CN111266063A - Heating system for acid regeneration - Google Patents
Heating system for acid regeneration Download PDFInfo
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- CN111266063A CN111266063A CN202010077126.4A CN202010077126A CN111266063A CN 111266063 A CN111266063 A CN 111266063A CN 202010077126 A CN202010077126 A CN 202010077126A CN 111266063 A CN111266063 A CN 111266063A
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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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
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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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
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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
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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
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00946—Features relating to the reactants or products
- B01J2208/00955—Sampling of the particulate material, the reactants or the products
- B01J2208/00964—Reactants
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention relates to a heating system for acid regeneration, which comprises a reaction device and a combustion device, wherein the reaction device comprises: the grid unit is provided with a plurality of first through holes and divides the reaction device into a reaction chamber and a combustion chamber from top to bottom; the combustion device is arranged on the outer side of the reaction device and is communicated with the combustion chamber. The method has the advantages that the reaction device is divided into the reaction chamber and the combustion chamber by the grid unit, at least one combustion device is arranged on the outer side of the reaction device and is communicated with the combustion chamber, so that the combustion device is not contacted with oxides in the reaction chamber, flame monitoring is continuously carried out on the combustion device, and discharging, combustion and refilling operations are not needed; the grid unit guides the hot combustion products in the combustion chamber into the reaction chamber and uniformly distributes the hot combustion products, so that the oxides in the reaction chamber are prevented from entering the combustion chamber; through burner, can adjust the temperature wantonly according to actual operation needs.
Description
Technical Field
The invention relates to the technical field of acid regeneration of a thermal hydrolysis process, in particular to a heating system for acid regeneration.
Background
In fluidized bed acid Regeneration Plants (FB-ARPs), a plurality of burners are generally installed in the bottom of the inside of a reactor. These burners usually use gas for combustion, and may use liquid fuel for combustion. For the safe operation of the burner, it must have the function of flame control. This ensures that all of the fuel has been combusted and avoids any uncontrolled combustion or explosion. There are a variety of flame monitoring systems on the market, the most common of which is an ultraviolet detector.
Fluidized bed acid regenerators typically employ an ultraviolet detector to heat the reactor. However, during operation, the reactor was filled with particulate oxides, which made optical flame monitoring impossible. Other systems, such as flame rods, cannot be used because the highly abrasive oxides can quickly damage such equipment. Therefore, the process temperature of fluidized bed Technology (FB-Technology) must be kept at a level well above the auto-ignition temperature of the fuel, since flame monitoring above such temperatures is not required. This is referred to as high temperature operation. National laws and standards specify a critical temperature above which high temperature operation is permitted without flame monitoring.
For example, in Europe, EN 746-2 specifies relevant content. From EN 746-2, the critical temperature of the fuel gas is 750 ℃. In practice, the actual process temperature is even higher to ensure continuous operation without sudden stops due to technical malfunctions. A typical process temperature for a fluidized bed acid regenerator is 850 ℃.
However, there are two major disadvantages to this mode of operation, as follows:
1) when the process temperature drops below the critical temperature, the process cannot be simply re-run; if a new run is required, all the oxide needs to be removed from the reactor first, which may last for several hours; secondly, reheating, wherein flame monitoring is needed in the reheating process; when the temperature rises to the process temperature, the reactor needs to be filled with oxides, and the process can also last for several hours;
2) the process temperature required for the actual pyrolysis reaction is far below the critical temperature; for safety reasons, it is desirable to operate above the critical temperature, however, lower process temperatures can reduce energy consumption and thereby significantly reduce carbon emissions, in view of environmental concerns.
Therefore, in order to solve the above problems, there is a need for an improved acid regeneration heating system to lower the process temperature and overcome the drawbacks of high temperature operation.
Disclosure of Invention
The invention aims to provide a heating system for acid regeneration, aiming at the defects in the prior art.
In order to achieve the purpose, the invention adopts the technical scheme that:
a heating system for acid regeneration comprising a reaction apparatus and a combustion apparatus, the reaction apparatus comprising:
the grid unit is provided with a plurality of first through holes and divides the reaction device into a reaction chamber and a combustion chamber from top to bottom;
the combustion device is arranged on the outer side of the reaction device and is communicated with the combustion chamber.
