Process and device for extracting strong ammonia water from ammonia distillation system adopted in coking plant
阅读说明：本技术 一种焦化厂采用蒸氨系统浓氨水的提取工艺及装置 (Process and device for extracting strong ammonia water from ammonia distillation system adopted in coking plant ) 是由 赵成书 于 2020-08-13 设计创作，主要内容包括：本发明公开了一种焦化厂采用蒸氨系统浓氨水的提取工艺及装置。其特征在于,在蒸氨氨解工艺中的蒸氨塔之前增加一台分解器,在分缩器后拆除氨分解炉、尾气冷却塔和冷却塔循环泵,采用汽液分离器、冷凝冷却器、浓氨水槽和浓氨水泵替代,将蒸馏后氨含量为8-10%氨水提取成氨含量为18-20%的浓氨水。本发明的有益效果是:1.减轻氨水介质对化产蒸氨系统所涉及的设备、管道的腐蚀。2.提高氨法脱硫过程中废气排放标准,改善了周边环境。3.降低生产原料的资金投入和维修运营成本。4.本发明除了应用在电厂锅炉脱硫工艺中,还可应用在厂里焦炉尾气、管式炉尾气、锅炉尾气的脱硫脱硝工艺中,具有很大的经济效益和社会效益。(The invention discloses a process and a device for extracting strong ammonia water from an ammonia distillation system in a coking plant. The method is characterized in that a decomposer is added in front of an ammonia still in the ammonia still ammonolysis process, an ammonia decomposition furnace, a tail gas cooling tower and a cooling tower circulating pump are removed after a dephlegmator, a vapor-liquid separator, a condensation cooler, a concentrated ammonia water tank and a concentrated ammonia water pump are adopted for replacing, and the distilled ammonia water with the ammonia content of 8-10% is extracted into the concentrated ammonia water with the ammonia content of 18-20%. The invention has the beneficial effects that 1, the corrosion of the ammonia water medium to the equipment and the pipeline related to the chemical product ammonia distillation system is reduced. 2. The exhaust emission standard in the ammonia desulphurization process is improved, and the surrounding environment is improved. 3. The capital investment of production raw materials and the maintenance and operation cost are reduced. 4. The invention can be applied to the desulfurization and denitration process of factory coke oven tail gas, tubular furnace tail gas and boiler tail gas besides the desulfurization process of the power plant boiler, and has great economic and social benefits.)
1. An extraction process of strong ammonia water of an ammonia distillation system adopted by a coking plant is characterized in that raw material ammonia water with the temperature of 25-30 ℃ passes through a heat exchanger 2, the temperature of the raw material ammonia water is raised to 60-70 ℃, the raw material ammonia water passes through a heater 3, the temperature of the raw material ammonia water is raised to 80-90 ℃, the raw material ammonia water enters a decomposer 10 and is reheated by a heating mechanism at the bottom of the decomposer 10, and H in the raw material ammonia water2S and CO2Separating out, feeding ammonia water into ammonia still 4 for ammonia distillation, feeding the ammonia steam and a large amount of water vapor into dephlegmator 5 from the top of ammonia still 4, cooling by dephlegmator 5, condensing most water vapor to go back and forth to ammonia still 4, feeding the vapor phase with high ammonia concentration into vapor-liquid separator 11, further separating, returning the reflux liquid obtained by condensing most water vapor in the vapor phase to ammonia still 4 for re-evaporationThe vapor phase enters a condensation cooler 12 to form concentrated ammonia water with the ammonia content of 18-20%, and enters a concentrated ammonia water tank 13 for users to use.
2. The process for extracting concentrated ammonia water from an ammonia distillation system in a coke-oven plant as claimed in claim 1, wherein the temperature of the bottom of the decomposer 10 is 92-100 ℃, the temperature of ammonia gas at the outlet of the dephlegmator 5 is 88-92 ℃, and the temperature of concentrated ammonia water at the outlet of the condenser cooler 12 is 30-35 ℃.
