JP2014025641A - Operation method of heat exchange system - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a method for safely operating a heat exchange system even when mixture of a process liquid into a heat medium side is detected.SOLUTION: A heat exchange system conducts heat exchange between a process liquid which circulates in a process liquid passage and includes oxygen and a heat medium which circulates in a heat medium passage and is composed of molten salt containing nitrite in a non contact manner. The heat exchange system includes a gas detector which detects nitrogen oxide occurring when the heat medium contacts with the process liquid or oxygen included in the process fluid at a gas phase part in the heat medium passage. An operation method of the heat exchange system includes: a mixture detection process where the mixture of the process liquid into the heat medium passage is detected on the basis of a detection value of the gas detector; and a stop process where the supply of the process liquid to the process liquid passage is stopped when the mixture is detected in the mixture detection process.

Description

  The present invention relates to a method for operating a heat exchange system between a process fluid and a heat medium, and more particularly, to a method for operating a heat exchange system when mixing of a process fluid on the heat medium side is detected.

  A system for producing chlorine by using hydrogen chloride gas as a raw material and reacting it with oxygen in the gas phase in the presence of a catalyst (hydrochloric acid oxidation system), for example, a raw material gas containing hydrogen chloride and oxygen in the presence of a catalyst. A reactor to be reacted, a quenching tower for obtaining chlorine by absorbing unreacted hydrogen chloride by removing it by water or hydrochloric acid water by bringing the reaction gas after the reaction into contact with water or hydrochloric acid water, and the like are provided. The reaction in the reactor is usually carried out under high pressure and high temperature and is exothermic.

  The hydrochloric acid oxidation system heats the raw material gas in advance, removes reaction heat generated from the reaction gas in the reactor, and cools the reaction gas after the reaction. A heat exchange system is provided for heating, removing heat or cooling a process fluid (raw gas, reaction gas during reaction, reaction gas after reaction) containing hydrogen chloride or chlorine.

  In such a heat exchange system for heating, heat removal or cooling, heat exchange is usually performed through a heat conductor without directly contacting the process fluid and the heat medium. As the heat medium, for example, molten salt, steam, hot water, cold water, or the like is used according to the temperature of the process fluid.

  In such a heat exchange system, when a problem occurs in the flow path through which the process fluid flows and the process fluid is mixed into the heat medium side, it is necessary to quickly detect this. Patent Document 1 (Japanese Patent Application Laid-Open No. 2003-83833) describes a method for detecting mixing of a process fluid by detecting a gas component generated by contact between a heat medium and the mixed process fluid. Yes. Patent Document 2 (Japanese Patent Laid-Open No. 2012-47616) describes detecting the mixing of a process fluid on the heat medium side by detecting oxygen gas at a gas phase portion in the heat medium flow path. .

JP 2003-83833 A JP 2012-47616 A

  An object of the present invention is to provide a method capable of operating a heat exchange system safely even when mixing of a process fluid on the heat medium side is detected.

  The present invention circulates in a process fluid flow path and heats without direct contact between a process fluid containing oxygen and a heat medium that circulates in a heat medium flow path and is composed of a molten salt containing nitrite. An operation method of a heat exchange system for performing exchange, wherein the heat exchange system contains nitrogen oxide generated when the heat medium and the process fluid come into contact with each other, or oxygen contained in the process fluid. A gas detector for detecting in a gas phase portion in the heat medium flow path, and a mixing detection step for detecting the mixing of the process fluid into the heat medium flow path based on a detection value of the gas detector; And a stopping step of stopping the supply of the process fluid to the process fluid flow path when contamination is detected by the detection step.

  In one form of the present invention, the process fluid contains hydrogen chloride and / or chlorine, and when contamination is detected by the contamination detection step, all the process fluids in the process fluid flow path are treated with hydrogen chloride and / or Or it has a detoxification process step at the time of mixing that leads to a detoxification facility that detoxifies chlorine and releases it to the atmosphere.

  Further, the present invention allows direct contact between a process fluid containing oxygen and a process fluid containing oxygen and a heat medium made of a molten salt containing nitrite and flowing in the heat medium flow path. An operation method of a heat exchange system that performs heat exchange without the heat exchange system, wherein the heat exchange system includes nitrogen oxides generated when the heat medium and the process fluid come into contact with each other, or oxygen contained in the process fluid A gas detector that detects a gas phase in the heat medium flow path, and a mixing detection step of detecting mixing of the process fluid into the heat medium flow path based on a detection value of the gas detector; When mixing is detected by the mixing detection step, the mixing heat medium cooling step for cooling the heat medium in the heat medium flow path is an operating method of the heat exchange system.

