CN112158844A - System and process for preparing powdery active coke for desulfurization by three-stage furnace two-step method - Google Patents
System and process for preparing powdery active coke for desulfurization by three-stage furnace two-step method Download PDFInfo
- Publication number
- CN112158844A CN112158844A CN202011060136.3A CN202011060136A CN112158844A CN 112158844 A CN112158844 A CN 112158844A CN 202011060136 A CN202011060136 A CN 202011060136A CN 112158844 A CN112158844 A CN 112158844A
- Authority
- CN
- China
- Prior art keywords
- furnace
- activation
- coke
- gas
- combustion
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/30—Active carbon
- C01B32/39—Apparatus for the preparation thereof
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a system and a process for preparing powdery active coke for desulfurization by a three-section furnace two-step method, wherein the system comprises a combustion furnace, a carbonization furnace, an activation furnace and a powdery coke cyclone separator; the device comprises a combustion furnace and an activation furnace which are both vertically arranged, wherein a combustion coal powder inlet of the combustion furnace is arranged at the top, a smoke outlet of the combustion furnace is arranged at the bottom, a gas-phase inlet of the activation furnace is arranged at the bottom, a carbonized semicoke inlet of the activation furnace is arranged on the side wall of the lower part, an outlet of the activation furnace is arranged at the upper part, and the gas-phase inlet of the activation furnace is provided with a steam tempering nozzle and/or an air tempering nozzle; the flue gas outlet of the combustion furnace is connected with the gas-phase inlet of the activation furnace, the outlet of the activation furnace is connected with the inlet of the fine coke cyclone separator, the gas-phase outlet of the fine coke cyclone separator is connected with the gas-phase inlet of the carbonization furnace, the solid-phase outlet of the carbonization furnace is connected with the carbonization semi-coke inlet of the activation furnace, and the solid-phase inlet of the carbonization furnace is connected with the coking coal powder source. The invention fully utilizes the medium-high temperature grade waste heat, and simultaneously greatly improves the yield and the adsorption performance of the coke breeze.
Description
Technical Field
The invention relates to a system and a process for preparing powdery active coke for desulfurization by a three-stage furnace two-step method.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
Coal is the main power of energy consumption in China, about 70 percent of coal consumption is directly used for combustion, and SO is inevitably discharged during coal combustion2At present, the most widely applied flue gas desulfurization technology is calcium-based wet desulfurization technology, but the water consumption is high, so that limestone resources are over exploited, and CO is increased2The discharge, the generation of excessive desulfurized gypsum and the secondary pollution caused by the desulfurized wastewater, and the application of the desulfurized gypsum and the desulfurized wastewater is increasingly limited. The active coke desulfurization technology in the dry flue gas desulfurization technology basically does not consume water, does not generate waste water and waste residue, does not have the problem of secondary pollution, can realize the resource recycling of sulfur, and is a green desulfurization technology capable of realizing the resource recycling of sulfur.
At present, sulfur resources recovered by an active coke flue gas desulfurization technology are mainly sulfuric acid solutions, the sulfur resources are mainly used in the steel and metallurgy industries and cannot be widely popularized and applied due to the fact that the investment and the operation cost are high, the steel and metallurgy industries need to consume sulfuric acid, and the sulfur resources can be mainly applied to the steel and metallurgy industries and can offset part of the investment and the operation cost due to the recovered sulfuric acid solutions. One of the reasons for higher investment and operation costs is that the active coke adsorbent is higher in preparation cost, and currently, the active coke for flue gas desulfurization is columnar active coke with the diameter of 5-9 mm, and the preparation process is complex, so that the preparation cost is high and the market price is high; in addition, the utilization rate of the inner surface is low, so that the adsorption performance is poor, and the running cost is increased.
In order to reduce the production cost of the activated coke for desulfurization and improve the adsorption performance thereof, the inventors have proposed the rapid production of powdered activated coke for flue gas desulfurization in "a rapid production apparatus and method of powdered activated coke" of patent No. CN 104787761A. The inventor researches and discovers that the process is feasible, but the process has the defect of low heat utilization rate, high-temperature gas (about 900 ℃) after the coke breeze preparation is finished belongs to a medium-high temperature grade heat source, the coke breeze yield is low, and the coke breeze performance needs to be improved.
