Ammonia cracking system and ammonia cracking method

Abstract

An ammonia cracking system includes three heat exchangers, three adiabatic reactors, a tubular furnace reactor, and a scrubber. The three heat exchangers are coupled to each other. The three heat exchangers are configured to sequentially receive a mixture and heat the mixture using a heat transfer substance. The mixture includes ammonia. The three adiabatic reactors are coupled to each other. The three adiabatic reactors are configured to sequentially receive the mixture heated by the three heat exchangers and pre-crack the ammonia in the mixture, so that the ammonia in the mixture is partially cracked and generates hydrogen and nitrogen. The tubular furnace reactor is configured to receive the mixture pre-cracked by the three adiabatic reactors and further crack the ammonia in the mixture. The scrubber is configured to receive the mixture cracked by the tubular furnace reactor and remove the ammonia from the mixture through scrubbing.

Description

[Technical Field]

[0001] This disclosure relates to an ammonia cracking system and ammonia cracking method. [Previous Technology]

[0002] Because ammonia (NH3) can produce high-purity hydrogen (H2) through cracking, and ammonia has advantages such as high energy density, low cost of liquefaction storage and transportation, and high safety, systems and methods for hydrogen production through ammonia cracking are attracting increasing attention. However, currently common ammonia cracking systems and methods often face problems of thermal shock and high energy consumption, which still limit their large-scale application. Therefore, a more efficient ammonia cracking system and method is needed to solve the above problems. [Summary of the Invention]

[0003] In view of this, one object of this disclosure is to provide an ammonia cracking system and ammonia cracking method that can solve the above problems.

[0004] One aspect of this disclosure relates to an ammonia cracking system comprising three heat exchange units, three adiabatic reaction units, a tubular reactor, and a scrubbing unit. The three heat exchange units are coupled to each other. The three heat exchange units are configured to sequentially receive a mixture and heat the mixture using a heat transfer medium. The mixture includes ammonia. The three adiabatic reaction units are coupled to each other. The three adiabatic reaction units are configured to sequentially receive the mixture heated by the three heat exchange units and pre-crack the ammonia in the mixture, such that the ammonia in the mixture is partially cracked to produce hydrogen and nitrogen. The tubular reactor is configured to receive the pre-cracked mixture and further crack it. The scrubbing unit is configured to receive the cracked mixture and remove ammonia from the mixture by washing.

[0005] In some embodiments, the ammonia cracking system further includes an adsorption unit. The adsorption unit is configured to receive the washed mixture and separate hydrogen from the mixture.

[0006] In some embodiments, the three heat exchange devices are also configured to receive the pyrolyzed mixture and use the pyrolyzed mixture as a heat transfer medium.

[0007] In some embodiments, the ammonia cracking system further includes an intermediate heating device. The intermediate heating device is coupled between the first and second of the three adiabatic reaction devices. The intermediate heating device is configured to further heat the pre-cracked mixture.

[0008] Another aspect of this disclosure relates to an ammonia cracking method comprising: driving a mixture comprising ammonia sequentially through three heat exchange devices to heat the mixture; driving the heated mixture sequentially through three adiabatic reaction devices to pre-crack the ammonia in the mixture and produce hydrogen and nitrogen; driving the pre-cracked mixture through a tubular reactor for further cracking; driving the cracked mixture through a washing device to remove ammonia from the mixture; and driving the washed mixture through an adsorption device to separate hydrogen from the mixture.

[0009] In some embodiments, heating the mixture includes: heating the mixture to between 90°C and 100°C via a first of the three heat exchange devices; heating the mixture to between 180°C and 200°C via a second of the three heat exchange devices; and heating the mixture to between 290°C and 320°C via a third of the three heat exchange devices.

[0010] In some embodiments, pre-cracking of ammonia in the mixture includes: pre-cracking the ammonia in the mixture using a first of the three adiabatic reaction devices, such that the ammonia cracking rate is between 5% and 15%; pre-cracking the ammonia in the mixture using a second of the three adiabatic reaction devices, such that the ammonia cracking rate is between 20% and 30%; and pre-cracking the ammonia in the mixture using a third of the three adiabatic reaction devices, such that the ammonia cracking rate is between 35% and 45%. The three adiabatic reaction devices include the same catalyst.

