WO2012105311A1 - 温度制御システム - Google Patents
温度制御システム Download PDFInfo
- Publication number
- WO2012105311A1 WO2012105311A1 PCT/JP2012/050853 JP2012050853W WO2012105311A1 WO 2012105311 A1 WO2012105311 A1 WO 2012105311A1 JP 2012050853 W JP2012050853 W JP 2012050853W WO 2012105311 A1 WO2012105311 A1 WO 2012105311A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- refrigerant
- temperature
- reactor
- drum
- control system
- Prior art date
Links
- 239000003507 refrigerant Substances 0.000 claims abstract description 145
- 239000007788 liquid Substances 0.000 claims abstract description 58
- 238000006243 chemical reaction Methods 0.000 claims abstract description 38
- 238000009529 body temperature measurement Methods 0.000 claims abstract description 8
- 238000003786 synthesis reaction Methods 0.000 claims description 16
- 238000005507 spraying Methods 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 47
- 239000012071 phase Substances 0.000 description 23
- 239000007789 gas Substances 0.000 description 16
- 239000012808 vapor phase Substances 0.000 description 11
- 239000012530 fluid Substances 0.000 description 8
- 238000005259 measurement Methods 0.000 description 5
- 239000002826 coolant Substances 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000008400 supply water Substances 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
-
- 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
-
- 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
-
- 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
- C10G2/34—Apparatus, reactors
-
- 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
- B01J2219/00051—Controlling the temperature
- B01J2219/00054—Controlling or regulating the heat exchange system
- B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
- B01J2219/00058—Temperature measurement
- B01J2219/00063—Temperature measurement of the reactants
-
- 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
- B01J2219/00051—Controlling the temperature
- B01J2219/00054—Controlling or regulating the heat exchange system
- B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
- B01J2219/00065—Pressure measurement
-
- 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
- B01J2219/00051—Controlling the temperature
- B01J2219/00054—Controlling or regulating the heat exchange system
- B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
- B01J2219/00067—Liquid level measurement
-
- 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
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
- B01J2219/00081—Tubes
-
- 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
- B01J2219/00162—Controlling or regulating processes controlling the pressure
-
- 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
-
- 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
- B01J2219/00213—Fixed parameter value
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
- F28D2021/0033—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for cryogenic applications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
- F28D2021/0061—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for phase-change applications
- F28D2021/0064—Vaporizers, e.g. evaporators
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
- F28D2021/0077—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for tempering, e.g. with cooling or heating circuits for temperature control of elements
Definitions
- the present invention relates to a temperature control system.
- This application claims priority on Japanese Patent Application No. 2011-18263 filed in Japan on January 31, 2011, the contents of which are incorporated herein by reference.
- a heat recovery system for recovering reaction heat in the reactor for example, a configuration described in Patent Document 1 below is known.
- a jacketed conduit is disposed in the reactor, and the reaction water in the reactor is circulated by circulating the boiler feed water supplied to the external boiler through the jacket space in the jacketed conduit. Is recovered.
- the present invention has been made in view of the above-described circumstances, and its purpose is to quickly respond to temperature changes in the reactor and to control the temperature in the reactor with high accuracy. Is to provide.
- the 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, and stores the liquid refrigerant in a gas-liquid equilibrium state.
- a pressure control unit that controls the pressure in the drum, and the pressure control unit has an actual temperature in the reactor measured by the temperature measurement unit with respect to a temperature set value in the reactor.
- the temperature of the liquid refrigerant in the refrigerant drum is controlled by controlling the pressure in the refrigerant drum based on the deviation.
- the pressure in the refrigerant drum and the temperature of the liquid refrigerant correspond approximately one to one.
- the pressure control unit controls the pressure in the refrigerant drum, thereby directly controlling the temperature of the liquid refrigerant supplied from the refrigerant drum to the heat removal unit, and the reaction in the reactor by the heat removal unit. Control the amount of heat recovered and the temperature in the reactor. That is, in this temperature control system, first, the pressure controller controls the pressure in the refrigerant drum based on the deviation that the actual temperature in the reactor has with respect to the temperature set value.