Preferably, the longitudinal section of the combustion chamber is in the shape of an inverted cone.
Preferably, the combustion chamber further comprises:
the first pipeline is arranged at the bottom of the combustion chamber;
and the second pipeline is arranged at the bottom of the combustion chamber and is communicated with the first pipeline.
Preferably, the number of the first pipelines is several, the number of the combustion devices is several, and one of the first pipelines is connected with one of the combustion devices in a one-to-one correspondence manner.
Preferably, the reaction apparatus further comprises:
the metal pore plate is provided with a plurality of second through holes, the metal pore plate is detachably arranged on the upper parts of the grid units, and the second through holes of the metal pore plate correspond to the first through holes of the grid units one to one.
Preferably, each of the first through holes has a diameter such that a gas velocity of a gas passing through the first through hole is 20 to 200 m/s.
Preferably, each of the first through holes has a diameter such that a gas velocity of a gas passing through the first through hole is 40 to 120 m/s.
Preferably, each of the first through holes has a diameter such that a gas velocity of a gas passing through the first through hole is 60 to 100 m/s.
Preferably, each of the first through holes has a diameter of 2 to 30 mm.
Preferably, each of the first through holes has a diameter of 4 to 15 mm.
Preferably, each of the first through holes has a diameter of 5 to 8 mm.
Preferably, the first through hole includes:
an upper portion, a first end of the upper portion being proximate to the reaction chamber;
a lower portion, a first end of the lower portion connected to a second end of the upper portion, the second end of the lower portion adjacent to the combustion chamber;
the shape of the longitudinal section of the upper portion may be the same as or different from the shape of the longitudinal section of the lower portion.
Preferably, the longitudinal section of the upper part is quadrangular, and the included angle formed by the bottom edge and the side edge is 60-180 degrees.
Preferably, the longitudinal section of the upper part is quadrangular, and the included angle formed by the bottom edge and the side edge is 90-120 degrees.
Preferably, the first through hole further includes:
a transition portion, a first end of the transition portion being connected to the second end of the upper portion, a second end of the transition portion being connected to the first end of the lower portion.
Preferably, the upper portion has a limiting aperture at an angle to the reaction chamber.
Preferably, the angle is 60-180 °.
Preferably, the angle is 90-120 °.
Preferably, the reaction process temperature is 150-.
Preferably, the grid cells are made of a refractory material.
By adopting the technical scheme, compared with the prior art, the invention has the following technical effects:
according to the heating system for acid regeneration, the reaction device is divided into the reaction chamber and the combustion chamber by using the grid unit, and at least one combustion device is arranged on the outer side of the reaction device and is communicated with the combustion chamber, so that the combustion device is not in contact with oxides in the reaction chamber, flame monitoring can be continuously carried out on the combustion device, and discharging, combustion and refilling operations are not needed; the grid unit guides the hot combustion products in the combustion chamber into the reaction chamber, and the hot combustion products are uniformly distributed, and the oxides in the reaction chamber are prevented from entering the combustion chamber; the combustion device arranged outside the reaction device can adjust the temperature at will according to the actual operation requirement, and the application range is wide; in the heating process of the reaction chamber, the filling of the oxide can be carried out, so that the process time is effectively saved; by utilizing continuous flame monitoring, even if the process temperature is lower than the critical temperature, the process temperature is probably equivalent to the temperature required by the process, so that the operation is easy, the energy consumption is reduced, and a more environment-friendly process is formed.
Drawings
FIG. 1 is a schematic diagram of an exemplary embodiment of the present invention.
Fig. 2 is a top view of a grid cell of an exemplary embodiment of the present invention.
Fig. 3 is a schematic longitudinal sectional view of a grid cell of an exemplary embodiment of the present invention.
Fig. 4 is a schematic longitudinal sectional view of a grid cell of another embodiment of the present invention.