  In one form of this invention, it has a chlorine production | generation process which produces | generates chlorine by making hydrogen chloride and oxygen react within a process fluid flow path. In the chlorine generation step, hydrogen chloride and oxygen are preferably reacted in an atmosphere adjusted to a temperature of 280 to 400 ° C. by heat exchange with a heat medium adjusted to a temperature of 280 to 400 ° C. In the cooling step, the temperature of the heat medium is set to 200 to 250 ° C.

  According to the first aspect of the present invention, in the heat exchange system, even if the process fluid is mixed into the heat medium side, the amount of the mixed process fluid can be suppressed, so that safety can be ensured.

  According to the invention which concerns on Claim 3, since the temperature in the whole heat exchange system can be lowered | hung, while being able to suppress various reaction and ensuring safety | security, deterioration of molten salt and reaction heat It is possible to suppress the deterioration of the equipment due to the occurrence of.

It is the schematic which shows the heat exchange system which is one Embodiment of this invention. It is a figure which shows the simulation result of the time-dependent change of the temperature of the molten salt of a molten salt storage drum when a malfunction arises in the heat exchange system shown in FIG.

  The present invention relates to a method for operating a heat exchange system that performs heat exchange without direct contact between a process fluid containing oxygen and a heat medium made of a molten salt containing nitrite that circulates in the heat medium flow path. About.

  The process fluid means a gas or liquid subjected to a heat exchange process with a heat medium or a mixture thereof. The heat exchange process in the present invention may be accompanied by a reaction of the process fluid as well as heat exchange between the process fluid and the heat medium, or may be a process in which only heat exchange is performed. In the former case, the process fluid is a raw material, intermediate, product, by-product of the reaction, or a mixture of two or more thereof.

  The heat exchanger used in the heat exchange process between the process fluid and the heat medium is not particularly limited as long as the process fluid and the heat medium exchange heat through a partition such as a tube or a flat plate. Heat exchange reactors such as multitubular catalyst-filled reactors when the heat exchange process involves reaction of process fluids, multitubular cylindrical heat exchangers that are simply bulkhead heat exchangers that perform heat exchange, plate type A heat exchanger, a spiral heat exchanger, a block heat exchanger, etc. are mentioned. Examples of the heat exchange reactor include a multi-tube fixed bed catalyst reactor including a plurality of reaction tubes filled with an oxidation catalyst and performing a gas phase oxidation reaction with the fixed bed catalyst.

The process fluid is not particularly limited as long as it contains oxygen. As a preferred example of the process fluid involving a reaction, a reaction represented by the following formula (1) for producing chlorine by oxidizing hydrogen chloride gas with oxygen gas ( Hydrochloric acid oxidation reaction):
2HCl + 1 / 2O ₂ → Cl ₂ + H ₂ O + 58.6 kJ / mol Formula (1)
And process fluids.

  The process fluid involving the reaction of the formula (1) is a raw material gas containing hydrogen chloride gas and oxygen gas; an oxygen gas which is an unreacted raw material, a hydrogen chloride gas, and a product gas containing chlorine gas which is a product; Or a mixture thereof. The process fluid may contain an inert gas such as nitrogen, carbon dioxide, or argon in addition to the raw material gas and the product gas. In the reaction of formula (1), the theoretical molar amount of oxygen with respect to 1 mol of hydrogen chloride is 0.25 mol, but the oxygen gas exceeds the theoretical amount with respect to hydrogen chloride gas (for example, 0 mol with respect to 1 mol of hydrogen chloride). It is usual to use more than 25 moles and 2 moles or less. The hydrochloric acid oxidation reaction of formula (1) is an equilibrium reaction. In order to increase the hydrogen chloride conversion rate and increase the chlorine production rate, it is better that the reaction temperature is low, and the reaction heat is removed by a heat medium in order to bring out the performance of the catalyst used in the reaction.

In the present invention, the heat medium is composed of a molten salt (HTS), and a preferable molten salt is selected according to the temperature of the target process fluid. The molten salt (HTS) preferably contains nitrite (NaNO ₂ etc.) and further contains nitrate (NaNO ₃ , KNO ₃ etc.). From the viewpoint of handleability, the melting point is preferably about 100 to 200 ° C. Specific examples of the molten salt preferably used include a composition (melting point 142 ° C.) composed of NaNO ₂ (40% by mass), NaNO ₃ (7% by mass) and KNO ₃ (53% by mass); NaNO ₂ (34% by mass) , NaNO ₃ (13 mass%) and KNO ₃ (53 mass%) (melting point 152 ° C.); NaNO ₂ (50 mass%) and KNO ₃ (50 mass%) (melting point 139 ° C.) It is.

Among them, as a heat medium used for heat exchange with the process fluid in the hydrochloric acid oxidation reaction, a molten salt composed of NaNO ₂ (50% by mass) and KNO ₃ (50% by mass) from the viewpoint of the reaction temperature of the process fluid, etc. Is preferably used.