Disclosure of Invention
In order to solve the defects of the prior art, the invention aims to provide a system and a process for preparing powdery active coke for desulfurization by a three-stage furnace two-step method.
In order to achieve the purpose, the technical scheme of the invention is as follows:
on the one hand, the system for preparing powdery active coke for desulfurization by a three-section furnace two-step method comprises a combustion furnace, a carbonization furnace, an activation furnace and a powdered coke cyclone separator;
the device comprises a combustion furnace and an activation furnace, wherein the combustion furnace and the activation furnace are both vertically arranged, a combustion coal powder inlet of the combustion furnace is arranged at the top of the combustion furnace, a smoke outlet of the combustion furnace is arranged at the bottom of the combustion furnace, a gas-phase inlet of the activation furnace is arranged at the bottom of the activation furnace, a carbonized semicoke inlet of the activation furnace is arranged on the side wall of the lower part of the activation furnace, an outlet of the activation furnace is arranged at the upper part of the activation furnace, and the gas-phase inlet of the activation furnace;
the flue gas outlet of the combustion furnace is connected with the gas-phase inlet of the activation furnace, the outlet of the activation furnace is connected with the inlet of the fine coke cyclone separator, the gas-phase outlet of the fine coke cyclone separator is connected with the gas-phase inlet of the carbonization furnace, the solid-phase outlet of the carbonization furnace is connected with the carbonization semi-coke inlet of the activation furnace, and the solid-phase inlet of the carbonization furnace is connected with the coking coal powder source.
According to research, the flue gas temperature of the powdery active coke prepared by one step by using the combusted flue gas is higher, the grade of the flue gas as a heat source is higher, and the powdery active coke can be used for multiple purposes. Tests show that when the flue gas separated by the original coke oven is reintroduced into new carbonization equipment, the new carbonization equipment can partially carbonize the pulverized coal source for coking by using the flue gas separated by the original coke oven to prepare semicoke, and the original coke oven only needs to be activated at the moment, namely the new carbonization equipment is introduced to be used as a carbonization furnace for carbonization, and the original coke oven is used as an activation furnace for activation, so that the process is changed, the process for preparing the powdery active coke by using the changed system not only improves the utilization rate of energy, but also obviously improves the yield of the prepared powdery active coke and the adsorption performance of sulfur dioxide.
On the other hand, a process for preparing powdery active coke for desulfurization by a three-stage furnace two-step method is provided with the system;
the method comprises the steps of combusting fuel coal powder in a combustion furnace to generate combustion flue gas, utilizing steam and/or air to conduct temperature regulation and tempering on the combustion flue gas at a gas phase inlet of an activation furnace, mixing the combustion flue gas after temperature regulation and tempering with carbonized carbocoal to prepare powdery active coke, separating a mixture of the powdery active coke and the flue gas at an outlet of the activation furnace through a coke powder cyclone separator to obtain powdery active coke and activation flue gas, and mixing the activation flue gas with the coking coal powder to prepare the carbonized carbocoal.
The invention has the beneficial effects that:
(1) the invention simultaneously adds the carbonization furnace to change the preparation process of the powdered coke, can fully utilize the waste heat in the original one-step method for quickly preparing the powdered coke, and improves the yield of the powdered coke by 1.5 to 2.5 times under the same combustion working condition of a combustion section.
(2) SO of the prepared coke breeze of the present invention2The adsorption performance can be improved by 10-30%, wherein the adsorption performance of the brown coal-based coke breeze can be improved by about 10%, and the adsorption performance of the bituminous coal-based coke breeze can be improved by 30%.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description serve to explain the invention and not to limit the invention.
FIG. 1 is a schematic structural diagram of a system for preparing powdery activated coke for desulfurization by a two-step process in a three-stage furnace according to example 1;
wherein, 1, burning coal powder; 2. combustion-supporting air for combustion; 3. a combustion furnace; 4. an ash hopper; 5. ash and slag; 6. water/steam tempering nozzles; 7. air/oxygen quenching and tempering nozzles; 8. an activation furnace; 9. a coke breeze cyclone; 10. finished product of powdery active coke; 11. preparing coking coal powder; 12. a carbonization furnace; 13. a carbonized carbocoal cyclone separator; 14. pyrolysis gas; 15. and (5) carbonizing the semicoke.
