CN210710734U - Energy-saving synthetic ammonia decarburization system capable of avoiding foaming - Google Patents

Energy-saving synthetic ammonia decarburization system capable of avoiding foaming Download PDF

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CN210710734U
CN210710734U CN201921576674.0U CN201921576674U CN210710734U CN 210710734 U CN210710734 U CN 210710734U CN 201921576674 U CN201921576674 U CN 201921576674U CN 210710734 U CN210710734 U CN 210710734U
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pipeline
solution
outlet
lean
lean liquid
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李炜
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Sinochem Fuling Chongqing Chemical Industry Co Ltd
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Sinochem Fuling Chongqing Chemical Industry Co Ltd
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Abstract

The utility model discloses an energy-saving synthetic ammonia decarbonization system for avoiding bubbling, a solution preparation tank is connected with a desalted water pipeline and a defoaming agent pipeline, the bottom of the solution preparation tank is provided with a nitrogen stirring pipeline, introducing nitrogen into the solution preparation tank to stir the solution in the solution preparation tank, connecting an outlet pipeline of the solution preparation tank with a liquid inlet pipeline of an ejector, connecting an ejector branch pipe branched from an outlet pipeline of a lean solution pump with a power liquid inlet pipeline of the ejector, connecting two branch pipes branched from an outlet pipeline of the ejector with an outlet pipeline of a lean solution/desalted water heat exchanger and an outlet pipeline of a flash tank respectively, arranging a check valve on each branch pipe of the outlet pipeline of the ejector, the effect of energy conservation and consumption reduction is achieved, the phenomenon that the semi-barren solution is crystallized to block the pipeline due to the addition of the foaming agent is avoided, and the economic benefit and the social benefit of an enterprise are improved.

