CN110203986B - System and method for reducing ammonia nitrogen content - Google Patents
System and method for reducing ammonia nitrogen content Download PDFInfo
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- CN110203986B CN110203986B CN201910410357.XA CN201910410357A CN110203986B CN 110203986 B CN110203986 B CN 110203986B CN 201910410357 A CN201910410357 A CN 201910410357A CN 110203986 B CN110203986 B CN 110203986B
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Abstract
The invention relates to the technical field of coal gasification and coal gas conversion, and discloses a system and a method for reducing ammonia nitrogen content. The system comprises: the high-temperature condensate treatment device is used for steam stripping the input high-temperature conversion condensate by using the input high-pressure flash steam to generate high-temperature condensate with ammonia content meeting the condition, and outputting a gas-phase product and a liquid-phase product to the low-temperature condensate treatment device after gas-liquid separation treatment is carried out on the steam-stripped steam generated after steam stripping; the low-temperature condensate treatment device is used for stripping the liquid-phase product and the input low-temperature transformation condensate by using input low-pressure steam and gas-phase product to generate low-temperature condensate with the ammonia content meeting the condition, and carrying out gas-liquid separation treatment on stripped steam generated after stripping to generate ammonia-containing condensate and flash steam noncondensable gas. The invention can reduce the ammonia nitrogen content in the black water and the grey water of the gasification process unit, so that the ammonia nitrogen content of the grey water discharged by the gasification process unit is reduced to the extent that the sewage can be well accepted.
Description
Technical Field
The invention relates to the technical field of coal gasification and coal gas conversion, in particular to a system and a method for reducing ammonia nitrogen content.
Background
The gasification process of the water coal slurry is to carry out partial oxidation reaction on the water coal slurry and high-pressure oxygen at high temperature and high pressure, and the reaction products are crude gas and liquid slag. The gasified product enters a chilling chamber water bath with a certain water level through a downcomer, and the slag is solidified in the water bath and sinks to the bottom of the gasification furnace equipment and is periodically discharged through a lock hopper. The raw gas takes carbon monoxide, carbon dioxide and hydrogen as main components, and also has a part of impurities such as ammonia nitrogen and the like. The crude gas directly contacts with water in the chilling chamber, is cooled and then escapes to a gas outlet positioned at the upper part of the chilling chamber and is sent to a subsequent gas washing procedure.
A large amount of black water is generated in the gasification chilling process and the coal gas washing process (part of residual carbon and coal ash enter water in the process to enable the black water to be black water), the black water is clarified and settled after multi-stage flash evaporation, most of generated grey water is recycled, and a small part of the generated grey water is discharged for biochemical treatment.
In the gasification chilling process and the coal gas washing process, part of ammonia nitrogen in the coal gas can be dissolved and enter black water, and most of ammonia nitrogen enters a conversion process along with the crude coal gas. The ammonia nitrogen entering the conversion process enters black water of a gasification process unit along with heat recovery of crude gas and heat recovery of conversion gas after conversion reaction, a part of the ammonia nitrogen enters produced high-temperature conversion condensate after heat recovery, and returns to the gasification process unit, a part of the ammonia nitrogen enters ammonia washing water along with the conversion gas, is subjected to low-temperature low-pressure stripping, and then returns to the gasification process unit along with the low-temperature conversion condensate (tower bottom liquid), and the non-condensable gas of flash steam generated by stripping at the tower top can send a part of the ammonia nitrogen out. Most of the ammonia nitrogen in the raw gas entering the conversion returns to a washing tower of the gasification process unit along with the high-temperature conversion condensate to enter into the black water, and a small part of the ammonia nitrogen returns to a deaerator of the gasification process unit along with the low-temperature conversion condensate to enter into the grey water, so that the ammonia nitrogen content in the black water and the grey water of the gasification process unit is very high.
The quantity of ammonia nitrogen produced by gasification reaction is closely related to the coal feeding quantity, the gasification pressure and the temperature, and the ammonia nitrogen content in the ash water system tends to rise under the influence of the coal quality, the gasification pressure and the coal feeding quantity of raw materials after the coal water slurry gasification device is enlarged, generally the ammonia nitrogen content in the ash water system is 400-600 mg/L (mg/L), and some factories are even higher.
The requirement of the biochemical treatment system on ammonia nitrogen in the incoming water is less than 300mg/L, and the ammonia nitrogen in the discharged water exceeds the biochemical treatment design capacity. At present, various companies adopt an alkali-added air stripping process or an alkali-added steam stripping process for removing ammonia nitrogen in discharged grey water. In order to achieve good removal effect, alkali liquor is added to adjust the pH value of the grey water to about 11.5. Wherein, the grey water is not only high in ammonia nitrogen, but also high in hardness (total hardness is about 1000-1800mg/L) and alkalinity (total alkalinity is about 500-1300mg/L), the scaling rate is greatly increased after the PH value is increased, scaling and blockage are required to be stopped for maintenance when the equipment is operated for 7-15 days, and the stable operation cannot be realized. Thereby the problem of high ammonia nitrogen content in the black water is not effectively solved.
The high-pressure flash steam flashed by the black water in the gasification process unit in the high-pressure flash tank in the black water flash evaporation process is still at 173 ℃ after part of heat is recovered by the grey water heater. The condensed liquid is separated after the flash steam is cooled to about 40 to 50 ℃ by a water cooler, and the flash steam is sent to a sulfur recovery unit or a torch incineration disposal without condensing. A large amount of circulating water is consumed in the cooling process, and the proportion of carbon monoxide and hydrogen in the flash steam noncondensable gas accounts for more than 50%, so that the energy conservation and the environmental protection are not facilitated.
The prior reported patent technologies are more, and the patents only carry out steam stripping treatment and the like on the transformed low-temperature condensate (mainly the washing water of the transformed gas ammonia washing tower) and do not treat the transformed high-temperature transformed condensate with large proportion, so the problem of high ammonia nitrogen content in black water and grey water of a gasification process unit is not solved well.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a system and a method for reducing the ammonia nitrogen content, which can solve the technical problem that the ammonia nitrogen content of black water and grey water in a gasification process unit is high in the prior art.
