CN110591767A - Tar condenser, tar condensing system and tar condensing method - Google Patents
Tar condenser, tar condensing system and tar condensing method Download PDFInfo
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- CN110591767A CN110591767A CN201910892062.0A CN201910892062A CN110591767A CN 110591767 A CN110591767 A CN 110591767A CN 201910892062 A CN201910892062 A CN 201910892062A CN 110591767 A CN110591767 A CN 110591767A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
- C10K1/046—Reducing the tar content
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Abstract
The invention discloses a tar condenser, a tar condensing system and a tar condensing method. The tube bundle of the tar condenser is positioned in the shell and sequentially penetrates through the pretreatment chamber, the steam superheating chamber, the evaporation chamber and the oil-gas separation chamber, the top of the tube bundle is spaced from the inner wall of the top of the pretreatment chamber, and the distance from the top of the tube bundle to the bottom of the pretreatment chamber is 50-100 d; the pretreatment chamber is provided with an air inlet pipe; the steam superheating chamber is provided with a saturated steam inlet and a superheated steam outlet; the evaporation chamber is provided with a water inlet pipe and a saturated steam outlet; the saturated steam outlet is communicated with the saturated steam inlet; the oil-gas separation chamber is provided with an air outlet pipe and a coke outlet oil pipe; the tar condenser is also provided with a differential pressure transmitter for measuring the differential pressure before and after the oil-containing pyrolysis gas enters the tube bundle, and transmits a differential pressure signal to the differential pressure controller; the pressure difference controller acts on a flow actuator arranged on the water inlet pipe to maintain the pressure difference to be (1-1.5) p. The tar condenser, the tar condensing system and the tar condensing method are resistant to blockage.
Description
Technical Field
The invention relates to a tar condenser, a tar condensing system and a tar condensing method.
Background
The energy reserve structure of China is rich coal, less gas and lean oil, and the poly-generation technology that low-cost gas and tar are obtained by first pyrolysis and the rest semicoke is sent to a boiler for combustion and power generation is adopted, so that the resource utilization level and the utilization value of coal are greatly improved, and the shortage of oil gas supply of China is relieved.
The oil-gas separation process of high-temperature oil-containing pyrolysis gas is one of key technologies for preparing pyrolysis tar and fuel gas, wherein a tar condenser is key equipment of a system, and the long-period operation of the system is directly influenced by the operation state of the tar condenser. At present, after dust removal processes such as whirlwind, cloth bag, electric trapping are carried out to the dusty oily high-temperature pyrolysis gas produced from the pyrolysis furnace, tar is generally recovered by directly spraying process condensation, separation of fuel gas and tar is realized, and then recovery of tar is realized.
However, due to the complex tar components and wide molecular weight distribution, the oil classification and heat cascade recovery cannot be realized by using a conventional single-stage condenser. In addition, because different components of tar have great difference in mobility in the condensation process, the single-stage condenser is blocked in operation, and the normal operation of the oil-gas separation process is seriously influenced.
The inventor of the present invention has found in research that if the existing multi-stage shell and tube condenser is adopted, a plurality of cooling mediums are required to be adopted. In addition, the oil-containing pyrolysis gas flows through the tube pass, and the cooling medium flows through the shell pass, so that the temperature of the inner wall surface of the tube array is equal to that of the cooling medium, and thus, the temperature of tar contacting with the inner wall surface of the tube array is equal to that of the cooling medium, and further, the liquidity of the tar is deteriorated, and the blocking phenomenon is caused.
Disclosure of Invention
The invention aims to overcome the defect that the existing single-stage condenser and multi-stage condenser can cause blockage when used for condensing oil-containing pyrolysis gas, and provides a novel tar condenser, a tar condensing system and a tar condensing method. The tar condenser, the tar condensing system and the tar condensing method are resistant to blockage, and only one cooling medium is used. In addition, the tar condenser of the invention has simple structure; the tar condensation system and the tar condensation method can realize grading and heat gradient recovery of oil products.
The tar condenser of the invention essentially realizes pipeline blockage by adjusting the heat exchange area of cold and hot fluid in an evaporation chamber. In the prior art, for a specific device, when the blockage is faced, a person skilled in the art usually adjusts the flow rate and the temperature of the cold fluid and the hot fluid to solve the blockage without changing the heat exchange area. However, the method of adjusting the flow rate and temperature of the cold fluid and the hot fluid is not only complicated, but also can solve the problem of blockage only after the blockage occurs, and cannot act in advance to avoid the blockage when the blockage does not occur like the method of the present invention.