3. The extraction process of the concentrated ammonia water from the ammonia distillation system in the coke plant as claimed in claim 1, wherein the temperature at the top of the ammonia distillation tower 4 is 100-.
4. The extraction process of concentrated ammonia water of an ammonia distillation system adopted in a coke-oven plant according to claim 1, characterized in that the raw material ammonia water is prepared by a dry distillation section, a condensation section, a desulfurization section and an ammonia washing section.
5. The extraction process of the strong ammonia water of the ammonia distillation system in the coke-oven plant according to claim 4, wherein the dry distillation section is to distill the ammonia-containing clean coal in a coke oven, then the ammonia and other impurities are separated out from the coal, most of the ammonia and other impurities enter the coal gas to form coal gas with the ammonia content of 5-6g/㎥, a small part of the ammonia enters the circulating ammonia water, the amount of the circulating ammonia water is continuously increased to form residual ammonia water with the ammonia content of 0.6-0.8%, and the residual ammonia water passes through the condensation section and is directly sent to the ammonia washing section.
6. The process for extracting concentrated ammonia water from an ammonia distillation system in a coke-oven plant as claimed in claim 4, wherein the condensation section is to remove naphthalene from coal gas with ammonia content of 5-6g/㎥ after passing through a condensation cooler, and the temperature of the cooled coal gas is 20-30 ℃.
7. The extraction process of concentrated ammonia water in an ammonia distillation system in a coke-oven plant as claimed in claim 4, wherein the desulfurization section is to desulfurize the gas after the condensation section by PDS desulfurization to remove hydrogen sulfide in the gas.
8. The extraction process of the strong ammonia water of the ammonia distillation system adopted in the coke-oven plant according to claim 4, characterized in that the ammonia washing section is to feed the coal gas after the desulfurization section into an ammonia washing tower and wash the coal gas by using ammonia distillation wastewater with the ammonia content of 0.01-0.03%, residual ammonia water with the ammonia content of 0.6-0.8% and industrial water to form raw material ammonia water with the ammonia content of 0.5-1.0%.
9. The device adopted by the extraction process of the concentrated ammonia water of the ammonia still system adopted by the coke-oven plant according to claim 1 is characterized in that the device for extracting the concentrated ammonia water of the ammonia still system adopted by the coke-oven plant comprises a raw material ammonia water tank 1, a heat exchanger 2, a heater 3 and an ammonia still 4, and is characterized in that a decomposer 10 is added in front of the ammonia still 4 in the ammonia still ammonolysis process, an ammonia decomposing furnace 6, a tail gas cooling tower 7 and a cooling tower circulating pump 8 are removed after a dephlegmator 5, a vapor-liquid separator 11, a condensing cooler 12, a concentrated ammonia water tank 13 and a concentrated ammonia water pump 14 are adopted for replacement, the inlet end of the raw material ammonia water tank 1 is connected with the outlet end of an ammonia washing section, a raw material pump 9 is arranged between the outlet end of the raw material ammonia water tank 1 and the first inlet end of the heat exchanger 2, the second outlet end of the heat exchanger 2 is connected with the first outlet end at the bottom of the ammonia still 4, the second outlet end of the heat exchanger 2 is connected with the first inlet end of the heater 3, the second inlet end of the heater 3 is a steam inlet end, the first outlet end of the heater 3 is a condensed water outlet end, the second outlet end of the heater 3 is connected with the first inlet end of the decomposer 10, the second inlet end of the decomposer 10 is a raw material ammonia water inlet end, the first outlet end at the top of the decomposer 10 is a steam-state escape outlet end, the third inlet end at the bottom of the decomposer 10 is a steam inlet end, the second outlet end at the bottom of the decomposer 10 is a condensed water outlet end, the third outlet end at the bottom of the decomposer 10 is connected with the first inlet end of the ammonia still 4, the first outlet end at the bottom of the ammonia still 4 is an ammonia still wastewater outlet end, the second inlet end at the bottom of the ammonia still 4 is a steam inlet end, the third inlet end of the ammonia still 4 is connected, the first inlet end of the dephlegmator 5 is a circulating cooling water inlet end, the first outlet end of the dephlegmator 5 is a circulating cooling water outlet end, the second outlet end of the dephlegmator 5 is connected with the first inlet end of the gas-liquid separator 11, the first outlet end of the gas-liquid separator 11 is a reflux liquid outlet end, the second outlet end of the gas-liquid separator 11 is connected with the first inlet end of the condensation cooler 12, the second inlet end of the condensation cooler 12 is a circulating cooling water inlet end, the first outlet end of the condensation cooler 12 is a circulating cooling water inlet end, the second outlet end of the condensation cooler 12 is connected with the inlet end of a concentrated ammonia water tank 13, and the outlet end of the concentrated ammonia water tank 13 is connected with a concentrated ammonia water pump 14.
