阅读说明：本技术 一种合成氨的脱碳废气回收制碱装置 (Decarbonization waste gas recovery system alkali device of synthetic ammonia ) 是由 孙彩军 徐松 郑健 于 2019-09-30 设计创作，主要内容包括：本发明提供一种合成氨的脱碳废气回收制碱装置,其特征在于：它包括用管线连通的鼓泡吸收塔(1)、二氧化碳储罐(2)、风机(3)、稀液槽(4)、离心机(5)、分离液槽(6)、烘干机(7)、输送泵(8)、吸收泵(9)、制碱槽(10)。本发明结构简单、使用方便,通过将脱碳净化后的二氧化碳在次输入到鼓泡吸收塔内直接吸收制碱,变废为宝,减少工业废气的排放,以及排放带来的环境气味问题得到解决。(The invention provides an alkali making device by recovering decarbonized waste gas of synthetic ammonia, which is characterized in that: the device comprises a bubbling absorption tower (1), a carbon dioxide storage tank (2), a fan (3), a dilute liquid tank (4), a centrifuge (5), a separation liquid tank (6), a dryer (7), a delivery pump (8), an absorption pump (9) and an alkali preparation tank (10) which are communicated by pipelines. The invention has simple structure and convenient use, and the carbon dioxide after decarburization and purification is input into the bubbling absorption tower for the second time to directly absorb the soda, thereby changing waste into valuable, reducing the emission of industrial waste gas and solving the problem of environmental odor caused by emission.)

1. A decarbonization waste gas recovery alkali making device for synthetic ammonia comprises a bubbling absorption tower (1), wherein one side of the bubbling absorption tower (1) is communicated with a decarbonization waste gas input pipe (11), the decarbonization waste gas input pipe (11) is also provided with a waste gas inlet valve (11 a) correspondingly matched with the decarbonization waste gas input pipe, one side of the bubbling absorption tower (1) is provided with an alkali making tank (10), a spray pipe (10 a) is communicated between the alkali making tank (10) and the bubbling absorption tower (1), the spray pipe (10 a) is also provided with an absorption pump (9) correspondingly matched with the spray pipe, one end of the spray pipe (10 a) is inserted into the bubbling absorption tower (1), and the end part of the spray pipe is connected with a liquid distributor (10 c);

a dilute liquid tank (4) is arranged on one side of the lower part of the bubbling absorption tower (1), an outflow pipe (4 a) is communicated between the lower part of the bubbling absorption tower (1) and the dilute liquid tank (4), and an outflow control valve (4 b) which is correspondingly matched with the outflow pipe (4 a) is arranged on the outflow pipe;

a centrifugal machine (5) is further arranged on one side of the bottom of the tower body of the bubbling absorption tower (1), a pipeline (5 a) is communicated between the bottom of the liquid accumulation part (1 a) and the centrifugal machine (5), a solid outlet of the centrifugal machine (5) is communicated with a dryer (7), and a liquid outlet of the centrifugal machine (5) is communicated with a separation liquid tank (6);

a second liquid return pipe (8 a) is communicated between the separation liquid tank (6) and the other side of the lower part of the bubbling absorption tower (1), and a delivery pump (8) is arranged on the second liquid return pipe (8 a).

2. The apparatus for producing soda by recycling decarbonized exhaust gas from ammonia synthesis according to claim 1, wherein: the device is characterized in that a carbon dioxide storage tank (2) is arranged on the other side of the bubbling absorption tower (1), a pressure gauge (a pressure transmitter) (2 b) and a liquid level meter which is displayed in the figure are correspondingly matched and arranged on the carbon dioxide storage tank (2), the upper part of the carbon dioxide storage tank (2) is communicated with the upper part of the bubbling absorption tower (1) through a carbon return tube (a pipeline) (2 a), a carbon inlet tube (12) is communicated between one side of the bottom of the carbon dioxide storage tank (2) and the decarburization waste gas input tube (11), and a fan (3) which is correspondingly matched is arranged on the carbon inlet tube (12).

