WO2013021908A1 - 温度制御システム - Google Patents
温度制御システム Download PDFInfo
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- WO2013021908A1 WO2013021908A1 PCT/JP2012/069692 JP2012069692W WO2013021908A1 WO 2013021908 A1 WO2013021908 A1 WO 2013021908A1 JP 2012069692 W JP2012069692 W JP 2012069692W WO 2013021908 A1 WO2013021908 A1 WO 2013021908A1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B35/00—Control systems for steam boilers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
- F25D7/00—Devices using evaporation effects without recovery of the vapour
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/001—Controlling catalytic processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
- F25D1/00—Devices using naturally cold air or cold water
- F25D1/02—Devices using naturally cold air or cold water using naturally cold water, e.g. household tap water
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B11/00—Controlling arrangements with features specially adapted for condensers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B9/00—Auxiliary systems, arrangements, or devices
- F28B9/02—Auxiliary systems, arrangements, or devices for feeding steam or vapour to condensers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B9/00—Auxiliary systems, arrangements, or devices
- F28B9/04—Auxiliary systems, arrangements, or devices for feeding, collecting, and storing cooling water or other cooling liquid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00026—Controlling or regulating the heat exchange system
- B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
- B01J2208/00044—Temperature measurement
- B01J2208/00061—Temperature measurement of the reactants
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00191—Control algorithm
- B01J2219/00193—Sensing a parameter
- B01J2219/00195—Sensing a parameter of the reaction system
- B01J2219/002—Sensing a parameter of the reaction system inside the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00191—Control algorithm
- B01J2219/00211—Control algorithm comparing a sensed parameter with a pre-set value
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00191—Control algorithm
- B01J2219/00222—Control algorithm taking actions
- B01J2219/00227—Control algorithm taking actions modifying the operating conditions
- B01J2219/00238—Control algorithm taking actions modifying the operating conditions of the heat exchange system
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
Definitions
- the present invention relates to a temperature control system that enables precise temperature control of a reactor by making the temperature in a refrigerant drum such as a steam drum uniform.
- Patent Documents 1 and 2 Conventionally, as a water supply system to a steam drum, for example, there are those described in Patent Documents 1 and 2.
- water is supplied from an economizer through a water supply pipe to a drum through gas supply, and vapor is generated by gas-liquid separation using an evaporator-gas-liquid separator.
- the feed water outlet temperature of the economizer rises and becomes higher than the saturation temperature with respect to the drum pressure.
- the pressure is higher than the internal pressure of the drum. Therefore, in order to prevent steaming in the drum, a steam-liquid separation device is provided to separate the steam and water in the drum. ing.
- a water supply inner pipe is provided in the drum instead of the gas-liquid separator, and a small hole is formed in the upper half and a through hole having a larger diameter is formed in the lower half. The steam and water supply flow out.
- the above-described configuration is for a general boiler.
- the temperature of makeup water is lower than the temperature of the vapor phase in the steam drum, a temperature difference occurs between the vapor phase and the liquid phase.
- the supply water temperature of the makeup water to the steam drum is low, the liquid phase temperature becomes lower than the saturation temperature. Therefore, when this configuration is applied to the temperature control of an FT (Fischer-Tropsch) reactor, the control becomes unstable.
- the amount of steam generated becomes unstable because the liquidus temperature is lowered by the amount of water supplied to the steam drum.
- the reactor converts hydrogen gas and carbon monoxide gas-rich synthesis gas into hydrocarbons using a catalyst. Since the FT synthesis reaction is an exothermic reaction and the temperature range for proper reaction is very narrow, it is necessary to precisely control the reaction temperature in the reactor while recovering the generated reaction heat.
- the temperature control system 100 sends water stored in a vapor-liquid equilibrium state on the steam drum 101 to a heat removal pipe 104 in a reactor 103 that performs a Fischer-Tropsch synthesis reaction (exothermic reaction) with a pump 102 from the bottom. Then, the water in the heat removal pipe 104 is partially evaporated by the reaction heat accompanying the exothermic reaction generated in the reactor 103 to recover the heat, and the two-phase fluid of the steam and water is returned to the steam drum 101 by the return pipe 105. And returned to the steam drum 101. Then, the steam is supplied to the steam user outside the system through the steam outlet pipe 107.
- a Fischer-Tropsch synthesis reaction exothermic reaction
- an amount of make-up water commensurate with the steam supplied to the outside of the system is supplied to the steam drum 101 through the supply pipe 106.
- the replenishment amount of the replenishing water is adjusted so that the liquid level is constant based on the measurement result of the level measuring unit 108 that measures the water level in the steam drum 101.
- the temperature control system 100 described above since the opening of the replenishing water supply pipe 106 is submerged below the water surface in the steam drum 101, the relatively low temperature replenishing water having a large specific gravity directly flows into the bottom of the steam drum 101. And a temperature difference is generated between the steam phase and the water phase in the steam drum 101. Then, since the correlation between the vapor phase pressure of the steam drum 101 and the temperature of the aqueous phase is lost, there is a drawback that the control by the temperature control system 100 may not be performed with high accuracy.
