperature is 45 DEG C ~ 55 DEG C, and ammonia quantity is 40mg/m
3~ 60mg/m
3.
6. coke-oven gas deamination method according to claim 1, is characterized in that, described step 6) in the distilled ammonia wastewater amount filled in mother liquor be 10m
3/ time ~ 15m
3/ time, flow is 0.3m
3/ h ~ 0.5m
3/ h.
7. coke-oven gas deamination method according to claim 1, it is characterized in that, by described step 6) in remaining distilled ammonia wastewater through second interchanger cooling after be sent to biological phenol removal process, the temperature of described second heat exchanger exit distilled ammonia wastewater is 25 DEG C ~ 40 DEG C.
8. coke-oven gas deamination method according to claim 7, is characterized in that, described First Heat Exchanger and the second interchanger are plate-type heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510140324.XA CN104726141A (en) | 2015-03-27 | 2015-03-27 | Method for ammonia removal of coke oven gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510140324.XA CN104726141A (en) | 2015-03-27 | 2015-03-27 | Method for ammonia removal of coke oven gas |
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| CN104726141A true CN104726141A (en) | 2015-06-24 |
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| CN201510140324.XA Pending CN104726141A (en) | 2015-03-27 | 2015-03-27 | Method for ammonia removal of coke oven gas |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105238450A (en) * | 2015-09-29 | 2016-01-13 | 山东钢铁股份有限公司 | Purifying method of coke oven gas |
| CN105271305A (en) * | 2015-09-29 | 2016-01-27 | 山东钢铁股份有限公司 | Method for treating ammonia water obtained after ammonia distillation of residual ammonia water |
| CN105692654A (en) * | 2016-03-17 | 2016-06-22 | 山东钢铁股份有限公司 | Method and system for producing ammonium sulfate through gas deamination |
| CN105776394A (en) * | 2016-03-17 | 2016-07-20 | 山东钢铁股份有限公司 | Coal gas deamination and residual ammonia liquor vacuum distillation integrated production method and system |
| CN109179774A (en) * | 2018-10-17 | 2019-01-11 | 临涣焦化股份有限公司 | Waste water treatment and reclamation utilizes device after coking of coal ammonia |
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| JPS56100132A (en) * | 1980-01-09 | 1981-08-11 | Nippon Steel Corp | Manufacture of ammonium sulfate using sensible heat of coke oven gas |
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| CN201990641U (en) * | 2011-01-24 | 2011-09-28 | 江苏中显集团有限公司 | Special device for coke oven gas desulfuration and deamination combined purification method |
| CN102485851A (en) * | 2010-12-01 | 2012-06-06 | 鞍钢集团工程技术有限公司 | Method and apparatus for removing acid-containing droplet in gas from soda acid neutralization deamination |
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2015
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| CN102485851A (en) * | 2010-12-01 | 2012-06-06 | 鞍钢集团工程技术有限公司 | Method and apparatus for removing acid-containing droplet in gas from soda acid neutralization deamination |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105238450A (en) * | 2015-09-29 | 2016-01-13 | 山东钢铁股份有限公司 | Purifying method of coke oven gas |
| CN105271305A (en) * | 2015-09-29 | 2016-01-27 | 山东钢铁股份有限公司 | Method for treating ammonia water obtained after ammonia distillation of residual ammonia water |
| CN105692654A (en) * | 2016-03-17 | 2016-06-22 | 山东钢铁股份有限公司 | Method and system for producing ammonium sulfate through gas deamination |
| CN105776394A (en) * | 2016-03-17 | 2016-07-20 | 山东钢铁股份有限公司 | Coal gas deamination and residual ammonia liquor vacuum distillation integrated production method and system |
| CN109179774A (en) * | 2018-10-17 | 2019-01-11 | 临涣焦化股份有限公司 | Waste water treatment and reclamation utilizes device after coking of coal ammonia |
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Application publication date: 20150624 |