3. The apparatus for producing soda by recycling decarbonized exhaust gas from ammonia synthesis according to claim 2, wherein: a second carbon return tube (7 a) is also communicated between the gas outlet of the dryer (7) and the carbon return tube (2 a).

4. The apparatus for producing soda by recycling decarbonized exhaust gas from ammonia synthesis according to claim 2, wherein: a liquid return pipe (6 a) is connected between the other side of the bottom of the carbon dioxide storage tank (2) and the separation liquid tank (6), and a liquid return control valve (6 b) which is correspondingly matched with the liquid return pipe (6 a) is arranged on the liquid return pipe.

5. The apparatus for producing soda by recycling decarbonized exhaust gas from ammonia synthesis according to claim 1, wherein: a concentrated product groove (13) is arranged on one side of the dilute liquid groove (4), a pipeline (13 a) is communicated between the dilute liquid groove (4) and the concentrated product groove (13), and a low-temperature steam input pipe (14) is also arranged on one side of the concentrated product groove (13).

6. The apparatus for producing soda by recycling decarbonized exhaust gas from ammonia synthesis according to claim 1, wherein: a branch pipe (8 b) communicated with the dilute liquid tank (4) is also arranged on the second liquid return pipe (8 a), and a branch pipe control valve (8 c) is arranged on the branch pipe (8 b).

7. The apparatus for producing soda by recycling decarbonized exhaust gas from ammonia synthesis according to claim 1, wherein: a second branch pipe (8 d) communicated with the spray pipe (10 a) is further arranged on the second liquid return pipe (8 a), and a third liquid return control valve (8 f) correspondingly matched with the second branch pipe (8 d) is further arranged on the second branch pipe.

The technical field is as follows:

the invention relates to the field of recovery of decarbonization waste gas of synthetic ammonia, in particular to a decarbonization waste gas recovery alkali-making device of synthetic ammonia.

Background art:

with the needs of various technical progress and environmental improvement requirements of ammonia synthesis enterprises, in recent years, the chemical industry is famous for high pollution, the environmental problem becomes one of bottlenecks restricting the development of the chemical industry, and the search for a proper mode and a method is an irreparable task.

The decarbonization process adopted by the current ammonia synthesis enterprise generally comprises a pressure swing adsorption decarbonization process and a carbon-propane liquid decarbonization process, the pressure swing adsorption decarbonization process is a decarbonization process which is adopted in a large area at present, but the existing process has effective gas loss, the ton ammonia cost which influences the ammonia synthesis to different degrees influences the economic benefit of the enterprise, the carbon-propane decarbonization process does not have the effective gas loss, the absorption cycle discharges high-concentration CO2 gas which is generally directly discharged into the atmosphere, the emission of greenhouse gas is invisibly increased, and the high-concentration CO2 gas is accompanied with special odor, so that the process is not environment-friendly and is not beneficial to a low-carbon economic mode advocated by the current enterprise economy.

The invention content is as follows:

the invention aims to overcome the defects in the prior art and provides the device for recovering the decarbonized waste gas of the synthetic ammonia to prepare the alkali.

The application provides the following technical scheme:

a decarbonization waste gas recovery alkali making device for synthetic ammonia comprises a bubbling absorption tower, wherein one side of the bubbling absorption tower is communicated with a decarbonization waste gas input pipe, the decarbonization waste gas input pipe is also provided with a waste gas inlet valve correspondingly matched with the decarbonization waste gas input pipe, one side of the bubbling absorption tower is provided with an alkali making tank, a spray pipe is communicated between the alkali making tank and the bubbling absorption tower, the spray pipe is also provided with an absorption pump correspondingly matched with the spray pipe, one end of the spray pipe is inserted into the bubbling absorption tower, and the end part of the spray pipe is connected with a liquid distributor; a dilute liquid tank is arranged on one side of the lower part of the bubbling absorption tower body, an outflow pipe is communicated between the lower part of the bubbling absorption tower body and the dilute liquid tank, and an outflow control valve which is correspondingly matched with the outflow pipe is arranged on the outflow pipe;

a centrifugal machine is further arranged on one side of the bottom of the bubbling absorption tower body, a pipeline is communicated between the bottom of the liquid accumulating part and the centrifugal machine, a solid outlet of the centrifugal machine is communicated with a dryer, and a liquid outlet of the centrifugal machine is communicated with a separation liquid tank;

a second liquid return pipe is communicated between the separation liquid tank and the other side of the lower part of the bubbling absorption tower, and a delivery pump is arranged on the second liquid return pipe.

