CN114042355B - Tobacco leaf raw fluidized bed dry distillation product filtering system and cyclone separation process thereof - Google Patents
Tobacco leaf raw fluidized bed dry distillation product filtering system and cyclone separation process thereof Download PDFInfo
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- CN114042355B CN114042355B CN202111137605.1A CN202111137605A CN114042355B CN 114042355 B CN114042355 B CN 114042355B CN 202111137605 A CN202111137605 A CN 202111137605A CN 114042355 B CN114042355 B CN 114042355B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Abstract
The invention provides a tobacco leaf raw fluidized bed dry distillation product filtering system, which comprises at least one cyclone separation unit, wherein the cyclone separation unit comprises: the cyclone separator is provided with a cyclone separation cylinder body, and the cyclone separation cylinder body is provided with a flue gas inlet for flue gas to enter, a flue gas outlet for flue gas to be discharged and a slag discharge port for coke to be discharged from the bottom of the cyclone separation cylinder body; the buffer tank is communicated and connected with a slag discharge port at the bottom of the cyclone separation cylinder and is used for storing the separated coke, and the temperature of the buffer tank is controlled to be more than 350 ℃; and the collecting tank is communicated with the bottom of the cache tank.
Description
Technical Field
The invention belongs to the field of novel tobacco products, and particularly relates to a multistage cyclone separation device and a multistage cyclone separation process for a tobacco fluidized bed dry distillation product.
Background
The dry distillation of tobacco means that the tobacco is heated and decomposed to generate various gases, steam, solid residues and the like, and the gases and the liquid are obtained after the cooling. Dry distillation is a complex chemical reaction process involving dehydration, pyrolysis, dehydrogenation, thermal condensation, hydrogenation, coking, and the like. The heating temperature can be from 100 ℃ to about 1000 ℃, and the pressure can be normal pressure or reduced pressure. The relative amount of gas, liquid and solid products obtained by dry distillation varies with the heating temperature and time, and more liquid products can be obtained in low-temperature dry distillation. And separating solid carbon from the product obtained by dry distillation through multi-stage cyclone separation, and collecting the solid carbon. And the rest gas-liquid mixture is condensed and collected after being subjected to multi-stage cyclone separation, and is further used for developing novel tobacco product flavor raw materials.
The separation of solid carbon and volatile pyrolysis products in the dry distillation process is a key step for obtaining high-quality incense raw materials, and the poor separation effect of the solid carbon can cause more solid impurities in the incense raw materials, thus having adverse effects on the smoking quality and long-term storage. Cyclone separators are a common means of solid-gas separation. The carbon particles generated after the dry distillation of the tobacco have small particle size and low density. For the separation of such ultra-fine and ultra-light powder, most of the commercially available cyclone separators cannot handle it. In order to improve the quality of the flavor raw material, it is necessary to develop a cyclone separator suitable for dry distillation charcoal of tobacco in a targeted manner.
Disclosure of Invention
Aiming at the technical problems, the invention aims to provide a multistage cyclone separation device and a process for tobacco fluidized bed dry distillation products, wherein solid carbon is separated and collected after the products obtained by fluidized bed dry distillation are subjected to multistage cyclone separation; the rest gas-liquid mixture is condensed and collected after being separated by multi-stage cyclone separation, and is further used for developing novel tobacco product flavor raw materials.
Specifically, in a first aspect, the present invention provides a tobacco leaf raw fluidized bed dry distillation product filtering system, which comprises at least one cyclone separation unit, wherein the cyclone separation unit comprises:
the cyclone separator is provided with a cyclone separation cylinder body, and the cyclone separation cylinder body is provided with a flue gas inlet for flue gas to enter, a flue gas outlet for flue gas to be discharged and a slag discharge port for coke to be discharged from the bottom of the cyclone separation cylinder body;
the buffer tank is communicated and connected with a slag discharge port at the bottom of the cyclone separation cylinder and is used for storing the separated coke, and the temperature of the buffer tank is controlled to be more than 350 ℃;
and the collecting tank is communicated with the bottom of the cache tank.
As a preferred embodiment, the filtering system comprises two cyclone separation units, the two cyclone separation units comprise a first-stage cyclone separation unit and a second-stage cyclone separation unit, and a flue gas inlet of the second-stage cyclone separation unit is communicated with an air outlet of the first-stage cyclone separation unit.
In a preferred embodiment, the filtration system is used to separate particles in the size range of 10 microns to 1 mm.