- the present invention has been made in view of the above-described circumstances, and provides a temperature control system capable of performing highly accurate temperature control by maintaining the gas-liquid temperature in the steam drum at a saturation temperature. With the goal.
- a temperature control system is a temperature control system that recovers reaction heat in a reactor in which an exothermic reaction occurs and controls the temperature in the reactor, in which vapor and liquid refrigerant are in a gas-liquid equilibrium state.
- a stored refrigerant drum, a heat removal unit that is disposed in the reactor and evaporates a part of the liquid refrigerant supplied from the refrigerant drum by reaction heat, and a mixed phase of vapor and liquid refrigerant generated in the heat removal unit A return pipe for returning the fluid to the refrigerant drum, a steam outlet pipe for supplying the steam in the refrigerant drum to the outside of the system, and a supply pipe for supplying a supply water amount corresponding to the amount of steam discharged outside the system to the return pipe.
- the amount of reaction heat in the reactor is the heat capacity per unit refrigerant amount determined from the difference between the relatively high temperature in the refrigerant drum and the relatively low temperature of the makeup water and the physical properties of the refrigerant (specific heat, latent heat of vaporization).
- the amount of makeup water determined by the control means is preferably calculated by the following equation.
- WL3 Q / ⁇ Cp ⁇ (t1-t3) + r ⁇
- WL3 Amount of makeup water
- Q Amount of heat of reaction in the reactor
- Cp Specific heat of liquid refrigerant
- t1 Temperature in the heat removal part of the refrigerant drum
- reactor t3 Temperature of makeup water
- r Latent latent heat of liquid refrigerant.
- the supply pipe may be connected to the return pipe at an acute angle along the traveling direction of the multiphase fluid in the return pipe.
- the refilling pipe may be provided with a seal portion for preventing the backflow of steam.
- a spray nozzle that sprays supply water into the return pipe may be provided in the supply pipe at the junction of the return pipe and the supply pipe.
- the temperature control system supplies a supply water amount corresponding to the amount of steam discharged out of the system to a return pipe that returns the mixed phase fluid of the steam and liquid refrigerant generated in the heat removal section of the reactor to the refrigerant drum.
- Supply water is supplied to the refrigerant drum by merging the amount of makeup water commensurate with the amount of steam discharged out of the system into the return piping and mixing it directly with the steam at the saturation temperature in the return piping. It is possible to heat to the saturation temperature before being performed, and the gas-liquid temperature in the refrigerant drum can always be maintained at the saturation temperature.
- the temperature in the refrigerant drum can be made uniform while avoiding the complexity of the structure and the size of the equipment.
- the temperature of the reactor can be controlled with high accuracy and precision.
- the amount of reaction heat in the reactor is the heat capacity per unit refrigerant amount determined from the difference between the relatively high temperature in the refrigerant drum and the relatively low temperature of the makeup water and the physical properties of the refrigerant (specific heat, latent heat of vaporization).
- the amount of makeup water determined by the control means is specifically calculated by the following equation, so the amount of makeup water can be accurately calculated to be equal to the steam flow rate supplied to the outside of the system, and the makeup water amount can be calculated as the steam flow rate. It can be limited not to exceed.
- WL3 Q / ⁇ Cp ⁇ (t1-t3) + r ⁇
- WL3 Amount of makeup water
- Q Amount of reaction heat in the reactor
- Cp Specific heat of the liquid refrigerant
- t1 Temperature in the heat removal part of the refrigerant drum and the reactor t3: Temperature of makeup water
- r Latent latent heat of liquid refrigerant.
- the replenishment pipe is connected to the return pipe at an acute angle along the traveling direction of the multiphase fluid at the junction of the return pipe and the replenishment pipe.
- the makeup water can be supplied along the flow direction of the mixed phase fluid. Generation of a ring can be prevented.
- the supply pipe is provided with a seal that prevents the reverse flow of steam, when the supply amount of the supply water is small, the steam in the return pipe flows back into the supply pipe, causing hammering due to condensation. Can be prevented.
- a spray nozzle for spraying makeup water into the return pipe is provided in the return pipe at the junction between the return pipe and the supply pipe, when supplying makeup water from the supply pipe to the return pipe at the junction, If the make-up water is sprayed and evenly dispersed by the spray nozzle and brought into contact with the vapor of the mixed phase fluid, rapid vapor condensation due to the make-up water bias can be suppressed and occurrence of hammering can be prevented.
- water is stored at a saturation temperature as a liquid refrigerant in a vapor-liquid equilibrium state in a steam drum 2 that is a refrigerant drum, and steam is saturated above the liquid level of the water. Is filled with.
- a supply pipe 3 is connected to the bottom of the steam drum 2, and an FT reactor (hereinafter simply referred to as a reactor) 5 in which a Fischer-Tropsch synthesis reaction (exothermic reaction) is performed by a feed water pump 4 through the supply pipe 3.
- Water is sent to the heat removal pipe (heat removal section) 7. Water is partially evaporated in the heat removal tube 7 by the reaction heat accompanying the exothermic reaction generated by the reactor 5, and this heat of reaction is recovered.