- the temperature of the liquid refrigerant in the refrigerant drum changes according to the correlation of the gas-liquid equilibrium state in the refrigerant drum. Since this liquid refrigerant is supplied to the heat removal section, the amount of heat recovered by the heat removal section changes according to the temperature change of the liquid refrigerant. And the temperature in a reactor is controllable by changing the calorie
- the exothermic reaction may be a Fischer-Tropsch synthesis reaction.
- a refrigerant replenishment section that replenishes the liquid refrigerant in the refrigerant drum is provided in the refrigerant drum, and the refrigerant replenishment section is disposed in a gas phase portion of the refrigerant drum. May be.
- the refrigerant replenishing portion is disposed in the gas phase portion of the refrigerant drum, even if liquid refrigerant having a temperature lower than the temperature in the refrigerant drum is replenished from the refrigerant replenishing portion, the liquid refrigerant Between the gas phase portion and the liquid phase portion in the refrigerant drum, and the liquid refrigerant is stored in the liquid phase portion in the refrigerant drum at the same temperature as the vapor. There is no temperature difference between the two.
- the refrigerant replenishment part may be formed with a spraying part for spraying the liquid refrigerant to the gas phase part.
- the spraying part for spraying the liquid refrigerant to the gas phase part is formed in the refrigerant supply part, the surface area of the liquid refrigerant supplied from the refrigerant supply part is increased, so that the inside of the refrigerant drum Heat transfer between the steam and the liquid refrigerant can be performed more smoothly.
- the refrigerant replenishing portion may be formed in a tubular shape, and the spraying portion may include a through hole formed in the refrigerant replenishing portion.
- the pressure control unit controls the pressure in the refrigerant drum based on the deviation of the actual temperature in the reactor from the temperature set value, whereby the liquid supplied to the heat removal unit.
- the amount of heat recovered by the heat removal unit can be adjusted by changing the temperature of the refrigerant. Therefore, when the actual temperature in the reactor is higher than the temperature set value, the amount of heat recovered by the heat removal unit is increased, and when the actual temperature is lower than the temperature set value.
- the pressure controller directly controls the temperature of the liquid refrigerant supplied from the refrigerant drum to the heat removal unit by controlling the pressure of the refrigerant drum corresponding to the temperature of the liquid refrigerant supplied to the heat removal unit. Can be controlled. Therefore, by supplying the liquid refrigerant whose temperature is controlled outside the refrigerant drum to the refrigerant drum, the temperature control in the reactor can be performed more quickly than the method of controlling the temperature of the liquid refrigerant in the refrigerant drum. . As a result, it is possible to reliably prevent the exothermic reaction from running away and the temperature in the reactor from rising rapidly.
- the exothermic reaction is a Fischer-Tropsch synthesis reaction in which the temperature range in which the reaction is properly performed is very narrow, the above-described effects are remarkably achieved.
- the refrigerant replenishment unit is disposed in the gas phase part of the refrigerant drum, heat is efficiently generated between the liquid refrigerant and the vapor in the refrigerant drum in the gas phase part. Therefore, even if the liquid refrigerant replenished from the refrigerant replenishing part is not preheated outside the system, the temperature difference between the gas phase part and the liquid phase part does not occur in the refrigerant drum, and the pressure in the refrigerant drum The temperature can be kept in the correlation of the vapor-liquid equilibrium state.
- the heat transfer between the vapor in the refrigerant drum and the liquid refrigerant can be performed more smoothly, so that the pressure and temperature in the refrigerant drum are brought into a gas-liquid equilibrium state. It is possible to reliably maintain the correlation.
- the spraying portion since the spraying portion includes the through-hole formed in the coolant supply portion, the liquid coolant can be sprayed reliably.
- the temperature control system 20 uses a Fischer-Tropsch synthesis reaction (exothermic reaction) for water (liquid refrigerant) stored in the refrigerant drum 1 in a gas-liquid equilibrium state by a pump 4 from the bottom of the refrigerant drum 1.
