Patent Application
20230364553
This application claims priority under 35 U.S.C. § 119 of Chinese Patent Application No. CN202210531132.1, filed on May 16, 2022, which is hereby incorporated in its entirety herein.
The present invention belongs to the technical field of environmental protection, and specifically relates to a pre-cooling apparatus for staged cooling of a process gas prior to ammonia-based decarbonization and a method therefor.
In recent years, the greenhouse effect has gradually become one of the most serious problems faced by humankind. Carbon dioxide (CO2) is the most important greenhouse gas, and the use of fossil energy is the main source of emission. China's total CO2 emissions have ranked first in the world, and the situation where China's energy structure is dominated by coal will continue for a period of time, and therefore energy from coal will still be the foundation of new energy peak regulation and energy security. China has promised the world that peak carbon emissions will be reached by 2030 and carbon neutrality by 2060. The capture, storage and resource recovery of CO2 in the emission gases is of great significance for controlling and reducing greenhouse gas emissions and dealing with the greenhouse effect and global warming.
At present, the amine-based method is the most widely used carbon capture technology in the world. However, the operating cost may be high and it may have a large amount of waste discharge that is difficult to treat. New decarbonization technologies have also been actively explored both at home and abroad. Compared with the amine-based method, the ammonia-based method has the advantages that the regeneration is easy, the operating cost is low, and the by-product of decarbonization is the ammonium bicarbonate fertilizer. Ammonium bicarbonate is a typical compound fertilizer, which can supply nitrogen nutrient and CO2 to plants at the same time. It is especially suitable for modern agriculture with soilless culture and greenhouse plant growth, realizing the resource utilization of CO2, achieving carbon cycle, and avoiding secondary pollutions and CO2 environmental accidents that may be caused by underground carbon storage. Compared with amine, ammonia is more efficient in absorbing CO2, and the resulting product ammonium bicarbonate can be generated more easily, which greatly reduces the cost of decarbonization.
Ammonia-based decarbonization technology has been the focus of research, and is a way to manage greenhouse gases. However, ammonia is volatile, resulting in increased ammonia escape. If left unsolved, a large amount of ammonia escape will not only increase the cost of decarbonization but also cause secondary pollution. Aiming at this problem, lowering the temperature of decarbonization can reduce ammonia escape.
Patent CN201210410873.0 discloses a multi-stage cooling tower system, comprising a plurality of cooling towers, wherein the outlet water of the preceding cooling tower is used as the inlet water of the subsequent cooling tower to perform multi-stage cooling. This apparatus only performs multi-tower cooling on the same cooling gradient to improve the cooling efficiency, and uses the same cold source.
Patent CN200880122376.2 discloses a multi-stage CO2 removal system and method for treating flue gas flow, wherein an absorber vessel is used to make the flue gas flow in contact with an ionic solution containing ammonia at a low temperature of 0-20° C., while the solution of the first absorption stage has a higher temperature and a lower ammonia-carbon ratio than the solution of the third absorption stage. By controlling the ionic solution at a low temperature and controlling the ionic solution of the third stage at a still lower temperature, ammonia escape can be reduced; however, this patent does not mention how to reduce the temperature in an efficient and energy-saving way.
It would be desirable to provide a multi-stage cooling apparatus for wet ammonia-based decarbonization and a method therefor. The apparatus may cool a desulfurized gas in a cooling tower by stages through different cold sources, and may reduce capital costs and energy consumption.