The invention provides a system for reducing ammonia nitrogen content in a first aspect, which comprises:
the high-temperature condensate treatment device is used for steam stripping the input high-temperature conversion condensate by using the input high-pressure flash steam to generate high-temperature condensate with ammonia content meeting the conditions, and outputting a gas-phase product and a liquid-phase product to the low-temperature condensate treatment device after heat recovery and gas-liquid separation treatment are carried out on the steam-stripped steam generated after steam stripping;
the low-temperature condensate treatment device is used for stripping the liquid-phase product and the input low-temperature transformation condensate by using the input low-pressure steam and the input gas-phase product to generate low-temperature condensate with the ammonia content meeting the condition, and carrying out gas-liquid separation treatment on the stripped steam generated after stripping to generate ammonia-containing condensate and flash steam noncondensable gas.
Optionally, the high-temperature condensate treatment device includes: the high-temperature condensate stripping tower, the high-temperature condensate pump, the waste boiler and the stripping separator; the low-temperature condensate treatment device comprises: the system comprises a low-temperature condensate stripping tower, an air cooler, a water cooler, a low-temperature condensate pump, a separation washer, a flash steam compressor and an ammonia-containing condensate pump;
the bottom of the high-temperature condensate stripping tower is communicated with the high-temperature condensate pump, and the top of the high-temperature condensate stripping tower is communicated with the waste boiler;
the waste pot is communicated with the middle part of the stripping separator;
the top of the stripping separator is communicated with the middle part of the low-temperature condensate stripping tower, and the bottom of the stripping separator is communicated with the middle part of the low-temperature condensate stripping tower;
the bottom of the low-temperature condensate stripping tower is communicated with the low-temperature condensate pump, and the top of the low-temperature condensate stripping tower is connected to the air cooler and the water cooler in sequence and then communicated with the middle of the separation washer;
the top of the separation scrubber is communicated with the flash steam compressor, and the bottom of the separation scrubber is communicated with the ammonia-containing condensate pump.
Optionally, the high-temperature condensate treatment device further comprises a hydraulic turbine, and the hydraulic turbine is communicated with the upper part of the high-temperature condensate stripping tower.
Optionally, the hydraulic turbine is configured to recycle the high-pressure potential energy of the input high-temperature shift condensate and output the high-temperature shift condensate to the upper portion of the high-temperature condensate stripping tower;
the lower part of the high-temperature condensate stripping tower is used for inputting high-pressure flash steam from a gasification process unit to be used as stripping steam for stripping out the soluble gas in the high-temperature conversion condensate; the bottom of the high-temperature condensate pump is used for outputting the high-temperature condensate to the high-temperature condensate pump; the high-temperature condensate pump is used for boosting the pressure of the high-temperature condensate and then sending the high-temperature condensate to the gasification process unit; the top of the waste heat recovery device is used for outputting stripping steam to the waste heat recovery device; the waste boiler is used for accommodating and generating and outputting low-pressure steam through the heat of the input stripping steam;
the stripping separator is used for carrying out gas-liquid separation on stripping steam from the waste boiler, and the top of the stripping separator is used for inputting a generated gas-phase product to the middle part of the low-temperature condensate stripping tower to be used as a stripping heat source; the bottom of the low-temperature condensate stripper is used for inputting the generated liquid-phase product to the middle part of the low-temperature condensate stripper to be stripped continuously;
the upper part of the low-temperature condensate stripping tower is also used for inputting the low-temperature shift condensate from a shift ammonia washing tower; the lower part of the low-pressure conversion condensate is also used for inputting the low-pressure steam to be used as stripping steam to strip out the soluble gas in the low-temperature conversion condensate; the bottom of the low-temperature condensate pump is used for outputting the low-temperature condensate to the low-temperature condensate pump; the low-temperature condensate pump is used for pressurizing the low-temperature condensate and then sending the low-temperature condensate to the gasification process unit; the top of the separator is used for outputting flash steam, and the flash steam is conveyed to the middle part of the separation washer after passing through the air cooler and the water cooler in sequence;
the separation scrubber is used for carrying out gas-liquid separation and washing on the flash steam, and the upper part of the separation scrubber is used for inputting washing water so as to wash the generated gas-phase product and remove ammonia; the top of the flash evaporation compressor is used for outputting the generated flash evaporation non-condensable gas to the flash evaporation compressor; the flash steam compressor is used for pressurizing and conveying the flash steam noncondensable gas to the conversion unit to be used as a raw material gas; the bottom of the condenser is used for outputting ammonia-containing condensate to the ammonia-containing condensate pump; and the ammonia-containing condensate pump is used for pressurizing the ammonia-containing condensate and then sending the ammonia-containing condensate to the ammonia refining unit.
Optionally, the lower part of the high-temperature condensate stripping tower is also used for inputting low-pressure steam to serve as standby stripping steam under the condition of load fluctuation or abnormal operation.
The second aspect of the invention provides a method for reducing the content of ammonia nitrogen, which comprises the following steps:
steam stripping the high-temperature conversion condensate by using high-pressure flash steam to generate high-temperature condensate with ammonia content meeting the conditions, and outputting a gas-phase product and a liquid-phase product after heat recovery and gas-liquid separation treatment of the steam-stripped steam;
and (3) carrying out steam-liquid separation treatment on the stripped steam generated after steam stripping to generate ammonia-containing condensate and flash steam noncondensable gas.
Optionally, the step of steam stripping the high-temperature shift condensate by using high-pressure flash steam to generate a high-temperature condensate with ammonia content meeting the condition, and outputting the gas-phase product and the liquid-phase product after performing gas-liquid separation treatment on the steam-stripped steam generated after steam stripping further comprises: and introducing the high-temperature transformation condensate into a hydraulic turbine to recycle the high-pressure potential energy of the high-temperature transformation condensate.