Description

Energy-saving synthetic ammonia decarburization system capable of avoiding foaming
Technical Field
The utility model relates to an energy-saving synthetic ammonia decarbonization system for avoiding bubbling, which belongs to the field of synthetic ammonia.
Background
The total flow of the process for synthesizing ammonia in a nitrogenous fertilizer plant is as follows: the natural gas from long-distance pipeline firstly enters natural gas distribution station, the natural gas is buffered and pressure-regulated in the distribution station and then enters normal-temperature desulfurization system of synthetic ammonia device, and then natural gas is compressed, desulfurized at high temperature and converted into heat-exchange type first-stage steamTwo-stage oxygen-enriched air conversion, high-low temperature carbon monoxide conversion, improved hot potash decarburization, methanation and deep purification to remove residual CO and CO2Compressing the synthesis gas, synthesizing ammonia under 14.0MPa, and freezing and separating to obtain the product liquid ammonia.
The decarburization system adopts a Benfel method (namely an improved hot potash method) to remove CO2, and the currently adopted process flow is as follows: the process gas from the low shift process enters CO from the lower part2Absorption column, process gas and secondary CO2The semi-barren solution and barren solution entering from the middle part and the upper part of the absorption tower are subjected to countercurrent contact washing in the tower, and CO in the low-shift gas is reduced2The gas is absorbed and removed by the solution reaction, and the purified process gas is subjected to demethanization.
In CO2In the absorption tower, the solution and CO2The gas becomes rich liquid (i.e. K) after reaction2CO3The solution is mostly reacted to KHCO3Solution), CO2The operating pressure of the absorption column is about 2.8MPa, and CO2The operating pressure of the regeneration tower is about 0.06MPa, the pressure difference of the rich liquid entering the regeneration tower from the absorption tower is very large, and the rich liquid is separated from CO in order to recover the energy2The rich liquid enters into a hydraulic turbine for energy recovery after coming out from the bottom of the absorption tower, and then enters into CO from the upper part2And (4) a regeneration tower. Rich solution in CO2The regeneration tower is heated and stripped by steam from the middle part and the bottom part of the tower to obtain KHCO3Decomposition of the solution to K2CO3And CO2Gas, CO2The gas is directly discharged from the top of the tower. Semi-lean solution from CO2The solution enters a flash evaporation tank after coming out from the middle part of the regeneration tower, the solution is subjected to pressure reduction flash evaporation in the flash evaporation tank, and part of KHCO is obtained3Decomposition of the solution to K2CO3Then becomes semi-barren liquor, is pressurized to about 3.0MPa by a semi-barren liquor pump and then is sent to CO2The middle part of the absorption tower is recycled. CO coming out of the top of the flash drum2The gas and part of the steam are returned to CO2The regeneration tower participates in heating and stripping the rich liquid. A small portion of the solution in CO2The bottom of the regeneration tower is continuously heated and decomposed by a reboiler to become barren liquor, and the heat of the reboiler comes from high-temperature process gas in the low-temperature process. Lean liquid from CO2The lean solution enters a lean solution/desalted water heat exchanger for heat exchange and cooling after coming out of the bottom of the regeneration tower, then enters a lean solution water cooler and circulating water for continuous heat exchange and cooling, the temperature of the lean solution is reduced from about 116 ℃ to about 70 ℃, and most of the solution is directly sent to CO after being pressurized to about 3.0MPa by a lean solution pump2The upper part of the absorption tower is recycled, and a small part of solution enters a filter to remove impurities in the solution and then is sent to CO2The upper part of the absorption tower is recycled.
In the production process, the decarbonizing solution becomes more and more dirty along with the prolonging of the operation time of the ammonia synthesis device. This is mainly due to the fact that the corrosion of the equipment, pipes, packings, etc. of the decarbonization system is increasing, configuration K2CO3The solution will bring some impurities into the decarbonizing solution, and the catalyst powder in the conversion process is brought into the decarbonizing solution by the process gas. If the impurities in the solution are not cleaned in time, the decarbonizing solution will continuously bubble, which will cause CO2Absorption column and CO2The pressure difference of the regeneration tower becomes large, and flooding and CO generation can be caused in severe cases2The decarbonized liquid in the absorption tower is carried into a methanation process to obtain CO2The decarbonization liquid in the regeneration tower is carried out of the system, and the like. This can result in significant losses of decarbonated liquor and also in failure of the methanation catalyst, eventually leading to the failure of the ammonia synthesis plant to operate and shut down. In order to solve the problem of foaming of the decarbonized solution, the filter is only arranged behind the barren liquor pump in the prior art to enhance the filtration of the solution, and the method has slow effect and needs to be continuously carried out for a long time. If the decarbonizing liquid is suddenly foamed in a large amount, the system cannot solve the problem.
SUMMERY OF THE UTILITY MODEL
In view of the above technical problems, an object of the present invention is to provide an energy-saving synthetic ammonia decarbonization system that avoids bubbling.
In order to realize the purpose, the technical scheme of the utility model is that: an energy-saving synthetic ammonia decarbonization system capable of avoiding foaming comprises a carbon dioxide absorption tower and a carbon dioxide regeneration tower, wherein a bottom rich liquid discharge pipeline of the carbon dioxide absorption tower is connected with a hydraulic turbine, an outlet pipeline of the hydraulic turbine is connected with an upper rich liquid inlet pipeline of the carbon dioxide regeneration tower, a semi-lean liquid and a lean liquid at the bottom of the carbon dioxide regeneration tower respectively enter a flash tank and a lean liquid/desalted water heat exchanger, an outlet pipeline of the flash tank is connected with a semi-lean liquid pump, an outlet pipeline of the semi-lean liquid pump is connected with a semi-lean liquid inlet in the middle of the carbon dioxide absorption tower, a lean liquid outlet pipeline of the lean liquid/desalted water heat exchanger is connected with a lean liquid water cooler, an outlet of the lean liquid water cooler is connected with a lean liquid pump, an outlet pipeline of the lean liquid pump is connected with a lean liquid filter, and an outlet pipeline of the lean liquid filter is connected with a lean liquid, the method is characterized in that: still include solution preparation groove and sprayer, be connected with desalination water pipe way and defoaming agent pipeline on the solution preparation groove, the bottom of solution preparation groove is provided with stirring nitrogen pipeline let in nitrogen gas and play the stirring effect to the solution in the solution preparation groove, the outlet line of solution preparation groove links to each other with the liquid inlet pipeline of sprayer, the outlet line of barren liquor pump divides an sprayer branch pipe and links to each other with the power liquid inlet pipeline of sprayer, the outlet line of sprayer divides two branch pipes and communicates with the outlet line of barren liquor/desalination water heat exchanger and the outlet line of flash drum respectively, be provided with the check valve on every branch pipe of the outlet line of sprayer, be provided with low pressure steam on the branch pipe of the outlet line of the sprayer that links to each other with flash drum outlet line and add the pipeline.