In the drawings, the various reference marks have the following meanings:
Process gas 1; Decarbonization cooling tower 2; First-stage cooling zone (of cooling tower) 2-1; Second-stage cooling zone (of cooling tower) 2-2; Third-stage cooling zone (of cooling tower) 2-3; Circulation pump (of first-stage cooling zone of cooling tower) 3-1; Circulation pump (of second-stage cooling zone of cooling tower) 3-2; Circulation pump (of third-stage cooling zone of cooling tower) 3-3; Heat exchanger (of first-stage cooling zone of cooling tower) 4-1; Heat exchanger (of second-stage cooling zone of cooling tower) 4-2; Heat exchanger (of third-stage cooling zone of cooling tower) 4-3; Air cooler 4-4; Circulating cooling water 5-1; Chilled water 5-2; Process gas outlet pipeline (of cooling tower) 6; Decarbonization absorption tower 7; Circulation pump (of decarbonization absorption tower) 8; Process gas outlet pipeline (of decarbonization absorption tower) 9; Circulation pump (of water washing zone of ammonia escape control system) 10; Process gas discharge 11; and Ammonia escape control system 12.
Apparatus and methods for pre-cooling process gas are provided.
The apparatus may include a first-stage cooling function zone. The first-stage cooling function zone may use a first circulating liquid to cool a process gas to a temperature of Tgas 1. The apparatus may include a second-stage cooling function zone. The second-stage cooling function zone may use a second circulating liquid to cool the process gas to a temperature of Tgas 2. The apparatus may include a third-stage cooling function zone. The third-stage cooling function zone may use a third circulating liquid to cool the process gas to a temperature of Tgas 3. The apparatus may include a first cold source for cooling the first circulating liquid. The apparatus may include a second cold source for cooling the second circulating liquid. The apparatus may include a third cold source for cooling the third circulating liquid. Tgas 3 may be less that Tgas 2, which may be less than Tgas 1, which may be less than Tgas 0. Tgas 0 may be an initial temperature of the process gas when entering the first-stage cooling function zone. The three cold sources may be distinct.
The first cold source may include cooling water. The cooling water may be obtained from a circulating cooling water or a closed cooling tower. The first circulating liquid may be cooled by a first heat exchanger.
The first cold source may include air. The first circulating liquid may be directly cooled by an air cooler.
The second cold source may include a decarbonized cold process gas. The second circulating liquid may be cooled by indirect heat exchange through a second heat exchanger.
The second cold source may include a decarbonized cold process gas. The second circulating liquid may be cooled by direct heat exchange through cross spraying of spraying liquid.
The third cold source may include a chilled liquid. The chilled liquid may be obtained from a chiller. The third circulating liquid may be cooled by a third heat exchanger. The third circulating liquid may be directly cooled by the cold source of the chiller.
Devices that only allow gas to pass through may be provided between the cooling function zones. At least one layer of liquid distributor may be provided in each cooling function zone. The liquid distributor may include a trough distributor or a spray distributor. The three function zones may be disposed in one tower. The three function zones are distributed through multiple towers.
Tgas 0 may be in the range 40-80° C. Tgas 1 may be in the range 35-48° C. Tgas 2 may be in the range 15-40° C. Tgas 3 may be in the range 10-30° C.
The temperature at which the first circulating liquid enters a tower may be defined as Tliquid 1. The temperature at which the first circulating liquid exits the tower may be defined as Tliquid 1′. Tliquid 1 may be less than Tliquid 1′. Tgas 0−Tliquid 1′ may be defined as ΔT1.
The temperature at which the second circulating liquid enters the tower may be defined as Tliquid2. The temperature at which the second circulating liquid exits the tower may be defined as Tliquid2′. Tliquid 2 may be less than Tliquid 2′. Tgas 1−Tliquid 2′ may be defined as ΔT2.
The temperature at which the third circulating liquid enters the tower may be defined as Tliquid3. The temperature at which the third circulating liquid exits the tower may be defined as Tliquid 3′. Tliquid 3 may be less than Tliquid 3′. Tgas 2−Tliquid 3′ may be defined as ΔT3. Each of ΔT1, ΔT2 and ΔT3 may be, independently of the others, in the range 2-5° C.