Optionally, the step of using low-pressure steam and the gas-phase product to strip the liquid-phase product and the low-temperature shift condensate to generate a low-temperature condensate with ammonia content meeting the condition, and performing gas-liquid separation treatment on stripped steam generated after stripping to generate an ammonia-containing condensate and a flash steam noncondensable gas comprises:
inputting the high-temperature shift condensate to the upper part of a high-temperature condensate stripping tower;
inputting the high pressure flash steam from the gasification process unit into a lower portion of the high temperature condensate stripper column to strip out the dissolved gases in the high temperature shift condensate as stripping steam;
boosting the high-temperature condensate output from the bottom of the high-temperature condensate stripping tower by a high-temperature condensate pump and then sending the boosted high-temperature condensate to the gasification process unit;
inputting stripping steam output from the top of the high temperature condensate stripper to a waste pot, such that the waste pot contains and generates and outputs low and low pressure steam from the heat of the input stripping steam;
and inputting the stripping steam from the waste boiler into a stripping separator to perform gas-liquid separation and obtain a gas-phase product and a liquid-phase product.
Optionally, the method further includes: and inputting low-pressure steam to the lower part of the high-temperature condensate stripping tower to serve as standby stripping steam under the condition of load fluctuation or abnormal operation.
Optionally, the step of using low-pressure steam and the gas-phase product to strip the liquid-phase product and the low-temperature shift condensate to generate a low-temperature condensate with ammonia content meeting the condition, and performing gas-liquid separation treatment on stripped steam generated after stripping to generate an ammonia-containing condensate and a flash steam noncondensable gas comprises:
inputting a gas-phase product generated at the top of the stripping separator into the middle part of a low-temperature condensate stripping tower to be used as a stripping heat source;
inputting the liquid-phase product generated at the bottom of the stripping separator into the middle part of the low-temperature condensate stripping tower for continuous stripping;
feeding the low temperature shift condensate from the shift ammonia wash column to an upper portion of the low temperature condensate stripper column;
feeding the low-pressure steam to a lower portion of the cryogenic condensate stripper column to combine the vapor phase product as a stripping steam to strip out the dissolved gases in the cryogenic shift condensate and the liquid phase product;
boosting the low-temperature condensate output from the bottom of the low-temperature condensate stripping tower by a low-temperature condensate pump and then sending the low-temperature condensate to the gasification process unit;
the flash steam output from the top of the low-temperature condensate stripping tower is sequentially sent to the middle part of a separation washer through an air cooler and a water cooler to carry out gas-liquid separation;
feeding wash water into the upper part of the separator scrubber to wash and remove ammonia from the resulting gas phase product;
pressurizing and conveying the flash steam noncondensable gas output from the top of the separation scrubber to a conversion unit by a flash steam compressor to be used as raw material gas;
and pressurizing the ammonia-containing condensate output from the bottom of the separator scrubber by an ammonia-containing condensate pump, and then sending the ammonia-containing condensate to an ammonia refining unit.
The invention can reduce the ammonia nitrogen content in the black water and the grey water of the gasification process unit, so that the ammonia nitrogen content of the discharged grey water is reduced to the extent that the sewage can be well accepted. Meanwhile, the waste heat and effective components of the high-pressure flash steam of the gasification process unit can be recovered.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a schematic structural diagram of a system for reducing ammonia nitrogen content according to a first embodiment of the present invention;
FIG. 2 is a schematic structural diagram of a system for reducing ammonia nitrogen content according to a second embodiment of the present invention;
fig. 3 is a schematic flow chart of a method for reducing ammonia nitrogen content according to a third embodiment of the present invention.
Detailed Description
In order to make the objects, features and advantages of the present invention more obvious and understandable, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, not all of the embodiments. All other embodiments, which can be obtained by a person skilled in the art without making creative efforts based on the embodiments of the present invention, belong to the protection scope of the present invention.
Referring to fig. 1, fig. 1 is a schematic structural diagram of a system for reducing ammonia nitrogen content according to an embodiment of the present invention.
As shown in fig. 1, the first aspect of the present invention provides a system for reducing ammonia nitrogen content, comprising:
the high-temperature condensate treatment device 1 is used for steam stripping the input high-temperature conversion condensate by using the input high-pressure flash steam to generate high-temperature condensate with ammonia content meeting the conditions, and outputting a gas-phase product and a liquid-phase product to the low-temperature condensate treatment device 2 after heat recovery and gas-liquid separation treatment are carried out on the steam-stripped steam generated after steam stripping. Preferably, the high-temperature condensate treatment device 1 is also used for generating low-pressure steam as a byproduct by using the heat of the stripping steam.
And the low-temperature condensate treatment device 2 is used for stripping the liquid-phase product and the input low-temperature transformation condensate by using input low-pressure steam and gas-phase product to generate low-temperature condensate with the ammonia content meeting the condition, and carrying out gas-liquid separation treatment on stripped steam generated after stripping to generate ammonia-containing condensate and flash steam noncondensable gas. The gas phase product is flash steam non-condensable gas, and the liquid phase product is ammonia-containing condensate.
In the present invention, the ammonia content in both the high temperature condensate and the low temperature condensate is less than 200ppm (parts per million). Preferably, the low-pressure steam input into the low-temperature condensate treatment device 2 comprises the low-pressure steam output from the high-temperature condensate treatment device 1.
Referring to fig. 2, fig. 2 is a schematic structural diagram of a system for reducing ammonia nitrogen content according to a second embodiment of the present invention.
Further, as shown in fig. 2, the high-temperature condensate treatment apparatus 1 includes: a high temperature condensate stripper 20, a high temperature condensate pump 30, a waste pot 40, and a stripping separator 50. The low-temperature condensate treatment device 2 comprises: a low-temperature condensate stripper 60, an air cooler 70, a water cooler 80, a low-temperature condensate pump 90, a separation scrubber 100, a flash steam compressor 110, and an ammonia-containing condensate pump 120.