- a two-phase fluid composed of steam and water from which a part of water has evaporated in the heat removal pipe 7 is returned to the steam drum 2 through the return pipe 8 to the steam drum 2, and discharged from the return pipe 8.
- the outlet is opened in the steam region above the water surface in the steam drum 2. Then, the steam is supplied to a steam user (not shown) outside the system through the steam outlet pipe 9.
- the steam outlet pipe 9 is provided with steam discharge measuring means 11 for measuring the amount of steam discharged outside the system.
- a replenishment pipe 10 is provided for replenishing the steam drum 2 with an amount of liquid refrigerant corresponding to the amount of vapor discharged supplied outside the system. They are connected at section 6. Thereby, the relatively low temperature (for example, temperature t3) makeup water is directly mixed with the relatively high temperature (for example, temperature t1, t1> t3) vapor evaporated in the reactor 5 in the return pipe 8. Heated to a saturation temperature.
- the supply pipe 10 is provided with a supply temperature measuring unit 16 for measuring the temperature of the supply water. The replenishing water in the replenishing pipe 10 reaches the saturation temperature in the return pipe 8 and is supplied into the steam drum 2.
- the reactor 5 that performs an exothermic reaction is provided with a reaction heat temperature measurement unit 14 that measures the temperature in the reactor 5 and a reaction heat amount calculation unit 15 that calculates a reaction heat amount Q. Further, based on the measurement result of the reaction heat temperature measurement unit 14 that measures the temperature in the reactor 5 that performs the exothermic reaction, the pressure control unit 18 that controls the pressure in the steam drum 2 is connected to the outside of the system from the steam outlet pipe 9. The temperature of the reactor 5 that performs the exothermic reaction is controlled by adjusting the amount of steam discharged to the reactor by cascade control.
- reaction heat temperature measurement unit 14 may include, for example, a plurality of temperature sensors (not shown) that are spaced apart from each other in the vertical direction in the reactor 5, and an average value of each temperature measured by these temperature sensors. Can be measured as the temperature in the reactor 5.
- the steam phase pressure of the steam drum 2 and the temperature of the water phase have a certain correlation. Accordingly, when a deviation occurs in the actual temperature in the reactor 5 measured by the reaction heat temperature measuring unit 14 with respect to the temperature setting value of the reactor 5 that performs the exothermic reaction, the pressure control unit 18 is operated to operate the steam drum. Change the vapor phase pressure of 2.
- the pressure control unit 18 controls the steam outlet pipe 9, the pressure control valve 19 provided in the steam outlet pipe 9, and the pressure control valve 19 to control the inside of the steam drum 2 through the steam outlet pipe 9.
- a pressure setting unit 21 for setting the pressure.
- the temperature setting result of the reaction heat temperature measuring unit 14 is input to the pressure setting unit 21, and the pressure setting unit 21 calculates a deviation of the actual temperature in the reactor 5 from the temperature setting value from the temperature measurement result. Based on this deviation, the pressure control valve 19 is controlled to change the vapor phase pressure of the steam drum 2.
- the temperature of the water phase in the steam drum 2 (that is, the temperature of water supplied to the heat removal pipe 7 in the reactor 5 that performs the exothermic reaction). And the amount of heat recovered by the heat removal tube 7 can be changed, and the temperature of the reactor 5 performing the exothermic reaction can be brought close to the temperature set value.
- the temperature of the water phase in the steam drum 2 can be measured by the water phase temperature measurement unit 23 provided at the bottom of the steam drum 2.
- the steam drum 2, the supply pipe 3, the heat removal pipe 7 and the return pipe 8 constitute a system in which water as a liquid refrigerant circulates.
- the temperature in the steam drum 2 is always the saturation temperature at any pressure, so that the reactor temperature can be precisely and accurately controlled.
- the temperature control system 1 is provided with a control means 25 for controlling the amount of makeup water so that the amount of makeup water from the makeup piping 10 does not exceed the amount of steam discharged from the steam outlet discharge pipe 9 to the outside of the system.
- a control means 25 for controlling the amount of makeup water so that the amount of makeup water from the makeup piping 10 does not exceed the amount of steam discharged from the steam outlet discharge pipe 9 to the outside of the system.
- each measured value by the water phase temperature measurement part 23 which measures the water phase temperature in the steam drum 2, the reaction heat amount calculation part 15, and the replenishment temperature measurement part 16 which measures the replenishment water temperature in the replenishment piping 10 is measured. Is calculated and determined so that the amount of makeup water does not exceed the amount of steam discharged from the steam discharge pipe 9.
- the calculated supplementary water amount data is output to the flow rate adjusting means 26 provided in the supplemental piping 10, and the opening amount of the flow rate adjusting valve 13 is adjusted to control the supplemental water amount.
- the steam drum 2 is provided with a level measuring unit 12 that measures the water level (liquid level) in the steam drum 2. In order to prevent excessive water supply to the steam drum 2 (overflow prevention), the level measuring unit 12 When the valve opening degree of the flow rate control valve 13 output from the measurement result is smaller than the valve opening degree corresponding to the calculated makeup water amount, the opening degree is selected. Thus, the amount of makeup water is controlled so as not to exceed the steam flow rate.