Tliquid 1 may be in the range 10-40° C. Tliquid 1′ may be in the range 15-50° C. Tliquid 2 may be in the range 15-36° C. Tliquid 2′ may be in the range 20-45° C. Tliquid 3 may be in the range 0-25° C. Tliquid 3′ may be in the range 10-40° C.
The temperature of the first cold source, before heat exchange, may be defined as Tsource 1 and, after heat exchange, as Tsource 1′. Tsource 1 may be less than Tsource 1′.
The temperature of the second cold source, before heat exchange, may be defined as Tsource 2 and, after heat exchange, as Tsource 2′. Tsource 2 may be less than Tsource 2′.
The temperature of the third cold source, before heat exchange, may be defined as Tsource 3 and, after heat exchange, as Tsource 3′. Tsource 3 may be less than Tsource 3′.
Tsource 1 may be in the range 5-35° C. Tsource 1′ may be in the range 10-45° C. Tsource 2 may be in the range 10-30° C. Tsource 2′ may be in the range 15-40° C. Tsource 3 may be in the range −17 to 10° C. Tsource 3′ may be in the range 0-30° C.
The cooling apparatus may be part of an ammonia-based desulfurization and decarbonization system. An upstream end of the cooling apparatus may be connected to a desulfurization apparatus. A downstream end of the cooling apparatus may be connected to a decarbonization apparatus. The process gas may come from the desulfurization apparatus and may enter the decarbonization apparatus after being cooled by the cooling apparatus.
The method may include passing the process gas successively through: a first-stage cooling function zone which uses a first circulating liquid to cool a process gas to a temperature of Tgas 1; a second-stage cooling function zone which uses a second circulating liquid to cool the process gas to a temperature of Tgas 2; and a third-stage cooling function zone which uses a third circulating liquid to cool the process gas to a temperature of Tgas 3.
The method may include using a first cold source to cool the first circulating liquid. The method may include using a second cold source to cool the second circulating liquid. The method may include using a third cold source to cool the third circulating liquid.
Tgas 3 may be less than Tgas 2, which may be less than Tgas 1, which may be less than Tgas 0. Tgas 0 may be defined as an initial temperature of the process gas when entering the first-stage cooling function zone. The three cold sources may be distinct. The three cold sources may be different.
The first cold source may include cooling water from a circulating cooling water or a closed cooling tower. The first circulating liquid may be cooled by a first heat exchanger.
The first cold source may include air. The first circulating liquid may be directly cooled by an air cooler.
The second cold source may include a decarbonized cold process gas. The second circulating liquid may be cooled by indirect heat exchange through a second heat exchanger.
The second cold source may include a decarbonized cold process gas. The second circulating liquid may be cooled by direct heat exchange through cross spraying of spraying liquid.
The third cold source may include a chilled liquid obtained from a chiller. The third circulating liquid may be cooled by a third heat exchanger.
Tgas 0 may be in the range 40-80° C. Tgas 1 may be in the range 35-48° C. Tgas 2 may be in the range 15-40° C. Tgas 3 may be in the range 10-30° C.
The temperature at which the first circulating liquid enters a tower may be defined as Tliquid1. The temperature at which the first circulating liquid exits the tower may be defined as Tliquid 1′. Tliquid 1 may be less than Tliquid 1′. Tgas 0−Tliquid 1′ may be defined as ΔT1.
The temperature at which the second circulating liquid enters the tower may be defined as Tliquid 2. The temperature at which the second circulating liquid exits the tower may be defined as Tliquid2′. Tliquid 2 may be less than Tliquid 2′. Tgas 1−Tliquid 2′ may be defined as ΔT2. The temperature at which the third circulating liquid enters the tower may be defined as Tliquid3. The temperature at which the third circulating liquid exits the tower may be defined as Tliquid 3′. Tliquid 3 may be less than Tliquid 3′. Tgas 2−Tliquid 3′ may be defined as ΔT3. Each of ΔT1, ΔT2 and ΔT3 may be, independently of the others, in the range 2-5° C.
