WO1995021692A1 - Reacteur a lit fluidifie et procede de gestion de la temperature pour reacteur a lit fluidifie - Google Patents
Reacteur a lit fluidifie et procede de gestion de la temperature pour reacteur a lit fluidifie Download PDFInfo
- Publication number
- WO1995021692A1 WO1995021692A1 PCT/JP1995/000163 JP9500163W WO9521692A1 WO 1995021692 A1 WO1995021692 A1 WO 1995021692A1 JP 9500163 W JP9500163 W JP 9500163W WO 9521692 A1 WO9521692 A1 WO 9521692A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- refrigerant
- fluidized bed
- heat removal
- bed reactor
- temperature
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims description 25
- 239000002826 coolant Substances 0.000 claims abstract description 8
- 238000000605 extraction Methods 0.000 claims abstract description 4
- 239000003507 refrigerant Substances 0.000 claims description 119
- 238000006243 chemical reaction Methods 0.000 claims description 30
- 239000002245 particle Substances 0.000 claims description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- 239000003054 catalyst Substances 0.000 claims description 17
- 238000001514 detection method Methods 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 4
- 239000000843 powder Substances 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims description 2
- 239000010419 fine particle Substances 0.000 claims 1
- 239000007789 gas Substances 0.000 description 9
- 150000002430 hydrocarbons Chemical class 0.000 description 6
- 229930195733 hydrocarbon Natural products 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 4
- 229920006395 saturated elastomer Polymers 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical group CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- 239000001273 butane Substances 0.000 description 2
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- LGRFSURHDFAFJT-UHFFFAOYSA-N Phthalic anhydride Natural products C1=CC=C2C(=O)OC(=O)C2=C1 LGRFSURHDFAFJT-UHFFFAOYSA-N 0.000 description 1
- 230000004931 aggregating effect Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 1
- JHIWVOJDXOSYLW-UHFFFAOYSA-N butyl 2,2-difluorocyclopropane-1-carboxylate Chemical compound CCCCOC(=O)C1CC1(F)F JHIWVOJDXOSYLW-UHFFFAOYSA-N 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Classifications
-
- 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
- B01J8/1809—Controlling processes
-
- 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
- B01J8/1836—Heating and cooling 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
- 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
-
- 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
- B01J2208/00141—Coils
-
- 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
- B01J2219/18—Details relating to the spatial orientation of the reactor
- B01J2219/185—Details relating to the spatial orientation of the reactor vertical
Definitions
- the present invention relates to a fluidized bed reactor suitable for performing a gas phase exothermic reaction and easy to control the reaction temperature, and to a temperature control method for the fluidized bed reactor. More specifically, the present invention relates to a fluidized-bed reactor and a method for controlling the reaction temperature of a fluidized-bed reactor when a gas-phase exothermic reaction, for example, an oxidation reaction of a hydrocarbon compound is performed in a large-scale fluidized-bed reactor on an industrial scale.
- a gas-phase exothermic reaction for example, an oxidation reaction of a hydrocarbon compound is performed in a large-scale fluidized-bed reactor on an industrial scale.
- the reaction temperature of an industrial-scale fluidized bed reactor is controlled by installing a heat removal pipe in the fluidized bed and circulating water to recover the reaction heat as steam.
- a heat removal pipe in the fluidized bed and circulating water to recover the reaction heat as steam.
- attempts have been made to arrange heat removal tubes separately in the upper and lower portions of the fluidized bed to separately control the temperatures in the upper and lower portions of the fluidized bed (US Pat. No. 3,080,382). See).
- the method of finely controlling the temperature of the fluidized bed by adjusting the temperature of the reaction material supplied to the reactor, and the amount of heat generated by adjusting the supply speed of the reaction material It is also known to finely control the temperature of the fluidized bed by increasing or decreasing the temperature.
- catalysts used in fluidized bed reactors generally have a large effect on the reaction results and catalyst life depending on the conditions of use. It is also necessary to keep the fluidized bed in good condition. It is known that the flow condition is greatly affected by the gas flow rate and the catalyst particle size. You. Therefore, it is preferable to maintain the composition and supply rate of the reaction raw materials as constant as possible.