- the amount of steam discharged from the steam outlet pipe 9 is WV1
- the temperature is t1
- the flow rate of water supplied to the reactor 5 by the supply pipe 3 is WL4, the temperature t1, and the return pipe from the reactor 5
- the amount of steam discharged to 8 is WV2
- the flow rate of water is WL2
- each temperature t1 the flow rate of water supplied from the replenishment pipe 10 to the return pipe 8 is WL3, the temperature t3, and the return pipe 8 after joining the steam drum 2
- the amount of steam returned to WV1 is WV1, the flow rate of water is WL4, and each temperature t1.
- the flow rate of water is unit kg / h
- the flow rate of steam is unit kg / h
- the temperature is ° C.
- the amount of reaction heat in the reactor 5 is Q (kcal / h)
- the latent heat of vaporization is r (kcal / kg)
- the specific heat of water is Cp (kcal / kg / ° C.).
- the temperature of the makeup water amount WL3 is the low temperature t3, and the other is the high temperature t1 (> t3).
- the amount of steam agglomeration the amount of preheated water / the latent heat of vaporization.
- WV2 ⁇ WV1) ⁇ r WL3 ⁇ Cp ⁇ (t1 ⁇ t3) (4) It becomes.
- the makeup water amount WL3 can be obtained from the relationship between the reaction heat amount Q and the feed water temperatures t1 and t3.
- the reaction heat quantity Q can be determined from the product of the reaction quantity in the reactor 5 separately measured and calculated or the temperature difference between the steam drum 2 and the reactor 5, the heat transfer area of the heat removal tube, and the overall heat transfer coefficient. .
- the temperature control system 1 has the above-described configuration, and the control method will be described next.
- the flow rate WL 4 of water at the temperature t 1 is supplied from the steam drum 2 to the reactor 5.
- a part of the water flow rate WL4 is evaporated in the heat removal pipe 7 by the reaction heat accompanying the exothermic reaction generated in the reactor 5, and becomes a two-phase of a steam flow rate WV2 at a temperature t1 and a water flow rate WL2, and this two-phase fluid (mixed phase) Fluid) is fed by the return pipe 8.
- the steam phase and the water phase in the steam drum 2 are such that the water level is lowered by discharging the above-described flow rate WL4 of water toward the reactor 5 by the pump 4, and therefore the amount of makeup water determined by the control means 25 WL3 is adjusted and supplied by the flow control valve 13.
- the replenishment pipe 10 is replenished with a replenishment water amount WL3 at a relatively low temperature t3 determined by the control means 25, and merges with the two-phase fluid (WV2 + WL2) in the return pipe 8 at the junction 6 with the return pipe 8. .
- the makeup water amount WL 3 at the temperature t 3 is heated by being directly mixed with the steam WV 2 at the high temperature t 1 in the return pipe 8 and heated to the saturation temperature t 1.
- the flow rate of water in the return pipe 8 becomes the same as the water flow rate WL4 supplied from the steam drum 2 to the supply pipe 3 by condensing a part of the steam in the junction 6.
- the steam flow rate WV ⁇ b> 1 at the temperature t ⁇ b> 1 and the water flow rate WL ⁇ b> 4 are discharged above the water surface in the steam drum 2.
- the temperature t1 measured by the water phase temperature measurement unit 23 that measures the water phase temperature in the steam drum 2, the reaction heat quantity Q calculated by the reaction heat quantity calculation unit 15, and the replenishment measured by the replenishment temperature measurement unit 16 of the replenishment pipe 10 The water temperature t3 is input to the control means 25.
- the control means 25 calculates the makeup water amount WL3 by the above equation (6).
- the calculated value of the replenishing water amount WL3 is output to the flow rate adjusting means 26, the flow rate adjusting valve 13 is operated to supply the replenishing water flow rate WL3 to the replenishing pipe 10, and merged with the return pipe 8 at the merging portion 6 and steam drum 2 Will be discharged.
- the steam outlet pipe 9 supplies the steam flow rate WV1 from the steam drum 2 to the outside of the system, and the makeup water amount WL3 joins the two-phase fluid of steam and water at the junction 6 with the return pipe 8 to steam. It is supplied into the drum 2. Moreover, since the makeup water amount WL3 is controlled to be equal to the steam flow rate WV1 by the control means 25, the water surface in the steam drum 2 becomes constant.
- the makeup water amount WL3 at a relatively low temperature t3 equal to the steam flow rate WV1 supplied to the outside by the steam outlet pipe 9 is merged from the supplementary pipe 10 to the return pipe 8.
- the makeup water can be instantaneously heated to the saturation temperature. Therefore, the gas-liquid temperature in the steam drum 2 can always be maintained at the saturation temperature. As a result, the reactor temperature can be controlled precisely and with high accuracy.
- control means 25 can calculate the makeup water amount WL3 so as to be equal to the steam flow rate WV1 supplied outside the system, and can accurately limit the makeup water amount so that the makeup water amount WL3 does not exceed the steam flow rate WV1. Thus, hammering due to total condensation at the junction 6 can be prevented.