The bottom of the high-temperature condensate stripping tower 20 is communicated with a high-temperature condensate pump 30, the top of the high-temperature condensate stripping tower is communicated with a waste boiler 40, the upper part of the high-temperature condensate stripping tower is used for introducing high-temperature conversion condensate, and the lower part of the high-temperature condensate stripping tower is used for introducing high-pressure flash steam from a gasification process unit.
The waste pot 40 communicates with the middle of the stripping separator 50.
The top of the stripping separator 50 communicates with the middle of the low-temperature condensate stripper 60, and the bottom thereof communicates with the middle of the low-temperature condensate stripper 60.
As shown in fig. 2, a plurality of liquid-storing gas-guiding grooves are arranged in the high-temperature condensate stripping tower 20 and the low-temperature condensate stripping tower 60 in a staggered manner from top to bottom, and it can be understood that the liquid to be stripped is stored in the liquid-storing gas-guiding grooves, and stripping steam is introduced from the bottom to top to strip the liquid.
The bottom of the low-temperature condensate stripping tower 60 is communicated with a low-temperature condensate pump 90, and the top of the low-temperature condensate stripping tower is communicated with the middle of the separation washer 100 after being sequentially connected with the air cooler 70 and the water cooler 80.
The separation scrubber 100 is in communication at the top with a flash vapor compressor 110 and at the bottom with an ammonia-containing condensate pump 120.
Further, as shown in fig. 2, the high temperature condensate treatment apparatus 1 further includes a hydraulic turbine 10, and the hydraulic turbine 10 is communicated with an upper portion of the high temperature condensate stripping tower 20.
Further, the hydraulic turbine 10 is used to recycle the high-pressure potential energy of the input high-temperature shift condensate and output the high-temperature shift condensate to the upper portion of the high-temperature condensate stripper 20.
The lower part of the high-temperature condensate stripping tower 20 is used for inputting high-pressure flash steam from a gasification process unit to be used as stripping steam for stripping out soluble gas in the high-temperature conversion condensate; the bottom of which is used to output high temperature condensate to the high temperature condensate pump 30. The high-temperature condensate pump 30 is used for boosting the pressure of the high-temperature condensate and then sending the high-temperature condensate to the gasification process unit; the top of which is used to output stripping steam to the waste boiler 40. The waste boiler 40 is used for accommodating and generating low-pressure steam by the heat of the input stripping steam and outputting the low-pressure steam.
The stripping separator 50 is used for carrying out gas-liquid separation on the stripping steam from the waste boiler 40, and the top of the stripping separator is used for inputting the generated gas-phase product to the middle part of the low-temperature condensate stripping tower 60 to be used as a stripping heat source; the bottom of the low-temperature condensate stripper is used for inputting the generated liquid-phase product to the middle part of the low-temperature condensate stripper 60 for continuous stripping.
The upper part of the low-temperature condensate stripping tower 60 is also used for inputting low-temperature shift condensate from a shift ammonia washing tower; the lower part of the low-pressure conversion condenser is also used for inputting low-pressure steam which is used as stripping steam to strip out the soluble gas in the low-temperature conversion condensate; the bottom of which is used to output low temperature condensate to a low temperature condensate pump 90. The low-temperature condensate pump 90 is used for pressurizing the low-temperature condensate and then sending the low-temperature condensate to the gasification process unit; the top of the separator is used for outputting flash steam, and the flash steam is sent to the middle part of the separation scrubber 100 after passing through the air cooler 70 and the water cooler 80 in sequence.
The separation scrubber 100 is used for separating gas from liquid and washing flash steam, and the upper part of the separation scrubber is used for inputting washing water so as to wash the generated gas-phase product and remove ammonia; the top of the flash evaporation compressor is used for outputting the generated flash evaporation non-condensable gas to the flash evaporation compressor 110. The flash steam compressor 110 is used for pressurizing and conveying flash steam non-condensable gas to the conversion unit to be used as raw material gas; the bottom of which is used to output ammonia-containing condensate to the ammonia-containing condensate pump 120. The ammonia-containing condensate pump 120 is configured to pressurize the ammonia-containing condensate and send the ammonia-containing condensate to the ammonia purification unit.
Further, the lower portion of the high temperature condensate stripper 20 is also used for input of low pressure steam as backup stripping steam under fluctuating loads or abnormal operating conditions.
Referring to fig. 3, fig. 3 is a schematic flow chart of a method for reducing ammonia nitrogen content according to a third embodiment of the present invention.
As shown in fig. 3, the second aspect of the present invention provides a method for reducing ammonia nitrogen content, which comprises:
s100, steam stripping is carried out on the high-temperature conversion condensate by using high-pressure flash steam to generate high-temperature condensate with ammonia content meeting the conditions, heat recovery and gas-liquid separation treatment are carried out on the steam stripping steam generated after steam stripping, and then a gas-phase product and a liquid-phase product are output. Preferably, the heat of the stripping steam can be used to generate low-pressure steam as a byproduct.
S200, carrying out steam stripping on the liquid-phase product and the low-temperature transformation condensate by using low-pressure steam and a gas-phase product to generate low-temperature condensate with ammonia content meeting the condition, and carrying out gas-liquid separation treatment on the stripped steam generated after steam stripping to generate ammonia-containing condensate and flash steam non-condensable gas.
Further, the steps of using high-pressure flash steam to steam strip the high-temperature conversion condensate to generate high-temperature condensate with ammonia content meeting the conditions, carrying out gas-liquid separation treatment on the steam-stripped steam generated after steam stripping, and outputting a gas-phase product and a liquid-phase product further comprise the following steps: the high temperature shift condensate is fed into the hydraulic turbine 10 to recycle the high pressure potential energy of the high temperature shift condensate.
Further, the steps of using low-pressure steam and gas phase products to carry out steam stripping on the liquid phase products and the low-temperature transformation condensate liquid to generate low-temperature condensate liquid with ammonia content meeting the conditions, and carrying out gas-liquid separation treatment on the steam stripping steam generated after steam stripping to generate ammonia-containing condensate liquid and flash steam non-condensable gas comprise:
the high temperature shift condensate is fed to the upper part of the high temperature condensate stripper 20.