- the temperature of the fluidized bed will inevitably change.
- the reaction temperature was excessively increased, and the catalyst was degraded, and in severe cases, it could even hinder safe operation.
- the fluidized state of the fluidized bed was kept good, and the temperature, moisture.
- the temperature distribution inside the fluidized bed is reduced by keeping the factors that may influence the temperature of the fluidized bed such as the composition and the feed rate as constant as possible, the temperature of the fluidized bed will still change. Inevitable. Therefore, in order for the catalyst to achieve its best reaction reading, it is essential to actively control the temperature of the fluidized bed and maintain it at the optimum temperature.
- An object of the present invention is to provide a fluidized bed reactor capable of quickly responding to such a small temperature change in a fluidized bed and a method for rapidly and accurately controlling the reaction temperature of the fluidized bed reactor. It is. Disclosure of the invention
- the first aspect of the present invention is a fluidized bed reactor, in which a fluidized bed forming section is provided with a plurality of heat removing tubes and at least one temperature detecting section, and the heat removing tubes are the same as a refrigerant supply pipe outside the reactor. At least one heat removal pipe is connected to the extraction pipe, and at least one heat removal pipe is supplied with refrigerant at a constant speed, and at least one other heat removal pipe is composed of a heat removal pipe supplied with refrigerant at a variable speed. Maintain the temperature of the fluidized bed at the optimum temperature.
- a second aspect of the present invention is to provide a fluidized bed reactor in which a plurality of heat removal tubes are installed in a fluidized bed in performing a gas phase exothermic reaction in a fluidized bed reactor.
- a fluidized bed characterized in that a refrigerant is supplied to at least one heat removal tube at a steady speed using a heat exchanger, and the heat is removed by supplying a refrigerant at a variable speed to at least one other heat removal tube.
- An object of the present invention is to provide a temperature control method for quickly and accurately controlling the reaction temperature of a reactor.
- FIG. 1 is a conceptual diagram of one example of a fluidized bed reactor for carrying out the present invention.
- FIG. 2 is a diagram showing the transition of the reaction temperature in the example.
- FIG. 3 is a diagram showing the transition of the supply speed of n-butane in the example.
- the catalyst used in the fluidized bed reactor of the present invention is a conventional fluidized bed reactor.
- the catalyst used in the reactor can be used as it is, but its weight average particle size is 30 to 100 ⁇ m, preferably 40 to 80 ⁇ m, and the particle size is 4 Group A (G e 1 dert, D) of the Ge 1 dert particle classification map containing 20 to 70% by weight of fine powder having a particle size of 4 m or less and having a particle density of 300 kg / m 3 or less , Powder Technology, 7, 285 (see 197 3)).
- the fluidized-bed reactor of the present invention is capable of producing a maleic anhydride by an oxidation reaction of butane, butene, butadiene, and benzene, and a phthalic anhydride by an oxidation reaction of ortho-xylene and naphthalene.
- Large-scale fluidized bed reactor for industrial scale production oxidation reaction such as production of propylene, isopylene, and ammonium, and oxidation reaction of ethylene, etc.
- the fluidized state of the catalyst in the fluidized bed is effective for aggregating fluidization of Bubbling R egime, Slug low R egime, furbulent R egime, etc. This is a fluidized bed reactor called Conventional Fluidized Bed.
- the catalyst particles are preferably kept in a fluidized state by gas introduced from the lower part of the reactor.
- the gas velocity is usually maintained at 35 to 80 cm / sec based on the effective area of the reactor.
- the temperature detector is for detecting the temperature of the fluidized bed, and it may be installed alone, but it is usually preferable to install a plurality of temperature detectors so that the temperature of the entire fluidized bed can be correctly grasped.
- the heat removal tubes are for removing heat from the fluidized bed and need to be installed in multiple rows.
- the heat removal pipe is connected to a refrigerant supply pipe and a refrigerant discharge pipe outside the reactor, and the refrigerant flows from the refrigerant supply pipe to the refrigerant discharge pipe via the heat removal pipe.