By adopting the scheme, the solution preparation tank is arranged, the defoaming agent solution is prepared in the solution preparation tank, and the solution is stirred by nitrogen so as to be uniform. According to long-term observation, the phenomenon of foaming of the decarbonization solution is mainly generated in a carbon dioxide absorption tower, and the phenomenon of foaming does not occur in a carbon dioxide regeneration tower basically, so that the foaming of the decarbonization solution is avoided by adding a defoaming agent into the barren solution and the semi-barren solution through an ejector, the method is high in speed and takes effect quickly, and bubbles in the solution can be broken away within a few minutes. The ejector is adopted to eject the defoaming agent, and the high-pressure solution at the outlet of the lean solution pump is used as the power of the ejector, so that the energy is saved compared with an injection pump. And because the defoaming agent system is frequently used, the ejector is adopted to replace the injection pump, so that the problems that the starting and stopping frequency of the injection pump is high, the faults are more, the overhauling workload is high, the maintenance cost is high and the labor intensity of workers is reduced can be avoided.
The crystallization temperature of the semi-barren solution is high, and when the temperature is low in winter, the solution from the defoaming agent added into the pipeline to the inlet section of the semi-barren solution pump is easy to crystallize and block, so that the defoaming agent cannot be added into the carbon dioxide absorption tower in time, and the production is unstable. Therefore, a low-pressure steam adding pipeline is arranged, and the problem of blockage of semi-barren liquor crystallization is avoided through adding the low-pressure steam.
In the scheme, the method comprises the following steps: and valves are respectively arranged on the inlet pipeline and the outlet pipeline of the ejector.
In the scheme, the method comprises the following steps: the lean solution pump outlet pipeline is also divided into a branch pipe which is connected with an outlet pipeline of the lean solution filter, and a valve is arranged on the branch pipe.
In the scheme, the method comprises the following steps: and a control valve is arranged on the low-pressure steam adding pipeline. The adding amount of the steam is convenient to control.
Has the advantages that: the utility model discloses an avoid foamy energy-conserving synthetic ammonia decarbonization system is through adding the foaming agent in barren solution and half barren solution, avoids the decarbonization liquid to blister. The foaming agent is stirred in the solution preparation tank by nitrogen, so that energy is saved and the uniform preparation of the foaming agent is ensured. The foaming agent is sprayed through the sprayer, so that the effects of saving energy and reducing consumption are achieved. By adding low-pressure steam, the phenomenon that the semi-barren solution is crystallized and blocks a pipeline due to the addition of the foaming agent is avoided. Is beneficial to improving the economic benefit and the social benefit of enterprises.
Drawings
Fig. 1 is a process flow diagram of the present invention.
Detailed Description
The invention will be further described by way of examples with reference to the accompanying drawings:
example 1, as shown in fig. 1, an energy-saving synthetic ammonia decarbonization system for avoiding foaming is composed of a carbon dioxide absorption tower 1, a carbon dioxide regeneration tower 2, a hydraulic turbine 3, a flash tank 4, a semi-lean liquid pump 5, a lean liquid/desalted water heat exchanger 6, a lean liquid water cooler 7, a lean liquid pump 8, a lean liquid filter 9, a solution preparation tank 10, an ejector 11, a nitrogen stirring pipeline 12, a check valve 13, a control valve 14, a valve 15, a reboiler 16 and connecting pipes.
A rich liquid discharge pipeline at the bottom of the carbon dioxide absorption tower 1 is connected with a hydraulic turbine 3, an outlet pipeline of the hydraulic turbine 3 is connected with a rich liquid inlet pipeline at the upper part of a carbon dioxide regeneration tower 2, a semi-lean liquid and a lean liquid at the bottom of the carbon dioxide regeneration tower 2 respectively enter a flash tank 4 and a lean liquid/desalted water heat exchanger 6, part of solution of the carbon dioxide regeneration tower 2 also enters a reboiler 16, and returns to the carbon dioxide regeneration tower 2 after being heated and decomposed in the reboiler 16.
The outlet pipeline of the flash tank 4 is connected with a semi-barren liquor pump 5, the outlet pipeline of the semi-barren liquor pump 5 is connected with a semi-barren liquor inlet in the middle of the carbon dioxide absorption tower 1, the solution is subjected to pressure reduction flash evaporation in the flash tank 4, and part of KHCO is obtained3Decomposition of the solution to K2CO3Then becomes semi-barren liquor, is pressurized to about 3.0MPa by a semi-barren liquor pump 5 and is sent to the middle part of the carbon dioxide absorption tower 1 for recycling. CO coming out of the top of the flash drum 42The gas and part of the steam return to the carbon dioxide regeneration tower 2 to participate in heating and stripping the rich liquid.
A lean solution outlet pipeline of the lean solution/desalted water heat exchanger 6 is connected with a lean solution water cooler 7, an outlet of the lean solution water cooler 7 is connected with a lean solution pump 8, an outlet pipeline of the lean solution pump 8 is connected with a lean solution filter 9, and an outlet pipeline of the lean solution filter 9 is connected with a lean solution inlet of the carbon dioxide absorption tower 1.
The solution preparation tank 10 is connected with a desalted water pipeline and an antifoaming agent pipeline, the bottom of the solution preparation tank 10 is provided with a nitrogen stirring pipeline 12, the nitrogen stirring pipeline 12 is provided with a valve 15, nitrogen is introduced into the solution preparation tank 10 to stir the solution in the solution preparation tank 10, and the prepared antifoaming agent is ensured to be uniform in concentration. An outlet pipeline of the solution preparation tank 10 is connected with a liquid inlet pipeline of an ejector 11, an outlet pipeline of a barren liquor pump 8 is divided into an ejector branch pipe to be connected with a power liquid inlet pipeline of the ejector 11, an outlet pipeline of the ejector 11 is divided into two branch pipes to be respectively communicated with an outlet pipeline of the barren liquor/desalted water heat exchanger 6 and an outlet pipeline of the flash tank 4, each branch pipe of the outlet pipeline of the ejector 11 is provided with a check valve 13, a branch pipe of the outlet pipeline of the ejector 11 connected with the outlet pipeline of the flash tank is provided with a low-pressure steam adding pipeline, and the low-pressure steam adding pipeline is provided with a control valve 14. Valves 15 are provided on the inlet and outlet lines of the ejector 11, respectively. The lean solution pump outlet line is further branched to be connected to an outlet line of the lean solution filter 9, and a valve 15 is provided in the branched line.
The present invention is not limited to the above embodiments, and those skilled in the art can understand that: various changes, modifications, substitutions and alterations can be made to the embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the claims and their equivalents.