- the reaction heat is sent to a heat removal pipe (heat removal section) 7 in the reactor 5 where the reaction is performed, and water is partially evaporated in the heat removal pipe 7 by the reaction heat accompanying the exothermic reaction generated in the reactor 5. to recover.
- the vapor in which a part of the water has evaporated in the heat removal pipe 7 and the mixed phase fluid of water are returned to the refrigerant drum 1 through the return pipe 12 to the refrigerant drum 1, and the vapor passes through the vapor outlet pipe 11 to the system. Supplied to outside steam users.
- a steam trap (not shown) may be provided on the downstream side of the steam outlet pipe 11.
- an amount of make-up water (liquid refrigerant) corresponding to the vapor supplied outside the system is supplied through the make-up water pipe 10.
- the replenishing water replenishment amount is adjusted by the level control valve 2 based on the measurement result of the level measuring unit 17 that measures the water level (liquid level) in the refrigerant drum 1.
- the pressure control unit 18 for controlling the pressure in the reactor 5 based on the measurement result of the temperature measuring unit 6 that measures the temperature in the reactor 5 that performs an exothermic reaction is provided with the steam outlet pipe 11.
- the temperature of the reactor 5 that performs the exothermic reaction is controlled by adjusting the amount of steam supplied from outside to the system by cascade control.
- the temperature measurement unit 6 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 the average value of each temperature measured by these temperature sensors is calculated. The temperature in the reactor 5 can be measured.
- this control will be described in detail.
- the vapor phase (gas phase portion) and the water phase (liquid phase portion) in the refrigerant drum 1 are in a gas-liquid equilibrium state, the vapor phase pressure of the refrigerant drum 1 and the temperature of the water phase of the refrigerant drum 1 are constant. There is a correlation. Therefore, when there is a deviation in the actual temperature in the reactor 5 measured by the temperature measuring unit 6 with respect to the temperature set value of the reactor 5 that performs an exothermic reaction, the pressure control unit 18 is operated and the vapor of the refrigerant drum 1 is activated. Change the phase pressure.
- the pressure control unit 18 controls the steam outlet pipe 11 by controlling the steam outlet pipe 11, the pressure control valve 3 provided in the steam outlet pipe 11, and the pressure control valve 3. And a pressure setting unit 9 for setting the pressure in the refrigerant drum 1.
- the measurement result of the temperature measurement unit 6 is sent to the pressure setting unit 9, and the pressure setting unit 9 calculates the deviation of the actual temperature in the reactor 5 from the temperature set value from the measurement result, and this deviation Based on the above, the pressure control valve 3 is controlled to change the vapor phase pressure of the refrigerant drum 1.
- the temperature of the water phase in the refrigerant drum 1 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 refrigerant drum 1 is the temperature provided at the end of the refrigerant drum 1 side in the pipe 13 for supplying water from the refrigerant drum 1 to the heat removal pipe 7 by the pump 4.
- a total of 8 can be measured.
- the refrigerant drum 1, the pipe 13, the heat removal pipe 7, and the return pipe 12 constitute a system in which water as a liquid refrigerant circulates.
- a supply water supply inner pipe (refrigerant supply section) 14 connected to the supply water pipe 10 extends along the longitudinal direction of the refrigerant drum 1 in the refrigerant drum 1.
- the makeup water supply inner pipe 14 is installed in the vapor phase.
- One or more holes (through holes) 15 are provided in the side surface 14a of the makeup water supply inner pipe 14 along the pipe axis direction, and one or more holes 15 are also provided in the pipe end 14b.
- These holes 15 constitute a sprinkling section (spreading section) 19 that sprinkles (spreads) makeup water from the makeup water supply inner pipe 14 into the steam phase.
- the hole 15 may be a watering nozzle.
- a return internal pipe 12a connected to the return pipe 12 is also provided.
- a vapor and water mixed phase fluid partially evaporated in the heat removal pipe 7 is supplied into the refrigerant drum 1 from the return internal pipe 12a.