In a preferred embodiment, the inlet airflow rate of the first stage cyclone separation unit is 16-35m/s, and the inlet airflow rate of the second stage cyclone separation unit is 24-51 m/s.
In a preferred embodiment, the first buffer tank and the second buffer tank are externally provided with heating modules so as to control the temperature of the first buffer tank and the second buffer tank to be more than 350 ℃.
In a preferred embodiment, the collection tank is equipped with a cooling module for cooling the coke and an exhaust module for purging the interior of the collection tank of air.
As a preferred embodiment, the top of the buffer tank is communicated with the cyclone separation cylinder body through an inlet valve, and the bottom of the buffer tank is communicated with the collection tank through an outlet valve; the upside and the downside of buffer tank are equipped with material level indicator and unloading level indicator respectively, it is connected with inlet valve control to go up the material level indicator, unloading level indicator and outlet valve control connection.
As a preferred embodiment, the flue gas air inlet is arranged at the top end of the side surface of the cyclone separation cylinder, and the inlet section of the cyclone separation cylinder communicated with the air inlet forms a gradual change pipeline.
In a preferred embodiment, the collection tank is provided with a window.
In a second aspect, the invention provides a multistage cyclone separation process for dry distillation products of tobacco aroma components, which adopts the filtering system, and the multistage cyclone separation process comprises the following steps: after the tobacco is subjected to dry distillation by the fluidized bed, pyrolysis products mixed with coke enter the two-stage cyclone separation unit in sequence, when no solid material is detected by the level indicator, an inlet valve of the buffer tank is opened, and an outlet valve is closed; when the coke is accumulated to the position of the material loading level indicator, the inlet valve is automatically closed, and the outlet valve is opened, so that the solid in the buffer tank is smoothly discharged into the solid coke collecting tank; when the material is discharged below the blanking level indicator, the outlet valve is closed, and the inlet valve is opened; the automatic operation is circulated in the way.
Compared with the prior art, the invention has the following beneficial effects:
(1) The solid carbon of the dry distillation product can be effectively separated through multi-stage cyclone separation, and the gas condensed through the multi-stage cyclone separation is cleaner and has stronger usability.
(2) A buffer tank is arranged between the cyclone separator and the collecting tank, so that the separation smoothness can be effectively ensured.
(3) The automatic valve is arranged at the joint among the separator main body, the buffer tank and the collecting tank, the automatic discharging of the materials is realized through the charge level indicator, the tightness and the pressure stability of the separator and the main system are ensured, and the long-time smooth running of the dry distillation system is ensured
(4) The number of stages of the separator can be reduced or added and the size of the separator can be changed according to the conditions of the particle size, the working condition and the like of the tobacco raw material, so that the optimal separation effect is realized
Drawings
FIG. 1 is a schematic view of the general flow of the process for dry distillation and extraction of aroma components from tobacco according to the present invention;
FIG. 2 is a schematic view of a system for extracting aroma components by dry distillation of tobacco according to the present invention;
FIG. 3 is a schematic diagram of the specific structure of the cyclone separator and the buffer tank of the present invention;
FIG. 4 is a schematic view showing a specific structure of a collection tank of the present invention;
wherein the reference numerals are as follows:
A. a first-level storage bin; B. a secondary storage bin; C. an arch breaking machine; D. a feeder; E. a feeding machine; F. a fluidized bed; G. a primary cyclone separator; H. a first-stage cyclone buffer tank; I. a first-stage cyclone storage tank; J. a secondary cyclone separator; K. a secondary cyclone buffer tank; l, a secondary cyclone storage tank; m, a high-temperature micro-dust separator; n, a high-temperature micro-dust collecting tank; o, a first-stage condenser; p, a first-stage condenser collecting tank; q, a secondary condenser; r, a secondary condenser collecting tank; s, primary electric catching; t, a first-level electric catching and collecting tank; u, secondary electric catching; v, a secondary electric catching collection tank; w, a tail gas treatment system; x, a preheater;
1. a flue gas outlet; 2. a flue gas inlet; 3. an exhaust core tube; 4. a coke buffer tank; 5. a loading level indicator; 6. a thermocouple; 7. a level meter; 8. a connecting flange;
31. an air inlet; 32. an exhaust port 33, a sight glass; 34. hoisting a ring; 35. a circulating water inlet; 36. a fortune wheel; 37. a pressure gauge; 38. an air inlet; 39. an opposite view mirror; 51. a circulating water vent; 100. a cooling water jacket 110, a circulating water outlet; 120. a butterfly valve slag discharge port; 130. fork truck participates in.