Fig. 5 is a schematic longitudinal sectional view of a grid cell of another embodiment of the present invention.
Wherein the reference numerals are: the device comprises a reaction device 1, a combustion device 2, a grid unit 3, a first through hole 4, a reaction chamber 5, a combustion chamber 6, a first pipeline 7, a second pipeline 8, a metal pore plate 9, a second through hole 10, an upper part 11, a lower part 12 and a transition part 13.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
The invention is further described with reference to the following drawings and specific examples, which are not intended to be limiting.
Example 1
An exemplary embodiment of the present invention, as shown in fig. 1, is a heating system for acid regeneration, comprising a reaction apparatus 1 and a combustion apparatus 2, wherein the combustion apparatus 2 is disposed outside the bottom of the reaction apparatus 1 and is communicated with the reaction apparatus 1.
The reaction device 1 comprises a grid unit 3, the grid unit 3 comprises a plurality of first through holes 4, and the plurality of first through holes 4 are uniformly distributed. The mesh unit 3 is provided inside the reaction apparatus 1, and divides the reaction apparatus 1 into a reaction chamber 5 and a combustion chamber 6. Wherein, the reaction chamber 5 is positioned at the upper part of the reaction device 1 and is filled with oxide; the combustion chamber 6 is located at the lower portion of the reaction apparatus 1 and communicates with the combustion apparatus 2.
Further, the ratio of the volume of the combustion chamber 6 to the volume of the reaction chamber 5 is less than or equal to 0.15: 1.
further, the longitudinal section of the combustion chamber 6 is reverse tapered.
Further, the combustion chamber 6 comprises a first pipe 7 and a second pipe 8, wherein the first pipe 7 is arranged at the bottom of the combustion chamber 6 and the second pipe 8 is arranged at the side of the first pipe 7.
Wherein the first conduit 7 is used for collecting and discharging waste oxides to avoid the accumulation of oxides in the combustion chamber 6, and the second conduit 8 is used for feeding air or combustion air to the bottom of the combustion chamber 2 for cooling the bottom of the combustion chamber 6 and the oxides therein to avoid the sintering and accumulation of oxides, and the combustion air is mixed with the combustion exhaust gas to help complete the combustion process.
Further, the combustion devices 2 are plural, all the combustion devices 2 communicate with the side portion of the combustion chamber 6, and the temperature can be adjusted more effectively by on-off controlling the plurality of combustion devices 2.
Specifically, the plurality of combustion devices 2 are uniformly distributed around the combustion chamber 6, thereby uniformly supplying the combustion gas into the combustion chamber 6.
The grid unit 3 may be fixedly installed inside the reaction apparatus 1 or detachably installed inside the reaction apparatus 1, and is capable of uniformly introducing the combustion gas in the combustion chamber 6 into the reaction chamber 5 and restricting the oxide in the reaction chamber 5 from entering the combustion chamber 6.
As shown in fig. 2-3, the first through holes 4 of the grid cells 3 are regular cylindrical through holes.
Further, the diameter of the first through-hole 4 is 2 to 30mm, preferably 4 to 15mm, and more preferably 5 to 8 mm. With this particular diameter, the entry of oxides into the combustion chamber 6 can be effectively limited.
Further, the diameter of the first through holes 4 may be designed such that the gas velocity of the gas passing through each first through hole 4 is 20 to 200m/s, preferably 40 to 120m/s, and more preferably 60 to 100 m/s.
Further, the grid cells 3 are made of a heat-resistant or fire-resistant material, which is able to withstand a temperature of at least 1000 ℃.
Specifically, the grid cells 3 may be made of a heat-resistant material such as heat-resistant stone or heat-resistant ceramic.
The using method of the invention is as follows: before starting the fluidized bed acid regeneration unit, the reaction chamber 5 needs to be heated to the working temperature, since the reaction unit is usually a steel shell with a refractory lining, which has to be heated according to a specified temperature/time curve, which can be achieved by the combustion unit 2, hot combustion gas passes through the combustion chamber 6 and then enters the reaction chamber 5 through the grid unit 3; during the heating, the oxide filling operation may be performed into the reaction chamber 1; according to the actual operation requirement, the plurality of combustion devices 2 can be switched on and off to control the temperature and the energy consumption in the operation process, and specifically, the actual process temperature fluctuates within the range of 150-.