- the return internal pipe 12 a is located above the make-up water supply inner pipe 14 and is disposed at a position avoiding the vertical upper side of the make-up water supply inner pipe 14.
- the return internal pipe 12 a is curved toward the make-up water supply inner pipe 14, whereby the steam that has flowed through the return internal pipe 12 a is supplied toward the make-up water supply inner pipe 14. It becomes.
- the temperature difference between the vapor phase and the water phase is eliminated, and the vapor phase pressure of the refrigerant drum 1 and the temperature of the water phase in the refrigerant drum 1 always maintain a correlation based on the gas-liquid equilibrium state.
- the control by the temperature control system 20 is performed with high accuracy.
- the Fischer-Tropsch synthesis reaction is performed in the reactor 5, but the Fischer-Tropsch synthesis reaction may not be performed as long as an exothermic reaction is performed in the reactor 5.
- the post-reaction fluid (reaction product) is derived
- the position which guides the post-reaction fluid from the reactor 5 is changed suitably.
- the post-reaction fluid may be derived from the body (side surface) or the bottom of the reactor 5, or may be derived from a plurality of locations of the top, body, and bottom of the reactor 5.
- the position where the post-reaction fluid is derived may be changed according to the type of exothermic reaction in the reactor 5, for example.
- the vapor and water mixed phase fluid partially evaporated in the heat removal pipe 7 is returned to the refrigerant drum 1 through the return pipe 12, but the mixed phase fluid is returned to the refrigerant drum 1. It does not have to be.
- reaction heat is recovered by partially evaporating the water that has passed through the heat removal tube, and that it can be used in general refrigerant drums attached to the reactor or a system that controls the reaction temperature itself.
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Physics & Mathematics (AREA)
- General Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Control Of Temperature (AREA)
Abstract
Description
本願は、2011年1月31日に日本に出願された特願2011-18263号について優先権を主張し、その内容をここに援用する。
このFT合成反応において、発熱反応を行なう反応器は、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。
さらに、反応器において温度制御が正しく行われない結果、反応器内の温度がFT合成反応の適正な温度域から高温側に外れた場合には、FT合成反応が暴走を起こして急激な温度上昇を引き起こすため、触媒の劣化、損傷のみならず、反応器の強度上の問題も発生するといった課題がある。
すなわち、この温度制御システムでは、まず、反応器内の実温度が温度設定値に対して有する偏差に基づいて、圧力制御部が冷媒ドラム内の圧力を制御する。すると、冷媒ドラム内の気液平衡状態の相関関係に応じて冷媒ドラム内の液体冷媒の温度が変化する。この液体冷媒は除熱部に供給されるため、液体冷媒の温度変化に応じて除熱部にて回収される熱量が変化する。そして、このように回収される熱量を変化させることで、反応器内の温度を制御することができる。