- the supply rate of the refrigerant to the steady-state heat removal tube to which the refrigerant is supplied at the steady speed is calculated based on the total heat removal amount to be removed by all the heat removal tubes and the ratio of the heat removal by the steady-state heat removal tube. be able to.
- the total heat removal is mainly determined by the heat generation determined by the composition and supply rate of the reactants supplied to the reactor, and the set reaction temperature, and in some cases, the temperature of the reactants and the outer wall of the reactor It is slightly affected by the amount of heat released from the air. Therefore, as long as these conditions do not change, the supply rate of the refrigerant to the steady-state heat removal tube is kept constant.
- the fluidized bed reactor of the present invention is not particularly limited in its heat removal quantity, remove heat total heat in all the heat removal tubes 1 0, 0 0 0 ⁇ 2 0 0, 0 0 0 kca 1 / m 2 ⁇ hr Is appropriate.
- it is usually designed to remove most of the heat to be removed by the regular heat removal tube, preferably 50% or more of the total heat removal, especially 80% or more, and the rest is removed. It is preferable to remove the heat with an adjusting heat removal tube to which the refrigerant is supplied at a variable speed.
- a liquid that can remove heat by utilizing the latent heat of vaporization of water or other refrigerant is usually used.
- Ri can Do overall heat transfer coefficient of the constant for the heat removal tubes rather large by using such refrigerant, properly preferred c which can increase the quantity of heat removed per unit surface area of the heat removal tubes used in the water and refrigerant, and the At least a part should be converted to steam in the pipe.
- the temperature of the supplied ice is appropriately selected depending on the reaction conditions and the like. Since the pressure of the steam at the outlet is determined, it is preferable that the saturation temperature at the arbitrary pressure is within a range of ⁇ 5 O, and preferably a saturation temperature of ⁇ 1 O.
- the pressure of the water vapor constant for heat removal tube exit usually SSO kg Z m 2 it can. Therefore, as a refrigerant, heated ice in the range of 50 to 50% of saturated temperature soil at the pressure is supplied, and 3 to 15%, preferably 5 to 10% of the heated ice is supplied. Evaporate in the tube and recover from the outlet as a high-pressure gas-liquid multiphase flow.
- the stationary heat removal pipe is not only an evaporating pipe that supplies water as a refrigerant to generate steam, but also a superheated pipe that supplies ice steam as a refrigerant to generate superheated steam. It is preferred to be composed of two types, a pipe and a tube. In this way, the heat of reaction of the fluidized bed reactor can be recovered from the superheater as dry steam that is convenient for use. Even in this case, it is advantageous to remove 50% or more, preferably 80% or more of the total heat removal by a heat removal pipe that supplies water to generate steam.
- the supply rate of the refrigerant to the supplied adjusting heat removal tube is adjusted so as to maintain the temperature in the reactor at a predetermined value. That is, according to the difference between the temperature detected by the temperature detector provided in the fluidized bed and the set temperature of the reactor, the supply speed of the refrigerant is determined so as to reduce the difference.
- heat removal tubes for adjustment and temperature detectors are installed at the upper and lower parts of the fluidized bed, respectively, and the upper and lower parts of the fluidized bed are independently temperature controlled. It is preferable to be able to make adjustments.
- the heat removal amount and the refrigerant flow rate are almost proportional.
- it is preferable that the phase change of the refrigerant is not caused and the sensible heat of the refrigerant is used. The reason is as follows.
- the heat removal amount Q in the heat removal tube is determined by the product of the heat transfer area A of the tube, the overall heat transfer coefficient U, and the logarithmic average temperature difference ⁇ . (Formula (1) below)
- the overall heat transfer coefficient U is the external heat transfer coefficient h. It is a function of the pipe heat transfer coefficient h i, the pipe thickness d, the pipe thermal conductivity; I and the pipe fouling coefficient r. (Formula (2) below)
- Outer tube heat transfer coefficient h Is usually about 100,000 kcal Zm 2 , ⁇ , hr, and can be regarded as constant while controlling the temperature of the reactor. Similarly, d, s, and r can also be considered constant, so that the overall heat transfer coefficient U changes in accordance with the change in the pipe heat transfer coefficient hi.