High pressure flash steam from the gasification process unit is input to the lower portion of the high temperature condensate stripper 20 to be used as stripping steam to strip out the soluble gases in the high temperature shift condensate.
The high-temperature condensate output from the bottom of the high-temperature condensate stripping tower 20 is pressurized by a high-temperature condensate pump 30 and then sent to the gasification process unit.
The stripping steam output from the top of the high temperature condensate stripper 20 is input to the waste pot 40 such that the waste pot 40 receives and generates and outputs low and low pressure steam by the heat of the input stripping steam.
The stripping gas from the waste pot 40 is inputted to a stripping separator 50 to perform gas-liquid separation and obtain a gas-phase product and a liquid-phase product.
Further, the method further comprises: the low pressure steam is fed into the lower portion of the high temperature condensate stripper 20 as backup stripping steam under fluctuating loads or abnormal operating conditions.
Further, the steps of using low-pressure steam and gas phase products to carry out steam stripping on the liquid phase products and the low-temperature transformation condensate liquid to generate low-temperature condensate liquid with ammonia content meeting the conditions, and carrying out gas-liquid separation treatment on the steam stripping steam generated after steam stripping to generate ammonia-containing condensate liquid and flash steam non-condensable gas comprise:
the gas phase product produced at the top of the stripping separator 50 is fed to the middle of the low temperature condensate stripper 60 as a stripping heat source.
The liquid phase product produced at the bottom of the stripping separator 50 is fed to the middle of the low temperature condensate stripper 60 for further stripping.
The low temperature shift condensate from the shift ammonia scrubber is fed to the upper portion of the low temperature condensate stripper 60.
Low pressure steam is fed to the lower portion of the low temperature condensate stripper 60 to strip out the dissolved gases in the low temperature shift condensate and the liquid phase product in combination with the vapor phase product as stripping steam.
The low-temperature condensate output from the bottom of the low-temperature condensate stripper 60 is pressurized by a low-temperature condensate pump 90 and then sent to the gasification process unit.
The flash steam output from the top of the low-temperature condensate stripping tower 60 passes through the air cooler 70 and the water cooler 80 in sequence and then is sent to the middle of the separation scrubber 100 for gas-liquid separation.
Wash water is fed into the upper portion of the separator scrubber 100 to scrub and remove ammonia from the resulting gas phase product.
The flash steam noncondensable gas output from the top of the separation scrubber 100 is pressurized and sent to the conversion unit by a flash steam compressor 110 to be used as raw material gas.
The ammonia-containing condensate output from the bottom of the separator scrubber 100 is pressurized by the ammonia-containing condensate pump 120 and then sent to the ammonia purification unit.
The invention can reduce the ammonia nitrogen content in the black water and the grey water of the gasification process unit, so that the ammonia nitrogen content of the discharged grey water is reduced to the extent that the sewage can be well accepted. Meanwhile, the waste heat and effective components of high-pressure flash steam in the gasification process unit can be recovered.
As shown in fig. 2, the working principle of the present invention is as follows: the conversion process adopts partial conversion of carbon monoxide, high-temperature conversion condensate with the pressure of about 192 ℃ and the pressure of 5.7MPaG (gauge pressure MPa) obtained by a conversion loop and a non-conversion loop is reduced to about 1.0MPaG after energy is recovered by a hydraulic turbine 10, the high-temperature conversion condensate enters a high-temperature condensate stripping tower 20 from the upper part of the tower, and high-pressure flash steam with the pressure of about 173 ℃ and 0.8MPaG from a gasification process unit enters the high-temperature condensate stripping tower 20 from the lower part of the tower for stripping. In the high-temperature condensate stripping tower 20, high-pressure flash steam of the gasification process unit is used as stripping steam, the heat carried by the steam is used for stripping out the soluble gas in the high-temperature conversion condensate, the ammonia content in the high-temperature condensate flowing out from the bottom of the high-temperature condensate stripping tower 20 is less than 200ppm (parts per million), and the high-temperature condensate is directly sent to the gasification process unit for recycling after being boosted by a high-temperature condensate pump 30. 1.1 the low pressure steam of MPaG is the spare stripping steam with fluctuating load or abnormal operation condition, and is not used normally.
The 165 ℃ stripping steam output from the top outlet of the high-temperature condensate stripper 20 firstly passes through the waste pot 40 to recover heat, the low-pressure steam (preferably, saturated steam) with a byproduct of 0.3MPaG is sent to the whole plant for use, and the temperature is reduced to 160 ℃ after passing through the waste pot 40 and then enters the stripping stripper separator 50 for gas-liquid separation. The gas phase product at the top of the stripping separator 50 is sent to the low-temperature condensate stripping tower 60 to be used as a stripping heat source, and the liquid phase product at the bottom of the stripping separator 50 is sent to the middle part of the low-temperature condensate stripping tower 60 to be further stripped. The low-temperature shift condensate of the shift ammonia scrubber enters the low-temperature condensate stripper 60 from the upper part. Low pressure steam (preferably, low pressure superheated steam) at 0.46MPaG enters the lower portion of the low temperature condensate stripper 60 and serves as stripping steam to strip out the low temperature condensate and the dissolved gases in the liquid phase product. The content of the low-temperature condensed liquid ammonia flowing out of the bottom of the low-temperature condensed liquid stripping tower 60 is less than 200ppm, and the low-temperature condensed liquid ammonia is pressurized by a low-temperature condensed liquid pump 90 and then is sent to a gasification process unit for recycling.
The flash steam discharged from the top of the low-temperature condensate stripping tower 60 has the pressure of about 0.3MPaG and the temperature of about 130 ℃, is cooled to 50-80 ℃ through an air cooler 70, is cooled to 40 ℃ through a water cooler 80, and then enters a separation washer 100. The separated gas phase product is washed by washing water to further remove ammonia, and then sent to a flash steam compressor 110 to be pressurized and sent to the inlet of the conversion unit to be used as raw material gas for recycling. The ammonia-containing condensate at the bottom of the separator scrubber 100 is pressurized by the ammonia-containing condensate pump 120 and then sent to the ammonia purification unit for ammonia recovery.