また、圧力制御部が、除熱部に供給する液体冷媒の温度と1対1に対応する冷媒ドラムの圧力を制御することで、冷媒ドラムから除熱部に供給される液体冷媒の温度を直接制御することができる。したがって、冷媒ドラムの外で温度を制御した液体冷媒を冷媒ドラムへ供給することで、冷媒ドラム内の液体冷媒の温度を制御する方法よりも、反応器内の温度制御を迅速に行うことができる。これにより、発熱反応が暴走して反応器内が急激に温度上昇するのを確実に抑制することができる。
なお前述のように、外部で温度を制御した液体冷媒を冷媒ドラムへ供給することで、冷媒ドラム内の液体冷媒の温度を制御する方法では、外部から供給された液体冷媒と、冷媒ドラム内の液体冷媒と、の温度が均一になりにくく、反応器の温度制御が高精度になされないおそれがある。
図1に示すように、温度制御システム20は、冷媒ドラム1に気液平衡状態で貯えられた水(液体冷媒)を冷媒ドラム1の底部よりポンプ4にてフィッシャー・トロプシュ合成反応(発熱反応)を行なう反応器5内の除熱管(除熱部)7に送り、反応器5にて発生した発熱反応に伴う反応熱により除熱管7内で水を一部蒸発させることで、この反応熱を回収する。
以下、本制御について詳しく説明する。
したがって、発熱反応を行なう反応器5の温度設定値に対し、温度測定部6により測定された反応器5内の実温度に偏差が生じた場合、圧力制御部18を作動させ冷媒ドラム1の蒸気相圧力を変更する。
次に、前記温度制御システム20の冷媒ドラム1について詳しく説明する。
図2および図3に示すように、この冷媒ドラム1内には、前記補給水配管10に接続された補給水供給内管(冷媒補給部)14が冷媒ドラム1の長手方向に沿って延設されている。補給水供給内管14は、蒸気相中に設置されている。
この補給水供給内管14の側面14aには管軸方向に沿って孔(貫通孔)15が1個以上設けられ、同じく管端14bにも孔15が1個以上設けられている。そして、これらの孔15は、補給水を補給水供給内管14から蒸気相中に散水(散布)する散水部(散布部)19を構成している。なお孔15は、散水ノズルであってもよい。
補給水供給内管14から没水しない位置で補給水を供給することで、低温の補給水と蒸気相の蒸気とで熱交換がされ、補給水が低温のまま冷媒ドラム1の底部に流れる状況が回避できる。さらに、補給水供給内管14の側面14aおよび管端14bの孔15から補給水を散水させることにより、補給水と蒸気との接触面積を増やして熱交換の効率を向上させ、低温の補給水と蒸気の温度との熱交換の効率を高めることができる。これにより、蒸気相と水相との間の温度差がなくなり、冷媒ドラム1の蒸気相圧力と冷媒ドラム1内の水相の温度とは、気液平衡状態に基づいた相関関係が常に保たれることとなり、前述の温度制御システム20による制御が高精度に行われる。
例えば、前記実施形態では、反応器5内でフィッシャー・トロプシュ合成反応がなされているものとしたが、反応器5内で発熱反応がなされていれば、フィッシャー・トロプシュ合成反応でなくてもよい。
さらに前記実施形態では、除熱管7にて一部蒸発した蒸気および水の混相流体が、戻り配管12を通って冷媒ドラム1に戻されるものとしたが、該混相流体は冷媒ドラム1に戻されなくてもよい。
2 レベル調節弁
3 圧力調節弁
4 ポンプ
5 反応器
6 温度測定部
7 除熱管
8 温度計
9 圧力設定部
10 補給水配管
11 蒸気出口配管
12 戻り配管
12a 戻り内部配管
13 配管
14 補給水供給内管
14a 側面
14b 管端
15 孔
16 側面開孔
17 レベル測定部
18 圧力制御部
20 温度制御システム
Claims (5)
- 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、
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、前記冷媒ドラムから供給された前記液体冷媒が内部を流通する除熱部と、
前記反応器内の温度を測定する温度測定部と、
前記冷媒ドラム内の圧力を制御する圧力制御部とを備え、
該圧力制御部は、前記温度測定部により測定された前記反応器内の実温度が、前記反応器内の温度設定値に対して有する偏差に基づいて前記冷媒ドラム内の圧力を制御することで、前記冷媒ドラム内の前記液体冷媒の温度を制御する温度制御システム。 - 請求項1記載の温度制御システムであって、
前記発熱反応は、フィッシャー・トロプシュ合成反応である温度制御システム。 - 請求項1または2に記載の温度制御システムであって、
前記冷媒ドラム内には、該冷媒ドラム内に前記液体冷媒を補給する冷媒補給部が設けられ、
該冷媒補給部は、前記冷媒ドラムの気相部内に配設されている温度制御システム。 - 請求項3記載の温度制御システムであって、
前記冷媒補給部には、前記液体冷媒を前記気相部に散布する散布部が形成されている温度制御システム。 - 請求項4記載の温度制御システムであって、
前記冷媒補給部は管状に形成され、
前記散布部は、前記冷媒補給部に形成された貫通孔を含む温度制御システム。
Priority Applications (8)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA2825147A CA2825147C (en) | 2011-01-31 | 2012-01-17 | Temperature control system |
CN201280006679.4A CN103338854B (zh) | 2011-01-31 | 2012-01-17 | 温度控制系统 |
EA201391020A EA026314B1 (ru) | 2011-01-31 | 2012-01-17 | Система управления температурой |
BR112013018529A BR112013018529A2 (pt) | 2011-01-31 | 2012-01-17 | sistema de controle de temperatura |
AU2012212845A AU2012212845B2 (en) | 2011-01-31 | 2012-01-17 | Temperature control system |