- the heat transfer coefficient hi in the pipe is determined by the flow state of the refrigerant in the pipe, and is about 100 to 100 kca 1 / m 2 , hr when there is no phase change of the refrigerant. In some cases, it is usually more than 1000 kca 1 / m 2 , V, hr.
- the heat transfer coefficient hi in the pipe is the heat transfer coefficient h outside the pipe.
- the overall heat transfer coefficient U does not change much, so that it is difficult to control the heat removal amount by adjusting the flow rate of the refrigerant.
- water used as the refrigerant
- the refrigerant in the adjusting heat removal tube may be a substance that does not cause a phase change in the heat removal tube, usually a gas, and preferably water vapor.
- saturated steam at a pressure of 3 to 50 k / m 2 is supplied to generate superheated steam.
- the supply rate of the refrigerant to the adjusting heat removal pipe is adjusted by adjusting the discharge rate of the refrigerant supply device, providing a refrigerant flow control valve in the refrigerant supply pipe, or controlling the flow rate of the refrigerant in the refrigerant discharge pipe. It can be performed by a method such as providing a control valve.
- the refrigerant flows directly from the refrigerant supply pipe to the refrigerant discharge pipe without passing through the heat removal pipe between the refrigerant supply pipe and the refrigerant discharge pipe connected to the heat removal pipe for adjustment.
- a bypass pipe is provided so that the refrigerant can flow, and a refrigerant control valve for controlling the flow rate of the refrigerant flowing through the bypass pipe is provided.
- the refrigerant is supplied at a constant speed to the refrigerant supply pipe connected to the heat removal pipe for adjustment, and the required amount of the refrigerant is flowed into the heat removal pipe for adjustment by the refrigerant control valve, and the remainder flows into the refrigerant discharge pipe via the bypass pipe. Let it. By doing so, it is possible to control the supply amount of the refrigerant quickly and accurately. It is sufficient if the flow rate of the bypass pipe can be controlled so that the temperature of the refrigerant at the outlet does not fall within a range that does not damage the material of the device.
- the degree of opening of the refrigerant control valve provided in the bypass pipe may be set to an optimum state at an opening of 20 to 90%, preferably 30 to 60%.
- FIG. (2) is formed.
- the fluidized bed is supplied with air from an air supply pipe (3) and raw hydrocarbons from a hydrocarbon supply pipe (4).
- the feed rate of raw hydrocarbon is finely adjusted by the control valve (5).
- Gas containing reaction products is the reaction gas extraction pipe
- a stationary heat removal pipe (7) and an adjustment heat removal pipe (8) are installed in the fluidized bed (2). Only one series is shown, but usually each is installed in multiple rows).
- a refrigerant supply pipe (9), (9 ') and a refrigerant discharge pipe (10)> (10') are connected to the stationary heat removal pipe and the adjustment heat removal pipe, respectively.
- One heat removal pipe and one refrigerant removal pipe flow to remove heat from the fluidized bed (2).
- a bypass pipe (11) connecting the refrigerant supply pipe (9 ') connected to the heat removal pipe (8) for adjustment and the refrigerant discharge pipe (10) is connected to the reactor.
- the refrigerant can flow from the refrigerant supply pipe (9 ') to the refrigerant discharge pipe (10') via the bypass pipe (11).
- a refrigerant control valve (12) is installed in the bypass pipe (11) so that the flow rate of the refrigerant flowing through the bypass pipe can be adjusted.
- the fluidized bed (2) is provided with a temperature detecting section (13) (only one temperature detecting section is shown in the figure, but usually a plurality of temperature detecting sections are provided).
- the temperature information detected by the temperature detector (13) is transmitted to the thermometer body (14), and is detected as the temperature of the fluidized bed.
- the refrigerant control valve (1 2) Operate to adjust the amount of refrigerant flowing into the adjusting heat removal pipe (8). If only one temperature detector (13) is installed, it is usually installed at the center of the fluidized bed (2).
- the temperature detector (13) is usually installed at the center of the fluidized bed (2).
- the control temperature is calculated as a function of the temperature detected by each of these temperature detecting sections, and based on the difference between this temperature and the set temperature, the refrigerant control valve ( 1 2) can be operated.