Detailed Description
It is to be understood that the following detailed description is exemplary and is intended to provide further explanation of the invention as claimed. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the invention. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
In view of the defects of low heat utilization rate, low coke breeze yield, poor coke breeze performance and the like in the conventional process for quickly preparing coke breeze, the invention provides a system and a process for preparing powdery active coke for desulfurization by a three-stage furnace two-step method.
The invention provides a system for preparing powdery active coke for desulfurization by a three-section furnace two-step method, which comprises a combustion furnace, a carbonization furnace, an activation furnace and a fine coke cyclone separator, wherein the combustion furnace is connected with the carbonization furnace;
the device comprises a combustion furnace and an activation furnace, wherein the combustion furnace and the activation furnace are both vertically arranged, a combustion coal powder inlet of the combustion furnace is arranged at the top of the combustion furnace, a smoke outlet of the combustion furnace is arranged at the bottom of the combustion furnace, a gas-phase inlet of the activation furnace is arranged at the bottom of the activation furnace, a carbonized semicoke inlet of the activation furnace is arranged on the side wall of the lower part of the activation furnace, an outlet of the activation furnace is arranged at the upper part of the activation furnace, and the gas-phase inlet of the activation furnace;
the flue gas outlet of the combustion furnace is connected with the gas-phase inlet of the activation furnace, the outlet of the activation furnace is connected with the inlet of the fine coke cyclone separator, the gas-phase outlet of the fine coke cyclone separator is connected with the gas-phase inlet of the carbonization furnace, the solid-phase outlet of the carbonization furnace is connected with the carbonization semi-coke inlet of the activation furnace, and the solid-phase inlet of the carbonization furnace is connected with the coking coal powder source.
The invention takes the original system for preparing the powdery active coke by the one-step method as the basis, introduces the new carbonization equipment as the carbonization furnace for carbonization, and takes the original coke oven as the activation furnace for activation, thereby changing the process.
The activation furnace is an upstream air-flow bed reactor.
In one or more embodiments of this embodiment, the carbonization furnace is vertically arranged, the gas-phase inlet and the solid-phase inlet of the carbonization furnace are both arranged at the top of the carbonization furnace, the solid-phase outlet of the carbonization furnace is arranged at the bottom of the carbonization furnace, and the gas-phase outlet of the carbonization furnace is arranged at the lower side wall of the carbonization furnace. The carbonization furnace is a descending airflow bed reactor.
In one or more embodiments of the embodiment, the carbonization furnace comprises a carbonization semicoke cyclone separator, a gas-phase outlet of the carbonization furnace is connected with an inlet of the carbonization semicoke cyclone separator, and a solid-phase outlet of the carbonization semicoke cyclone separator is connected with an inlet of the activation furnace.
In one or more embodiments, the system comprises an ash bucket, wherein a flue gas outlet of the combustion furnace is connected with a gas phase inlet of the ash bucket, and a gas phase outlet of the ash bucket is connected with a gas phase inlet of the activation furnace.
In one or more embodiments, the water vapor conditioning jets and/or the air conditioning jets are disposed at the ash hopper gas phase outlet.
The invention also provides a process for preparing the powdery active coke for desulfurization by a three-section furnace two-step method, and the system is provided;
the method comprises the steps of combusting fuel coal powder in a combustion furnace to generate combustion flue gas, utilizing steam and/or air to conduct temperature regulation and tempering on the combustion flue gas at a gas phase inlet of an activation furnace, mixing the combustion flue gas after temperature regulation and tempering with charring semi-coke to prepare powdery active coke, separating a mixture of the powdery active coke and the flue gas at an outlet of the activation furnace through a coke breeze cyclone separator to obtain powdery active coke and activation flue gas, and mixing the activation flue gas with coking coal powder to prepare the charring semi-coke.
In some examples of this embodiment, the pulverized fuel coal is combusted in a slagging liquid combustion mode in the furnace. The ash slag after combustion is discharged from the bottom in a liquid state as much as possible, so that the influence on the quality of the coke breeze product caused by the fact that the combustion fly ash enters the activation furnace and the carbonization furnace and is finally mixed into the coke breeze is reduced.
In some examples of this embodiment, the upward gas velocity in the activation furnace is 4 to 6 m/s. Ensuring that the airflow can carry the carbonized carbocoal to go upwards without collapsing the bed.
In some examples of the embodiment, the retention time of the carbonized carbocoal in the activation furnace is 3-7 s.