On the basis of the technical scheme, the following further technical scheme can be provided:

the other side of the bubbling absorption tower is provided with a carbon dioxide storage tank, the carbon dioxide storage tank is also provided with a pressure gauge and a liquid level meter which are correspondingly matched with the pressure gauge and are displayed in the figure, the upper part of the carbon dioxide storage tank is communicated with the upper part of the bubbling absorption tower through a carbon return tube, a carbon inlet tube is also communicated between one side of the bottom of the carbon dioxide storage tank and the decarbonization waste gas input tube, and a fan which is correspondingly matched with the carbon inlet tube is also arranged on the carbon inlet tube.

And a second carbon return tube is communicated between the gas outlet of the dryer and the carbon return tube.

A liquid return pipe is connected between the other side of the bottom of the carbon dioxide storage tank and the separation liquid tank, and a liquid return control valve which is correspondingly matched with the liquid return pipe is arranged on the liquid return pipe.

And a thick liquid groove is arranged on one side of the thin liquid groove, a pipeline is communicated between the thin liquid groove and the thick liquid groove, and a low-temperature steam input pipe is also arranged on one side of the thick liquid groove.

And a branch pipe communicated with the dilute liquid tank is also arranged on the second liquid return pipe, and a branch pipe control valve is arranged on the branch pipe.

And a second branch pipe communicated with the spray pipe is further arranged on the second liquid return pipe, and a third liquid return control valve correspondingly matched with the second branch pipe is further arranged on the second branch pipe.

The invention has the advantages that:

the invention has simple structure and convenient use, and the carbon dioxide after decarburization and purification is input into the bubbling absorption tower for the second time to directly absorb the soda, thereby changing waste into valuable, reducing the emission of industrial waste gas and solving the problem of environmental odor caused by emission.

Description of the drawings:

FIG. 1 is a process flow diagram of the present invention.

The specific implementation mode is as follows:

as shown in figure 1, the decarbonization waste gas recovery alkali making device for synthetic ammonia comprises a bubbling absorption tower 1, wherein one side of the lower part of the bubbling absorption tower 1 is communicated with a decarbonization waste gas input pipe 11, and the decarbonization waste gas input pipe 11 is also provided with a waste gas inlet valve 11a which is correspondingly matched with the decarbonization waste gas input pipe 11. The carbon dioxide waste gas generated in the production of synthetic ammonia is delivered into a bubbling absorption tower 1 after being pretreated to remove the trace H2S of impurities

An alkali making tank 10 is arranged on one side of the bubbling absorption tower 1, a spray pipe 10a is communicated between the alkali making tank 10 and the upper part of the bubbling absorption tower 1, an absorption pump 9 correspondingly matched with the spray pipe 10a is further arranged on the spray pipe 10a, and a solution control valve 10b is respectively arranged on the spray pipes 10a on two sides of the absorption pump 9. One end of the shower pipe 10a is inserted into the bubbling absorption tower 1 from one side of the upper part of the bubbling absorption tower 1, and a liquid distributor 10c is connected to the end thereof.

The solution control valves 10b on both sides of the absorption pump 9 are opened, then the sodium hydroxide solution in the alkali making tank 10 is input into the bubbling absorption tower 1 through the absorption pump 9, and the liquid is distributed downwards from the upper part in the tower body of the bubbling absorption tower 1 through the liquid distributor 10b, so that the sodium hydroxide solution reacts with the carbon dioxide waste gas entering from the lower part of the bubbling absorption tower 1.