Tliquid 1 may be in the range 10-40° C. Tliquid 1′ may be in the range 15-50° C. Tliquid 2 may be in the range 15-36° C. Tliquid 2′ may be in the range 20-45° C. Tliquid 3 may be in the range 0-25° C. Tliquid 3′ may be in the range 10-40° C.
the temperature of the first cold source is Tsource 1 before heat exchange and Tsource 1′ after heat exchange, wherein Tsource 1<Tsource 1′;
the temperature of the second cold source is Tsource 2 before heat exchange and Tsource 2′ after heat exchange, wherein Tsource 2<Tsource 2′; and
the temperature of the third cold source is Tsource 3 before heat exchange and Tsource 3′ after heat exchange, wherein Tsource 3<Tsource 3′.
Tsource 1 may be in the range 5-35° C. Tsource 1′ may be in the range 10-45° C. Tsource 2 may be in the range 10-30° C. Tsource 2′ may be in the range 15-40° C. Tsource 3 may be in the range −17 to 10° C. Tsource 3′ may be in the range 0-30° C.
The method may include performing on the process gas ammonia-based desulfurization. The method may include performing on the process gas ammonia-based decarbonization. The method may include performing the cooling stages after the ammonia-based desulfurization. The method may include performing the cooling stages before the ammonia-based decarbonization.
A content of ammonium sulfate in the cooling circulating liquid is in the range 0-5 wt % (weight-percent). A content of ammonium sulfate in the first stage may be greater than that in the second stage, which may be greater than that in the third stage.
The apparatus and methods may provide a pre-cooling apparatus prior to ammonia-based decarbonization. The apparatus and methods may include: a first-stage cooling function zone which may use a first circulating liquid to cool a process gas to a temperature of Tgas 1, a second-stage cooling function zone which may use a second circulating liquid to cool the process gas to a temperature of Tgas 2, and a third-stage cooling function zone which may use a third circulating liquid to cool the process gas to a temperature of Tgas 3, wherein Tgas 3<Tgas 2<Tgas 1<Tgas 0, and wherein Tgas 0 is an initial temperature of the process gas when entering the first-stage cooling function zone; a first cold source for cooling the first circulating liquid, a second cold source for cooling the second circulating liquid, and a third cold source for cooling the third circulating liquid, wherein the three cold sources are different.
The apparatus may provide for, and the methods may include, passing the process gas successively through: a first-stage cooling function zone which may use a first circulating liquid to cool the process gas to a temperature of Tgas 1, a second-stage cooling function zone which may use a second circulating liquid to cool the process gas to a temperature of Tgas 2, and a third-stage cooling function zone which may use a third circulating liquid to cool the process gas to a temperature of Tgas 3, wherein Tgas 3<Tgas 2<Tgas 1<Tgas 0, and wherein Tgas 0 is an initial temperature of the process gas when entering the first-stage cooling function zone; using a first cold source to cool the first circulating liquid, using a second cold source to cool the second circulating liquid, and using a third cold source to cool the third circulating liquid, wherein the three cold sources may be different.
The first cold source may include cooling water from a circulating cooling water or a closed cooling tower, and the first circulating liquid may be cooled by a first heat exchanger. The first cold source may include air. The first circulating liquid may be directly cooled by an air cooler. The second cold source may include a decarbonized cold process gas. The second circulating liquid may be cooled by indirect heat exchange through a second heat exchanger. The second circulating liquid may be cooled by direct heat exchange through cross spraying of spraying liquid. The third cold source may include a chilled liquid. The chilled liquid may be obtained from a chiller. The third circulating liquid may be cooled by a third heat exchanger. The third circulating liquid may be directly cooled by the cold source of the chiller.