In some examples of this embodiment, the downward gas velocity in the carbonization furnace is 3 to 5 m/s. And ensuring that the coking coal powder stays in the section for 3-7 s to finish the fast pyrolysis and carbonization.
In some examples of the embodiment, the retention time of the coking coal powder in the carbonization furnace is 3-7 s.
In some examples of this embodiment, the temperature of the flue gas entering the activation furnace is 1100-1200 ℃.
In some examples of this embodiment, the volume concentration of oxygen in the flue gas entering the activation furnace is 4-8%.
In some examples of this embodiment, the volume concentration of water vapor in the flue gas entering the activation furnace is 15-35%.
In some examples of this embodiment, the temperature of the vapor phase outlet of the carbonization furnace is 600 to 700 ℃. Can effectively avoid the tar problem.
In order to make the technical solution of the present invention more clearly understood by those skilled in the art, the technical solution of the present invention will be described in detail below with reference to specific examples and comparative examples.
Example 1
A system for preparing powdery active coke for desulfurization by a three-stage furnace through a two-step method is shown in figure 1 and comprises three core devices: a (high temperature section) combustion furnace 3, a (middle temperature section) activation furnace 8 and a (low temperature section) carbonization furnace 12.
The high-temperature section combustion furnace 3 belongs to the existing common system, is in the form of a vertical pulverized coal combustion boiler, and mainly comprises a combustor, a furnace body and the like. Wherein, the burning adopts a liquid slag-off burning mode, so that ash slag burnt by the coal dust is discharged from the ash hopper 4 in a liquid state, and the influence on the quality of a final product caused by the mixture of the ash slag and the carbonized carbocoal in the preparation of the medium-temperature and low-temperature sections is avoided.
The medium-temperature section activation furnace 8 is an ascending entrained flow bed, the lower end of the medium-temperature section activation furnace is communicated with the high-temperature section combustion furnace through an ash hopper 4, and the upper end of the medium-temperature section activation furnace is communicated with a cyclone separator 9. Specifically, high-temperature flue gas from a high-temperature section combustion furnace enters a medium-temperature section activation furnace 8 after the temperature of the flue gas and the concentration of steam and oxygen in the flue gas are adjusted by a water/steam nozzle 6 and an air/oxygen nozzle 7 at an ash hopper 4, the high-temperature flue gas ascends together with carbonized semicoke 15 fed from the bottom of the medium-temperature section activation furnace to complete the rapid preparation of powdery activated coke, the powdery activated coke 10 is obtained after gas-solid separation by a cyclone separator 9, and the gas outlet end of the cyclone separator 9 enters a low-temperature section carbonization furnace 12.
The low-temperature section carbonization furnace 12 is a descending entrained flow bed, the upper end of the low-temperature section carbonization furnace is connected with the gas outlet end of the cyclone separator 9, the lower end of the low-temperature section carbonization furnace is connected with the carbonized carbocoal conveying pipeline through solid settling, and the lower end of the low-temperature section carbonization furnace is connected with the carbonized carbocoal cyclone separator 13 through a gas outlet. Specifically, high-temperature gas from the middle-temperature section activation furnace enters the low-temperature section activation furnace from the top, and is mixed with pulverized coal 11 fed from the top and flows downwards together to complete the rapid pyrolysis of the pulverized coal and prepare the precursor carbonized carbocoal for activation.
Specifically, the furnace body structure of the high-temperature section combustion furnace 3 can be provided with a water-cooling unheated surface, the combustion mode of liquid slag discharge is ensured on the premise that the temperature of the outlet smoke is controlled to be 100-150 ℃ above the ash melting point of the used coal. If the water wall heating surface is arranged, part of the generated steam can be used for the water/steam nozzle 6 to adjust the flue gas entering the low-temperature section gasification furnace 8, and the rest is used for external supply.
Specifically, the high-temperature section combustion furnace 3 and the medium-temperature section activation furnace 8 are connected by an ash hopper 4, and the two sections are arranged in a U shape.
Specifically, after the flue gas from the high-temperature section combustion furnace 3 is subjected to temperature regulation and tempering in an ash hopper, the temperature of the flue gas entering the medium-temperature section activation furnace 8 is controlled to be 1100-1200 ℃, the oxygen concentration in the flue gas can be regulated to be 4-8%, and the water vapor concentration can be regulated to be 15-35%.