- the conventional temperature control system is configured to supply makeup water directly to the steam drum 2, the makeup water is heated by heat transfer (condensation of steam) in the steam drum 2, and the temperature of the makeup water is set to the saturation temperature.
- the temperature of the makeup water is set to the saturation temperature.
- the cost is increased.
- the present invention can uniformly control the temperature in the steam drum 2 while avoiding the complexity of the structure and the size of the equipment.
- FIG. 3 shows a configuration of the junction 6 according to the first modification.
- the replenishment pipe 10 is connected and joined so as to form an acute angle ⁇ with respect to the flow direction of the two-phase fluid in the return pipe 8.
- the makeup water smoothly merges with the two-phase fluid of steam and water flowing through the return pipe 8, so that the impact of the makeup water colliding with the mixed phase fluid at the time of merge and the hammering due to the rapid condensation of the mixed phase fluid do not occur.
- the supply pipe 10 is joined and joined at an acute angle with respect to the flow direction of the two-phase fluid in the return pipe 8, and upstream of the merging section 6.
- a substantially U-shaped concave portion 10 a is formed, and a water seal portion 27 is provided as a seal portion.
- a check valve may be provided in place of the water seal portion 27 as a seal portion for preventing the reverse flow of steam.
- FIG. 5 shows a configuration of the merging portion 6 according to the third modification.
- the supply pipe 10 is connected so as to form an acute angle with respect to the flow direction of the two-phase fluid in the return pipe 8, and the supply water is dispersed in the return pipe 8 at the tip of the supply pipe 10.
- a spray nozzle 28 for spraying is formed.
- the makeup water that joins the steam and water in the return pipe 8 is sprayed widely by the spray nozzle 28, so that rapid steam condensation can be suppressed and hammering can be prevented.
- any two or three of the configurations of the first to third modifications described above may be combined.
- the temperature t1 of the water amount WL4 and the water amount WL2 supplied through the supply pipe 3 and the temperature t1 of the steam flow rates WV1 and WV2 are all set to a saturation temperature of 195 ° C.
- the water temperature t3 of the makeup water amount WL3 is set to 110 ° C.
- reaction heat quantity Q 8000000 kcal / h
- Water latent heat of vaporization r 470 kcal / kg (property value (constant))
- Specific heat of water Cp 1 kcal / kg / ° C. (property value (constant))
- the control means 25 of the temperature control system 1 replenishes the steam drum 2 with the same amount as the steam flow rate WV1 by making the temperature inside the steam drum 2 uniform and making the liquid level constant.
- FIG. 6 is a graph of an embodiment showing a change in the steam ratio at the front and rear positions of the junction 6 between the return pipe 8 and the supply pipe 10 in the temperature control system 1.
- the ratio (WV2 / WL4) of the steam WV2 generated in the reactor 5 to the circulation amount WL4 of water supplied from the steam drum 2 to the reactor 5 is plotted on the horizontal axis, and the return before and after the junction 6
- the ratio of the amount of steam in the two-phase fluid in the pipe 8 is taken as the ratio of the vapor phase on the vertical axis.
- the broken line M indicates the ratio (WV2 / (WL2 + WV2)) of the gas phase (steam) at the outlet (return pipe 8) of the reactor 5, and the solid line N indicates the return pipe 8 after the supply pipe 10 joins.
- the ratio of the evaporation amount WV2 to the circulation flow rate WL4 in the reactor 5 (WV2 / WL4) is normally operated at 30%.
- hammering may occur if the vapor WV2 in the return pipe 8 is fully condensed, but in the embodiment of the present invention, the steam flow rate If the balance between WV1 and the makeup water amount WL3 is balanced, the change in the ratio of the steam WV1 in the return pipe 8 after the merge of the makeup water amount WL3 is in the range of about 1% to 3% as described above. Does not occur.
- the present invention relates to a temperature control system that enables precise temperature control of a reactor by making the temperature in a refrigerant drum such as a steam drum uniform. According to the present invention, highly accurate temperature control can be performed by maintaining the gas-liquid temperature in the steam drum at the saturation temperature.