The circulating cooling water or the cooling water from the closed cooling tower, air from the air cooler, the cold process gas and the chilled liquid may be used respectively as the cold sources, and the process gas may be cooled by spraying the circulating liquids, so cooling capacity with low energy consumption may be achieved. The cooling capacity of the process gas may be recycled. This may save investment costs and reduce energy consumption. The temperature of the process gas may be reduced to a low level, e.g. 10-30° C. This may significantly reduce ammonia escape in the subsequent decarbonization process.
The apparatus and methods may include a pre-cooling apparatus prior to ammonia-based decarbonization. The pre-cooling apparatus may include: a first-stage cooling function zone which may use a first circulating liquid to cool a process gas to a temperature of Tgas 1, a second-stage cooling function zone which may use a second circulating liquid to cool the process gas to a temperature of Tgas 2, and a third-stage cooling function zone which may use a third circulating liquid to cool the process gas to a temperature of Tgas 3, wherein Tgas 3<Tgas 2<Tgas 1<Tgas 0, and wherein Tgas 0 is an initial temperature of the process gas when entering the first-stage cooling function zone; a first cold source for cooling the first circulating liquid, a second cold source for cooling the second circulating liquid, and a third cold source for cooling the third circulating liquid, wherein the three cold sources are different.
The first cold source may include cooling water from a circulating cooling water or a closed cooling tower. The first circulating liquid may be cooled by a first heat exchanger.
The first cold source may include air. The first circulating liquid may be directly cooled by an air cooler.
The second cold source may include a decarbonized cold process gas. The second circulating liquid may be cooled by indirect heat exchange through a second heat exchanger. The second circulating liquid may be cooled by direct heat exchange through cross spraying of spraying liquid.
The third cold source may include a chilled liquid. The chilled liquid may be obtained by a chiller. The third circulating liquid may be cooled by a third heat exchanger. The third circulating liquid may be directly cooled by the cold source of the chiller.
The first heat exchanger and the third heat exchanger may be liquid-liquid heat exchangers. The first heat exchanger and the third heat exchanger may include plate heat exchangers. The second heat exchanger may include a gas-liquid heat exchanger. The second heat exchanger may include a shell-and-tube heat exchanger.
Devices or components that only allow gas to pass through may be provided between the cooling function zones.
One or more layers of circulating distributor may be provided in each cooling function zone.
The circulating distributor may include a trough distributor or a spray distributor.
The three function zones may be combined into one tower or may be present as a plurality of towers.
When the three function zones are combined into one tower, i.e. a cooling tower, the cooling apparatus may include a cooling tower and cold sources. The cooling tower may include, from bottom to top, a first-stage cooling function zone, a second-stage cooling function zone, and a third-stage cooling function zone, wherein each of the cooling function zones and the cold sources may be arranged as described herein.
Tgas 0 may be in the range 40-80° C.; and/or Tgas 1 may be in the range 35-48° C.; and/or Tgas 2 may be in the range 15-40° C.; and/or Tgas 3 may be in the range 10-30° C.
The temperature at which the first circulating liquid enters the tower is Tliquid 1, and the temperature at which the first circulating liquid exits the tower is Tliquid 1′, wherein Tliquid1<Tliquid 1′, and Tgas 0−Tliquid 1′=ΔT1. The temperature at which the second circulating liquid enters the tower is Tliquid 2. The temperature at which the second circulating liquid exits the tower is Tliquid 2′, wherein Tliquid 2<Tliquid 2′, and Tgas 1−Tliquid 2′=ΔT2. The temperature at which the third circulating liquid enters the tower is Tliquid 3, and the temperature at which the third circulating liquid exits the tower is Tliquid 3′, wherein Tliquid 3<Tliquid 3′, and Tgas 2−Tliquid 3′=ΔT3; wherein ΔT1, ΔT2 and ΔT3 are each independently of the others ≥1° C., in the range 2-15° C., or in the range 2-5° C.