  The heat medium flow path through which the heat medium flows includes a heat medium flow path (so-called jacket or the like) provided in a heat exchanger that performs heat exchange between the process fluid and the heat medium, and a heat medium tank that stores the heat medium; A heat exchanger (heater and / or cooler) for heating and / or cooling the medium; disposed between the heat exchanger in which heat exchange between the process fluid and the heat medium takes place and the heat medium tank; A buffer tank that performs fine adjustment of the heat medium temperature; a heater and / or cooler that adjusts the temperature of the heat medium in the buffer tank; a pipe that connects these devices; a pump that circulates the heat medium, etc. A heat medium circulation channel that is connected to the heat medium flow channel, and a pipe for introducing an inert gas such as nitrogen, carbon dioxide, and argon into the heat medium circulation flow channel and the heat medium flow channel. It connects the phase portion and the atmosphere or detoxification facilities, including a pipe for discharging the gas phase of the gaseous heating medium flow path to the outside.

The sealing of the heat medium flow path by introduction of the inert gas prevents the heat medium from deteriorating and the reaction of the following formula (2) due to the presence of air in the heat medium flow path:
NaNO ₂ + 1 / 2O ₂ → NaNO ₃ +111.7 kJ / mol Formula (2)
To prevent the occurrence of

When the reaction of the formula (2) occurs, NaNO ₃ is generated, whereby the melting point of the molten salt rises to about 300 ° C. or more, and there is a possibility that it is blocked at a low temperature part. Even if the gas phase portion of the heat medium flow path is sealed with an inert gas such as nitrogen gas, the process fluid contains oxygen gas. Therefore, when the process fluid and the molten salt come into contact, the equation (2 ) Reaction may occur. In the hydrochloric acid oxidation reaction, the pressure of the process fluid is usually operated higher than the pressure of the molten salt. There is a possibility that the reaction of formula (2) occurs by mixing into the salt side and coming into contact with the molten salt. Further, when the process fluid contains hydrogen chloride gas and / or chlorine gas, when the process fluid is mixed into the molten salt side, the chemical reaction of the following formula (3) and / or formula (4):
NaNO ₂ + HCl + 1 / 4O ₂ → NaCl + 1 / 2H ₂ O + NO ₂ +47.9 kJ / mol Formula (3)
NaNO ₂ + 1 / 2Cl ₂ → NaCl + NO ₂ +19.3 kJ / mol Formula (4)
May occur.

  In addition, when using a commercially available molten salt as a molten salt, what does not contain an organic anti-caking agent etc. is normally employ | adopted.

  The heat exchange system according to the present invention is contained in nitrogen oxides generated when the heat medium comes into contact with the process fluid, for example, nitrogen oxides generated by Formula (3) or Formula (4), or contained in the process fluid. A gas detector that detects oxygen in the gas phase portion in the heat medium flow path. Such a detector makes it possible to quickly detect the mixing of the process fluid into the heat medium.

  In one form of the operation method of the heat exchange system according to the present invention, the gas detector includes a mixing detection step of detecting mixing of the process fluid into the heat medium, and mixing is detected by the mixing detection step. And a stop step of stopping the supply of the process fluid into the process fluid flow path. The method for stopping the supply of the process fluid into the process fluid flow path is not limited, but can be stopped by closing the supply path, for example. With such an operation method, even if the process fluid is mixed into the heat medium side, the amount of mixed process fluid can be suppressed, and safety can be ensured.

  Further, in the above operation method, the contamination is detected by the contamination detection step, the supply of the process fluid into the process fluid channel is stopped by the stop step, and the process fluid existing in the process fluid channel is harmless. It is preferable to have a detoxification process step at the time of mixing that leads to the purification facility. Here, the detoxification facility is a device for detoxifying hydrogen chloride and / or chlorine and releasing it into the atmosphere. By having such a detoxification process step at the time of mixing, even if harmful gases such as hydrogen chloride and chlorine are contained in the process fluid, they are not released into the atmosphere as they are, and are rendered harmless. It is safe because it is discharged into the atmosphere.

  In one form of the operation method of the heat exchange system according to the present invention, the gas detector includes a mixing detection step of detecting mixing of the process fluid into the heat medium, and mixing is detected by the mixing detection step. And a mixing heat medium cooling step for cooling the heat medium in the heat medium flow path. The method for cooling the heat medium in the heat medium flow path is not particularly limited. For example, a method of adjusting the temperature of the heat medium that has been adjusted to a temperature of 280 to 400 ° C. to a temperature of 200 to 250 ° C. by the heat medium cooling process at the time of mixing is exemplified in the chlorine generation step by the hydrochloric acid oxidation reaction. With such an operation method, even if the process fluid is mixed into the heat medium side, the temperature of the entire heat exchange system can be lowered, so that various reactions can be suppressed and safety can be ensured. In addition, it is possible to suppress deterioration of the equipment due to deterioration of the molten salt and generation of reaction heat. The stop process and the mixing cooling process may be performed simultaneously. Hereinafter, the present invention will be described in more detail by showing specific embodiments.