Detailed Description
The invention is further illustrated by the following examples:
as shown in fig. 1 and 2, the invention provides a tobacco aroma component dry distillation extraction system, which comprises a tobacco leaf raw material processing system, a cracking reaction system, a gas-solid separation system, a condensation system, a rectification system (not shown), an electric capture system and a tail gas processing system which are sequentially connected in series. Wherein:
the tobacco raw material processing system comprises a first-stage storage bin A, a second-stage storage bin B, an arch breaking machine C, a feeder D and a feeder E, and can stably, continuously and quantitatively feed tobacco raw materials into the cracking reaction system.
The cracking reaction system comprises a fluidized bed F and a preheater X, wherein the preheater X is arranged at the bottom of the fluidized bed F, the bottom of the preheater X is communicated with an N2 steel cylinder so as to heat the fluidized gas and introduce the heated fluidized gas into the fluidized bed F for cracking and generating cracked gas, the pyrolysis temperature of the fluidized bed F is 100-400 ℃, and the cracked gas is sent into a gas-solid separation system to remove coke.
The gas-solid separation system comprises a primary cyclone separator G, a primary cyclone buffer tank H, a primary cyclone storage tank I, a secondary cyclone separator J, a secondary cyclone buffer tank K, a secondary cyclone storage tank L, a high-temperature micro-dust separator M and a high-temperature micro-dust collecting tank N. The first-stage cyclone separator G and the second-stage cyclone separator J are used for separating gas-phase aroma components and coke in the pyrolysis gas step by step; after the high-temperature micro-dust separator M further removes micro solid impurities in the gas-phase aroma components, the gas-phase aroma components are continuously fed. The high-temperature micro-dust separator M can specifically adopt a high-temperature electric catcher, a high-temperature ceramic filter, a high-temperature cloth bag filter and the like. And gas-solid phase products obtained by pyrolysis are separated by a primary cyclone separator G, a secondary cyclone separator J and a high-temperature fine dust separator M and then are respectively recovered in a primary cyclone buffer tank H, a primary cyclone storage tank I, a secondary cyclone buffer tank K, a secondary cyclone storage tank L and a high-temperature fine dust collection tank N.
The condensing system comprises a first-stage condenser O, a first-stage condenser collecting tank P, a second-stage condenser Q and a second-stage condenser collecting tank R. The liquid phase substance generated after the gas-phase aroma components pass through the first-stage condenser O is a first aroma condensate and is collected in a first-stage condenser collecting tank P. And continuously feeding the residual gas-phase substance into a secondary condenser Q, and collecting the generated liquid-phase substance which is second aroma condensate in a secondary condenser collecting tank R. The first and second aroma condensates may continue to be fed into the rectification system for treatment. The residual gas-phase aroma components can be continuously fed into the electric catching system.
The electric catching system comprises a primary electric catching S, a primary electric catching collecting tank T, a secondary electric catching U and a secondary electric catching collecting tank V. And the substance of the gas-phase aroma components collected by the first-stage electric catching S is the first-order aroma electric catching liquid and is collected in a first-stage electric catching collection tank T. And continuously feeding the residual gas-phase aroma components into a secondary electric catching U, wherein the collected substances are second aroma electric catching liquid and are collected in a secondary electric catching collection tank V. And finally, the residual gas is sent into a tail gas treatment system W at the tail part of the system.
The gas-solid separation system provided by the invention comprises a cyclone separation system, wherein the cyclone separation system comprises at least one cyclone separation unit, please refer to fig. 3 and 4, and the cyclone separation unit comprises a cyclone separator, a buffer tank and a collection tank; the structure of which is explained in detail below:
fig. 3 and fig. 4 are schematic structural diagrams of the cyclone separator, the buffer tank and the collection tank in the embodiment, both of which include a cyclone separation cylinder, the cyclone separation cylinder is provided with a flue gas inlet 2, a flue gas outlet 1, an exhaust core pipe 3 and a slag discharge port, flue gas enters the exhaust core pipe 3 through the flue gas inlet and is discharged through the flue gas outlet, and separated coke is discharged out of the cylinder through the slag discharge port;
the buffer tank 4 is communicated and connected with a slag discharge port at the bottom of the cyclone separation cylinder body, the buffer tank is used for storing separated coke, and the temperature of the buffer tank is controlled to be more than 350 ℃ so as to prevent condensation of pyrolysis gas; in some preferred embodiments, a heating furnace is arranged outside the buffer tank, so that the temperature in the buffer tank is kept above 350 ℃; in some embodiments, the buffer tank is internally provided with a thermocouple 6 to heat the buffer tank.