In one embodiment, Tliquid 1 may be 10-40° C., and Tliquid 1′ may be 15-50° C.; and/or Tliquid 2 may be 15-36° C., and Tliquid 2′ may be 20-45° C.; and/or Tliquid 3 may be 0-25° C., and Tliquid 3′ may be 10-40° C.
The temperature of the first cold source is Tsource 1 before heat exchange and Tsource 1′ after heat exchange, wherein Tsource 1 may be less than Tsource 1′. The temperature of the second cold source is Tsource 2 before heat exchange and Tsource 2′ after heat exchange, wherein Tsource 2 may be less than Tsource 2′. The temperature of the third cold source is Tsource 3 before heat exchange and Tsource 3′ after heat exchange, wherein Tsource 3 may be less than Tsource 3′.
Tsource 1 may be in the range 5-35° C., and Tsource 1′ may be in the range 10-45° C.; and/or Tsource 2 may be in the range 10-30° C., and Tsource 2′ may be in the range 15-40° C.; and/or Tsource 3 may be in the range −17 to 10° C., and Tsource 3′ may be in the range 0-30° C.
The cooling apparatus may be part of an ammonia-based desulfurization and decarbonization system. The upstream end of the cooling apparatus may be connected to a desulfurization apparatus. The downstream end of the cooling apparatus may be connected to a decarbonization apparatus. The process gas may come from the desulfurization apparatus and may enter the decarbonization apparatus after being cooled by the cooling apparatus.
The process gas may include a desulfurized process gas from the desulfurization apparatus. The process gas may have a temperature of 40-80° C. The process gas may have a temperature of 40-60° C. The desulfurization process may remove most of SO2 from the process gas, so that the desulfurized process gas mainly contains CO2 and a small amount of H2O.
The methods may include a method for cooling a process gas. The method may include passing the process gas successively through: a first-stage cooling function zone which may use a first circulating liquid to cool the process gas to a temperature of Tgas 1, a second-stage cooling function zone which may use a second circulating liquid to cool the process gas to a temperature of Tgas 2, and a third-stage cooling function zone which may use a third circulating liquid to cool the process gas to a temperature of Tgas 3, wherein Tgas 3<Tgas 2<Tgas 1<Tgas 0, and wherein Tgas 0 is an initial temperature of the process gas when entering the first-stage cooling function zone; using a first cold source to cool the first circulating liquid, using a second cold source to cool the second circulating liquid, and using a third cold source to cool the third circulating liquid, wherein the three cold sources are different.
The first cold source may include cooling water. The cooling water may be from a circulating cooling water or a closed cooling tower. The first circulating liquid may be cooled by a first heat exchanger.
The first cold source may include air. The first circulating liquid may be directly cooled by an air cooler.
The second cold source may include a decarbonized cold process gas. The second circulating liquid may be cooled by indirect heat exchange through a second heat exchanger. The second circulating liquid may be cooled by direct heat exchange through cross spraying of spraying liquid.
The third cold source may include a chilled liquid. The chilled liquid may be obtained by a chiller. The third circulating liquid may be cooled by a third heat exchanger. The third circulating liquid may be directly cooled by the cold source of the chiller.
Tgas 0 may be in the range 40-80° C.; and/or Tgas 1 may be in the range 35-48° C.; and/or Tgas 2 may be in the range 15-40° C.; and/or Tgas 3 may be in the range 10-30° C.
The temperature at which the first circulating liquid enters the tower is Tliquid 1, and the temperature at which the first circulating liquid exits the tower is Tliquid 1′, wherein Tliquid 1′, and Tgas 0−Tliquid 1′=ΔT1; the temperature at which the second circulating liquid enters the tower is Tliquid 2, and the temperature at which the second circulating liquid exits the tower is Tliquid 2′, wherein Tliquid 2<Tliquid 2′, and Tgas 1−Tliquid 2′=ΔT2; and the temperature at which the third circulating liquid enters the tower is Tliquid 3, and the temperature at which the third circulating liquid exits the tower is Tliquid 3′, wherein Tliquid 3<Tliquid 3′, and Tgas 2−Tliquid 3=ΔT3; wherein ΔT1, ΔT2 and ΔT3 are each independently of the others ≥1° C., preferably 2-15° C., and more preferably 2-5° C.