The invention solves the technical problems through the following technical scheme:
the invention provides a tar condenser, which comprises a shell and a tube bundle; the interior of the shell is sequentially divided into a pretreatment chamber, a steam overheating chamber, an evaporation chamber and an oil-gas separation chamber by partition plates from top to bottom; the tube bundle is positioned in the shell and sequentially penetrates through the pretreatment chamber, the steam superheating chamber, the evaporation chamber and the oil-gas separation chamber, the top of the tube bundle is spaced from the inner wall of the top of the pretreatment chamber, the distance between the top of the tube bundle and the bottom of the pretreatment chamber is 50d-100d, and d is the nominal diameter of each tube of the tube bundle; the pretreatment chamber is provided with an air inlet pipe for inputting oil-containing pyrolysis gas; the steam superheating chamber is provided with a saturated steam inlet and a superheated steam outlet; the evaporation chamber is provided with a water inlet pipe and a saturated steam outlet which are used for inputting boiler water; the saturated steam outlet is communicated with the saturated steam inlet; the oil-gas separation chamber is provided with an air outlet pipe for outputting purified gas and a tar outlet pipe for outputting tar; the tar condenser is also provided with a differential pressure transmitter which is used for measuring the differential pressure of the oily pyrolysis gas before entering the tube array bundle and after exiting the tube array bundle and transmitting a differential pressure signal to a differential pressure controller; the pressure difference controller acts on a flow executing mechanism arranged on the water inlet pipe to adjust the flow of boiler water entering the evaporation chamber and maintain the pressure difference to be (1-1.5) p, wherein p is the pressure difference of the oily pyrolysis gas measured by the pressure difference transmitter before entering the tube bundle and after exiting the tube bundle during normal operation.
The tar condenser described above can be used to treat an oily pygas as is conventional in the art (i.e., an oily pygas containing high, medium and low boiling range tars).
In the present invention, preferably, the top of the row of tube bundles is at a distance of 50d to 75d, more preferably 75d, from the bottom of the pretreatment chamber.
In the invention, the tar condenser is preferably provided with a sewage discharge pipeline, and the sewage discharge pipeline is arranged on the side wall of the bottom of the pretreatment chamber.
In the present invention, the saturated steam inlet is preferably provided on the bottom side wall of the steam superheating chamber, and the superheated steam outlet is preferably provided on the top side wall of the steam superheating chamber.
In the present invention, preferably, the pressure difference controller acts on a flow actuator provided on the water inlet pipe to regulate the flow of boiler water into the evaporation chamber and maintain the pressure difference at (1-1.2) p, more preferably p.
In the present invention, the pressure difference controller preferably further has functions of displaying and alarming.
In the invention, the water inlet of the water inlet pipe is preferably arranged on the side wall of the bottom of the evaporation chamber, and the saturated steam outlet is preferably arranged on the side wall of the top of the evaporation chamber.
In the invention, the evaporation chamber can be also provided with a liquid level meter which is used for measuring the liquid level of the evaporation chamber and transmitting a liquid level signal to a liquid level indicating alarm.
In the invention, preferably, the water inlet pipe is also provided with a flow meter and a flow indication alarm.
In the invention, preferably, the lower part of the oil-gas separation chamber is a tar storage area, the bottom of the tube bundle extends to the tar storage area, and the gas outlet of the gas outlet pipe is positioned above the tar storage area. Therefore, the gas discharged from the bottom of the tube bundle is washed by the tar storage area and then discharged from the gas outlet and the gas outlet pipe. Preferably, the oil-gas separation chamber is further provided with a liquid level meter, the liquid level meter is used for measuring the liquid level of the oil-gas separation chamber and transmitting a liquid level signal to the liquid level indication control alarm to control the liquid level to be higher than the bottom of the tube bundle.
In the invention, preferably, a flow meter and a flow indication alarm are further arranged on the coke discharging oil pipe.
In the invention, preferably, the air outlet pipe is further provided with a thermometer and a temperature indicating alarm.
The invention also provides a tar condensation system, which comprises a plurality of tar condensers connected in series. The tar condensing system can respectively obtain tar with different distillation ranges.