[Heat exchange system]
FIG. 1 is a schematic diagram showing a heat exchange system according to an embodiment of the present invention. In the heat exchange system shown in FIG. 1, chlorine is produced by oxidizing hydrogen chloride with oxygen. The heat exchange system shown in FIG. 1 is a multi-tubular fixed bed catalyst reactor 1 which is a heat exchanger, a molten salt storage drum 2 for storing molten salt, and unreacted hydrogen chloride gas in the reaction product gas as water. A quenching tower 3 to be absorbed into the reactor, a heater 4 for heating the raw material gas of the hydrochloric acid oxidation reaction, a cooler 5 for cooling the reaction product gas, a cooler 6 for cooling the aqueous solution containing the components in the reaction product gas, And a cooler 7 for cooling the molten salt. The multitubular fixed bed catalyst reactor 1 includes a plurality of reaction tubes (not shown) that are process fluid flow paths and a jacket (not shown) that is a heat medium flow path. The molten salt storage drum 2 includes a gas phase portion 22 and a liquid phase portion 21 made of a molten salt.

  In the heat exchange system shown in FIG. 1, the process fluid flow path includes a line 11, a process fluid flow path in the multitubular fixed bed catalyst reactor 1, and the process fluid is rapidly cooled from the multitubular fixed bed catalyst reactor 1. A line 12 leading to the tower 3, a line 13 leading the process fluid containing chlorine gas from the quenching tower 3 to the chlorine drying step, a line 14 leading the process fluid from the quenching tower 3 to the detoxification facility, and the quenching tower 3 being discharged. And a line 15 for removing the hydrochloric acid water from the process fluid containing the hydrochloric acid water and returning it to the quenching tower 3.

  In the process fluid flow path, the raw material gas is guided to the multitubular fixed bed catalyst reactor 1 via the line 11. The line 11 includes a valve 31 and switches supply / stop of the source gas to the process fluid flow path by switching the open / closed state of the valve 31. The line 11 includes a heater 4, and the raw material gas supplied to the multitubular fixed bed catalyst reactor 1 is heated by the heater 4. In the multitubular fixed-bed catalyst reactor 1, hydrochloric acid oxidation reaction in the process fluid and heat exchange between the process fluid and the heat medium are performed, and a reaction product gas in the hydrochloric acid oxidation reaction passes through a line 12 to quench the tower. Led to 3. The line 12 includes a cooler 5 and cools the reaction product gas. In the quenching tower 3, water is supplied, and unreacted hydrogen chloride in the process fluid is absorbed into water to form hydrochloric acid water. The line 15 includes a pump 32 and circulates a liquid component of the process fluid including hydrochloric acid water, and removes the hydrochloric acid water from the process fluid circulating through the line 15 to the outside. The line 15 includes a cooler 6, and the cooler 6 cools the process fluid circulating in the line 15 with cooling water. The gas component in the process fluid in the quenching tower 3 is led to a chlorine drying process via a line 13 or led to a detoxification facility via a line 14. The line 13 includes a valve 33 and switches whether the process fluid is conducted to the chlorine drying process by switching the open / closed state of the valve 33. The line 14 includes a valve 34, and switches whether the process fluid can be conducted to the detoxification facility by switching the open / closed state of the valve 34.

  The process fluid supplied to the multi-tube fixed bed catalytic reactor 1 through the line 11 contains hydrogen chloride gas and oxygen gas, or in the case of recycling unreacted oxygen to the reaction system, hydrogen chloride gas, oxygen gas and chlorine. Contains gas. On the other hand, the process fluid coming out of the multi-tube fixed bed catalyst reactor 1 contains chlorine gas, hydrogen chloride gas, oxygen gas, and water vapor.

  In the heat exchange system shown in FIG. 1, the heat medium flow path includes a first circulation path, a second circulation path, a third circulation path, and a fourth flow path. In the first circulation path, the molten salt is led from the molten salt storage drum 2 to the heat medium flow path in the multitubular fixed bed catalyst reactor 1 via the line 41, and the multitubular fixed bed catalyst reactor. 1 functions as a heat medium for exchanging heat with the process fluid. Thereafter, the molten salt is returned to the molten salt storage drum 2 via the line 42. In the second circulation path, the molten salt is led from the molten salt storage drum 2 to the heater 4 via the line 41, and the raw material gas supplied to the multitubular fixed bed catalyst reactor 1 in the heater 4 is supplied to the molten salt. Functions as a heating medium for heating. Thereafter, the molten salt is returned to the molten salt storage drum 2 via the line 43. In the third circulation path, the molten salt is led to the cooler 5 via the line 41 and functions as a heat medium for cooling the reaction product gas sent from the multi-tubular fixed bed catalyst reactor 1 in the cooler 5. To do. Thereafter, the molten salt is returned to the molten salt storage drum 2 via the line 45.