A carbon dioxide storage tank 2 is arranged at the other side of the bubbling absorption tower 1, and a pressure gauge 2b and a liquid level meter which is shown in the figure are correspondingly matched with the carbon dioxide storage tank 2. A carbon return tube 2a is arranged between the upper part of the carbon dioxide storage tank 2 and the other side of the upper part of the bubbling absorption tower 1 and is communicated with each other through the carbon return tube 2 a. So that the carbon dioxide gas which has not reacted in the bubbling absorption tower 1 flows into the carbon dioxide storage tank 2 through the carbon return tube 2 a.

A carbon inlet tube 12 is communicated between one side of the bottom of the carbon dioxide storage tank 2 and the decarburization waste gas input tube 11, a blower 3 which is correspondingly matched with the carbon inlet tube 12 is also arranged on the carbon inlet tube 12, and the blower 3 is a Roots blower. The carbon desorption pipes 12 on both sides of the fan 3 are respectively provided with a waste gas input control valve 12 a. The fan 3 is also connected with an adjusting valve 3a, and the power of the fan 3 is adjusted through the adjusting valve 3a, so that the situation of negative pressure suck back of the carbon dioxide storage tank 2 is prevented.

When the pressure in the carbon dioxide storage tank 2 reaches a certain value, the waste gas input control valve 12a is opened, so that the carbon dioxide gas in the carbon dioxide storage tank 2 enters the fan 3, enters the decarburization waste gas input pipe 11 under the acceleration action of the fan, and then enters the bubbling absorption tower 1 again for reaction. The worker turns on the blower 3 by the value displayed by the pressure gauge 2b to provide proper acceleration for the carbon dioxide gas in the carbon inlet tube 12.

The carbon dioxide gas that has accelerated simultaneously also can accelerate the carbon dioxide waste gas in the decarbonization waste gas input tube 11 for the fan 3 with the effect of accelerating also can extend to decarbonization waste gas input tube 11, improve the airflow velocity of decarbonization waste gas input tube 11 and bubble absorption tower 1 intercommunication department.

The lower part of the tower body of the bubbling absorption tower 1 is provided with a conical liquid accumulation part 1a, one side of the liquid accumulation part 1a is provided with a dilute liquid tank 4, an outflow pipe 4a is communicated between the dilute liquid tank 4 and the middle part of the liquid accumulation part 1a, and the outflow pipe 4a is provided with an outflow control valve 4b correspondingly matched with the outflow control valve. The liquid accumulation part 1a is also provided with a liquid accumulation liquid level meter which is not shown in the figure.

Still be equipped with centrifuge 5 in hydrops portion 1a bottom one side, the intercommunication has pipeline 5a between hydrops portion 1a bottom and centrifuge 5, is equipped with corresponding complex control valve 5b on pipeline 5 a. The carbon dioxide gas is liquid after reaction in the bubbling absorption tower 1, and at the same time, some crystal precipitate of NaHCO3 is produced, and the crystal precipitate collects at the bottom of the liquid accumulation part 1a, and the clearer sodium carbonate solution collects in the middle of the liquid accumulation part 1 a.

The worker opens the liquid preparation control valve 4b according to the liquid level data detected by the effusion level gauge to enable the clarified sodium carbonate solution to enter the dilute liquid tank 4, and opens the control valve 5b to enable the muddy sodium carbonate solution liquid mixed with a large amount of crystal precipitates to enter the pipeline 5a under the pressure action of the bubbling absorption tower 1 and then enter the centrifuge 5 for solid-liquid centrifugal separation. The concentration of the sodium carbonate solution flowing into the dilute liquid tank 4 is more than 10 percent.

The solid outlet of the centrifuge 5 is communicated with a dryer 7 through a pipeline, and the liquid outlet of the centrifuge 5 is communicated with a separation liquid tank 6 through a pipeline. The dryer 7 dries the substance separated by the centrifuge 5 to obtain dry sodium carbonate powder, and a second carbon return tube 7a is also communicated between the gas outlet of the dryer 7 and the carbon return tube 2a, so that the carbon dioxide gas generated in the drying process of the dryer 7 can flow back to the carbon dioxide storage tank 2 to participate in the reaction again.