Example 2
This embodiment is an embodiment of the present invention, which is substantially the same as embodiment 1 except that a metal orifice plate 9 is detachably mounted on the upper and/or lower portion of the grid unit 3.
As shown in fig. 4, the metal orifice plate 9 has a plurality of second through holes 10, and when the metal orifice plate 9 is installed on the upper portion of the grid unit 3, the plurality of second through holes 10 correspond to the plurality of first through holes 4 one to one.
The metal orifice plate 9 is made of a heat-resistant metal, such as 309 stainless steel, 316 stainless steel.
Since the temperature of the combustion gas is usually between 1200 ℃ and 1600 ℃, covering the grid cells 3 with the metal orifice plates 9 made of heat-resistant metal can be well adapted to the above temperature range. In addition, the metal orifice plate 9 has high abrasion resistance, so that the metal orifice plate can be applied to a fluidized bed process requiring high abrasion resistance.
Further, with the excellent heat transfer performance of the heat-resistant metal, the metal orifice plate 9 can be cooled when the fluidized bed is brought into contact with the metal orifice plate 9.
Example 3
This embodiment is another embodiment of the present invention, which is substantially the same as embodiment 1 except that the shape of the first through holes 4 of the grid unit 3 is different.
As shown in fig. 5, the first through hole 4 includes an upper portion 11, a lower portion 12 and a transition portion 13, a first end of the upper portion 11 is adjacent to the reaction chamber 5, a second end of the lower portion 12 is adjacent to the combustion chamber 6, a first end of the transition portion 13 is communicated with a second end of the upper portion 11, and a second end of the transition portion 13 is communicated with a first end of the lower portion 12.
The longitudinal section of the upper portion 11 is quadrilateral, and the upper portion may be trapezoidal, rectangular, or inverted trapezoidal.
Specifically, the bottom edge and the side edges of the upper portion 11 form an included angle α, the included angle α being in the range of 60 to 180, and preferably in the range of 90 to 120.
The lower portion 12 is quadrilateral in longitudinal cross-section, preferably trapezoidal.
The transition portion 13 has a rectangular or trapezoidal longitudinal section.
Further, the ratio of the length of the base of the trapezoid of the lower portion 12 to the length of the base of the transition portion 13 is 1.1-3: 1, preferably 1.5 to 2.5: 1, more preferably 1.8 to 2.2: 1.
in the present embodiment, the case where the upper portion 11 has an inverted trapezoidal longitudinal section, the lower portion 12 has a trapezoidal longitudinal section, and the transition portion 13 has a trapezoidal longitudinal section will be described. In this embodiment, the first through hole 4 has a substantially gourd-shaped longitudinal section, and with this shape, when the oxide in the reaction chamber 5 enters the first through hole 4, the oxide is caught in the first through hole 4, and cannot enter the combustion chamber 6. Furthermore, this shape also allows sufficient combustion gas to enter the reaction chamber 5 from the combustion chamber 6.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention.
Claims (14)
1. A heating system for acid regeneration, comprising a reaction device and a combustion device, wherein the reaction device comprises:
the mesh unit is provided with a plurality of first through holes and divides the reaction device into a reaction chamber and a combustion chamber from top to bottom;
the combustion device is arranged on the outer side of the reaction device and is communicated with the combustion chamber.
2. The heating system for acid regeneration according to claim 1, wherein a longitudinal section of the combustion chamber is in an inverted cone shape.
3. The heating system for acid regeneration of claim 1, wherein the combustion chamber further comprises:
the first pipeline is arranged at the bottom of the combustion chamber;
and the second pipeline is arranged at the bottom of the combustion chamber and is communicated with the first pipeline.
4. The heating system for acid regeneration according to claim 1, wherein said combustion means is a plurality of combustion means, and a plurality of said combustion means are in communication with a side portion of said combustion chamber.