Specifically, the retention time of the carbonized carbocoal 15 in the medium-temperature section activation furnace 8 is 3-7 s, and the preparation of the powdered coke is rapidly completed in the smoke atmosphere after temperature adjustment and tempering.
Specifically, the retention time of the pulverized coal 11 for coke making in the low-temperature section carbonization furnace 12 is 3-7 s, and the pulverized coal pyrolysis carbonization is rapidly completed by using the high-temperature gas after the activation of the carbonized carbocoal to prepare the carbonized carbocoal.
Specifically, the final gas outlet pyrolysis gas 14 is directly sent to an incinerator/boiler for combustion, so as to completely eliminate the tar problem, and the used follow-up equipment and process are the conventional equipment and process.
In a one-dimensional settling furnace test system, firstly, controlling the reaction temperature at 750 ℃ for 4s in a pure nitrogen atmosphere, and feeding the soft coal at 2.5g/min to prepare about 500g of carbonized carbocoal; then, the carbonized semicoke is taken as a raw material, and in the system, the reaction temperature is 950 ℃, and the reaction temperature is measured under the condition of simulating smoke (6 percent of O)2，12％CO2，20％H2O，62％N2) In the atmosphere, the retention time is controlled to be 4s, the feeding amount is 5.0g/min, and the powdery active coke of the two-step method is prepared. The specific surface area of the active coke prepared by the process is 291m2The sulfur capacity of the fixed bed in two hours is 73.79mg/g, and the coke yield is about 2.38 g/min.
As a comparison, the Jinqian bituminous coal was used as a raw material, and the reaction temperature was 950 ℃ in a one-dimensional settling furnace test system under simulated flue gas (6% O)2，12％CO2，20％H2O，62％N2) In the atmosphere, the retention time is controlled to be 4s, the coal feeding amount is controlled to be 2.5g/min, and the one-step preparation of the powdery active coke of the coal powder in the flue gas atmosphere is directly completed. The specific surface of the active coke prepared by the process is 213m2The sulfur capacity of the fixed bed in two hours is 55.56mg/g, and the coke yield is about 1.23 g/min. The comparison shows that the specific surface area of the powdery active coke prepared by the two-step method is improved by 36.6 percent, the sulfur adsorption capacity is improved by 32.8 percent, and the yield of the powdery active coke is improved by 1.93 percent under the same conditionAnd the advantages of the two-step method are obvious by times of overall analysis.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A system for preparing powdery active coke for desulfurization by a three-section furnace two-step method is characterized by comprising a combustion furnace, a carbonization furnace, an activation furnace and a powdery coke cyclone separator;
the device comprises a combustion furnace and an activation furnace, wherein the combustion furnace and the activation furnace are both vertically arranged, a combustion coal powder inlet of the combustion furnace is arranged at the top of the combustion furnace, a smoke outlet of the combustion furnace is arranged at the bottom of the combustion furnace, a gas-phase inlet of the activation furnace is arranged at the bottom of the activation furnace, a carbonized semicoke inlet of the activation furnace is arranged on the side wall of the lower part of the activation furnace, an outlet of the activation furnace is arranged at the upper part of the activation furnace, and the gas-phase inlet of the activation furnace;
the flue gas outlet of the combustion furnace is connected with the gas-phase inlet of the activation furnace, the outlet of the activation furnace is connected with the inlet of the fine coke cyclone separator, the gas-phase outlet of the fine coke cyclone separator is connected with the gas-phase inlet of the carbonization furnace, the solid-phase outlet of the carbonization furnace is connected with the carbonization semi-coke inlet of the activation furnace, and the solid-phase inlet of the carbonization furnace is connected with the coking coal powder source.
2. The system for preparing powdery activated coke for desulfurization by the three-stage furnace two-step process according to claim 1, wherein the carbonization furnace is vertically arranged, the gas phase inlet and the solid phase inlet of the carbonization furnace are both arranged at the top of the carbonization furnace, the solid phase outlet of the carbonization furnace is arranged at the bottom of the carbonization furnace, and the gas phase outlet of the carbonization furnace is arranged at the lower side wall of the carbonization furnace.
3. The system for preparing the powdery active coke for desulfurization by the three-stage furnace two-step method according to claim 1, which is characterized by comprising a carbonized semicoke cyclone separator, wherein a gas-phase outlet of the carbonized furnace is connected with an inlet of the carbonized semicoke cyclone separator, and a solid-phase outlet of the carbonized semicoke cyclone separator is connected with a carbonized semicoke inlet of the activation furnace.