Technical Field
The invention relates to the field of extraction of concentrated ammonia water in a coking plant, in particular to an extraction process and an extraction device of concentrated ammonia water in an ammonia distillation system adopted by the coking plant.
Technical Field
The boiler of a coke-oven plant requires a desulfurization system, and the existing desulfurization processes are various, one of which is ammonia desulfurization, and the ammonia desulfurization process needs a large amount of ammonia water with higher concentration. The existing designed chemical production nitrogen evaporation section process adopts ammonia evaporation decomposition, namely: the distilled ammonia water with the ammonia content of 8-10% is sent to an ammonia decomposition furnace for combustion decomposition, and the decomposed waste gas enters a cooling tower for cooling and then is discharged, so that the traditional ammonia distillation ammonolysis process has many problems after being put into operation.
Firstly, because the medium is too corrosive, each device, pipeline, transmitter, valve and the like are seriously corroded, the maintenance and the replacement are very frequent, the operation cost is increased year by year, and great pressure is brought to the normal operation of a company.
Secondly, the ammonia gas is not sufficiently combusted and decomposed, the exhaust emission does not reach the standard, the site and surrounding odor is heavy, the environment is poor, and meanwhile, the environmental requirements of the environmental protection department on chemical production are not met.
Thirdly, the distilled ammonia water with the ammonia content of 8-10% is combusted and decomposed, so that the environment is polluted, waste of ammonia water resources is formed invisibly, and the concentrated ammonia water with the ammonia content of 18-20% in the existing market is used for desulfurization and is a short chemical product.
Disclosure of Invention
The invention aims to solve the problems, most of equipment in the original ammonia distillation decomposition process is utilized for process transformation, and the distilled ammonia water with the ammonia content of 8-10% is extracted into the concentrated ammonia water with the ammonia content of 18-20%.
In order to achieve the purpose, the invention adopts the technical scheme that: an extraction process of concentrated ammonia water of an ammonia distillation system adopted by a coking plant is characterized in that raw material ammonia water with the temperature of 25-30 ℃ passes through a heat exchanger, the temperature of the raw material ammonia water rises to 60-70 ℃, then passes through a heater, the temperature of the raw material ammonia water rises to 80-90 ℃, enters a decomposer, is reheated by a heating mechanism at the bottom of the decomposer, and H in the raw material ammonia water2S and CO2Separating out ammonia water, feeding ammonia water into ammonia still for ammonia distillation, feeding the evaporated ammonia steam and a large amount of water vapor into a dephlegmator from the top of the ammonia still, cooling by the dephlegmator, condensing most of the water vapor to return to the ammonia still, feeding the vapor phase with high ammonia concentration into a vapor-liquid separator, further separating, returning the reflux liquid obtained by condensing most of the water vapor in the vapor phase to the ammonia still for re-evaporation, feeding the vapor phase into a condensing cooler to form concentrated ammonia water with 18-20% of ammonia content, and feeding the concentrated ammonia water into a concentrated ammonia water tank for users to use.