US13/982,060 US20130306299A1 (en) | 2011-01-31 | 2012-01-17 | Temperature control system |
EP12742759.9A EP2671635A4 (en) | 2011-01-31 | 2012-01-17 | TEMPERATURE CONTROL SYSTEM |
ZA2013/05535A ZA201305535B (en) | 2011-01-31 | 2013-07-22 | Temperature control system |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2011-018263 | 2011-01-31 | ||
JP2011018263A JP5802397B2 (ja) | 2011-01-31 | 2011-01-31 | 温度制御システム |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2012105311A1 true WO2012105311A1 (ja) | 2012-08-09 |
Family
ID=46602531
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2012/050853 WO2012105311A1 (ja) | 2011-01-31 | 2012-01-17 | 温度制御システム |
Country Status (11)
Country | Link |
---|---|
US (1) | US20130306299A1 (ja) |
EP (1) | EP2671635A4 (ja) |
JP (1) | JP5802397B2 (ja) |
CN (1) | CN103338854B (ja) |
AU (1) | AU2012212845B2 (ja) |
BR (1) | BR112013018529A2 (ja) |
CA (1) | CA2825147C (ja) |
EA (1) | EA026314B1 (ja) |
MY (1) | MY164095A (ja) |
WO (1) | WO2012105311A1 (ja) |
ZA (1) | ZA201305535B (ja) |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP5815324B2 (ja) * | 2011-08-05 | 2015-11-17 | 独立行政法人石油天然ガス・金属鉱物資源機構 | 温度制御システム |
ES2762875T3 (es) * | 2014-04-25 | 2020-05-26 | Franke Technology & Trademark | Intercambiador de calor |
GB2550677B (en) * | 2014-10-20 | 2018-07-25 | Velocys Tech Limited | Process of removing heat |
CN105806091B (zh) * | 2014-12-31 | 2018-03-06 | 国家电网公司 | 燃气热电厂开式冷却水系统及其启停控制方法 |
KR102132581B1 (ko) * | 2018-03-06 | 2020-08-05 | 한국가스공사 | 개질기 반응관 내부 온도 추정 방법 |
CN111774021A (zh) * | 2019-04-04 | 2020-10-16 | 应急管理部化学品登记中心 | 反应釜及其用途 |
CN110274512B (zh) * | 2019-07-15 | 2024-05-03 | 北京凯瑞英科技有限公司 | 一种精确控制热反应温度的反应器系统和工艺 |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH03127625A (ja) * | 1989-10-13 | 1991-05-30 | Tlv Co Ltd | 蒸気加熱及び気化冷却装置 |
JPH06257703A (ja) * | 1993-03-05 | 1994-09-16 | Toshiba Corp | 排熱回収ボイラ |
JPH07305934A (ja) * | 1994-05-14 | 1995-11-21 | Tlv Co Ltd | 減圧気化冷却装置 |
JPH08200915A (ja) * | 1995-01-30 | 1996-08-09 | Ikegami Kanagata Kogyo Kk | 冷却装置 |
JPH10182103A (ja) * | 1996-12-20 | 1998-07-07 | Toyota Motor Corp | 一酸化炭素選択酸化装置及び燃料改質装置並びに燃料電池システム |
JP2008537507A (ja) | 2005-03-17 | 2008-09-18 | サソール テクノロジー(プロプライエタリー)リミテッド | 気体反応物からの液体生成物および任意に気体生成物の生成 |
Family Cites Families (18)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5869011A (en) * | 1994-02-01 | 1999-02-09 | Lee; Jing Ming | Fixed-bed catalytic reactor |
DE4435839A1 (de) * | 1994-10-07 | 1996-04-11 | Bayer Ag | Schlammphasenreaktor und dessen Verwendung |
US5561987A (en) * | 1995-05-25 | 1996-10-08 | American Standard Inc. | Falling film evaporator with vapor-liquid separator |
FR2768740B1 (fr) * | 1997-09-19 | 2001-07-06 | Bp Chem Int Ltd | Procede de polymerisation continue d'un monomere vinylique |