4. The system for preparing the powdery active coke for desulfurization by the three-stage furnace two-step method as claimed in claim 1, which is characterized by comprising an ash hopper, wherein a flue gas outlet of the combustion furnace is connected with a gas phase inlet of the ash hopper, and a gas phase outlet of the ash hopper is connected with a gas phase inlet of the activation furnace;
preferably, the water vapor tempering nozzle and/or the air tempering nozzle are/is arranged at the gas phase outlet of the ash bucket.
5. A process for preparing powdery active coke for desulfurization by a three-stage furnace two-step method is characterized in that the system of any one of claims 1 to 4 is provided;
the method comprises the steps of combusting fuel coal powder in a combustion furnace to generate combustion flue gas, utilizing steam and/or air to conduct temperature regulation and tempering on the combustion flue gas at a gas phase inlet of an activation furnace, mixing the combustion flue gas after temperature regulation and tempering with charring semi-coke to prepare powdery active coke, separating a mixture of the powdery active coke and the flue gas at an outlet of the activation furnace through a coke breeze cyclone separator to obtain powdery active coke and activation flue gas, and mixing the activation flue gas with coking coal powder to prepare the charring semi-coke.
6. The process for preparing powdery activated coke for desulfurization by the three-stage furnace two-step process according to claim 5, wherein the pulverized fuel coal is burned in a combustion furnace by slagging combustion.
7. The process for preparing powdery active coke for desulfurization by the three-stage furnace two-step method according to claim 5, wherein the upward gas velocity in the activation furnace is 4 to 6 m/s;
or the retention time of the carbonized carbocoal in the activation furnace is 3-7 s.
8. The process for preparing powdery active coke for desulfurization by the three-stage furnace two-step method according to claim 5, characterized in that the downward gas velocity in the carbonization furnace is 3 to 5 m/s;
or the retention time of the coking coal powder in the carbonization furnace is 3-7 s.
9. The process for preparing the powdery active coke for desulfurization by the three-stage furnace two-step method as claimed in claim 5, wherein the temperature of the flue gas entering the activation furnace is 1100-1200 ℃;
or the concentration of oxygen in the flue gas entering the activation furnace is 4-8%;
or the concentration of the water vapor in the flue gas entering the activation furnace is 15-35%.
10. The process for preparing powdery activated coke for desulfurization by the three-stage furnace two-step method as claimed in claim 5, wherein the temperature of the gas phase outlet of the carbonization furnace is 600-700 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011060136.3A CN112158844B (en) | 2020-09-30 | 2020-09-30 | System and process for preparing powdery active coke for desulfurization by three-stage furnace two-step method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011060136.3A CN112158844B (en) | 2020-09-30 | 2020-09-30 | System and process for preparing powdery active coke for desulfurization by three-stage furnace two-step method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112158844A true CN112158844A (en) | 2021-01-01 |
| CN112158844B CN112158844B (en) | 2021-12-28 |
Family
ID=73862247
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011060136.3A Active CN112158844B (en) | 2020-09-30 | 2020-09-30 | System and process for preparing powdery active coke for desulfurization by three-stage furnace two-step method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112158844B (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10338513A (en) * | 1997-06-04 | 1998-12-22 | Nittetsu Elex Co Ltd | Device for producing charcoal and activated carbon |
| JP2001220121A (en) * | 2000-02-10 | 2001-08-14 | Nkk Design & Engineering Corp | Method for manufacturing activated carbon from waste and manufacturing device |
| CN104787761A (en) * | 2015-04-16 | 2015-07-22 | 山东大学 | Device and method for quickly preparing powdered active coke |
| CN204529317U (en) * | 2015-04-16 | 2015-08-05 | 山东大学 | The burnt quick preparation device of a kind of powder activity |
| CN108910874A (en) * | 2018-07-19 | 2018-11-30 | 山东大学 | A kind of technique and system of lignite preparation high yield high activity powdered activated coke |
| CN108949209A (en) * | 2018-07-19 | 2018-12-07 | 山东大学 | The system and technique that a kind of powdered activated coke, heat, Electricity Federation produce |