In the present invention, the number of the tar condenser may be, for example, 2 to 4 or 3.
In the invention, the series connection means that the air outlet pipe of the tar condenser of the previous stage is communicated with the air inlet pipe of the tar condenser of the next stage.
The invention also provides a tar condensation system, which comprises a tar condenser I, a tar condenser II and a tar condenser III which are arranged in series; the tar condenser I is the tar condenser, and the tar condenser II is not provided with the steam superheating chamber on the basis of the tar condenser I; the tar condenser III is not provided with the steam superheating chamber and the evaporation chamber on the basis of the tar condenser I.
In the invention, the series connection means that the air outlet pipe of the tar condenser I is communicated with the air inlet pipe of the tar condenser II, and the air outlet pipe of the tar condenser II is communicated with the air inlet pipe of the tar condenser III.
The invention also provides a tar condensation method adopting the tar condensation system, which is characterized in that the oily pyrolysis gas is fed from the gas inlet pipe of the first-stage tar condenser, and the oily pyrolysis gas flows out from the gas outlet pipe of the last-stage tar condenser.
When the number of the tar condensers of the tar condensing system is 3, the temperature of the gas in the gas outlet pipe of the first-stage tar condenser is controlled to be preferably 350-500 ℃, and more preferably 450 ℃. The temperature of the gas in the gas outlet pipe of the second-stage tar condenser is controlled to be preferably 200-300 ℃, and more preferably 250 ℃. The temperature of the gas in the gas outlet pipe of the third-stage tar condenser is controlled to be preferably 50-200 ℃, and more preferably 150 ℃.
When the number of the tar condensers of the tar condensing system is 3, preferably, the temperature of the gas in the gas outlet pipe of the first-stage tar condenser is controlled to be 450 ℃; controlling the temperature of gas in an air outlet pipe of the second-stage tar condenser to be 250 ℃; the temperature of the gas in the outlet pipe of the third stage tar condenser is controlled to be 150 ℃.
The above preferred conditions can be arbitrarily combined to obtain preferred embodiments of the present invention without departing from the common general knowledge in the art.
The reagents and starting materials used in the present invention are commercially available.
The positive progress effects of the invention are as follows: the tar condenser and the tar condensing system are resistant to blockage, and only one cooling medium is used. In addition, the tar condenser of the invention has simple structure; the tar condensation system and the tar condensation method can realize grading and heat gradient recovery of oil products.
Drawings
FIG. 1 is a schematic structural diagram of a tar condenser according to an embodiment of the present invention.
FIG. 2 is a schematic structural diagram of a tar condensing system according to an embodiment of the present invention.
Description of reference numerals:
housing 10
Pretreatment chamber 101
Steam superheating chamber 102
Evaporation chamber 103
Oil-gas separation chamber 104
Tube bundle 20
Intake pipe 30
Air outlet pipe 40
Coke discharging oil pipe 50
Differential pressure transmitter 60
Pressure difference controller 70
Flow actuator 80
Liquid level meter 90
Liquid level indicating alarm 100
Level indicating control alarm 110
Flow meter 120
Flow indicator alarm 130
Thermometer 140
Temperature indicating alarm 150
Tar condenser I160
Tar condenser II 170
Tar condenser III180
Detailed Description
The invention is further illustrated by the following examples, which are not intended to limit the scope of the invention. The experimental methods without specifying specific conditions in the following examples were selected according to the conventional methods and conditions, or according to the commercial instructions.
Generally, the oil-containing pyrolysis gas contains about 10% of tar (coal-based), and this value means that the tar in the oil-containing pyrolysis gas accounts for 10% by mass of the coal from which the oil-containing pyrolysis gas is generated; in the following examples, the yield of tar (coal-based) with a high distillation range (boiling point >450 ℃) means that the obtained tar with a high distillation range accounts for the mass percentage of the coal generating the oil-containing pyrolysis gas; the yield of tar (coal base) in the middle distillation range (the boiling point is more than 250 ℃ and less than or equal to 450 ℃) refers to the mass percentage of the obtained middle distillation range tar in the coal generating the oil-containing pyrolysis gas; the yield of tar (coal base) with low distillation range (the boiling point is more than 150 ℃ and less than or equal to 250 ℃) means that the obtained tar with the middle distillation range accounts for the mass percent of the coal generating the oil-containing pyrolysis gas; the yield of tar (coal base) of light oil (the boiling point is more than 50 ℃ and less than or equal to 150 ℃) means that the obtained light oil accounts for the mass percent of the coal generating the oil-containing pyrolysis gas.