- the refrigerant control valve (12) is not installed in a bypass pipe, but in a refrigerant supply pipe (gz) or a refrigerant discharge pipe (10 '), a heat removal pipe (8) for adjustment, and a bypass pipe (11).
- a three-way valve may be installed at the branch point.
- Maleic anhydride was produced from butane using a 0.8 m diameter fluidized bed reactor as shown in Fig. 1.
- the reactor with the average content of the particles size and at 6 0 in 4 4 um or less of fine powder 4 0 wt%, particle density 2 8 8 0 kg Zm 3 of Banajiumu * composite oxide of Li down system 150 kg of catalyst is charged.
- the fluidized bed (2) formed with this catalyst has five series of stationary heat removal tubes (7) with an outer diameter of 60.5 mm and a length of 4 m, which also have an outer diameter of 60.5 mm and a length of 4 m.
- One set of adjustment heat removal pipes (8 m) with a length of 4 m is installed. Refrigerant supply pipe for each heat removal pipe
- a refrigerant discharge pipe (10, 1 (T)) A midway between the refrigerant supply pipe and the refrigerant discharge pipe connected to the heat removal pipe for adjustment is provided.
- a bypass pipe (11) having a refrigerant control valve (12) is installed in the fluidized bed, and a temperature detector (13) is installed in the center of the fluidized bed.
- feedstock hydrocarbon supply pipe from the n- pig emissions (4) approximately 18 5 ice was supplied to the stationary heat removal tube, which was supplied at 42 Nm 3 Z hr, respectively, and 5 to 10% of the ice was evaporated in the tube, and 19 4 and 13 kg / It was collected as a gas-liquid mixed phase flow of cm 2 G.
- the control valve of the raw hydrocarbon feed pipe was operated according to the temperature detected by the temperature detection section (13) without operating the refrigerant control valve (12), and the n-butane The feed rate was fine-tuned so that the temperature of the fluidized bed was constant. Then 5 days from Day 5 performs supply of n- blanking evening down at a constant rate of 4 2 N m 3 Bruno hr, the temperature detecting unit (1 3) in accordance with the detected temperature by the refrigerant control valve (1 By adjusting the opening of 2) in the range of 30 to 60%, the supply amount of the saturated steam to the heat removal tube for adjustment was finely adjusted to keep the temperature of the fluidized bed constant.
- Figure 2 shows the temperature of the fluidized bed during these 9 days
- Figure 3 shows the feed rate of n-peptane. From FIG. 2, it can be seen that, according to the present invention, the temperature is controlled in a range of ⁇ 0.5 with respect to the set temperature of the fluidized bed of 42.5.5.
- the temperature of the fluidized bed reactor can be controlled very precisely. You. In a fluidized bed reaction, the reaction is usually performed at a temperature of 200 or more. However, according to the present invention, even at a set temperature of about 450, the range of temperature change can be kept within ⁇ 0.5, so that a wide reaction is performed. Long-term stable operation is possible near the maximum yield point in the temperature range. A large part of the heat removal amount is borne by the stationary heat removal tube, and the adjustment heat removal tube can be operated only for the purpose of adjusting the heat removal amount, so it can accurately follow minute fluctuations in the required heat removal amount. it can.