[0011] In some embodiments, the pre-pyrolyzed mixture has a temperature between 650°C and 850°C before passing through the tubular reactor.

[0012] In some embodiments, the ammonia cracking method further includes driving the cracked mixture sequentially through the three heat exchange devices before passing through the washing device, so as to provide heat to the three heat exchange devices.

[0013] In some embodiments, the pyrolyzed mixture has a temperature between 30°C and 40°C before passing through a washing device.

[0014] In summary, in the ammonia cracking systems and methods of some embodiments disclosed herein, by setting up multiple heat exchange devices and multiple adiabatic reaction devices, the mixture including ammonia is gradually heated and pre-cracked, thereby reducing the load on the tubular reactor that subsequently performs the cracking. This allows the mixture to heat up and crack more uniformly, while reducing the number of times the catalyst in the tubular reactor needs to be replaced. Compared to common ammonia cracking systems and methods, this improves the overall cracking efficiency of the system and reduces the downtime of the tubular reactor.

[0015] These and other aspects of this disclosure will become apparent from the following description of preferred embodiments in conjunction with the drawings, but variations and modifications may be made therein without departing from the spirit and scope of the novel concept of this disclosure.

Implementation Method

[0016] The following disclosure will be described more fully herein through drawings and references, some exemplary embodiments of which are illustrated in the drawings. This disclosure may be implemented in different forms and should not be limited to the embodiments mentioned below. However, these embodiments are provided to aid in a more complete understanding of the contents of this disclosure and to fully convey the scope of this disclosure to those skilled in the art.

[0017] Please refer to Figure 1, which is a schematic diagram of an ammonia cracking system 10 according to some embodiments of the present disclosure. The ammonia cracking system 10 includes an air inlet device 102, an ammonia storage device 104, a pump 106, a heating device 108, a heat exchanger 110, heat exchangers 112 and 114, a heating device 116, an adiabatic reactor 118, an intermediate heating device 120, an adiabatic reactor 122, an intermediate heating device 124, an adiabatic reactor 126, a heat exchanger 128, a tubular furnace reactor 130, a heat exchanger 132, a scrubber 134, a collection device 136, a heating device 138, a condenser 140, an adsorption device 142, a collection device 144, an adsorption device 146, a cooling device 148, a compressor 150, and a hydrogen storage device 152.

[0018] By setting up multiple heat exchange devices and multiple adiabatic reaction devices, ammonia can be gradually and fully heated and pre-cracked before entering the tubular reactor, which can ensure that ammonia is uniformly heated and cracked, improve cracking efficiency, and reduce the risk of thermal shock.

[0019] The functions and connections between the components of the ammonia cracking system 10 will be explained below.

[0020] The intake device 102 is configured to introduce external gas G1 to mix with the ammonia to be cracked to form a mixture. In some embodiments, the intake device 102 is an exhaust fan. In some embodiments, the external gas G1 includes air or an inert gas such as argon (Ar). By mixing the external gas G1, impurities generated from other chemical reactions of the ammonia can be reduced.

[0021] The ammonia storage device 104 includes liquid ammonia stored at temperatures below -32°C. The ammonia storage device 104 is coupled to a pump 106.

[0022] Pump 106 is configured to extract and pressurize liquid ammonia from ammonia storage device 104 (e.g., pressurize to between 1 bar and 30 bar).

[0023] Heating device 108 is coupled to pump 106. Heating device 108 is configured to receive pressurized liquid ammonia from pump 106 and preheat it to maintain the temperature of the ammonia between 40°C and 50°C in a liquid state. In some embodiments, heating device 108 may be an electric heating device.

[0024] The external gas G1 introduced by the air intake device 102 and the ammonia output by the heating device 108 converge and form a mixture before entering the heat exchange device 110.

[0025] Heat exchange device 110 is coupled to heating device 108, and heat exchange devices 110, 112, and 114 are coupled to each other. Heat exchange devices 110, 112, and 114 sequentially receive the mixture and progressively heat it through heat exchange with the heat transfer material to gradually reduce the bond strength of ammonia. This is beneficial for improving the uniformity of subsequent cracking. After passing through heat exchange device 114, the ammonia in the mixture is superheated vapor.

[0026] In some embodiments, the heating device 116 is coupled between the heat exchange device 114 and the adiabatic reaction device 118. The heating device 116 is configured to further heat the mixture to ensure that the mixture reaches an appropriate temperature before entering the adiabatic reaction device 126. In some embodiments, the heating device 116 may be an electric heating device.

[0027] Adiabatic reaction devices 118, 122, and 126 are coupled to each other and configured to sequentially receive heated mixtures and pre-cracking the ammonia in the mixtures, thereby partially decomposing the ammonia in the mixtures to produce hydrogen and nitrogen. In some embodiments, an intermediate heating device is provided between two adiabatic reaction devices to regulate the temperature range of the pre-cracking mixture before it enters the next adiabatic reaction device.

[0028] Specifically, the adiabatic reaction apparatus 118 is configured to perform a first pre-cracking. The chemical reaction formula for this process is 2NH3 → N2 + 3H2. In some embodiments, the adiabatic reaction apparatus 118 includes catalysts such as nickel-based catalysts, ruthenium-based catalysts, transition metal-doped nickel-based catalysts, mixed metal oxide composites, etc.

[0029] An intermediate heating device 120 is coupled between the adiabatic reaction device 118 and the adiabatic reaction device 122. The intermediate heating device 120 is configured to further heat the mixture after the first pre-pyrolysis. In some embodiments, the intermediate heating device 120 may be an electric heating device.

[0030] The adiabatic reaction apparatus 122 is configured to receive the mixture from the intermediate heating device 120 and perform a second pre-cracking. In some embodiments, the adiabatic reaction apparatus 122 includes the same catalyst as the adiabatic reaction apparatus 118.

[0031] An intermediate heating device 124 is coupled between the adiabatic reaction device 122 and the adiabatic reaction device 126. The intermediate heating device 124 is configured to further heat the mixture after the second pre-pyrolysis. In some embodiments, the intermediate heating device 124 may be an electric heating device.

[0032] The adiabatic reaction apparatus 126 is configured to receive the mixture from the intermediate heating device 124 and perform a third pre-cracking. In some embodiments, the adiabatic reaction apparatus 126 includes the same catalyst as the adiabatic reaction apparatus 118.

[0033] A heat exchange device 128 is coupled to an adiabatic reaction device 126 and a tubular reactor 130. The heat exchange device 128 is configured to receive a mixture from the adiabatic reaction device 126, heat the mixture through heat exchange with a heat transfer substance, and then input the mixture into the tubular reactor 130.

[0034] The tubular reactor 130 is configured to receive the pre-cracked mixture and further crack it. Since the mixture is sufficiently heated before entering the tubular reactor 130, the energy applied in the tubular reactor 130 is primarily used for the cracking reaction. This improves the cracking efficiency and reduces catalyst consumption in the tubular reactor 130. In some embodiments, the catalyst included in the tubular reactor 130 is a nickel-based catalyst.

[0035] The tubular reactor 130 is also configured to feed the pyrolyzed mixture back into the heat exchange device 128, so as to use the high-temperature pyrolyzed mixture as a heat transfer medium to exchange heat with the pre-pyrolyzed and heated mixture in the heat exchange device 128, so as to achieve the effect of heat recovery.

[0036] Similarly, heat exchange device 128 may also be coupled to heat exchange device 114, while heat exchange device 114, heat exchange device 112 and heat exchange device 110 are configured to receive the pyrolyzed mixture in sequence and use the pyrolyzed mixture as a heat transfer medium to exchange heat with the unpyrolyzed mixture to be heated therein, while the pyrolyzed mixture can be gradually cooled.

[0037] In some embodiments, gas G2 may also be introduced into the tubular reactor 130 to absorb waste heat, so as to make the heat distribution in the tubular reactor 130 more uniform and avoid local overheating. The high-temperature gas G2' formed after gas G2 absorbs waste heat can be recovered for preheating or to bring the process gas to a high temperature, so as to improve the overall energy efficiency of the process. For example, the high-temperature gas G2' can be introduced into the heat exchange device 110 as a heat transfer medium to provide heat. In some embodiments, gas G2 and gas G2' may include nitrogen and / or inert gas such as helium (He), argon (Ar), etc.

[0038] Heat exchange device 132 is coupled to heat exchange device 110 and washing device 134. Heat exchange device 132 is configured to receive the pyrolyzed and cooled mixture and control its temperature (e.g., cooling) to make it suitable for input into washing device 134.

[0039] The scrubbing apparatus 134 is configured to receive the pyrolyzed and cooled mixture, and to absorb residual ammonia in the mixture by scrubbing with a scrubbing liquid to produce ammonium hydroxide (NH4OH), thereby removing ammonia from the mixture. In some embodiments, the scrubbing liquid may be water.

[0040] The washing device 134 is also coupled to the collecting device 136. The collecting device 136 is configured to collect ammonium hydroxide and washing liquid. In some embodiments, the collecting device 136 may be a sealed storage tank.

[0041] The heating device 138 is coupled between the washing device 134 and the condensing device 140. The heating device 138 and the condensing device 140 are configured to regulate the temperature of the washed mixture. It is worth noting that the mixture remains in a gaseous state after passing through the condensing device 140.

[0042] Adsorption device 142 is coupled between condensation device 140 and another adsorption device 146. Adsorption device 142 is configured to receive a washed and condensed mixture and separate hydrogen from the mixture by, for example, pressure swing adsorption (PSA). The mixture including hydrogen is fed to adsorption device 146 for further adsorption, while nitrogen is fed to collection device 144 coupled to adsorption device 142. In some embodiments, the adsorbent included in adsorption device 142 is a molecular sieve, silica gel, activated alumina, ionic liquid, or a combination thereof.

[0043] Adsorption device 146 is configured to receive the adsorbed mixture including hydrogen and perform further adsorption. The separated nitrogen is also fed into a collection device 144 coupled to adsorption device 146. In some embodiments, the adsorbent included in adsorption device 146 is a molecular sieve, silica gel, activated alumina, ionic liquid, or a combination thereof. In some embodiments, adsorption device 146 includes the same adsorbent as adsorption device 142.

[0044] A cooling device 148 is coupled between the adsorption device 146 and the compressor 150. The cooling device 148 is configured to receive and cool the mixture containing hydrogen that has undergone two adsorption processes, and then input it into the compressor 150 for pressurization to form liquid hydrogen.

[0045] The hydrogen storage device 152 is configured to receive and store liquid hydrogen via a self-compressor 150. In some embodiments, the hydrogen storage device 152 is a high-pressure hydrogen storage cylinder.

[0046] Next, the ammonia cracking method 20 performed based on the ammonia cracking system 10 will be described. Please refer to Figure 2, which is a flowchart of the ammonia cracking method 20 according to some embodiments of the present disclosure. The ammonia cracking method 20 includes steps S202, S204, S206, S208, S210, and S212.

[0047] Before performing step S202, liquid ammonia from the ammonia storage device 104, which has been heated and pressurized, is mixed with external gas G1 introduced via the air intake device 102 to form a mixture.

[0048] Next, in step S202, the mixture including ammonia is driven sequentially through a plurality of heat exchange devices (e.g., at least three) to heat the mixture. For example, the mixture is heated to between 90°C and 100°C by heat exchange device 110. Then, the mixture is heated to between 180°C and 200°C by heat exchange device 112. Then, the mixture is heated to between 290°C and 320°C by heat exchange device 114.

[0049] Next, in step S204, the heated mixture is driven sequentially through a plurality of adiabatic reaction devices (e.g., at least three) to pre-crack the ammonia in the heated mixture and produce hydrogen and nitrogen. For example, the ammonia in the mixture is pre-cracked for the first time through adiabatic reaction device 118, such that the ammonia cracking rate reaches between 5% and 15%. Then, the ammonia in the mixture is pre-cracked for the second time through adiabatic reaction device 122, such that the ammonia cracking rate reaches between 20% and 30%. Then, the adiabatic reaction device 126 is pre-cracked for the third time, such that the ammonia cracking rate reaches between 35% and 45%. It is worth noting that the term "cracking rate" here refers to the proportion of reaction products converted into small molecules through the cracking reaction to the total reaction products.

[0050] In some embodiments, between step S202 and step S204, the mixture is further heated by heating device 116 so that the temperature of the mixture before entering the adiabatic reaction device 118 can reach between 350°C and 440°C.

[0051] In some embodiments, step S204 further includes passing the mixture through an intermediate heating device after passing through one of the adiabatic reaction devices, and then feeding it into the next adiabatic reaction device. For example, after passing through adiabatic reaction device 118, the mixture first passes through an intermediate heating device 120 to raise its temperature to between 450°C and 540°C, and then feeds it into adiabatic reaction device 122. Next, after passing through adiabatic reaction device 122, the mixture first passes through an intermediate heating device 124 to raise its temperature to between 550°C and 640°C, and then feeds it into adiabatic reaction device 126.

[0052] Next, in step S206, the pre-cracked mixture is driven through a tubular reactor 130 to further crack the pre-cracked mixture. In some embodiments, the cracking in the tubular reactor 130 results in a cracking rate of ammonia in the mixture of between 90% and 99%.

[0053] In some embodiments, between step S204 and step S206, the mixture is further heated by a heat exchanger 128, such that the mixture has a temperature between 650°C and 850°C before passing through the tubular reactor 130.

[0054] Next, in step S208, the pyrolyzed mixture is driven through the plurality of heat exchange devices in the reverse order of step S202. At this time, since the temperature of the pyrolyzed mixture is higher than the temperature of the unpyrolyzed mixture in the heat exchange devices, the pyrolyzed mixture can be used as a heat transfer medium to provide heat to the plurality of heat exchange devices to heat the unpyrolyzed mixture. This improves energy efficiency. Simultaneously, the pyrolyzed mixture can be gradually cooled to facilitate subsequent purification processes. For example, heat exchange devices 110, 112, and 114 are shell-and-tube heat exchangers. The unpyrolyzed mixture passes through the tubes of the shell-and-tube heat exchanger, while the pyrolyzed mixture passes through the shell side of the shell-and-tube heat exchanger for heat exchange, but this disclosure is not limited to this.

[0055] Similarly, in some embodiments, between step S206 and step S208, the pyrolyzed mixture may be passed through the heat exchange device 128 first, so as to use the high-temperature pyrolyzed mixture as a heat transfer medium to exchange heat with the pre-pyrolyzed and heated mixture in the heat exchange device 128, and then step S208 is performed.

[0056] Similarly, heat exchange device 128 may also be coupled to heat exchange device 114, while heat exchange device 114, heat exchange device 112 and heat exchange device 110 are configured to receive the pyrolyzed mixture in sequence and use the pyrolyzed mixture as a heat transfer medium to exchange heat with the unpyrolyzed mixture to be heated therein, while the pyrolyzed mixture can be gradually cooled.

[0057] Next, in step S210, the pyrolyzed and cooled mixture is driven through a washing device 134 to remove ammonia from the mixture. In some embodiments, between steps S208 and S210, the pyrolyzed mixture is first subjected to a temperature between 30°C and 40°C via a heat exchanger 132 before being fed into the washing device 134. After passing through the washing device 134, the mixture mainly comprises hydrogen and nitrogen.

[0058] Next, in step S212, the washed mixture is driven through at least one adsorption device to separate hydrogen from the mixture. In some embodiments, the washed mixture passes sequentially through adsorption device 142 and adsorption device 146. Specifically, the purity of hydrogen after passing through adsorption device 142 can reach between 95% and 99%, while the purity after passing through adsorption device 146 can reach 99.99% or higher. The separated impurities, including nitrogen, are collected in collection device 144.

[0059] In some embodiments, between step S210 and step S212, the mixture is first heated by the heating device 138 and the condensing device 140 to adjust the temperature, and then input into the washing device 134.

[0060] After step S212, in order to facilitate hydrogen storage, the obtained high-purity hydrogen-containing mixture can be driven through the cooling device 148 and the compressor 150 to cool and pressurize, forming liquid hydrogen and storing it in the hydrogen storage device 152.

[0061] As can be clearly seen from the detailed description of the specific embodiments disclosed above, in some embodiments of the ammonia cracking system and ammonia cracking method disclosed herein, by setting up multiple heat exchange devices and multiple adiabatic reaction devices, the mixture including ammonia is gradually heated and pre-cracked, thereby reducing the load on the tubular reactor that subsequently performs cracking. In this way, the mixture can be heated and cracked more uniformly, while reducing the number of times the catalyst in the tubular reactor needs to be replaced. Compared with common ammonia cracking systems and methods, this is beneficial for improving the overall cracking efficiency of the system and reducing the downtime of the tubular reactor.

[0062] The foregoing description is only intended to illustrate and describe exemplary embodiments of the present disclosure and is not intended to exhaustively describe or limit the precise form of the invention disclosed herein. The above teachings may be modified or varied.