TABLE 1 Properties of the feed coal
Example 1
(1) Tar condenser
A tar condenser as shown in fig. 1, the tar condenser includes a shell 10 and a tube bundle 20; the interior of the shell 10 is sequentially divided into a pretreatment chamber 101, a steam overheating chamber 102, an evaporation chamber 103 and an oil-gas separation chamber 104 from top to bottom; the tube bundle 20 is positioned in the shell 10, the tube bundle 20 sequentially penetrates through the pretreatment chamber 101, the steam superheating chamber 102, the evaporation chamber 103 and the oil-gas separation chamber 104, the top of the tube bundle 20 is spaced from the inner wall of the top of the pretreatment chamber 101, the distance between the top of the tube bundle 20 and the bottom of the pretreatment chamber 101 is 75d, and d is the nominal diameter of each tube of the tube bundle 20; the pretreatment chamber 101 is provided with an air inlet pipe 30 for inputting oil-containing pyrolysis gas; the steam overheating chamber 102 is provided with a saturated steam inlet and a superheated steam outlet; the evaporation chamber 103 is provided with a water inlet pipe for inputting boiler water and a saturated steam outlet; the saturated steam outlet is communicated with the saturated steam inlet; the oil-gas separation chamber 104 is provided with an air outlet pipe 40 for outputting purified gas and a tar outlet pipe 50 for outputting tar; the tar condenser is also provided with a differential pressure transmitter 60, and the differential pressure transmitter 60 is used for measuring the differential pressure of the oil-containing pyrolysis gas before entering the tube bundle 20 and after exiting the tube bundle 20 and transmitting a differential pressure signal to the differential pressure controller 70; the pressure differential controller 70 acts on a flow actuator 80 provided on the inlet line to regulate the flow of boiler water into the evaporation chamber 103 and maintain a pressure differential p, where p is the pressure differential measured by the pressure differential transmitter 60 before the oily pyrolysis gas enters the tube bundle 20 and after the oily pyrolysis gas exits the tube bundle 20 during normal operation.
Wherein, the tar condenser is provided with a sewage pipeline which is arranged on the side wall of the bottom of the pretreatment chamber 101.
Wherein, the saturated steam inlet is arranged on the bottom side wall of the steam superheating chamber 102, and the superheated steam outlet is arranged on the top side wall of the steam superheating chamber 102.
The pressure difference controller 70 also has display and alarm functions.
Wherein, the water inlet of the water inlet pipe is arranged on the bottom side wall of the evaporation chamber 103, and the saturated steam outlet is arranged on the top side wall of the evaporation chamber 103.
Wherein, evaporation chamber 103 is still provided with level gauge 90, and level gauge 90 is used for determining evaporation chamber 103's liquid level, and sends the liquid level signal to liquid level indicator alarm 100.
Wherein, the water inlet pipe is also provided with a flowmeter 120 and a flow indicating alarm 130.
Wherein, the lower part of the oil-gas separation chamber 104 is a tar storage area, the bottom of the tube bundle 20 extends to the tar storage area, and the gas outlet of the gas outlet tube 40 is positioned above the tar storage area. The oil-gas separation chamber 104 is also provided with a liquid level meter 90, and the liquid level meter 90 is used for measuring the liquid level of the oil-gas separation chamber 104 and transmitting a liquid level signal to a liquid level indication control alarm 110 so as to control the liquid level to be higher than the bottom of the tube bundle 20.
Wherein, the coke discharging oil pipe 50 is also provided with a flowmeter 120 and a flow indicating alarm 130.
Wherein, the outlet pipe 40 is also provided with a thermometer 140 and a temperature indicating alarm 150.
(2) Tar condensing system
As shown in fig. 2, the tar condensing system includes 3 tar condensers, which are respectively marked as tar condenser I160, tar condenser II 170 and tar condenser III180 (the control systems of tar condenser I, tar condenser II and tar condenser III are not shown, and the control system refers to fig. 1); the air outlet pipe of the tar condenser I is communicated with the air inlet pipe of the tar condenser II, and the air outlet pipe of the tar condenser II is communicated with the air inlet pipe of the tar condenser III.