Referring to fig. 3 and 4, a collection tank is disposed in communication with the bottom of the surge tank to collect coke discharged from the surge tank.
Further preferably, as shown in fig. 4, the collection tank is equipped with a cooling module for cooling the coke and an exhaust module for exhausting air inside the collection tank; specifically, the outer part of the collecting tank is sleeved with a water cooling sleeve 100, and the heat of the pyrolytic coke is taken away by condensing circulating water; an inert gas inlet 38 and an exhaust 32 are arranged at the upper part of the collecting pipe, and before the reaction starts, external nitrogen is flushed into the collecting tank V to replace the air in the collecting tank and is exhausted through the exhaust.
In addition, flue gas air intake 2 sets up on the side top of cyclone cylinder, for guaranteeing entry speed and separation effect, the entry of cyclone cylinder is square, and its cyclone cylinder forms the gradual change pipeline with the entry section of air intake intercommunication, reduces the influence of air current disturbance.
The connection of each separation unit adopts standard connecting pieces with uniform size, so that the size adjustment and replacement in the later period are facilitated; in some embodiments, as shown in FIG. 4, the cooling device comprises a water jacket 100 disposed on the outer wall of the tank, the water jacket having a circulating water inlet 35 and a circulating water outlet 110 for circulating water, and a circulating water vent 51
Optionally, the tank is provided with a pressure gauge 37; the tank body is provided with a sight glass window 33,38, so that the carbon collection state can be observed at any time; the slag discharge port 120 is provided with a butterfly valve, and carbon slag is discharged by screwing the butterfly valve to store carbon.
The bottom of the tank body is provided with a Fuma wheel 36 and a fork lift pin 130, so that the collection tank can be transferred; the tank is further provided with a lifting ring 34.
Preferably, the top of buffer tank 4 is through setting up import valve and cyclone cylinder intercommunication, and the bottom of buffer tank is through setting up the air inlet 31 intercommunication of outlet valve and holding vessel, the upside and the downside of buffer tank are equipped with charge level indicator 5 and lower charge level indicator 7 respectively, go up charge level indicator 5 and import valve control connection, lower charge level indicator and outlet valve control connection. The invention provides a secondary cyclone separation unit as a preferred embodiment, and specifically, the secondary cyclone separation unit comprises a primary cyclone unit and a secondary cyclone separation unit, wherein a flue gas inlet of the secondary cyclone separation unit is communicated with an air outlet of the primary cyclone separation unit; the cyclone separators are connected through pipelines, and the pipelines are provided with active heat preservation to keep the temperature of the fluid to be up to 600 ℃.
Illustratively, pyrolysis gas carrying coke firstly enters a cyclone separation system through an air inlet of a first-stage cyclone separator, an improved air inlet is tangentially arranged at the top end of the side surface of a separation cylinder body, gas-solid separation is realized under the centrifugal action, the gas enters a system unit of next-stage cyclone separation or downstream through an exhaust core pipe inserted into the separation cylinder body and an air outlet connected with the exhaust core pipe, the solid enters a coke cache tank through a slag discharge port of the cyclone separation cylinder body, the coke enters a coke collecting tank through an outlet valve of the cache tank, electronic induction material level meters are respectively arranged at a position 20 cm below an inlet of the cache tank and at a position 20 cm above an outlet of the cache tank, and the inlet and the outlet are linked through a control system.
In one embodiment, the invention provides a cyclone separation process, when a system starts to operate, no solid material is detected by an upper level gauge and a lower level gauge, an inlet valve of a buffer tank is opened, and an outlet valve is closed; when the coke is accumulated to the position of the material loading level indicator, the valve at the inlet is automatically closed, and the outlet valve is opened, so that the solid in the buffer tank is smoothly discharged into the solid coke collecting tank; when the material is discharged below the blanking level indicator, the outlet valve is closed, and the inlet valve is opened; the automatic operation is circulated, so that the gas tightness of the reaction system can be ensured while smooth slag discharge is realized.
The present embodiment can separate particles with size of millimeter to 10 micron, the inlet airflow speed of the first stage cyclone separator is 16-35m/s, the inlet speed of the second stage cyclone separator is 24-51m/s, and the corresponding pressure drop is 1550Pa-2630Pa. The inlet air velocity of the two-stage cyclone at different carbonization temperatures is shown in the following table 1.