For example, taking a methanol plant producing 180 ten thousand tons per year as an example, the gasification process unit adopts a 6.5MPaG coal water slurry gasification chilling process, and the conversion adopts a sulfur-resistant wide-temperature carbon monoxide partial conversion process. The high-pressure flash steam from the gasification process unit is 0.8MPaG, 173 ℃, the flow rate is 57t/h (ton/hour), the ammonia nitrogen content is 331ppm, the high-temperature flash steam enters the high-temperature condensate stripping tower 20 from the lower part, the high-temperature conversion condensate from the conversion separator is 192 ℃, 5.7MPaG, 564t/h and the ammonia nitrogen content is 500-700ppm, the high-temperature flash steam is decompressed to 1.0MPaG by the hydraulic turbine 10 and then enters the high-temperature condensate stripping tower 20 from the upper part, and the hydraulic turbine 10 recovers about 500KW (kilowatt) of power per hour to drive the high-temperature condensate pump 30 to be matched with the electric pump for use. 1.1MPaG of low pressure steam (preferably, low pressure superheated steam) enters from the bottom of the high temperature condensate stripper 20 with a normal usage of zero (driving or abnormal operating conditions). The high-temperature condensate at the bottom of the tower after stripping contains ammonia nitrogen of about 100ppm, 164 ℃ and 528t/h, and is pressurized to 8.5MPaG by a high-temperature condensate pump 30 and sent to a gasification process unit for recycling. The tower top gas enters the waste boiler 40, and low-pressure deoxygenated water is used for recovering heat, so that low-pressure steam (preferably, saturated steam) of 0.3MPaG and 62t/h can be generated. The temperature of the gas at the top of the waste boiler 40 is reduced to 160 ℃, and after passing through the steam stripping separator 50, the gas-phase product and the liquid-phase product both enter the middle part of the low-temperature condensate steam stripping tower 60. About 139t/h, 40 ℃ and 2000 ammonia nitrogen contentThe low-temperature shift condensate of ppm enters the upper part of a low-temperature condensate stripping tower 60, low-pressure steam (preferably low-pressure superheated steam) of 0.46MPaG is stripped in the tower to consume low-pressure steam for 20t/h, and the condensate at the bottom of the tower contains about 129ppm and 214t/h of ammonia nitrogen and is pressurized by a low-temperature condensate pump 90 and then is sent to a gasification process unit for recycling. The overhead gas is cooled to 40 ℃ by an air cooler 70 and a water cooler 80, then enters a separation scrubber 100, and the gas-phase product is scrubbed to further remove ammonia and then has a flow of 4000Nm3H (standard cubic meter per hour), 0.3MPaG (the composition of hydrogen and carbon monoxide accounts for 51 percent, and ammonia is close to 0ppm), and is pressurized and sent to the transformation process gas by a flash evaporation gas compressor 110 for utilization. 30t/h of ammonia-containing condensate with ammonia concentration of 2.0% at the bottom of the flash steam separation scrubber 100 is pressurized and sent to an ammonia refining unit by an ammonia-containing condensate pump 120 to recover ammonia.
After ammonia nitrogen is reduced by stripping the transformed high-temperature condensate and low-temperature condensate, the transformed high-temperature condensate and low-temperature condensate are sent back to the coal slurry gasification process unit, so that the ammonia nitrogen amount brought into the gasification process unit is greatly reduced, the ammonia nitrogen in black water and grey water of the gasification process unit is well reduced, and the ammonia nitrogen in the grey water discharged from the gasification process unit for biochemical treatment can be reduced to be below 300 ppm. The device is beneficial to long-period stable operation, simultaneously recovers the waste heat and the effective gas of the high-pressure flash steam, and improves the economic benefit and the environmental protection benefit of the operation of the device.
The invention mainly aims to reduce the ammonia nitrogen content in black water and grey water of a gasification process unit, so that the ammonia nitrogen content of the grey water discharged by the gasification process unit is reduced to a degree that sewage can be well accepted. Meanwhile, the waste heat and effective components of high-pressure flash steam in the gasification process unit are recovered.
A small part of ammonia nitrogen produced by the gasification reaction of the gasification process unit enters black water, and most of ammonia nitrogen enters the conversion unit along with the crude gas. Most of the ammonia nitrogen entering the conversion unit returns to the gasification process unit along with the high-temperature conversion condensate, and a small part of the ammonia nitrogen enters the low-temperature conversion condensate to be stripped and also returns to the gasification process unit along with the tower bottom liquid in a certain amount. Thereby leading to high ammonia nitrogen content of black water and grey water in the gasification process unit. Therefore, the high-temperature conversion condensate and the low-temperature conversion condensate after conversion are subjected to steam stripping treatment to remove ammonia nitrogen, so that the ammonia nitrogen in the returned high-temperature conversion condensate and low-temperature conversion condensate is reduced to a very low level, and the ammonia nitrogen in black water and grey water of a gasification process unit is greatly reduced.
Because of the high-pressure flash steam in the gasification process unit, a large amount of waste heat and effective gas (carbon monoxide and hydrogen) can be recycled. The waste heat of the generated high-pressure flash steam is recovered by a stripping system to generate 0.3MPaG saturated steam for the whole plant. Meanwhile, the high-pressure flash steam is subjected to steam stripping, washing and other treatments, and then the non-condensable gas of the flash steam is compressed and returned to the conversion process gas to recover the effective gas.
The invention provides a process for reducing ammonia nitrogen and heat recovery in black ash water of a conversion condensate and gasification process unit, which has the following characteristics:
(1) the hydraulic turbine 10 is arranged, the high-pressure potential energy of the high-temperature transformation condensate is recovered by the hydraulic turbine 10, and the pump is driven to work, so that the reasonable recycling of energy is achieved.
(2) A high-temperature condensate stripping tower 20 is arranged to strip the high-temperature condensate, so that the ammonia nitrogen in the high-temperature condensate is reduced to a lower level.