(3) Tar condensation method
A tar condensation method adopting the tar condensation system is characterized in that the oily pyrolysis gas flowing out of a certain circulating fluidized bed is fed in from the air inlet pipe of a tar condenser I and flows out from the air outlet pipe of a tar condenser III; wherein, the temperature of the gas in the gas outlet pipe of the tar condenser I is controlled to be 450 ℃, the temperature of the gas in the gas outlet pipe of the tar condenser II is controlled to be 250 ℃, and the temperature of the gas in the gas outlet pipe of the tar condenser III is controlled to be 150 ℃.
Wherein the coal quality data of the oil-containing pyrolysis gas flowing out of a certain circulating fluidized bed is shown in Table 1The pyrolysis temperature is 600 ℃, the coal processing amount is 2000 t/day, and the yield of the pyrolysis gas is 23000Nm3The temperature of boiler water supplemented into the system is 104 ℃.
The technical effects are as follows: the tar condenser, the tar condensing system and the tar condensing method in example 1 were not clogged during the operation, and the tar condensing system and the tar condensing method in example 1 were used to separate high-distillation range, medium-distillation range and low-distillation range tars and to co-produce high-pressure, medium-pressure and low-pressure superheated steam.
Effect data:
example 2
(1) Tar condenser
As shown in FIG. 1, the tar condenser was constructed in such a manner that the top of the tube bundle 20 was spaced from the bottom of the pretreatment chamber 101 by 50d, and the pressure difference controller 70 was operated on the flow actuator 80 provided on the inlet pipe to adjust the flow rate of the boiler water into the evaporation chamber 103 and maintain the pressure difference at 1.2p, as in the tar condenser of example 1.
(2) Tar condensing system
As shown in FIG. 2, the tar condensing system includes 3 tar condensers connected in series, and the rest is the same as the tar condensing system of example 1.
(3) Tar condensation method
A tar condensing method using the tar condensing system, and the rest of the method is the same as the tar condensing method of example 1.
The technical effects are as follows: the tar condenser, the tar condensing system and the tar condensing method in example 2 were not clogged during the operation, and the tar condensing system and the tar condensing method in example 2 were used to separate high-distillation range, medium-distillation range and low-distillation range tars, and high-pressure, medium-pressure and low-pressure superheated steam was obtained as byproducts.
Effect data:
example 3
(1) Tar condenser
As shown in FIG. 1, the tar condenser is similar to that of example 1 in that the top of the tube bundle 20 is spaced from the bottom of the pretreatment chamber 101 by a distance of 100d, and the pressure difference controller 70 is operated on the flow actuator 80 provided on the water inlet tube to adjust the flow rate of the boiler water into the evaporation chamber 103 and maintain the pressure difference at 1.5 p.
(2) Tar condensing system
As shown in FIG. 2, the tar condensing system includes 3 tar condensers connected in series, and the rest is the same as the tar condensing system of example 1.
(3) Tar condensation method
A tar condensing method using the tar condensing system, and the rest of the method is the same as the tar condensing method of example 1.
The technical effects are as follows: the tar condenser, the tar condensing system, and the tar condensing method in example 3 were not clogged during the operation, and the tar condensing system and the tar condensing method in example 3 separated high-distillation range, medium-distillation range, and low-distillation range tars, and high-pressure, medium-pressure, and low-pressure superheated steam was obtained as byproducts.
Effect data:
while specific embodiments of the invention have been described above, it will be appreciated by those skilled in the art that this is by way of example only, and that the scope of the invention is defined by the appended claims. Various changes and modifications to these embodiments may be made by those skilled in the art without departing from the spirit and scope of the invention, and these changes and modifications are within the scope of the invention.