Tliquid 1 may be in the range 10-40° C., and Tliquid 1′ may be in the range 15-50° C.; and/or Tliquid 2 may be in the range 15-36° C., and Tliquid 2′ may be in the range 20-45° C.; and/or Tliquid 3 may be in the range 0-25° C., and Tliquid 3′ may be in the range 10-40° C.
The temperature of the first cold source is Tsource 1 before heat exchange and Tsource 1′ after heat exchange, wherein Tsource 1<Tsource 1′; the temperature of the second cold source is Tsource 2 before heat exchange and Tsource 2′ after heat exchange, wherein Tsource 2<Tsource 2′; and the temperature of the third cold source is Tsource 3 before heat exchange and Tsource 3′ after heat exchange, wherein Tsource 3<Tsource 3′.
Tsource 1 may be in the range 5-35° C., and Tsource 1′ may be in the range 10-45° C.; and/or Tsource 2 may be in the range 10-30° C., and Tsource 2′ may be in the range 15-40° C.; and/or Tsource 3 may be in the range −17 to 10° C., and Tsource 3′ may be in the range 0-30° C.
The method may be part of an ammonia-based desulfurization and decarbonization method. Upstream of the cooling method may be the desulfurization process. Downstream of the cooling method may be the decarbonization process. The process gas may come from the desulfurization process and may enter the decarbonization process after being cooled by the cooling method.
The circulating liquid may include water. During the circulation, components entrained by the process gas may enter the circulating liquid, so that the circulating liquid may include such components as ammonium sulfate.
The content of ammonium sulfate in the cooling circulating liquid may be in the range 0-5 wt %, and that in the first stage may be greater than that in the second stage, which may be greater that in the third stage.
The method may be carried out by the cooling apparatus as described herein. The cooling apparatus described herein may be used to perform the method for cooling a process gas described herein. The various features described herein for the cooling apparatus are also applicable to the method, and vice versa.
The following embodiments are provided to illustrate the present invention without limiting its scope.
Illustrative embodiments of apparatus and methods in accordance with the principles of the invention will now be described with reference to the accompanying drawings, which form a part hereof. It is to be understood that other embodiments may be utilized and that structural, functional and procedural modifications, additions or omissions may be made, and features of illustrative embodiments, whether apparatus or method, may be combined, without departing from the scope and spirit of the present invention.
Example 1 is a cooling apparatus according to the present invention and is shown in
As shown in
The process gas after the first-stage cooling entered the second-stage cooling zone 2-2 through a liquid collector. The process gas was cooled to 39° C. by means of spraying. The circulating liquid reached the gas heat exchanger 4-2 for heat exchange with decarbonized process gas to reduce the temperature, and then returned to the second-stage cooling zone 2-2 for cooling the process gas. The temperature at which the circulating liquid entered the tower was 30° C., and the temperature at which the circulating liquid exited the tower was 40° C. The temperature of the decarbonized process gas increased from 20° C. to 31° C.
Then, the process gas after the second-stage cooling entered the third-stage cooling zone 2-3 through a liquid collector. The circulating liquid was cooled by chilled water 5-2 through heat exchanger 4-3, and entered the tower for spraying to cool the process gas to 25° C. The temperature at which the circulating liquid entered the tower was 20° C., and the temperature at which the circulating liquid exited the tower was 37° C. The temperature at which the chilled water entered the heat exchanger 4-3 was 7° C., and the temperature at which the chilled water exited the heat exchanger 4-3 was 17° C.