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Abstract
Description
本願は、2011年8月5日に日本に出願された特願2011-171812号について優先権を主張し、その内容をここに援用する。
また、特許文献2に記載されたものでは、気液分離装置に変えてドラム内に給水内管を設け、その上半部に小孔を下半部にこれより口径の大きい透孔を形成して蒸気と給水を流出するようにしている。
このようなFT合成反応において、反応器は、水素ガスおよび一酸化炭素ガスリッチの合成ガスを、触媒を用いて炭化水素に変換する。FT合成反応は発熱反応であり、かつ適正に反応する温度域が非常に狭いため、発生する反応熱を回収しながら反応器内の反応温度を緻密に制御する必要がある。
一方、系外に供給された蒸気に見合った量の補給水が、補給配管106を通してスチームドラム101に補給される。補給水の補給量は、スチームドラム101内の水面レベルを測定するレベル測定部108の測定結果に基づいて液面が一定になるように調節される。
WL3=Q/{Cp×(t1-t3)+r}
但し、WL3:補給水量
Q:前記反応器内での反応熱量
Cp:液体冷媒の比熱
t1:前記冷媒ドラムおよび反応器の除熱部内の温度
t3:補給水の温度
r:液体冷媒の蒸発潜熱。
また、補給配管には、蒸気の逆流を防ぐシール部が設けられていてもよい。
或いは、戻り配管と補給配管との合流部において、補給配管に補給水を戻り配管内に噴霧するスプレーノズルが設けられていてもよい。
しかも、補給水を直接冷媒ドラムへ供給する従来の温度制御システムと比較して、構造の複雑化や設備の大型化を避けて冷媒ドラム内の温度を均一にできる。
以上より、効率よく冷媒ドラム内の温度が均一にできることから、高精度かつ緻密な反応器の温度制御が可能となる。
WL3=Q/{Cp×(t1-t3)+r}
但し、WL3:補給水量
Q:反応器内での反応熱量
Cp:液体冷媒の比熱
t1:冷媒ドラムおよび反応器の除熱部内の温度
t3:補給水の温度
r:液体冷媒の蒸発潜熱。
補給配管10の補給水は、戻り配管8で飽和温度となってスチームドラム2内へ供給される。
また、発熱反応を行なう反応器5内の温度を測定する反応熱温度測定部14の測定結果に基づいて、スチームドラム2内の圧力を制御する圧力制御部18が、蒸気出口配管9から系外に排出する蒸気量をカスケード制御にて調節することで、発熱反応を行なう反応器5の温度を制御している。なお反応熱温度測定部14は、例えば反応器5において上下方向に互いに離間して配置された図示しない複数の温度センサを備えていてもよく、これらの温度センサにより測定された各温度の平均値を、反応器5内の温度として測定することができる。
なお本実施形態では、スチームドラム2内の水相の温度は、スチームドラム2の底部に設けられた水相温度測定部23により測定可能となっている。本実施形態では、スチームドラム2、供給配管3、除熱管7および戻り配管8により、液体冷媒としての水が循環する系が構成されている。また、補給水を戻り配管8に供給しているため、スチームドラム2内の温度は、いずれの圧力においても常に飽和温度になることから、反応器温度を緻密かつ高精度で制御できる。
これらによって補給水量が蒸気流量を超えないように制御される。
図2に示すように、蒸気出口配管9で排出される蒸気量をWV1,温度をt1,供給配管3で反応器5に供給される水の流量をWL4、温度t1、反応器5から戻り管8へ吐出される蒸気量をWV2、水の流量をWL2、各温度t1、補給配管10から戻り配管8へ供給される水の流量をWL3、温度t3、合流後の戻り管8からスチームドラム2へ戻される蒸気量をWV1、水の流量をWL4、各温度t1とする。なお、水の流量は単位kg/h,蒸気の流量は単位kg/hとし、温度は℃とする。
また、反応器5での反応熱量をQ(kcal/h)、水の蒸発潜熱をr(kcal/kg)、水の比熱をCp(kcal/kg/℃)とする。
WV1=WL3 …(1)
上記(1)式を導き出す手順について以下に説明する。
図2において、まずスチームドラム2から供給される温度t1の水の流量WL4は反応器5で反応熱を回収することで、温度t1の蒸気流量WV2+水流量WL2となるから、反応器5で相変化する入出の物質収支を示すと下記(2)式になる。
WL4=WV2+WL2 …(2)
更に、補給配管10から補給水量WL3が供給されることで、戻り配管8と補給配管10の合流部6での物質収支(給水+相変化)は次の式(3)になる。
WV2+WL2+WL3=WV1+WL4 …(3)
(2)式を(3)式に代入して整理すると次式になる。
WV1=WL3 …(1)
(WV2-WV1)×r=WL3×Cp×(t1-t3) …(4)
となる。
反応熱量Qと反応器5での蒸気発生量WV2との関係は以下の通りである。
WV2=Q/r …(5)
そして、式(1)と(5)を(4)式に代入して整理する。
WL3=Q/{Cp×(t1-t3)+r} …(6)
このようにして、反応熱量Qと給水温度t1,t3との関係から補給水量WL3を求めることができる。
なお、反応熱量Qは、別途測定・計算される反応器5での反応量またはスチームドラム2と反応器5の温度差と除熱管の伝熱面積と総括伝熱係数の積から求めることができる。
例えば、給水用のポンプ4を駆動することで、スチームドラム2から温度t1の水の流量WL4が反応器5へ供給される。反応器5で発生する発熱反応に伴う反応熱により除熱管7内で水流量WL4は一部が蒸発されて温度t1の蒸気流量WV2と水の流量WL2の二相となり、この二相流体(混相流体)は戻り配管8によって給送される。