The temperature of the bottom of the decomposer is 92-100 ℃, the temperature of the ammonia gas at the outlet of the dephlegmator is 88-92 ℃, the temperature of the concentrated ammonia water at the outlet of the condensing cooler is 30-35 ℃,
the temperature of the top of the ammonia distillation tower is 100-102 ℃, the temperature of the bottom of the ammonia distillation tower is 100-103 ℃, the pressure of the top of the ammonia distillation tower is less than or equal to 0.25 kg/㎠ kg, the pressure of the bottom of the ammonia distillation tower is less than or equal to 0.35 kg/㎠ kg, the ammonia content of ammonia at the top of the ammonia distillation tower is 5-8%, the ammonia distillation efficiency is 97-99%, and the direct steam consumption is 160-200 kg/㎥.
The raw material ammonia water is prepared by a dry distillation working section, a condensation working section, a desulfurization working section and an ammonia washing working section.
The dry distillation section is characterized in that ammonia and other impurities are separated out from coal after ammonia-containing clean coal is subjected to dry distillation in a coke oven, most of ammonia and other impurities enter coal gas to form coal gas with the ammonia content of 5-6g/㎥, a small part of ammonia enters circulating ammonia water, the amount of the circulating ammonia water is continuously increased to form residual ammonia water with the ammonia content of 0.6-0.8%, and the residual ammonia water passes through a condensation section and is directly sent to an ammonia washing section.
The condensation section is to remove naphthalene from coal gas with ammonia content of 5-6g/㎥ after passing through a condensation cooler, and the temperature of the cooled coal gas is 20-30 ℃.
And the desulfurization section is used for desulfurizing the coal gas after the condensation section by adopting a PDS desulfurization method to remove hydrogen sulfide in the coal gas.
And the ammonia washing section is to feed the gas after the desulfurization section into an ammonia washing tower, and wash the gas by using ammonia distillation wastewater with the ammonia content of 0.01-0.03%, residual ammonia water with the ammonia content of 0.6-0.8% and industrial water to form raw material ammonia water with the ammonia content of 0.5-1.0%.
A device for extracting concentrated ammonia water of an ammonia distillation system adopted by a coking plant comprises a raw material ammonia water tank, a heat exchanger, a heater and an ammonia distillation tower, and is characterized in that a decomposer is added in front of the ammonia distillation tower in the ammonia distillation ammonolysis process, an ammonia decomposition furnace, a tail gas cooling tower and a cooling tower circulating pump are removed after a dephlegmator, and are replaced by a vapor-liquid separator, a condensation cooler, the concentrated ammonia water tank and a concentrated ammonia water pump, wherein the inlet end of the raw material ammonia water tank is connected with the outlet end of an ammonia washing working section, a raw material pump is arranged between the outlet end of the raw material ammonia water tank and the first inlet end of the heat exchanger for connection, the second outlet end of the heat exchanger is connected with the first outlet end at the bottom of the ammonia distillation tower, the first outlet end of the heat exchanger is an ammonia distillation wastewater outlet end, the second outlet end of the heat exchanger is connected with the first, the second outlet end of the heater is connected with the first inlet end of the decomposer, the second inlet end of the decomposer is a raw material ammonia water inlet end, the first outlet end of the top of the decomposer is a steam-state escape outlet end, the third inlet end of the bottom of the decomposer is a steam inlet end, the second outlet end of the bottom of the decomposer is a condensate water outlet end, the third outlet end of the bottom of the decomposer is connected with the first inlet end of the ammonia still, the first outlet end of the bottom of the ammonia still is an ammonia still wastewater outlet end, the second inlet end of the bottom of the ammonia still is a steam inlet end, the third inlet end of the ammonia still is connected with the first outlet end of the vapor-liquid separator, the top of the ammonia still is connected with the dephlegmator, the first inlet end of the dephlegmator is a circulating cooling water inlet end, the first outlet end of the dephle, the first outlet end of the vapor-liquid separator is a reflux outlet end, the second outlet end of the vapor-liquid separator is connected with the first inlet end of the condensation cooler, the second inlet end of the condensation cooler is a circulating cooling water inlet end, the first outlet end of the condensation cooler is a circulating cooling water inlet end, the second outlet end of the condensation cooler is connected with the inlet end of the concentrated ammonia water tank, and the outlet end of the concentrated ammonia water tank is connected with a concentrated ammonia water pump.