US6306917B1 (en) * | 1998-12-16 | 2001-10-23 | Rentech, Inc. | Processes for the production of hydrocarbons, power and carbon dioxide from carbon-containing materials |
US6516627B2 (en) * | 2001-05-04 | 2003-02-11 | American Standard International Inc. | Flowing pool shell and tube evaporator |
US7108835B2 (en) * | 2003-10-08 | 2006-09-19 | Rentech, Inc. | Fischer-tropsch slurry reactor cooling tube arrangement |
KR100903685B1 (ko) * | 2004-10-13 | 2009-06-18 | 요크 인터내셔널 코포레이션 | 유하액막(遊下液漠) 증발기 |
US20070131583A1 (en) * | 2005-12-13 | 2007-06-14 | Syntroleum Corporation | Fischer-Tropsch product condensing process for cold climates |
TWI320094B (en) * | 2006-12-21 | 2010-02-01 | Spray type heat exchang device | |
CN101918514A (zh) * | 2007-09-27 | 2010-12-15 | 新日铁工程技术株式会社 | 气泡塔型碳氢化合物合成反应器及具备其的碳氢化合物合成反应系统 |
WO2009089446A2 (en) * | 2008-01-11 | 2009-07-16 | Johnson Controls Technology Company | Vapor compression system |
CA2738043C (en) * | 2008-09-30 | 2014-08-05 | Japan Oil, Gas And Metals National Corporation | Catalyst separation system |
JP5364715B2 (ja) * | 2008-09-30 | 2013-12-11 | 独立行政法人石油天然ガス・金属鉱物資源機構 | 炭化水素化合物合成反応ユニット及びその運転方法 |
EP2351815A4 (en) * | 2008-09-30 | 2012-03-14 | Japan Oil Gas & Metals Jogmec | HYDROCARBON SYNTHESIS REACTOR, HYDROCARBON SYNTHESIS REACTION SYSTEM, AND HYDROCARBON SYNTHESIS METHOD |
CN101575044A (zh) * | 2009-06-11 | 2009-11-11 | 上海宝钢工程技术有限公司 | 轧机乳化液原油温度控制方法及控制装置 |
CN201672834U (zh) * | 2010-03-24 | 2010-12-15 | 浙江西子联合工程有限公司 | 温控变压式蓄热器控制系统 |
JP5815324B2 (ja) * | 2011-08-05 | 2015-11-17 | 独立行政法人石油天然ガス・金属鉱物資源機構 | 温度制御システム |
-
2011
- 2011-01-31 JP JP2011018263A patent/JP5802397B2/ja not_active Expired - Fee Related
-
2012
- 2012-01-17 EA EA201391020A patent/EA026314B1/ru not_active IP Right Cessation
- 2012-01-17 US US13/982,060 patent/US20130306299A1/en not_active Abandoned
- 2012-01-17 WO PCT/JP2012/050853 patent/WO2012105311A1/ja active Application Filing
- 2012-01-17 MY MYPI2013701276A patent/MY164095A/en unknown
- 2012-01-17 CA CA2825147A patent/CA2825147C/en not_active Expired - Fee Related
- 2012-01-17 AU AU2012212845A patent/AU2012212845B2/en not_active Ceased
- 2012-01-17 BR BR112013018529A patent/BR112013018529A2/pt not_active IP Right Cessation
- 2012-01-17 EP EP12742759.9A patent/EP2671635A4/en not_active Withdrawn
- 2012-01-17 CN CN201280006679.4A patent/CN103338854B/zh not_active Expired - Fee Related
-
2013
- 2013-07-22 ZA ZA2013/05535A patent/ZA201305535B/en unknown
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH03127625A (ja) * | 1989-10-13 | 1991-05-30 | Tlv Co Ltd | 蒸気加熱及び気化冷却装置 |
JPH06257703A (ja) * | 1993-03-05 | 1994-09-16 | Toshiba Corp | 排熱回収ボイラ |