一方、補給配管10では、制御手段25で決定された比較的低温t3の補給水量WL3が補給されて、戻り配管8との合流部6で戻り配管8内の二相流体(WV2+WL2)と合流する。すると、合流部6では、温度t3の補給水量WL3が戻り配管8内で高温t1の蒸気WV2と直接混合して加熱され、飽和温度t1まで加熱される。また、合流部6では一部の蒸気が凝縮することで戻り配管8内の水の流量は、スチームドラム2から供給配管3に供給される水流量WL4と同じになる。
そして、合流部6以降の戻り配管8では、温度t1の蒸気流量WV1と水の流量WL4となってスチームドラム2内の水面の上方に吐出される。
スチームドラム2内の水相温度を測定する水相温度測定部23で測定した温度t1と、反応熱量計算部15で計算した反応熱量Qと、補給配管10の補給温度測定部16で測定した補給水の温度t3とが制御手段25に入力される。そして、制御手段25では上記(6)式により補給水量WL3を演算する。
この補給水量WL3の演算値を流量調整手段26に出力して流量調節弁13を作動させて補給水流量WL3を補給配管10に供給し、合流部6で戻り配管8に合流させてスチームドラム2へ吐出させることになる。
また、蒸気出口配管9によってスチームドラム2内から蒸気流量WV1が系外に供給されると共に、補給水量WL3が戻り配管8との合流部6で蒸気と水との二相流体と合流してスチームドラム2内に供給される。しかも、制御手段25によって、補給水量WL3は蒸気流量WV1と等しく制御されるため、スチームドラム2内の水面は一定となる。
そのため、スチームドラム2内の気液温度を常に飽和温度に維持できる。その結果、反応器温度を緻密かつ高精度で制御できる。
更に、制御手段25によって、補給水量WL3が系外に供給する蒸気流量WV1と同等となるように演算でき、補給水量WL3が蒸気流量WV1を超えないように補給水量を正確に制限することができて、合流部6での全凝縮によるハンマリングを防止することができる。
次に、補給配管10が合流部6で戻り配管8に合流する際のハンマリングを防止するための構成について図3から図5により変形例として説明する。
図3は第一変形例による合流部6の構成を示すものである。図3において、補給配管10は戻り配管8の二相流体の流れ方向に対して鋭角αをなすように連結して合流する。これにより戻り配管8を流れる蒸気と水の二相流体に対して補給水がスムーズに合流するため、合流時に補給水が混相流体に衝突した衝撃や混相流体の急激な凝縮によるハンマリングを生じない。
この構成によれば、補給水量WL3が少ない場合、戻り配管8内の蒸気が補給配管10内に逆流しようとしても水シール部27で停止させられる。そのため、戻り配管8内の蒸気が補給配管10内に逆流して凝縮によるハンマリングが発生することを防止できる。
なお、蒸気の逆流を防ぐシール部として、水シール部27に代えて逆止弁を設けてもよい。
なお、実施形態による温度制御システム1においては、上述した第一から第三変形例の構成のいずれか二つまたは三つを組み合わせて構成してもよい。
まず、図2において、スチームドラム2内の温度や供給配管3を通して供給する水量WL4や水量WL2の各水温t1、そして蒸気流量WV1、WV2の温度t1をいずれも195℃の飽和温度とする。そして、補給水量WL3の水温t3を110℃とする。
さらに、反応熱量Q=8000000kcal/h
水の蒸発潜熱r=470kcal/kg(物性値(定数))
水の比熱Cp=1kcal/kg/℃(物性値(定数))
スチームドラム圧力=1.3MPaG
給水ポンプ4の循環量WL4=68000kg/h
とする。
WL3=Q/{Cp×(t1-t3)+r}
=8000000/{1×(195-110)+470}
=14400kg/h
となる。
WV1=WL3=14400kg/h
となる。また、(5)式により反応器5内での蒸気発生量WV2を求めると、
WV2=Q/r
=8000000/470
=17000kg/h
となる。また、反応器5の出口における水の流量WL2を(2)式から求めると
WL2=WL4-WV2
=68000-17000
=51000kg/h
となる。
図6において、スチームドラム2から反応器5へ供給される水の循環量WL4に対する反応器5内で生成される蒸気WV2の割合(WV2/WL4)を横軸にとり、合流部6の前後における戻り配管8内の二相流体中の蒸気量の割合を気相部の割合として縦軸にとった。
そして、水の循環量WL4に対する反応器5内で生成される蒸気WV2の割合(WV2/WL4)を変化させた場合における、戻り配管8中の合流部6の前後における二相液体中の蒸気量(気相部)の割合を計算した。
図6に示すグラフにおいて、スタート時点では反応器5での蒸発割合は0であるが(WV2/WL4=0)、反応器5の温度上昇に伴い蒸気WV2の発生量は増加する。反応器5での循環流量WL4に対する蒸発量WV2の割合(WV2/WL4)は通常30%で運転される。これを通常運転ポイントとする。この状態で、蒸気流量WV1と補給水量WL3のバランスがとれていれば、反応器5の出口で生成された蒸気量WV2の割合(WV2/WL4)から補給水WL3合流後の戻り配管8での蒸気量WV1の割合(WV1/(WV1+WL4))への変化は約1%程度の低下にすぎない。
ここで、戻り配管8の補給配管10との合流部6において、戻り配管8内の蒸気WV2の全凝縮が起こればハンマリングが生じる可能性があるが、本発明の実施例では、蒸気流量WV1と補給水量WL3のバランスがとれていれば、上記のように補給水量WL3の合流後の戻り配管8内での蒸気WV1の割合の変化は約1%~3%の範囲であり、ハンマリングは生じない。
また上述の実施形態や各変形例や実施例等では、液体冷媒として水を採用したが、水でなくてもよい。
本発明によれば、スチームドラム内の気液温度を飽和温度に維持することで、高精度の温度制御ができる。
2 スチームドラム
3 供給配管
4 ポンプ
5 反応器
6 合流部
7 除熱管
8 戻り配管
9 蒸気出口配管
10 補給配管
11 蒸気排出量測定手段
12 レベル測定部
13 流量調節弁
14 反応熱温度測定部
15 反応熱量計算部