5. The heating system for acid regeneration according to claim 1, wherein the reaction device further comprises:
the metal pore plate is provided with a plurality of second through holes, the metal pore plate is detachably arranged on the upper portion of the mesh unit, and the second through holes of the metal pore plate correspond to the first through holes of the mesh unit one to one.
6. The heating system for acid regeneration according to claim 1, wherein each of the first through holes has a diameter such that a gas velocity of a gas passing through the first through hole is 20 to 200 m/s.
7. The heating system for acid regeneration according to claim 1, wherein each of the first through holes has a diameter of 2 to 30 mm.
8. The heating system for acid regeneration of claim 1, wherein the first through hole comprises:
an upper portion, a first end of the upper portion being proximate to the reaction chamber;
a lower portion, a first end of the lower portion connected to a second end of the upper portion, the second end of the lower portion adjacent to the combustion chamber;
the shape of the longitudinal section of the upper portion may be the same as or different from the shape of the longitudinal section of the lower portion.
9. The heating system for acid regeneration of claim 8, wherein the first through-hole further comprises:
a transition portion, a first end of the transition portion being connected to the second end of the upper portion, a second end of the transition portion being connected to the first end of the lower portion.
10. The heating system for acid regeneration of claim 8, wherein said upper portion has a limiting orifice angled with respect to said reaction chamber.
11. The heating system for acid regeneration of claim 10, wherein said angle is 60-180 °.
12. The heating system for acid regeneration of claim 11, wherein said angle is 90-120 °.
13. The heating system for acid regeneration of any one of claims 1 to 12, wherein the mesh unit is made of a refractory material.
14. An acid regeneration process applied to the heating system for acid regeneration as claimed in any one of claims 1 to 13, wherein the reaction process temperature is 150-800 ℃.
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| CN202010077126.4A CN111266063B (en) | 2020-01-23 | 2020-01-23 | Heating system for acid regeneration |
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| CN202010077126.4A CN111266063B (en) | 2020-01-23 | 2020-01-23 | Heating system for acid regeneration |
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| CN111266063B CN111266063B (en) | 2021-11-02 |
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Citations (6)
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| CN1072219A (en) * | 1991-11-14 | 1993-05-19 | 清华大学 | The treatment technology of cold rolling chlorohydric acid pickling spent acid |
| US20080063593A1 (en) * | 2006-09-08 | 2008-03-13 | Catalytic Distillation Technologies | Low temperature process for regenerating spent sulfuric acid |
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| CN109967005A (en) * | 2019-04-02 | 2019-07-05 | 山东力山特智能科技有限公司 | A kind of reacting furnace using coke-stove gas fluidized bed acid regeneration process |
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2020
- 2020-01-23 CN CN202010077126.4A patent/CN111266063B/en active Active
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| GB1032592A (en) * | 1961-11-14 | 1966-06-15 | Fullers Earth Union Ltd | Chemical recovery process and apparatus |
| DE1442681A1 (en) * | 1961-11-14 | 1968-11-28 | Fullers Earth Union Ltd., Redhill, Surrey (Großbritannien) | Chemical recovery process and apparatus |
| CN1072219A (en) * | 1991-11-14 | 1993-05-19 | 清华大学 | The treatment technology of cold rolling chlorohydric acid pickling spent acid |
| US20080063593A1 (en) * | 2006-09-08 | 2008-03-13 | Catalytic Distillation Technologies | Low temperature process for regenerating spent sulfuric acid |
| CN205653510U (en) * | 2013-09-26 | 2016-10-19 | 安德里特斯公开股份有限公司 | Be used for palingenetic equipment of hydrochloric acid |
| CN107098529A (en) * | 2017-04-26 | 2017-08-29 | 西可林控制系统(上海)有限公司 | The no-drain treatment method and its device of a kind of hydrochloric acid pickling waste liquor |
| CN109967005A (en) * | 2019-04-02 | 2019-07-05 | 山东力山特智能科技有限公司 | A kind of reacting furnace using coke-stove gas fluidized bed acid regeneration process |
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