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US08/532,649 US5700432A (en) | 1994-02-08 | 1995-02-07 | Fluidized-bed reactor and a temperature-controlling method for the fluidized-bed reactor |
EP95907851A EP0695576A4 (en) | 1994-02-08 | 1995-02-07 | FLUIDIFIED BED REACTOR AND TEMPERATURE MANAGEMENT METHOD FOR FLUIDIFIED BED REACTOR |
KR1019950703288A KR960704626A (ko) | 1994-02-08 | 1995-02-07 | 유동층 반응기 및 유동층 반응기의 온도제어방법 |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP6/14336 | 1994-02-08 | ||
JP1433694 | 1994-02-08 | ||
JP6/96319 | 1994-05-10 | ||
JP9631994 | 1994-05-10 |
Publications (1)
Publication Number | Publication Date |
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WO1995021692A1 true WO1995021692A1 (fr) | 1995-08-17 |
Family
ID=26350261
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1995/000163 WO1995021692A1 (fr) | 1994-02-08 | 1995-02-07 | Reacteur a lit fluidifie et procede de gestion de la temperature pour reacteur a lit fluidifie |
Country Status (6)
Country | Link |
---|---|
US (1) | US5700432A (ja) |
EP (1) | EP0695576A4 (ja) |
KR (1) | KR960704626A (ja) |
CN (1) | CN1150057C (ja) |
TW (1) | TW314476B (ja) |
WO (1) | WO1995021692A1 (ja) |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2002088043A (ja) * | 2000-09-12 | 2002-03-27 | Mitsubishi Gas Chem Co Inc | ニトリル化合物の製造方法 |
JP2008043894A (ja) * | 2006-08-18 | 2008-02-28 | Asahi Kasei Chemicals Corp | 流動層反応器の温度制御方法 |
JP2008080219A (ja) * | 2006-09-27 | 2008-04-10 | Asahi Kasei Chemicals Corp | 流動層反応器の温度制御方法 |
KR100937374B1 (ko) | 2008-03-17 | 2010-01-20 | 아사히 가세이 케미칼즈 가부시키가이샤 | 유동층 반응기의 온도 제어 방법 |
JP2011225481A (ja) * | 2010-04-19 | 2011-11-10 | Asahi Kasei Chemicals Corp | 気相発熱反応方法 |
WO2012035881A1 (ja) * | 2010-09-14 | 2012-03-22 | 旭化成ケミカルズ株式会社 | 気相発熱反応方法及び気相発熱反応装置 |
KR101286407B1 (ko) * | 2008-05-30 | 2013-07-19 | 아사히 가세이 케미칼즈 가부시키가이샤 | 유동층 반응 장치 및 그것을 이용한 기상 발열 반응 방법 |
KR101356391B1 (ko) | 2011-04-20 | 2014-02-03 | 주식회사 실리콘밸류 | 다결정 실리콘 제조장치 |
JP2017511326A (ja) * | 2014-03-31 | 2017-04-20 | イネオス ユーロープ アクチェンゲゼルシャフト | 酸化又はアンモ酸化反応器のための冷却コイル設計 |
JP2017520510A (ja) * | 2014-03-31 | 2017-07-27 | イネオス ユーロープ アクチェンゲゼルシャフト | 酸化又はアンモ酸化反応器のための冷却コイル設計 |
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US5831113A (en) * | 1996-07-22 | 1998-11-03 | Jgc Corporation | Process for producing a carbonic acid diester |
DE19849709C2 (de) * | 1998-10-28 | 2000-09-14 | Krupp Uhde Gmbh | Verfahren und Wirbelschicht-Reaktor zur Oxichlorierung von Ethylen, Sauerstoff und HCl |
US6657097B1 (en) | 1999-03-08 | 2003-12-02 | Mitsubishi Chemical Corporation | Fluidized bed reactor |
DE60213752T2 (de) * | 2001-12-25 | 2006-12-07 | Mitsubishi Gas Chemical Co., Inc. | Reaktor zur Herstellung von Nitrilverbindungen und Verfahren dazu |
US7598197B2 (en) * | 2004-12-22 | 2009-10-06 | Exxonmobil Chemical Patents Inc. | Catalyst cooling processes utilizing steam superheating |