A liquid return pipe 6a is connected between the other side of the bottom of the carbon dioxide storage tank 2 and the separation liquid tank 6, and a liquid return control valve 6b which is correspondingly matched with the liquid return pipe 6a is arranged on the liquid return pipe 6 a. Because the gas phase of the carbon dioxide gas which is not reacted in the bubbling absorption tower 1 is provided with some sodium carbonate solution generated in the reaction, after the carbon dioxide gas flows back into the carbon dioxide storage tank 2 through the carbon return tube 2a, some liquid is separated out from the gas phase of the carbon dioxide gas and is gathered in the carbon dioxide storage tank 2, and when the liquid level is found to rise to a certain height by the liquid level meter of the carbon dioxide storage tank 2, the liquid return control valve 6b is opened to discharge the accumulated liquid of the sodium carbonate solution in the carbon dioxide storage tank 2 into the separation liquid tank 6. A PAT electrification indicator, not shown in the figure, is also mounted on the separation liquid tank 6.

A second liquid return pipe 8a is communicated between the separation liquid tank 6 and the other side of the lower part of the bubble absorption tower 1, and a delivery pump 8 is arranged on the second liquid return pipe 8 a. The sodium carbonate solution in the separation liquid tank 6 is pumped back to the bubble absorption column 1 by the transfer pump 8 for the re-reaction.

The second liquid return pipe 8a is also provided with a branch pipe 8b communicated with the dilute liquid tank 4, and the branch pipe 8b is provided with a branch pipe control valve 8 c. A concentrated solution tank 13 is provided on the dilute solution tank 4 side, and a pipe 13a is connected between the dilute solution tank 4 and the concentrated solution tank 13. A low-temperature steam input pipe 14 is also arranged at one side of the concentrated product tank 13, and a low-temperature steam control valve 14a which is correspondingly matched with the low-temperature steam input pipe 14 is arranged on the low-temperature steam input pipe. Boiler low-temperature steam enters the concentrated product tank 13 through the low-temperature steam input pipe 14 to evaporate the sodium carbonate solution to improve the concentration of the sodium carbonate solution, and meanwhile, the sodium carbonate solution with the concentration of more than 10 percent in the dilute liquid tank 4 enters the concentrated product tank 13 to ensure that the concentration of the sodium carbonate solution in the concentrated product tank 13 is not more than 50 percent, and powdery sodium carbonate solid can also be directly evaporated and crystallized.

A second branch pipe 8d communicated with the spray pipe 10a is further arranged on the second liquid return pipe 8a, and a second liquid return control valve 8e correspondingly matched with the second liquid return pipe 8a is arranged on one side of the second branch pipe 8d, which is close to the bubbling absorption tower 1. A third liquid return control valve 8f which is correspondingly matched with the second branch pipe 8d is also arranged on the second branch pipe.

The concentration (PH value) of the sodium carbonate solution in the separation liquid tank 6 is detected by the PAT electrification indicating instrument, when the concentration of the sodium carbonate solution discharged from the separation liquid tank 6 is higher than a certain concentration (when the PH value is higher than 9, the NaOH reaction is incomplete, and the reaction liquid is excessively discharged due to improper treatment operation), a worker closes the second liquid return control valve 8e and the branch pipe control valve 8c, opens the third liquid return control valve 8f to enable the sodium carbonate solution with higher concentration to directly enter the spray pipe 10a, and then enters the bubbling absorption tower 1 to react with the carbon dioxide gas input by the decarburization waste gas input pipe 11.

When the concentration of the sodium carbonate solution discharged from the separation liquid tank 6 is lower than a certain concentration (the pH value is less than 9), the second liquid return control valve 8e and the branch pipe control valve 8c are opened, the third liquid return control valve 9f is closed, so that a part of the sodium carbonate solution with lower concentration directly enters the dilute liquid tank 4, and the other part enters the accumulated liquid part 1a of the bubbling absorption tower 1 through the second liquid return pipe 8a to form circulation.