TABLE 1
| Dry distillation temperature/. Degree C | First cyclone separation inlet wind speed (m/s) | Inlet wind speed (m/s) of secondary cyclone separator |
| 400 | 35.5 | 51.1 |
| 500 | 24.4 | 35.2 |
| 600 | 16.8 | 24.2 |
The particle size of the tobacco raw material is generally between 0.1mm and 0.5mm, the particle size distribution of coke generated by dry distillation is changed along with different reaction working conditions, but the particle size distribution of the coke is generally between 0.01mm and 0.1mm, and as can be seen from the table 2, the particle size of the coke separated by the first-stage separator is obviously larger than that separated by the second-stage separator.
TABLE 2
Claims (8)
1. A tobacco leaf raw fluidized bed dry distillation product filtering system is characterized in that the filtering system comprises two cyclone separation units, the two cyclone separation units comprise a first-stage cyclone separation unit and a second-stage cyclone separation unit,
the first stage cyclonic separating unit comprises: the first-stage cyclone separator is provided with a first-stage cyclone separation cylinder body, and the first-stage cyclone separation cylinder body is provided with a flue gas inlet for flue gas to enter, an air outlet for flue gas to be discharged and a slag discharge port for coke to be discharged from the bottom of the first-stage cyclone separation cylinder body; the first-stage cache tank is communicated and connected with the deslagging port at the bottom of the first-stage cyclone separation barrel body and is used for storing the separated coke, and the temperature of the first-stage cache tank is controlled to be more than 350 ℃;
a first-stage collection tank which is communicated with the bottom of the buffer tank to collect coke discharged from the first-stage buffer tank, wherein the first-stage collection tank is provided with a cooling module for cooling the coke and an exhaust module for exhausting air in the first-stage collection tank;
the flue gas air inlet of the second-stage cyclone separation unit is connected with the air outlet of the first-stage cyclone separation unit through a pipeline, and the pipeline can actively keep the temperature of fluid to 600 ℃.
2. The tobacco leaf feed fluidized bed dry distillation product filtering system according to claim 1, wherein the filtering system is used for separating particles with a particle size of 10 micrometers-1 mm.
3. The tobacco leaf raw material fluidized bed dry distillation product filtering system as claimed in claim 1, wherein the air flow velocity at the inlet of the first stage cyclone separation unit is 16 to 35m/s, and the air flow velocity at the inlet of the second stage cyclone separation unit is 24 to 51m/s.
4. The tobacco leaf feed fluidized bed retort product filtering system according to claim 1, wherein the second stage cyclone separation unit comprises a second buffer tank exterior, and a heating module is arranged outside the second buffer tank to control the temperature of the second buffer tank to be above 350 ℃.
5. The tobacco leaf feed fluidized bed retort product filtering system according to claim 1, wherein the top of the first-stage buffer tank is communicated with the first-stage cyclone separation cylinder body through an inlet valve, and the bottom of the first-stage buffer tank is communicated with the first-stage collection tank through an outlet valve; the upside and the downside of first order buffer tank are equipped with material level indicator and unloading level indicator respectively, material level indicator with import valve control connection goes up the material level indicator with outlet valve control connection.
6. The tobacco leaf raw fluidized bed dry distillation product filtering system according to claim 1, wherein the flue gas inlet of the first-stage cyclone separator is arranged at the top end of the side surface of the first-stage cyclone separation cylinder, and a gradual change pipeline is formed at an inlet section of the first-stage cyclone separation cylinder communicated with the flue gas inlet.
7. The tobacco leaf feed fluidized bed retort product filtration system of claim 1, wherein the first stage collection tank is provided with a window.
8. A multi-stage cyclone separation process for dry distillation products of tobacco aroma components, which is characterized in that the multi-stage cyclone separation process adopts the filtering system of any one of claim 2~7, and comprises the following steps: after the tobacco is subjected to dry distillation by the fluidized bed, pyrolysis products mixed with coke enter the two cyclone separation units successively, when no solid material is detected by the material level meter, the inlet valve of the first-stage cache tank is opened, and the outlet valve is closed; when the coke is accumulated to the position of the material loading level indicator, the inlet valve is automatically closed, and the outlet valve is opened, so that the solid coke in the first-level cache tank is smoothly discharged into the first-level collecting tank; when the material is discharged below the blanking level gauge, the outlet valve is closed, and the inlet valve is opened; the automatic operation is circulated in the way.
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| 流化床式木质生物质快速热解焦油的净化研究;李进等;《科协论坛(下半月)》;20111125(第11期);全文 * |
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