KR100937373B1 (ko) * | 2008-02-14 | 2010-01-20 | 아사히 가세이 케미칼즈 가부시키가이샤 | 유동층 반응기의 온도 제어 방법 |
CN101507907B (zh) * | 2008-02-15 | 2012-01-25 | 旭化成化学株式会社 | 流化床反应器的温度控制方法 |
TWI486214B (zh) * | 2008-03-10 | 2015-06-01 | Asahi Kasei Chemicals Corp | 流動層反應器之溫度控制方法 |
FR3010916A1 (fr) * | 2013-09-26 | 2015-03-27 | Gdf Suez | Reacteur de methanation pour faire reagir du dihydrogene avec au moins un compose a base de carbone et produire du methane |
CN107206362A (zh) * | 2015-03-13 | 2017-09-26 | 三菱化学株式会社 | 向流化床反应器填充催化剂的方法及腈化合物的制造方法 |
CN104801259A (zh) * | 2015-04-16 | 2015-07-29 | 安徽扬子化工有限公司 | 一种化学药剂旋转散热反应釜 |
CN110390036B (zh) * | 2019-06-03 | 2020-04-10 | 惠安源和机械有限公司 | 双索引数据查询平台 |
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- 1995-02-07 CN CNB951901982A patent/CN1150057C/zh not_active Expired - Lifetime
- 1995-02-07 WO PCT/JP1995/000163 patent/WO1995021692A1/ja not_active Application Discontinuation
- 1995-02-07 KR KR1019950703288A patent/KR960704626A/ko not_active Application Discontinuation
- 1995-02-07 US US08/532,649 patent/US5700432A/en not_active Expired - Lifetime
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Cited By (15)
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JP2002088043A (ja) * | 2000-09-12 | 2002-03-27 | Mitsubishi Gas Chem Co Inc | ニトリル化合物の製造方法 |
JP2008043894A (ja) * | 2006-08-18 | 2008-02-28 | Asahi Kasei Chemicals Corp | 流動層反応器の温度制御方法 |
JP2008080219A (ja) * | 2006-09-27 | 2008-04-10 | Asahi Kasei Chemicals Corp | 流動層反応器の温度制御方法 |
KR100937374B1 (ko) | 2008-03-17 | 2010-01-20 | 아사히 가세이 케미칼즈 가부시키가이샤 | 유동층 반응기의 온도 제어 방법 |
KR101286407B1 (ko) * | 2008-05-30 | 2013-07-19 | 아사히 가세이 케미칼즈 가부시키가이샤 | 유동층 반응 장치 및 그것을 이용한 기상 발열 반응 방법 |
JP2011225481A (ja) * | 2010-04-19 | 2011-11-10 | Asahi Kasei Chemicals Corp | 気相発熱反応方法 |
CN103097014A (zh) * | 2010-09-14 | 2013-05-08 | 旭化成化学株式会社 | 气相放热反应方法及气相放热反应装置 |
WO2012035881A1 (ja) * | 2010-09-14 | 2012-03-22 | 旭化成ケミカルズ株式会社 | 気相発熱反応方法及び気相発熱反応装置 |
JP5770195B2 (ja) * | 2010-09-14 | 2015-08-26 | 旭化成ケミカルズ株式会社 | 気相発熱反応方法及び気相発熱反応装置 |
CN103097014B (zh) * | 2010-09-14 | 2015-12-09 | 旭化成化学株式会社 | 气相放热反应方法及气相放热反应装置 |
KR101356391B1 (ko) | 2011-04-20 | 2014-02-03 | 주식회사 실리콘밸류 | 다결정 실리콘 제조장치 |
JP2017511326A (ja) * | 2014-03-31 | 2017-04-20 | イネオス ユーロープ アクチェンゲゼルシャフト | 酸化又はアンモ酸化反応器のための冷却コイル設計 |
JP2017520510A (ja) * | 2014-03-31 | 2017-07-27 | イネオス ユーロープ アクチェンゲゼルシャフト | 酸化又はアンモ酸化反応器のための冷却コイル設計 |
JP2020073851A (ja) * | 2014-03-31 | 2020-05-14 | イネオス ユーロープ アクチェンゲゼルシャフト | 酸化又はアンモ酸化反応器のための冷却コイル設計 |
JP7216677B2 (ja) | 2014-03-31 | 2023-02-01 | イネオス ユーロープ アクチェンゲゼルシャフト | 酸化又はアンモ酸化反応器のための冷却コイル設計 |
Also Published As
Publication number | Publication date |
---|---|
EP0695576A1 (en) | 1996-02-07 |
CN1124465A (zh) | 1996-06-12 |
KR960704626A (ko) | 1996-10-09 |
EP0695576A4 (en) | 1996-07-17 |
US5700432A (en) | 1997-12-23 |
CN1150057C (zh) | 2004-05-19 |
TW314476B (ja) | 1997-09-01 |
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