After being cooled by the cooling tower, the process gas was introduced through the flue 6 to the decarbonization tower 7, and the circulating liquid was contacted with the process gas through the circulation pump 8 to absorb carbon dioxide. The decarbonized process gas entered the ammonia escape control system 12 through flue 9, and flue 9 was provided with the gas heat exchanger 4-2. The circulating liquid in the ammonia escape control system was washed by the circulation pump 10 and contacted with the process gas to absorb free ammonia, and the process gas 11 after ammonia removal was vented through a process gas discharge outlet.
The consumption of circulating cooling water was 1890 t/h, and the consumption of chilled water was 1894 t/h.
The main process parameters of the cooling treatment in Example 1 are shown in Table 1.
As shown in
The process gas after the first-stage cooling reached the second-stage cooling zone 2-2 through a liquid collector. The process gas was cooled to 32° C. by means of spraying, and the circulating liquid reached ammonia escape control system 12 for heat exchange by spraying with decarbonized process gas to reduce the temperature, and then returned to the second-stage cooling zone 2-2 for cooling the process gas. The temperature at which the circulating liquid entered the cooling tower was 25° C., and the temperature at which the circulating liquid exited the cooling tower was 40° C. The temperature of the decarbonized process gas increased from 20° C. to 35° C.
Then, the process gas after the second-stage cooling entered the third-stage cooling zone 2-3 through a liquid collector, the circulating liquid was cooled by the chilled water 5-2 through the heat exchanger 4-3, and entered the tower for spraying to cool the process gas to 25° C. The temperature at which the circulating liquid entered the tower was 20° C., and the temperature at which the circulating liquid exited the tower was 30° C. The temperature at which the chilled water entered the heat exchanger 4-3 was 7° C., and the temperature at which the chilled water exited the heat exchanger 4-3 was 17° C.
After being cooled by the cooling tower, the process gas was introduced through the flue 6 to the decarbonization tower 7, and the circulating liquid was contacted with the process gas through the circulation pump 8 to absorb carbon dioxide. The decarbonized process gas entered the ammonia escape control system 12 through flue 9. The circulating liquid in the ammonia escape control system was washed by the circulation pump 10, and contacted with the process gas to absorb free ammonia, and the process gas 11 after ammonia removal was vented through a process gas discharge outlet.
The consumption of chilled water was 818 t/h.
The main process parameters of the cooling treatment in Example 2 are shown in Table 2.
As shown in
The consumption of chilled water was 4267 t/h.
The main process parameters of the cooling treatment in Comparative Example are shown in Table 3.
Illustrative features may include:
While specific embodiments of the present invention have been described above, those skilled in the art should understand that these are only illustrations, and that the scope of the present invention is defined by the appended claims. Various changes and modifications may be made to these embodiments by those skilled in the art without departing from the principle and spirit of the present invention, and these changes and modifications all fall within the scope of the present invention. Moreover, it should be understood by those skilled in the art that the features described herein with respect to one or more embodiments may be combined with other embodiments so long as such combinations do not conflict with objects of the present invention.
All ranges and parameters disclosed herein shall be understood to encompass any and all subranges subsumed therein, every number between the endpoints, and the endpoints. For example, a stated range of “1 to 10” should be considered to include any and all subranges between (and inclusive of) the minimum value of 1 and the maximum value of 10; that is, all subranges beginning with a minimum value of 1 or more (e.g. 1 to 6.1), and ending with a maximum value of 10 or less (e.g., 2.3 to 9.4, 3 to 8, 4 to 7), and finally to each number 1, 2, 3, 4, 5, 6, 7, 8, 9, and 10 contained within the range.
Thus, apparatus and methods for pre-cooling apparatus prior to ammonia-based decarbonization have been provided. Persons skilled in the art will appreciate that the present invention may be practiced by other than the described embodiments, which are presented for purposes of illustration rather than of limitation. The present invention is limited only by the claims that follow.
| Number | Date | Country | Kind |
|---|---|---|---|
| 202210531132.1 | May 2022 | CN | national |