[0063] The selected and illustrated embodiments are intended to explain the content of this disclosure and their practical application, thereby inspiring those skilled in the art to utilize this disclosure and various embodiments, and to make various modifications to suit a particular intended use. Alternative embodiments will be apparent to those skilled in the art without departing from the spirit and scope of this disclosure. Therefore, the scope of this disclosure is determined by the claims of the appended invention claims, and not by the foregoing specification and the exemplary embodiments described therein. [Simplified Explanation of the Diagram]

[0064] The drawings illustrate one or more embodiments of the present disclosure and, together with the written description, serve to explain the principles of the present disclosure. Throughout the drawings, the same reference numerals are used wherever possible to refer to similar or identical elements of the embodiments, wherein: Figure 1 is a schematic diagram of an ammonia cracking system according to some embodiments of the present disclosure. Figure 2 is a flowchart of an ammonia cracking method according to some embodiments of the present disclosure. [Biomaterial Storage]

[0066] Domestic storage information (please note in order of storage institution, date, and number): None. International storage information (please note in order of storage country, institution, date, and number): None.

Claims

1. An ammonia cracking system comprising: three heat exchange devices coupled to each other and configured to sequentially receive a mixture and heat the mixture using a heat transfer medium, wherein the mixture contains ammonia, wherein the heat exchange devices comprise: a first device configured to heat the mixture to between 90°C and 100°C; a second device coupled to the first device and configured to heat the mixture to between 180°C and 200°C; and a third device coupled to the second device and configured to heat the mixture to between 290°C and 320°C; three adiabatic reaction devices coupled to each other and configured to sequentially receive the mixture heated by the heat exchange devices and pre-crack the ammonia in the mixture, such that the ammonia in the mixture is partially cracked to produce hydrogen and nitrogen; a tubular reactor configured to receive the pre-cracked mixture and further crack it; and a washing device configured to receive the cracked mixture and remove ammonia from the mixture by washing.

2. The ammonia cracking system as claimed in claim 1 further includes an adsorption device configured to receive the washed mixture and separate hydrogen from the mixture.

3. The ammonia cracking system as claimed in claim 1, wherein the heat exchange devices are further configured to receive the cracked mixture and use the cracked mixture as the heat transfer medium.

4. The ammonia cracking system as claimed in claim 1 further includes an intermediate heating device coupled between one of the adiabatic reaction devices and a second device, and configured to further heat the pre-cracked mixture.

5. An ammonia cracking method, comprising: driving a mixture containing ammonia sequentially through three heat exchange devices to heat the mixture, and comprising: heating the mixture to between 90°C and 100°C through a first of the heat exchange devices; heating the mixture to between 180°C and 200°C through a second of the heat exchange devices; and heating the mixture to between 290°C and 320°C through a third of the heat exchange devices; driving the heated mixture sequentially through three adiabatic reaction devices to pre-crack the ammonia in the mixture and produce hydrogen and nitrogen; driving the pre-cracked mixture through a tubular reactor for further cracking; driving the cracked mixture through a washing device to remove ammonia from the mixture; and driving the washed mixture through an adsorption device to separate hydrogen from the mixture.

6. The ammonia cracking method as claimed in claim 5, wherein pre-cracking of the ammonia in the mixture comprises: pre-cracking the ammonia in the mixture by a first of one of the adiabatic reaction devices, such that a cracking rate of the ammonia is between 5% and 15%; pre-cracking the ammonia in the mixture by a second of one of the adiabatic reaction devices, such that the cracking rate of the ammonia is between 20% and 30%; and pre-cracking the ammonia in the mixture by a third of one of the adiabatic reaction devices, such that the cracking rate of the ammonia is between 35% and 45%, wherein the adiabatic reaction devices comprise the same catalyst.

7. The ammonia cracking method as claimed in claim 5, wherein the pre-cracked mixture has a temperature between 650°C and 850°C before passing through the tubular reactor.

8. The ammonia cracking method as described in claim 5 further comprises driving the cracked mixture sequentially through the heat exchange devices before passing it through the washing apparatus, so as to provide heat to the heat exchange devices.

9. The ammonia cracking method as claimed in claim 5, wherein the cracked mixture has a temperature between 30°C and 40°C before passing through the washing apparatus.

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