(3) The high-pressure flash steam in the gasification process unit is sent into a high-temperature condensate stripping tower 20 to recover waste heat and effective non-condensable gas of the flash steam, so that the circulating cooling water consumption of the gasification process unit for cooling the high-pressure flash steam is reduced, the waste heat is fully utilized to produce low-pressure saturated steam as a byproduct, and the raw material consumption of the gasification process unit can be reduced by recycling the non-condensable gas of the flash steam. Achieves good energy-saving and emission-reducing effects and also generates good economic benefits and environmental protection benefits.
(4) The low-temperature condensate stripping tower 60 is arranged to reduce ammonia nitrogen in the low-temperature transformation condensate and reduce the ammonia nitrogen in the high-temperature condensate to a lower level.
(5) The energy is utilized in a gradient mode, the high-temperature condensate stripping tower 20 is used for utilizing the heat of high-pressure flash steam in a first level mode, the high-pressure flash steam is subjected to secondary heat recovery of a waste boiler 40 after passing through the stripping tower, and a gas-phase product and a liquid-phase product are sent back to the low-temperature condensate stripping tower 60 for tertiary heat recovery after being separated by a high-flash separator, so that the heat of the high-pressure flash steam and the heat of condensate are fully recovered, and the energy consumption is saved.
(6) The high-pressure flash steam compression and recovery process is arranged, and the non-condensable gas of the flash steam is sent to the conversion process gas to recover the product, so that the energy is saved and the environment is protected.
(7) Because the open-loop flow is arranged, the ammonia-containing condensate separated by stripping is sent to an ammonia refining unit for treatment, and the corrosion of the closed-loop flow tower top condensate returning to the stripping tower to equipment and pipelines is avoided.
(8) The ammonia nitrogen in the high-temperature condensate and the low-temperature condensate returned to the gasification process unit is reduced to a certain level, so that the ammonia nitrogen content in the black water and the grey water is reduced, and the grey water can be directly discharged to biochemical treatment. The problem that the grey water cannot be stably operated due to structural blockage caused by ammonia nitrogen reduction due to steam stripping or air stripping of the grey water is avoided.
The invention can reduce the ammonia nitrogen content in the black water and the grey water of the gasification process unit, so that the ammonia nitrogen content of the grey water discharged by the gasification process unit is reduced to the extent that the sewage can be well accepted. Meanwhile, the waste heat and effective components of high-pressure flash steam in the gasification process unit can be recovered.
In the above embodiments, the description of each embodiment has its own emphasis, and for parts not described in detail in a certain embodiment, reference may be made to the description of other embodiments. The above is a description of the system and method for reducing ammonia nitrogen content provided by the present invention, and for those skilled in the art, there may be changes in the specific implementation manners and application ranges according to the ideas of the embodiments of the present invention.
Claims (7)
1. A system for reducing the content of ammonia nitrogen is characterized by comprising:
the high-temperature condensate treatment device is used for steam stripping the input high-temperature conversion condensate by using the input high-pressure flash steam to generate high-temperature condensate with ammonia content meeting the conditions, and outputting a gas-phase product and a liquid-phase product to the low-temperature condensate treatment device after heat recovery and gas-liquid separation treatment are carried out on the steam-stripped steam generated after steam stripping; the high-temperature condensate treatment device comprises: the high-temperature condensate stripping tower, the high-temperature condensate pump, the waste boiler and the stripping separator; the bottom of the high-temperature condensate stripping tower is communicated with the high-temperature condensate pump, and the top of the high-temperature condensate stripping tower is communicated with the waste boiler; the waste pot is communicated with the middle part of the stripping separator; the lower part of the high-temperature condensate stripping tower is used for inputting high-pressure flash steam from a gasification process unit to be used as stripping steam for stripping out the soluble gas in the high-temperature conversion condensate; the bottom of the high-temperature condensate pump is used for outputting the high-temperature condensate to the high-temperature condensate pump; the high-temperature condensate pump is used for boosting the pressure of the high-temperature condensate and then sending the high-temperature condensate to the gasification process unit; the top of the waste heat recovery device is used for outputting stripping steam to the waste heat recovery device; the waste boiler is used for accommodating and generating and outputting low-pressure steam through the heat of the input stripping steam; the stripping separator is used for carrying out gas-liquid separation on stripping steam from the waste boiler, and the top of the stripping separator is used for inputting a generated gas-phase product to the middle part of the low-temperature condensate stripping tower to be used as a stripping heat source; the bottom of the low-temperature condensate stripper is used for inputting the generated liquid-phase product to the middle part of the low-temperature condensate stripper to be stripped continuously;
the low-temperature condensate treatment device is used for stripping the liquid-phase product and the input low-temperature transformation condensate by using input low-pressure steam and the input gas-phase product to generate low-temperature condensate with the ammonia content meeting the condition, and performing gas-liquid separation treatment on stripped steam generated after stripping to generate ammonia-containing condensate and flash steam noncondensable gas; the low-temperature condensate treatment device comprises: the system comprises a low-temperature condensate stripping tower, an air cooler, a water cooler, a low-temperature condensate pump, a separation washer, a flash steam compressor and an ammonia-containing condensate pump; the top of the stripping separator is communicated with the middle part of the low-temperature condensate stripping tower, and the bottom of the stripping separator is communicated with the middle part of the low-temperature condensate stripping tower; the bottom of the low-temperature condensate stripping tower is communicated with the low-temperature condensate pump, and the top of the low-temperature condensate stripping tower is connected to the air cooler and the water cooler in sequence and then communicated with the middle of the separation washer; the top of the separation scrubber is communicated with the flash steam compressor, and the bottom of the separation scrubber is communicated with the ammonia-containing condensate pump; the upper part of the low-temperature condensate stripping tower is also used for inputting the low-temperature shift condensate from a shift ammonia washing tower; the lower part of the low-pressure conversion condensate is also used for inputting the low-pressure steam to be used as stripping steam to strip out the soluble gas in the low-temperature conversion condensate; the bottom of the low-temperature condensate pump is used for outputting the low-temperature condensate to the low-temperature condensate pump; the low-temperature condensate pump is used for pressurizing the low-temperature condensate and then sending the low-temperature condensate to the gasification process unit; the top of the separator is used for outputting flash steam, and the flash steam is conveyed to the middle part of the separation washer after passing through the air cooler and the water cooler in sequence; the separation scrubber is used for carrying out gas-liquid separation and washing on the flash steam, and the upper part of the separation scrubber is used for inputting washing water so as to wash the generated gas-phase product and remove ammonia; the top of the flash evaporation compressor is used for outputting the generated flash evaporation non-condensable gas to the flash evaporation compressor; the flash steam compressor is used for pressurizing and conveying the flash steam noncondensable gas to the conversion unit to be used as a raw material gas; the bottom of the condenser is used for outputting ammonia-containing condensate to the ammonia-containing condensate pump; and the ammonia-containing condensate pump is used for pressurizing the ammonia-containing condensate and then sending the ammonia-containing condensate to the ammonia refining unit.