  The line 41 includes a pump 8 and circulates the molten salt in the first to third circulation paths. The line 41 includes a cooler 7 and cools the molten salt to adjust the temperature of the molten salt. In the line 41, the flow path that passes through the cooler 7 or the flow path that avoids the cooler 7 is appropriately switched so that the temperature of the molten salt becomes a desired temperature. Although the configuration of the cooler 7 is not particularly limited, the cooler 7 shown in FIG. 1 is a steam generator in which water is supplied and water is changed into steam by recovering the heat of the molten salt, and steam is discharged. . The steam discharged from the cooler 7 can be used, for example, for heating a process fluid supplied to the reaction.

  The fourth flow path is composed of a line 46 capable of communicating the gas phase part 22 of the molten salt storage drum 2 with a detoxification facility for detoxifying hydrogen chloride and / or chlorine. Gas is discharged outside. Nitrogen gas is supplied to the gas phase part 22 of the molten salt storage drum 2 via a line 51, and the gas phase part of the heat medium flow path is sealed by the nitrogen gas. By providing the line 46 for discharging the gas of the part to the outside, the nitrogen gas for sealing the gas phase part of the heat medium flow path can be discharged to the outside, for example, a detoxification facility.

  Further, even when the process fluid is mixed into the heat medium, the process fluid is discharged from the line 46, whereby an increase in the pressure of the gas phase portion in the heat medium flow path can be suppressed. Further, since the line 46 is configured to lead the gas phase portion in the heat medium flow path to a detoxification facility that detoxifies hydrogen chloride and / or chlorine, the process fluid is mixed in the heat medium. Even in such a case, hydrogen chloride and chlorine contained in the process fluid can be rendered harmless and discharged.

The line 46 includes a gas detector 47 for detecting gas in a gas phase portion in the heat medium flow path. The gas detector 47 has a configuration capable of quickly detecting the mixing of the process fluid into the heat medium by detecting at least one of oxygen gas and NO _x gas generated by the reaction of the equations (3) and (4). And The installation position of the gas detector 47 is not limited to the line 46 as long as the gas in the gas phase portion in the heat medium flow path can be detected. For example, the gas phase portion 22 in the molten salt storage drum 2 is installed. May be provided.

When using a gas detector 47 for detecting the contamination of the process fluid to the heat medium by the detection of the NO _x gases, depending on the flow rate of nitrogen gas for sealing to the heat medium flow path, for example of the NO _x gas A case where the concentration is 1000 ppm or more can be set to detect mixing of the process fluid into the heat medium as an abnormal value. Carbon steel is usually used as the material in contact with the molten salt, but some NO _x gas may be generated due to the presence of iron rust, etc., and considering this, for example, 1000 ppm or more It can be an abnormal value. In the case of using the gas detector 47 that detects the mixing of the process fluid into the heat medium by detecting the oxygen gas, for example, depending on the flow rate of the nitrogen gas for sealing into the heat medium flow path, the concentration of the oxygen gas is, for example, It can be set so that the mixing of the process fluid into the heat medium is detected with the case of 500 ppm or more as an abnormal value.

  Examples of the catalyst used in the hydrochloric acid oxidation reaction process include, but are not limited to, a ruthenium oxide catalyst and a chromium oxide catalyst. In the hydrochloric acid oxidation reaction process, a measuring means for constantly measuring the temperature of the catalyst layer may be provided, and the temperature of the catalyst layer can be controlled by such a measuring means so that the optimization of the reaction and the temperature runaway can be detected at an early stage. The reaction temperature, reaction pressure, and temperature control method of the catalyst layer in the multitubular fixed bed catalyst reactor 1 are not particularly limited, but in the hydrochloric acid oxidation reaction, 300 to 300 by heat exchange with a heat medium adjusted to a temperature of 300 to 400 ° C. It is preferable to react hydrogen chloride and oxygen in an atmosphere adjusted to a temperature of 400 ° C.

  The material of the equipment used in the heat exchange system of FIG. 1 is not particularly limited, but nickel is usually used for a portion in contact with the process gas, for example, a reaction tube of the multi-tubular fixed bed catalytic reactor 1, and a molten salt For example, carbon steel is usually used for the parts that come into contact with, for example, the jacket of the multi-tubular fixed bed catalytic reactor 1 and the molten salt storage drum 2. It is preferable that the reaction temperature is controlled and the reaction heat is removed so that the reaction temperature does not exceed about 450 ° C. Note that tantalum, Teflon (registered trademark), carbon, or the like is used for a portion in contact with hydrochloric acid water such as the quenching tower 3 that cools the process fluid and condenses the hydrochloric acid water.

[Operation method of heat exchange system]
In the operation when the hydrochloric acid oxidation reaction process of the heat exchange system shown in FIG. 1 is performed, the valve 31 on the line 11 is opened, and the raw material gas is supplied to the multitubular fixed bed catalyst reactor 1. In addition, the valve 33 is opened and the valve 34 is closed so that the reaction product gas containing chlorine gas sent from the quenching tower 3 is led to the chlorine drying step via the line 13. In operation during execution of the hydrochloric acid oxidation reaction process, the gas detector 47 always detects the gas in the gas phase portion of the heat medium flow path. When the gas detector 47 detects that the process fluid is mixed into the heat medium flow path, an operation is performed to simultaneously execute one or both of the stop process and the heat medium cooling process during mixing described below. .

(Stop process)
In the stop process, when the gas detector 47 detects the mixing of the process fluid into the heat medium flow path, the valve 31 is switched from the open state to the closed state, and the raw material to the multi-tube fixed bed catalyst reactor 1 is changed. Stop supplying gas. In addition, the valve 33 is switched from the open state to the closed state, and the valve 34 is switched from the closed state to the open state, so that the gas components sent from the quenching tower 3 are guided to the harmless equipment via the line 14. By operating in this way, even if the process fluid is mixed into the heat medium flow path, the amount of the process fluid mixed can be suppressed, which is safe, and further, the pressure in the process fluid flow path is reduced to be safe. The heat exchange system can be stopped. Further, the process fluid remaining in the quenching tower 3 from the multitubular fixed bed catalyst reactor 1 can be made harmless by the harmless equipment and can be safely treated. In the stop step, preferably, the supply of water to the quenching tower 3 and the operation of the pump 32 and the cooler 6 are continued.

(Heat medium cooling process when mixed)
In the mixing heat medium cooling step, when mixing of the process fluid into the heat medium flow path is detected by the gas detector 47, while continuing the circulation of the heat medium to the first to third circulation paths, The molten salt is cooled by the cooler 7. Preferably, the temperature of the molten salt is maintained at 280 to 400 ° C. in the operation when the hydrochloric acid oxidation reaction process is performed, and the temperature of the molten salt is cooled to 200 to 250 ° C. in the heat medium cooling step at the time of mixing. This mixing heat medium cooling step can reduce the temperature of the entire heat exchange system, so that various reactions can be suppressed, safety can be secured, deterioration of molten salt and reaction heat can be ensured. It is possible to suppress the deterioration of the equipment due to the occurrence of.

[Experiment 1]
In Experiment 1, in the hydrochloric acid oxidation process performed using the heat exchange system shown in FIG. 1, a simulation is performed when the process fluid is mixed on the molten salt side, and the temperature change of the molten salt in the molten salt storage drum 2 in the simulation is performed. Asked.

(procedure)
In this simulation, the configuration and conditions of each element were determined on the assumption that the chlorine production process is 100,000 tons of chlorine per year. The number of reaction tubes of the multi-tubular fixed bed catalyst reactor 1 is proportional to the chlorine production amount. In this simulation, the number of reaction tubes is set to 10,000, which is a normal number when the chlorine production amount is 100,000 tons per year. The inner diameter of the reaction tube of the multitubular fixed bed catalyst reactor 1 is usually 18 mm to 25 mm, and the length of the reaction tube is 4 m to 6 m. These values are constant regardless of the chlorine production. In this simulation, the inner diameter of each reaction tube was 21 mm and the length was 5.7 m.

The capacity of the molten salt storage drum 4 is proportional to the amount of chlorine produced. In this simulation, the capacity of the molten salt storage drum 4 is within the range of conditions normally employed when the chlorine production is 100,000 tons per year. the capacity 2.94m ^3, the capacity of the gas phase portion was 0.8m ^3. The pressure of the raw material gas and the pressure of the reaction product gas are substantially constant without depending on the chlorine production amount. Usually, the pressure of the raw material gas is 0.2 to 0.5 MPaG, and the pressure of the reaction product gas is 0.1 to 0.4 MPaG. In this simulation, the pressure of the process fluid was 0.413 MPaG.