Claims (10)
1. The tar condenser is characterized by comprising a shell and a tube bundle; the interior of the shell is sequentially divided into a pretreatment chamber, a steam overheating chamber, an evaporation chamber and an oil-gas separation chamber from top to bottom; the tube bundle is positioned in the shell and sequentially penetrates through the pretreatment chamber, the steam superheating chamber, the evaporation chamber and the oil-gas separation chamber, the top of the tube bundle is spaced from the inner wall of the top of the pretreatment chamber, the distance between the top of the tube bundle and the bottom of the pretreatment chamber is 50d-100d, and d is the nominal diameter of each tube of the tube bundle; the pretreatment chamber is provided with an air inlet pipe for inputting oil-containing pyrolysis gas; the steam superheating chamber is provided with a saturated steam inlet and a superheated steam outlet; the evaporation chamber is provided with a water inlet pipe and a saturated steam outlet which are used for inputting boiler water; the saturated steam outlet is communicated with the saturated steam inlet; the oil-gas separation chamber is provided with an air outlet pipe for outputting purified gas and a tar outlet pipe for outputting tar; the tar condenser is also provided with a differential pressure transmitter which is used for measuring the differential pressure of the oily pyrolysis gas before entering the tube array bundle and after exiting the tube array bundle and transmitting a differential pressure signal to a differential pressure controller; the pressure difference controller acts on a flow executing mechanism arranged on the water inlet pipe to adjust the flow of boiler water entering the evaporation chamber and maintain the pressure difference to be (1-1.5) p, wherein p is the pressure difference of the oily pyrolysis gas measured by the pressure difference transmitter before entering the tube bundle and after exiting the tube bundle during normal operation.
2. The tar condenser of claim 1, wherein the top of the row of tube bundles is located between 50d and 75d from the bottom surface of the pretreatment chamber;
and/or the tar condenser is provided with a sewage discharge pipeline, and the sewage discharge pipeline is arranged on the side wall of the bottom of the pretreatment chamber.
3. The tar condenser of claim 1, wherein the saturated steam inlet is disposed in a bottom sidewall of the steam superheating chamber and the superheated steam outlet is disposed in a top sidewall of the steam superheating chamber.
4. The tar condenser of claim 1 or 2, wherein said pressure differential controller acts on a flow actuator provided on said water inlet conduit to regulate the flow of boiler water into said evaporation chamber and maintain said pressure differential at (1-1.2) p;
and/or the pressure difference controller also has the functions of displaying and alarming;
and/or the water inlet of the water inlet pipe is arranged on the side wall of the bottom of the evaporation chamber, and the saturated steam outlet is arranged on the side wall of the top of the evaporation chamber;
and/or the evaporation chamber is also provided with a liquid level meter, and the liquid level meter is used for measuring the liquid level of the evaporation chamber and transmitting a liquid level signal to a liquid level indicating alarm;
and/or, still be equipped with the flowmeter and flow indication alarm on the inlet tube.
5. The tar condenser as claimed in claim 1, wherein the lower part of the oil-gas separation chamber is a tar storage area, the bottom of the tube bundle extends to the tar storage area, and the gas outlet of the gas outlet pipe is located above the tar storage area.
6. The tar condenser of claim 5, wherein the oil-gas separation chamber is further provided with a level gauge for measuring a liquid level in the oil-gas separation chamber and transmitting a liquid level signal to a level indicating control alarm to control the liquid level to be higher than the bottom of the tube bundle.
7. The tar condenser as claimed in claim 1, wherein the tar outlet pipe is further provided with a flow meter and a flow indication alarm;
and/or a thermometer and a temperature indication alarm are further arranged on the air outlet pipe.
8. A tar condensing system, comprising a plurality of tar condensers according to any of claims 1 to 7 arranged in series; the number of the tar condensers is preferably 2 to 4, more preferably 3.
9. The tar condensation system is characterized by comprising a tar condenser I, a tar condenser II and a tar condenser III which are connected in series; wherein the tar condenser I is the tar condenser according to any one of claims 1 to 7, and the tar condenser II is not provided with the steam superheating chamber in addition to the tar condenser I; the tar condenser III is not provided with the steam superheating chamber and the evaporation chamber on the basis of the tar condenser I.
10. A tar condensing method, characterized in that the tar condensing method adopts the tar condensing system of claim 8 or 9, and the oil-containing pyrolysis gas is fed from the gas inlet pipe of the first stage tar condenser and flows out from the gas outlet pipe of the last stage tar condenser.
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| CN201910892062.0A CN110591767A (en) | 2019-09-20 | 2019-09-20 | Tar condenser, tar condensing system and tar condensing method |
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| CN201910892062.0A CN110591767A (en) | 2019-09-20 | 2019-09-20 | Tar condenser, tar condensing system and tar condensing method |
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