2. The system of claim 1, wherein the high temperature condensate treatment device further comprises a hydraulic turbine in communication with an upper portion of the high temperature condensate stripper column.
3. The system of claim 2, wherein the hydraulic turbine is configured to recycle a high pressure potential of the input high temperature shift condensate and output the high temperature shift condensate to an upper portion of the high temperature condensate stripper column.
4. The system of claim 3, wherein the lower portion of the high temperature condensate stripper column is further configured to receive low pressure steam as a backup stripping stream for load fluctuations or abnormal operating conditions.
5. A method for reducing the content of ammonia nitrogen is characterized by comprising the following steps:
steam stripping the high-temperature conversion condensate by using high-pressure flash steam to generate high-temperature condensate with ammonia content meeting the conditions, and outputting a gas-phase product and a liquid-phase product after heat recovery and gas-liquid separation treatment of the steam-stripped steam generated after steam stripping: inputting the high-temperature shift condensate to the upper part of a high-temperature condensate stripping tower; inputting the high-pressure flash steam from the gasification process unit to the lower part of the high-temperature condensate stripping tower to be used as stripping steam for stripping out the soluble gas in the high-temperature shift condensate; boosting the high-temperature condensate output from the bottom of the high-temperature condensate stripping tower by a high-temperature condensate pump and then sending the boosted high-temperature condensate to the gasification process unit; inputting stripping steam output from the top of the high temperature condensate stripper to a waste pot, such that the waste pot contains and generates and outputs low and low pressure steam from the heat of the input stripping steam; inputting the stripping steam from the waste boiler into a stripping separator to perform gas-liquid separation and obtain a gas-phase product and a liquid-phase product;
and (2) stripping the liquid phase product and the low-temperature transformation condensate by using low-pressure steam and the gas phase product to generate low-temperature condensate with ammonia content meeting the condition, and carrying out gas-liquid separation treatment on stripped steam generated after stripping to generate ammonia-containing condensate and flash steam non-condensable gas: inputting a gas-phase product generated at the top of the stripping separator into the middle part of a low-temperature condensate stripping tower to be used as a stripping heat source; inputting the liquid-phase product generated at the bottom of the stripping separator into the middle part of the low-temperature condensate stripping tower for continuous stripping; feeding the low temperature shift condensate from the shift ammonia wash column to an upper portion of the low temperature condensate stripper column; feeding the low-pressure steam to a lower portion of the cryogenic condensate stripper column to combine the vapor phase product as a stripping steam to strip out the dissolved gases in the cryogenic shift condensate and the liquid phase product; boosting the low-temperature condensate output from the bottom of the low-temperature condensate stripping tower by a low-temperature condensate pump and then sending the low-temperature condensate to the gasification process unit; the flash steam output from the top of the low-temperature condensate stripping tower is sequentially sent to the middle part of a separation washer through an air cooler and a water cooler to carry out gas-liquid separation; feeding wash water into the upper part of the separator scrubber to wash and remove ammonia from the resulting gas phase product; pressurizing and conveying the flash steam noncondensable gas output from the top of the separation scrubber to a conversion unit by a flash steam compressor to be used as raw material gas; and pressurizing the ammonia-containing condensate output from the bottom of the separator scrubber by an ammonia-containing condensate pump, and then sending the ammonia-containing condensate to an ammonia refining unit.
6. The method of claim 5, wherein the step of stripping the high-temperature shift condensate with high-pressure flash steam to produce a high-temperature condensate with an ammonia content satisfying a condition, and outputting the gas-phase product and the liquid-phase product after the step of performing gas-liquid separation on the stripped steam produced after the stripping further comprises: and introducing the high-temperature transformation condensate into a hydraulic turbine to recycle the high-pressure potential energy of the high-temperature transformation condensate.
7. The method of claim 5, further comprising: and inputting low-pressure steam to the lower part of the high-temperature condensate stripping tower to serve as standby stripping steam under the condition of load fluctuation or abnormal operation.
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| CN111115734A (en) * | 2020-01-21 | 2020-05-08 | 恒力石化（大连）炼化有限公司 | Device and process for treating flash evaporation condensate of coal water slurry gasification system |
| CN111348712A (en) * | 2020-03-17 | 2020-06-30 | 安徽晋煤中能化工股份有限公司 | Fuel gas recovery device |
| CN112107875B (en) * | 2020-10-29 | 2023-08-15 | 上海华谊工程有限公司 | Flash evaporation steam stripping cooling system and black water treatment process using same |
| CN112520808A (en) * | 2020-11-26 | 2021-03-19 | 中国天辰工程有限公司 | CO conversion condensate refining process system and method |
| CN114212847A (en) * | 2021-11-30 | 2022-03-22 | 中石化南京工程有限公司 | Stripping device and method for realizing ammonia water concentration |
| CN115259259B (en) * | 2022-07-18 | 2023-06-16 | 陕西未来能源化工有限公司 | System and process for treating conversion condensate |
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