JPH07305934A (ja) * | 1994-05-14 | 1995-11-21 | Tlv Co Ltd | 減圧気化冷却装置 |
JPH08200915A (ja) * | 1995-01-30 | 1996-08-09 | Ikegami Kanagata Kogyo Kk | 冷却装置 |
JPH10182103A (ja) * | 1996-12-20 | 1998-07-07 | Toyota Motor Corp | 一酸化炭素選択酸化装置及び燃料改質装置並びに燃料電池システム |
JP2008537507A (ja) | 2005-03-17 | 2008-09-18 | サソール テクノロジー(プロプライエタリー)リミテッド | 気体反応物からの液体生成物および任意に気体生成物の生成 |
Non-Patent Citations (1)
Title |
---|
See also references of EP2671635A4 |
Also Published As
Publication number | Publication date |
---|---|
CN103338854B (zh) | 2016-01-20 |
AU2012212845B2 (en) | 2015-05-21 |
BR112013018529A2 (pt) | 2016-10-18 |
EP2671635A4 (en) | 2015-01-07 |
CA2825147A1 (en) | 2012-08-09 |
EA026314B1 (ru) | 2017-03-31 |
EA201391020A1 (ru) | 2013-12-30 |
MY164095A (en) | 2017-11-30 |
CA2825147C (en) | 2015-11-03 |
JP5802397B2 (ja) | 2015-10-28 |
JP2012158663A (ja) | 2012-08-23 |
US20130306299A1 (en) | 2013-11-21 |
ZA201305535B (en) | 2014-10-29 |
CN103338854A (zh) | 2013-10-02 |
EP2671635A1 (en) | 2013-12-11 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2012105311A1 (ja) | 温度制御システム | |
JP5793325B2 (ja) | 温度制御システム、炭化水素合成反応装置、炭化水素合成反応システム | |
CN101809122B (zh) | 合成反应系统 | |
AU2012293758B2 (en) | Temperature control system | |
JP2007501373A (ja) | 高温ガスの冷却装置及び方法 | |
JP6891868B2 (ja) | メタン製造装置、および、メタン製造方法 | |
TWI762498B (zh) | 製造經氯化之烴之方法 | |
JP2016534318A (ja) | 熱回収装置 | |
KR100986750B1 (ko) | Ft 슬러리 기포탑 반응기의 반응열 제거용 순환형 냉각장치 | |
RU2008129728A (ru) | Способ управления температурой экзотермических химических реакций | |
JP2002309276A (ja) | 液・液直接接触式lng気化装置 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 12742759 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 2825147 Country of ref document: CA |
|
REEP | Request for entry into the european phase |
Ref document number: 2012742759 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2012742759 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 13982060 Country of ref document: US |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
WWE | Wipo information: entry into national phase |
Ref document number: 1301004156 Country of ref document: TH |
|
WWE | Wipo information: entry into national phase |
Ref document number: 201391020 Country of ref document: EA |
|
ENP | Entry into the national phase |
Ref document number: 2012212845 Country of ref document: AU Date of ref document: 20120117 Kind code of ref document: A |
|
REG | Reference to national code |
Ref country code: BR Ref legal event code: B01A Ref document number: 112013018529 Country of ref document: BR |
|
ENP | Entry into the national phase |
Ref document number: 112013018529 Country of ref document: BR Kind code of ref document: A2 Effective date: 20130719 |