16 補給温度測定部
23 水相温度測定部
25 制御手段
26 流量調整手段
Claims (6)
- 内部で発熱反応が生じる反応器内の反応熱を回収して該反応器内の温度を制御する温度制御システムであって、
蒸気及び液体冷媒が気液平衡状態で収容された冷媒ドラムと、
前記反応器に配設されていて前記冷媒ドラムから供給された前記液体冷媒の一部を前記反応熱で蒸発させる除熱部と、
前記除熱部で生じた蒸気と液体冷媒との混相流体を前記冷媒ドラムに戻す戻り配管と、
前記冷媒ドラム内の蒸気を系外へ供給する蒸気出口配管と、
前記系外に排出される蒸気の量に見合った補給水量を前記戻り配管に供給する補給配管と
を備えている温度制御システム。 - 前記反応器内の反応熱量を前記冷媒ドラム内の比較的高い温度と補給水の比較的低い温度および冷媒の物性値(比熱、蒸発潜熱)から決定される単位冷媒熱量で除して前記補給水量を決定する制御手段と、
前記制御手段で決定された前記補給水量に応じて前記補給配管から戻り配管に供給する補給水量を設定する補給水調整手段と、
を更に備えている請求項1に記載された温度制御システム。 - 前記制御手段で決定する補給水量は次式によって演算されるようにした請求項2に記載された温度制御システム。
WL3=Q/{Cp×(t1-t3)+r}
但し、WL3:補給水量
Q:前記反応器内での反応熱量
Cp:液体冷媒の比熱
t1:前記冷媒ドラムおよび反応器の除熱部内の温度
t3:補給水の温度
r:液体冷媒の蒸発潜熱。 - 前記戻り配管と補給配管との合流部において、前記補給配管は前記戻り配管内の混相流体の進行方向に沿って前記戻り配管と鋭角の角度で接続されている請求項1から3のいずれか1項に記載された温度制御システム。
- 前記補給配管には、蒸気の逆流を防ぐシール部が設けられている請求項1から4のいずれか1項に記載された温度制御システム。
- 前記戻り配管と補給配管との合流部において、前記補給配管に補給水を前記戻り配管内に噴霧するスプレーノズルが設けられている請求項1から5のいずれか1項に記載された温度制御システム。
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2012
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- 2012-08-02 EP EP12822546.3A patent/EP2741030A4/en not_active Withdrawn
- 2012-08-02 BR BR112014002617A patent/BR112014002617A2/pt not_active IP Right Cessation
- 2012-08-02 WO PCT/JP2012/069692 patent/WO2013021908A1/ja active Application Filing
- 2012-08-02 CN CN201280037631.XA patent/CN103717986B/zh not_active Expired - Fee Related
- 2012-08-02 US US14/236,839 patent/US20140157813A1/en not_active Abandoned
- 2012-08-02 AU AU2012293758A patent/AU2012293758B2/en not_active Ceased
- 2012-08-02 MY MYPI2014700190A patent/MY166929A/en unknown
- 2012-08-02 CA CA2843842A patent/CA2843842C/en active Active
- 2012-08-02 EA EA201490365A patent/EA201490365A1/ru unknown
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2014
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JPH0353521B2 (ja) | 1982-04-24 | 1991-08-15 | Babcock Hitachi Kk | |
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Also Published As
Publication number | Publication date |
---|---|
MY166929A (en) | 2018-07-24 |
EP2741030A1 (en) | 2014-06-11 |
JP2013034930A (ja) | 2013-02-21 |
AU2012293758B2 (en) | 2015-10-08 |
US20140157813A1 (en) | 2014-06-12 |
CN103717986B (zh) | 2015-11-25 |
EP2741030A4 (en) | 2015-01-14 |
CN103717986A (zh) | 2014-04-09 |
ZA201401203B (en) | 2015-10-28 |
CA2843842A1 (en) | 2013-02-14 |
BR112014002617A2 (pt) | 2017-03-01 |
JP5815324B2 (ja) | 2015-11-17 |
CA2843842C (en) | 2016-05-10 |
AP2014007443A0 (en) | 2014-02-28 |
EA201490365A1 (ru) | 2014-07-30 |
AU2012293758A1 (en) | 2014-02-20 |
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