  The initial pressure on the molten salt side, that is, the pressure before the process fluid is mixed into the molten salt side, is usually almost constant regardless of the chlorine production. Usually, the pressure of the molten salt entering the jacket of the multitubular fixed bed catalyst reactor 1 is 0.1 MPaG, and the pressure of the molten salt exiting from the jacket of the multitubular fixed bed catalyst reactor 1 is 0.05 MPaG. In this simulation, the initial pressure of the molten salt in the jacket of the multitubular fixed bed catalyst reactor 1 was 0.063 MPaG.

  The inner diameter and length of the piping of the line 42, which is a flow path for the molten salt, are substantially proportional to the chlorine production. In this simulation, the internal diameter of the pipe of the line 42 is set to 400 mm and the length is set to 40 m within the range of conditions normally employed when the chlorine production is 100,000 tons per year. In FIG. 1, the length of the piping of the line 46 connecting the gas phase portion 22 of the molten salt storage drum 2 and the detoxification equipment for detoxifying hydrogen chloride gas and chlorine gas is substantially proportional to the chlorine production amount. In this simulation, it was set to 60 m, which is within the range of conditions normally employed when the chlorine production is 100,000 tons per year. The inner diameter of the line 46 was 80 mm. The pressure loss of the detoxification equipment is almost proportional to the chlorine production, and was set to 0.05 MPa in this simulation.

  There are various possible causes for the mixing of the process fluid on the molten salt side. In this simulation, one hole or multiple holes are generated in the reaction tube, and the total area of the generated holes is the inner diameter area of one reaction tube. Assuming the case where the same problem occurs. For example, a case where one reaction tube is cut perpendicular to the wall surface is also included in the problem assumed here. The jetting speed of the process fluid from the generated hole to the molten salt side was 370 m / s, which is the speed of sound.

  Usually, in the hydrochloric acid oxidation reaction, 1 mol of oxygen is supplied to 2 mol of hydrogen chloride, and the conversion rate of hydrogen chloride is 85%. In this case, the composition of the process fluid at the inlet and outlet of the multi-tube fixed bed catalytic reactor 1 is as shown in Table 1 below.

  In this simulation, the following composition, which is an average value of the composition at the reactor inlet and the composition at the reactor outlet, was used as the composition of the process fluid mixed on the molten salt side.

Hydrogen chloride concentration (mol%) = 40,
Oxygen concentration (mol%) = 20,
Chlorine concentration (mol%) = 20,
Water vapor concentration (mol%) = 20.

  Furthermore, when the process gas is mixed on the molten salt side, the reaction shown in the above formulas (2), (3), and (4) and the reaction rate are considered as the reaction between the molten salt and the process gas. .

(Experimental result)
In FIG. 2, a hole is formed in the reaction tube due to a malfunction as described above (this time is assumed to be 0 second after the occurrence of mixing), and then the process fluid is mixed into the heat medium flow path from the generated hole. The time-dependent change of the temperature of the molten salt in the molten salt storage drum 2 at the time of continuing is shown. In this simulation, the normal operation during the execution of the hydrochloric acid oxidation reaction process is continued even when the mixing of the process fluid into the heat medium flow path is detected. The heat medium cooling process is not performed.

(Discussion)
As shown in FIG. 2, even if the process fluid is mixed in the heat medium flow path, if the normal operation during the execution of the hydrochloric acid oxidation reaction process is continued without changing the operation method, the heat medium flow path of the process fluid The temperature of the molten salt in the molten salt storage drum 2 reaches 450 ° C. in 270 minutes after the contamination is detected. When the temperature reaches 450 ° C., the corrosion rate of the nickel reaction tube increases significantly.

  In the stopping step in the operating method of the present invention, when the mixing of the process fluid into the heat medium flow path is detected, the supply of the process fluid is stopped, so that the amount of mixing of the process fluid can be suppressed. The rise in temperature can be suppressed and is safe. Further, in the mixing heat medium cooling step in the operation method of the present invention, when the mixing of the process fluid into the heat medium flow path is detected, the molten salt is cooled, so that only an increase in the temperature of the molten salt can be prevented. Therefore, the temperature of the molten salt can be lowered and it is safe.

[Experiment 2]
In Experiment 2, in an environment close to the heat exchange system shown in FIG. 1, an experiment was performed in which the process fluid was mixed into the molten salt, and the change occurring when the process fluid was mixed into the molten salt in the heat exchange system was confirmed. .

(Experimental procedure)
(1) A 150 cc stainless steel pressure vessel was charged with 50 g of a molten salt consisting of 50 parts of sodium nitrite and 50 parts of potassium nitrate, and adjusted to 300 ° C. with an external heater.
(2) The air remaining in the gas phase portion of the pressure vessel was removed with a vacuum pump.
(3) The pressure of the pressure vessel is a mixed gas of hydrogen chloride gas: oxygen gas: chlorine gas having a molar ratio of 5: 4: 4 (a composition ratio obtained by removing water vapor from the mixed composition of the process fluid in Experiment 1). Was introduced until the pressure reached 0.5 MPaG.
(4) Pressure and temperature changes in the pressure vessel were measured for 5 minutes.
(5) After the measurement of pressure and temperature was completed, the pressure vessel was cooled with a fan, and the gas in the pressure vessel was sampled and analyzed.