Claims (4)

1. An energy-saving synthetic ammonia decarbonization system capable of avoiding foaming comprises a carbon dioxide absorption tower and a carbon dioxide regeneration tower, wherein a bottom rich liquid discharge pipeline of the carbon dioxide absorption tower is connected with a hydraulic turbine, an outlet pipeline of the hydraulic turbine is connected with an upper rich liquid inlet pipeline of the carbon dioxide regeneration tower, a semi-lean liquid and a lean liquid at the bottom of the carbon dioxide regeneration tower respectively enter a flash tank and a lean liquid/desalted water heat exchanger, an outlet pipeline of the flash tank is connected with a semi-lean liquid pump, an outlet pipeline of the semi-lean liquid pump is connected with a semi-lean liquid inlet in the middle of the carbon dioxide absorption tower, a lean liquid outlet pipeline of the lean liquid/desalted water heat exchanger is connected with a lean liquid water cooler, an outlet of the lean liquid water cooler is connected with a lean liquid pump, an outlet pipeline of the lean liquid pump is connected with a lean liquid filter, and an outlet pipeline of the lean liquid filter is connected with a lean liquid, the method is characterized in that: still include solution preparation groove and sprayer, be connected with desalination water pipe way and defoaming agent pipeline on the solution preparation groove, the bottom of solution preparation groove is provided with stirring nitrogen pipeline let in nitrogen gas and play the stirring effect to the solution in the solution preparation groove, the outlet line of solution preparation groove links to each other with the liquid inlet pipeline of sprayer, the outlet line of barren liquor pump divides an sprayer branch pipe and links to each other with the power liquid inlet pipeline of sprayer, the outlet line of sprayer divides two branch pipes and communicates with the outlet line of barren liquor/desalination water heat exchanger and the outlet line of flash drum respectively, be provided with the check valve on every branch pipe of the outlet line of sprayer, be provided with low pressure steam on the branch pipe of the outlet line of the sprayer that links to each other with flash drum outlet line and add the pipeline.
2. The energy-saving synthetic ammonia decarbonization system for avoiding the bubbling according to claim 1, characterized in that: and valves are respectively arranged on the inlet pipeline and the outlet pipeline of the ejector.
3. The energy-saving synthetic ammonia decarbonization system for avoiding the bubbling according to claim 2, characterized in that: the lean solution pump outlet pipeline is also divided into a branch pipe which is connected with an outlet pipeline of the lean solution filter, and a valve is arranged on the branch pipe.
4. The energy-saving synthetic ammonia decarbonization system for avoiding the bubbling according to any one of claims 1 to 3, characterized in that: and a control valve is arranged on the low-pressure steam adding pipeline.
CN201921576674.0U 2019-09-20 2019-09-20 Energy-saving synthetic ammonia decarburization system capable of avoiding foaming Active CN210710734U (en)

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CN201921576674.0U CN210710734U (en) 2019-09-20 2019-09-20 Energy-saving synthetic ammonia decarburization system capable of avoiding foaming

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Application Number Priority Date Filing Date Title
CN201921576674.0U CN210710734U (en) 2019-09-20 2019-09-20 Energy-saving synthetic ammonia decarburization system capable of avoiding foaming

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