Compared with the prior art, the invention has the beneficial effects that:
1. the corrosion of the ammonia water medium to the equipment and the pipeline related to the chemical product ammonia distillation system is reduced.
2. The exhaust emission standard in the ammonia desulphurization process is improved, and the surrounding environment is improved.
3. The capital investment of production raw materials and the maintenance and operation cost are reduced.
4. The invention can be applied to the desulfurization and denitration process of factory coke oven tail gas, tubular furnace tail gas and boiler tail gas besides the desulfurization process of the power plant boiler, and has great economic and social benefits.
Drawings
FIG. 1 is a schematic diagram of the process and apparatus for extracting strong ammonia water from an ammonia distillation system in a coking plant according to the present invention;
FIG. 2 is a schematic view of a process for preparing concentrated aqueous ammonia according to the present invention;
FIG. 3 is a schematic view of the ammonia distillation ammonolysis process and apparatus of the present invention;
in the figure: 1 raw materials ammonia water tank, 2 heat exchangers, 3 heaters, 4 ammonia stills, 5 condensers, 6 ammonia decomposers, 7 tail gas cooling towers, 8 cooling tower circulating pumps, 9 raw materials pumps, 10 decomposers, 11 vapor-liquid separators, 12 condensation coolers, 13 concentrated ammonia water tanks, 14 concentrated ammonia water pumps.
Detailed Description
The following description of the embodiments of the invention is provided in conjunction with the accompanying drawings:
as shown in attached figure 1, the extraction process of the strong ammonia water of the ammonia distillation system adopted by the coking plant is characterized in that after raw material ammonia water with the temperature of 25-30 ℃ passes through a heat exchanger 2, the temperature of the raw material ammonia water is raised to 60-70 ℃, then the raw material ammonia water passes through a
The temperature of the bottom of the
the temperature at the top of the ammonia still 4 is 100-102 ℃, the temperature at the bottom of the ammonia still 4 is 100-103 ℃, the pressure at the top of the ammonia still 4 is less than or equal to 0.25 kg/㎠, the pressure at the bottom of the ammonia still 4 is less than or equal to 0.35 kg/㎠, the ammonia content of ammonia gas at the top of the ammonia still 4 is 5-8%, the ammonia still efficiency is 97-99%, and the direct steam consumption is 160-200 kg/㎥.
The raw material ammonia water shown in figure 2 is prepared by a dry distillation section, a condensation section, a desulfurization section and an ammonia washing section.
The dry distillation section is characterized in that ammonia and other impurities are separated out from coal after ammonia-containing clean coal is subjected to dry distillation in a coke oven, most of ammonia and other impurities enter coal gas to form coal gas with the ammonia content of 5-6g/㎥, a small part of ammonia enters circulating ammonia water, the amount of the circulating ammonia water is continuously increased to form residual ammonia water with the ammonia content of 0.6-0.8%, and the residual ammonia water passes through a condensation section and is directly sent to an ammonia washing section.
The condensation section is to remove naphthalene from coal gas with ammonia content of 5-6g/㎥ after passing through a condensation cooler, and the temperature of the cooled coal gas is 20-30 ℃.
And the desulfurization section is used for desulfurizing the coal gas after the condensation section by adopting a PDS desulfurization method to remove hydrogen sulfide in the coal gas.
And the ammonia washing section is to feed the gas after the desulfurization section into an ammonia washing tower, and wash the gas by using ammonia distillation wastewater with the ammonia content of 0.01-0.03%, residual ammonia water with the ammonia content of 0.6-0.8% and industrial water to form raw material ammonia water with the ammonia content of 0.5-1.0%.
As shown in attached figures 1 and 3, the device for extracting the concentrated ammonia water of the ammonia distillation system adopted by a coking plant comprises a raw material ammonia water tank 1, a heat exchanger 2, a
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