(Experimental result)
(1) The temperature of the molten salt after 100 seconds of contact with the mixed gas increased from 300 ° C to 307 ° C.
(2) The pressure in the pressure vessel 100 seconds after contact with the mixed gas increased from 0.5 MPaG to 0.52 MPaG.
(3) When the gas in the pressure resistant vessel sampled by the above experimental procedure was analyzed, oxygen gas and NO _x gas were detected, but hydrogen chloride gas and chlorine gas were not detected. The reaction of the above reaction formula (2) was a first order reaction, and the reaction rate constant was 0.047 (1 / s). In this simulation, this reaction rate constant was used, and the reactions in the reaction formulas (3) and (4) were assumed to be instantaneous reactions.

(Discussion)
From the experimental results, it is predicted that when the process fluid is mixed in the heat medium flow path, the temperature of the molten salt increases and the pressure in the gas phase portion in the heat medium flow path increases. In the stop step in the operating method of the present invention, when the mixing of the process fluid into the heat medium flow path is detected, the supply of the process fluid is stopped, so that the temperature of the molten salt is increased and the gas phase in the heat medium flow path The increase in the pressure of the part can be suppressed, and it is safe. Further, in the mixing heat medium cooling step in the operation method of the present invention, when the mixing of the process fluid into the heat medium flow path is detected, the molten salt is cooled, so that only an increase in the temperature of the molten salt can be prevented. Therefore, the temperature of the molten salt can be lowered and it is safe. Further, based on the gas analysis results described above, the gas detector 47 of the heat exchange system shown in FIG. 1 is provided with a detector for detecting oxygen gas or NO _x gas, whereby the process into the heat medium flow path is performed. It can be seen that gas contamination can be detected quickly.

  1 multi-tube fixed bed catalyst reactor, 2 molten salt storage drum, 3 quenching tower, 4 heater, 5, 6, 7 cooler, 8 pump, 11, 12, 13, 14 line through which process fluid flows, 31 , 33, 34 Valve, 32 Pump, 41, 42, 43, 45 Line through which heat medium flows, 47 Gas detector.

Claims (5)

Heat that circulates in the process fluid channel and exchanges heat without direct contact between the process fluid containing oxygen and the heat medium that circulates in the heat medium channel and is composed of a molten salt containing nitrite. A method of operating the exchange system,
The heat exchange system detects a nitrogen oxide generated when the heat medium and the process fluid come into contact with each other, or a gas that detects oxygen contained in the process fluid in a gas phase portion in the heat medium flow path. Equipped with a detector,
A mixing detection step of detecting mixing of the process fluid into the heat medium flow path based on a detection value of the gas detector;
And a stopping step of stopping the supply of the process fluid to the process fluid flow path when the contamination is detected by the contamination detection step. The process fluid comprises hydrogen chloride and / or chlorine;
When contamination is detected by the contamination detection step, all the process fluid in the process fluid flow path is introduced into a harmless facility that detoxifies the hydrogen chloride and / or chlorine and releases it to the atmosphere. The operation method of the heat exchange system according to claim 1, further comprising a detoxification treatment step. Heat that circulates in the process fluid channel and exchanges heat without direct contact between the process fluid containing oxygen and the heat medium that circulates in the heat medium channel and is composed of a molten salt containing nitrite. A method of operating the exchange system,
The heat exchange system detects a nitrogen oxide generated when the heat medium and the process fluid come into contact with each other, or a gas that detects oxygen contained in the process fluid in a gas phase portion in the heat medium flow path. Equipped with a detector,
A mixing detection step of detecting mixing of the process fluid into the heat medium flow path based on a detection value of the gas detector;
A heat exchange system operating method comprising: a mixing heat medium cooling step for cooling the heat medium in the heat medium flow path when mixing is detected by the mixing detection step.   The operation method of the heat exchange system according to claim 3, further comprising a chlorine generation step of generating chlorine by reacting hydrogen chloride and oxygen in the process fluid flow path. In the chlorine generation step, hydrogen chloride and oxygen are reacted in an atmosphere adjusted to a temperature of 280 to 400 ° C by the heat exchange with the heat medium adjusted to a temperature of 280 to 400 ° C.
The operation method of the heat exchange system according to claim 4, wherein in the mixing heat medium cooling step, the temperature of the heat medium is set to 200 to 250 ° C.

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