| CN109485043A (en) * | 2018-11-26 | 2019-03-19 | 东南大学 | The system and method that biomass two-part prepares active carbon |
| CN110449024A (en) * | 2019-04-25 | 2019-11-15 | 北京清新环境技术股份有限公司 | A kind of desulfuring and denitrifying apparatus in situ and its method of the coke cutting of power plant's coal |
-
2020
- 2020-09-30 CN CN202011060136.3A patent/CN112158844B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10338513A (en) * | 1997-06-04 | 1998-12-22 | Nittetsu Elex Co Ltd | Device for producing charcoal and activated carbon |
| JP2001220121A (en) * | 2000-02-10 | 2001-08-14 | Nkk Design & Engineering Corp | Method for manufacturing activated carbon from waste and manufacturing device |
| CN104787761A (en) * | 2015-04-16 | 2015-07-22 | 山东大学 | Device and method for quickly preparing powdered active coke |
| CN204529317U (en) * | 2015-04-16 | 2015-08-05 | 山东大学 | The burnt quick preparation device of a kind of powder activity |
| CN108910874A (en) * | 2018-07-19 | 2018-11-30 | 山东大学 | A kind of technique and system of lignite preparation high yield high activity powdered activated coke |
| CN108949209A (en) * | 2018-07-19 | 2018-12-07 | 山东大学 | The system and technique that a kind of powdered activated coke, heat, Electricity Federation produce |
| CN109485043A (en) * | 2018-11-26 | 2019-03-19 | 东南大学 | The system and method that biomass two-part prepares active carbon |
| CN110449024A (en) * | 2019-04-25 | 2019-11-15 | 北京清新环境技术股份有限公司 | A kind of desulfuring and denitrifying apparatus in situ and its method of the coke cutting of power plant's coal |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112158844B (en) | 2021-12-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101245264B (en) | Single-bed self-heating type thermal decomposition gasification combustion reactor and thermal decomposition gasification combustion method | |
| CN102533345B (en) | Method and device for coal gasification in combined type fluidized bed | |
| CN103742899B (en) | A kind of circulating fluid bed burning in oxygen enrichment polygenerations systeme and technique | |
| CN106554826B (en) | Circulating fluidized bed coal gasification method and device with fine ash fusion | |
| CN107043641B (en) | Coal gasification method and device of circulating fluidized bed with fine ash return | |
| CN1219857C (en) | Solid slag-discharing dry-powder air-current bed gasification process and apparatus | |
| CN105062528B (en) | A kind of pyrolysis of coal multi-production process and its device suitable for coal-powder boiler | |
| CN103013576A (en) | IGCC (Integrated Gasification Combined Cycle) poly-generation device and method based on pyrolysis and gasification of low metamorphic powdered coal | |
| CN108504394B (en) | Catalytic pyrolysis-gasification integrated reaction device and method | |
| CN103911179B (en) | Coal gasification method and device | |
| CN108949209B (en) | Powdery active coke, heat and electricity cogeneration system and process | |
| CN101250419B (en) | Low-temperature dry distillation process with coal gas internal heat | |
| CN108178131B (en) | SO in regenerated gas by active coke desulfurization2Fluidized bed device and method for recovering sulfur | |
| CN201241071Y (en) | Single-bed self-heating type thermal decomposition gasification combusting reactor | |
| WO2017156824A1 (en) | Lignite semi-coke oxygen deficient combustion boiler | |
| SE470213B (en) | Methods and apparatus for producing fuels from solid carbonaceous natural fuels | |
| CN107652997B (en) | Powdery semi-coke preparation device and process | |
| CN103113923A (en) | Four-segment spray coal oxygen-enriched gasification method | |
| CN203048897U (en) | IGCC (integrated gasification combined cycle) polygeneration device based on low metamorphic coal pyrolysis and gasification | |
| CN105861069A (en) | Solid fuel double-fluidized bed partial gasification classified converting device and method | |
| CN112158844B (en) | System and process for preparing powdery active coke for desulfurization by three-stage furnace two-step method | |
| CN106947541B (en) | Combined method and system for hydrogen production based on low-rank coal pyrolysis water vapor coke quenching water gas | |
| CN1025568C (en) | Producing method and device for dry distilation coal gas | |
| CN104152184B (en) | Biomass whirlwind pyrolysis-suspension combustion combined gasification equipment and gasification process thereof | |
| CN114130311B (en) | Integrated device and method for preparing sulfur by activated coke regeneration and cooperative reduction |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |