CN215233316U - Converter and sulfur-containing waste treatment system - Google Patents

Converter and sulfur-containing waste treatment system Download PDF

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Publication number
CN215233316U
CN215233316U CN202121478711.1U CN202121478711U CN215233316U CN 215233316 U CN215233316 U CN 215233316U CN 202121478711 U CN202121478711 U CN 202121478711U CN 215233316 U CN215233316 U CN 215233316U
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catalyst layer
conversion
converter
heat exchanger
process gas
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徐晓燕
陈英斌
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China Petroleum and Chemical Corp
Research Institute of Sinopec Nanjing Chemical Industry Co Ltd
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China Petroleum and Chemical Corp
Research Institute of Sinopec Nanjing Chemical Industry Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/69—Sulfur trioxide; Sulfuric acid
    • C01B17/74—Preparation
    • C01B17/76—Preparation by contact processes
    • C01B17/80—Apparatus
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/69—Sulfur trioxide; Sulfuric acid
    • C01B17/74—Preparation
    • C01B17/76—Preparation by contact processes
    • C01B17/80—Apparatus
    • C01B17/806—Absorbers; Heat exchangers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22G—SUPERHEATING OF STEAM
    • F22G1/00—Steam superheating characterised by heating method
    • F22G1/16—Steam superheating characterised by heating method by using a separate heat source independent from heat supply of the steam boiler, e.g. by electricity, by auxiliary combustion of fuel oil
    • 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

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • Sustainable Development (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Sustainable Energy (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Treating Waste Gases (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Processing Of Solid Wastes (AREA)
  • Gas Separation By Absorption (AREA)
  • Regulation And Control Of Combustion (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Abstract

The utility model discloses a converter and a sulfur-containing waste treatment system, wherein a first conversion gas inlet and a first conversion gas outlet of the converter are both communicated with a first conversion chamber so that process gas can flow from the first conversion gas inlet to the first conversion gas outlet; the second conversion gas inlet and the second conversion gas outlet are both communicated with the second conversion chamber so that the process gas can flow from the second conversion gas inlet to the second conversion gas outlet; the first catalyst layer and the second catalyst layer are both arranged in the first conversion chamber and are arranged at intervals along the flowing direction of the process gas; the fourth catalyst layer is arranged in the second conversion chamber; the third catalyst layer is disposed in the first conversion chamber or the second conversion chamber and is spaced apart from the other catalyst layers in the flow direction of the process gas. The utility model discloses a converter has area is little, the heat loss is few, advantage that conversion efficiency is high.

Description

Converter and sulfur-containing waste treatment system
Technical Field
The utility model relates to a contain the processing of sulphur discarded object, specifically relate to a converter and contain sulphur waste processing system.
Background
Concentrated sulfuric acid is widely used as a catalyst in petrochemical and organic synthesis industries, and a large amount of waste sulfuric acid is produced in the process. Some organic synthesis processes, such as the synthesis of Methyl Methacrylate (MMA) and Acrylonitrile (AN), produce about 30 wt% to 45 wt% waste ammonium sulfate in addition to waste sulfuric acid. These sulfur-containing wastes cause serious environmental pollution, and therefore it is necessary to purify and recycle industrial waste acids and sulfur-containing waste liquids as much as possible.
The main equipment of the sulfur dioxide conversion process comprises a converter, and the design condition of the converter is related to whether the whole conversion reaction can be normally carried out or not and the overall conversion rate is high or low. However, the converter in the prior art has the problems of more matched heat exchangers, large occupied area, long pipeline, more heat loss and low conversion efficiency.
SUMMERY OF THE UTILITY MODEL
The utility model aims at overcoming the problem that prior art exists, provide a converter and contain sulphur waste processing system, this converter has supporting heat exchanger few, and area is few, and the heat loss is few, advantages such as conversion efficiency height.
In order to achieve the above object, an aspect of the present invention provides a reformer including a first reforming chamber, a second reforming chamber, a first catalyst layer, a second catalyst layer, a third catalyst layer, a fourth catalyst layer, a first reformed gas inlet, a second reformed gas inlet, a first reformed gas outlet, and a second reformed gas outlet; the first conversion gas inlet and the first conversion gas outlet are both in communication with the first conversion chamber to enable a process gas to flow from the first conversion gas inlet to the first conversion gas outlet; the second conversion gas inlet and the second conversion gas outlet are both in communication with the second conversion chamber to enable a process gas to flow from the second conversion gas inlet to the second conversion gas outlet; the first catalyst layer and the second catalyst layer are both arranged in the first conversion chamber and are arranged at intervals along the flowing direction of the process gas; the fourth catalyst layer is arranged in the second conversion chamber; the third catalyst layer is disposed in the first conversion chamber or the second conversion chamber and is spaced apart from other catalyst layers in a flow direction of the process gas.
Optionally, the converter includes a first heat exchanger and a second heat exchanger, and the first heat exchanger and the second heat exchanger are respectively disposed between two adjacent catalyst layers.
Optionally, the third catalyst layer is disposed in the first conversion chamber and located downstream of the second catalyst layer, the first heat exchanger is disposed between the first catalyst layer and the second catalyst layer, and the second heat exchanger is disposed between the second catalyst layer and the third catalyst layer.
Optionally, the third catalyst layer is disposed in the second conversion chamber and located at the upstream of the fourth catalyst layer, the first heat exchanger is disposed between the first catalyst layer and the second catalyst layer, and the second heat exchanger is disposed between the third catalyst layer and the fourth catalyst layer.
Optionally, the reformer comprises a reformer housing defining the first reforming chamber and the second reforming chamber, the first reforming gas inlet being disposed at a bottom of the reformer housing, and the second reforming gas outlet being disposed at a top of the reformer housing.
Optionally, the converter includes a plurality of support assemblies corresponding to the first catalyst layer, the second catalyst layer, the third catalyst layer, and the fourth catalyst layer one to one, and each support assembly includes a grate plate, and an edge of the grate plate is connected to an inner wall of the converter housing to support the catalyst layer.
Optionally, the support assembly comprises heat-resistant ceramic balls arranged between the grate plate and the catalyst layer.
Optionally, the converter comprises a plurality of thermocouple connection tubes arranged on the inner wall of the converter shell, and the thermocouple connection tubes are arranged at intervals along the flowing direction of the process gas.
Optionally, a pressure gauge connection pipe and/or a manhole is arranged at the bottom of the converter shell.
Through above-mentioned technical scheme, process gas passes through first change of gas entry gets into first conversion cavity, process gas earlier with first catalyst layer reaction, later process gas again with second catalyst layer reaction can directly pass through after the reaction first change of gas export gets into outside heat exchanger, also can earlier with third catalyst layer reaction back rethread first change of gas export gets into outside heat exchanger, and the temperature control after the heat transfer of the process gas that contains sulfur trioxide that the reaction is accomplished through outside heat exchanger is more than 150 ℃, the first order of reentrant multistage absorption tower. The conversion rate of the primary conversion is 95-96%, and the absorption rate is 99.99% by adopting 100 wt% sulfuric acid for absorption. The completely absorbed process gas sequentially passes through an external heat exchanger for heat exchange, the temperature of the process gas after heat exchange reaches 415-420 ℃, and the process gas enters the second conversion chamber through the second conversion gas inlet, and can be firstly mixed with the process gasThe third catalyst layer starts to react, the reacted process gas containing sulfur trioxide is subjected to heat exchange by the second heat exchanger and then reacts with the fourth catalyst layer, the process gas can also directly react with the fourth catalyst layer, and the temperature of the reacted process gas is controlled to be higher than 130 ℃ and enters the second stage of the multistage absorption tower through the second converted gas outlet. The absorption rate is 99.99 percent, and the absorbed process gas is discharged to realize SO2The concentration is less than or equal to 50mg/M3The concentration of NOx is less than or equal to 100mg/M3Acid mist is less than or equal to 5mg/M3The concentration of the particles is less than or equal to 30mg/M3. Therefore, the converter of the utility model has the advantage that conversion efficiency is high.
The utility model discloses the second aspect provides a contain sulphur waste disposal system, contain sulphur waste disposal system includes foretell converter.
The sulfur-containing waste treatment system has the same advantages as the converter described above over the prior art and will not be described herein again.
Other features and advantages of the present invention will be described in detail in the detailed description which follows.
Drawings
FIG. 1 is a schematic diagram of one embodiment of a converter of the present invention;
fig. 2 is a schematic diagram of another embodiment of the converter of the present invention.
Description of the reference numerals
101-a first conversion chamber, 102-a second conversion chamber,
201-a first catalyst layer, 202-a second catalyst layer, 203-a third catalyst layer, 204-a fourth catalyst layer,
301-the first conversion gas inlet, 302-the second conversion gas inlet,
401-the first converted gas outlet, 402-the second converted gas outlet,
501-a first heat exchanger, 502-a second heat exchanger,
601-the housing of the converter-the housing,
701-a grate plate, 702-a heat-resistant porcelain ball,
801-thermocouple connection pipe, 802-pressure gauge connection pipe, 803-manhole
Detailed Description
The following detailed description of the embodiments of the present invention will be made with reference to the accompanying drawings. It is to be understood that the description of the embodiments herein is for purposes of illustration and explanation only and is not intended to limit the invention.
As shown in fig. 1 and fig. 2, the reformer of the present invention includes a first reforming chamber 101, a second reforming chamber 102, a first catalyst layer 201, a second catalyst layer 202, a third catalyst layer 203, a fourth catalyst layer 204, a first reforming gas inlet 301, a second reforming gas inlet 302, a first reforming gas outlet 401, and a second reforming gas outlet 402; both the first conversion gas inlet 301 and the first conversion gas outlet 401 are in communication with the first conversion chamber 101 to enable the process gas to flow from the first conversion gas inlet 301 to the first conversion gas outlet 401; the second conversion gas inlet 302 and the second conversion gas outlet 402 are both in communication with the second conversion chamber 102 to enable the process gas to flow from the second conversion gas inlet 302 to the second conversion gas outlet 402; the first catalyst layer 201 and the second catalyst layer 202 are both disposed in the first conversion chamber 101 and arranged at intervals along the flow direction of the process gas; the fourth catalyst layer 204 is disposed in the second conversion chamber 102; the third catalyst layer 203 is disposed in the first conversion chamber 101 or the second conversion chamber 102 and is arranged spaced apart from the other catalyst layers in the flow direction of the process gas.
The utility model discloses in, process gas gets into first conversion cavity 101 through first change of gas entry 301, process gas earlier with first catalyst layer 201 reaction, later process gas reacts with second catalyst layer 202 again, can directly get into outside heat exchanger (corresponding the embodiment of fig. 1) through first change of gas export 401 after the reaction, also can react with third catalyst layer 203 earlier the back rethread first change of gas export 401 gets into outside heat exchanger (corresponding the embodiment of fig. 2), the temperature control after the heat transfer of the process gas that contains sulfur trioxide and that has reacted through outside heat exchanger is more than 150 ℃, get into the first order of multistage absorption tower again. The conversion rate of the primary conversion is 95-96%, and the absorption rate is 99.99% by adopting 100 wt% sulfuric acid for absorption. Completely absorbed toolThe process gas sequentially passes through an external heat exchanger for heat exchange, the temperature of the process gas after heat exchange reaches 415-420 ℃, and enters the second conversion chamber 102 through the second conversion gas inlet 302, and can firstly start to react with the third catalyst layer 203, the process gas containing sulfur trioxide after reaction exchanges heat through the second heat exchanger 502 and then reacts with the fourth catalyst layer 204 (corresponding to the embodiment of fig. 1), and can also directly react with the fourth catalyst layer 204 (corresponding to the embodiment of fig. 2), and the temperature of the process gas after reaction is controlled to be above 130 ℃ and enters the second stage of the multistage absorption tower through the second conversion gas outlet 401. The absorption rate is 99.99 percent, and the absorbed process gas is discharged to realize SO2The concentration is less than or equal to 50mg/M3The concentration of NOx is less than or equal to 100mg/M3Acid mist is less than or equal to 5mg/M3The concentration of the particles is less than or equal to 30mg/M3. Therefore, the converter of the utility model has the advantage that conversion efficiency is high.
In order to effectively control the temperature of the process gas and improve the conversion efficiency of the process gas, in an embodiment of the present invention, the converter includes a first heat exchanger 501 and a second heat exchanger 502, and the first heat exchanger 501 and the second heat exchanger 502 are respectively disposed between two adjacent catalyst layers.
Specifically, in one embodiment of the present invention, as shown in fig. 1, the third catalyst layer 203 is disposed in the second conversion chamber 102 and located upstream of the fourth catalyst layer 204, the first heat exchanger 501 is disposed between the first catalyst layer 201 and the second catalyst layer 202, and the second heat exchanger 502 is disposed between the third catalyst layer 203 and the fourth catalyst layer 204.
In the embodiment, the temperature of the process gas entering the first conversion chamber 101 through the first conversion gas inlet 301 is firstly enabled to reach 410-420 ℃, the temperature of the process gas after the reaction with the first catalyst layer 201 reaches 550-560 ℃, then the process gas exchanges heat with the first heat exchanger 501, the temperature of the process gas after heat exchange is 450-460 ℃, then the process gas reacts with the second catalyst layer 202, the reacted process gas containing sulfur trioxide enters the external heat exchanger through the first conversion gas outlet 401, the temperature of the process gas after heat exchange is controlled to be more than 150 ℃, and then the process gas enters the multi-catalyst layerThe first stage of the absorption column. The conversion rate of the primary conversion is 95-96%, and the absorption rate is 99.99% by adopting 100 wt% sulfuric acid for absorption. The completely absorbed process gas sequentially passes through an external heat exchanger and the first heat exchanger 501 of the converter to exchange heat, the temperature of the process gas after heat exchange reaches 415-420 ℃, the process gas enters the second conversion chamber 102 through the second conversion gas inlet 302 to start to react with the third catalyst layer 203, the process gas containing sulfur trioxide after reaction exchanges heat through the second heat exchanger 502 and then reacts with the fourth catalyst layer 204, and the temperature of the process gas after reaction is controlled to be above 130 ℃ and enters the second stage of the multistage absorption tower through the second conversion gas outlet 401. The absorption rate is 99.99 percent, and the absorbed process gas is discharged to realize SO2The concentration is less than or equal to 50mg/M3The concentration of NOx is less than or equal to 100mg/M3Acid mist is less than or equal to 5mg/M3The concentration of the particles is less than or equal to 30mg/M3。
Specifically, in another embodiment of the present invention, as shown in fig. 2, the third catalyst layer 203 is disposed in the first conversion chamber 101 and located downstream of the second catalyst layer 202, the first heat exchanger 501 is disposed between the first catalyst layer 201 and the second catalyst layer 202, and the second heat exchanger 502 is disposed between the second catalyst layer 202 and the third catalyst layer 203.
In this embodiment, the temperature of the process gas reacting with the first catalyst layer 201 is set to 400 to 410 ℃, the temperature of the reacted process gas is set to 600 to 610 ℃, and then the reacted process gas exchanges heat with the first heat exchanger 501 inside the converter, so that the process gas starts to react when the temperature of the process gas in the second catalyst layer 202 reaches 460 to 470 ℃, the process gas containing sulfur trioxide after the reaction exchanges heat with the second heat exchanger 502 inside, and the process gas in the third catalyst layer 203 reaches 440 to 450 ℃. Because the concentration of sulfur dioxide in the process gas is relatively high, the temperature of the process gas which is converted for one time and is discharged out of the third catalyst layer 203 is 220 ℃, the temperature of the process gas is controlled to be more than 150 ℃ through an external heat exchanger, and then the process gas enters the multistage absorption tower. The heat is recovered to improve the feed water temperature of the boiler and the steam yield. The conversion rate of the primary conversion is 95 to 96 percent, and 98 weight percent of sulfuric acid is adopted for absorptionThe absorption rate is 99.99%. The fully absorbed process gas is passed in turn through an external heat exchanger and a second heat exchanger 502 inside the converter for heat exchange. The temperature of the process gas reacted with the fourth catalyst layer 204 is brought to 410-415 ℃ and the reaction is started, and the reacted process gas containing sulfur trioxide enters the multistage absorption tower 41 through the second converted gas outlet 402. The absorption was carried out with 98 wt% sulfuric acid, the absorption rate was 99.99%. The absorbed process gas is discharged to realize SO2The concentration is less than or equal to 50mg/M3The concentration of NOx is less than or equal to 100mg/M3Acid mist is less than or equal to 5mg/M3The concentration of the particles is less than or equal to 30mg/M3。
It should be understood that the converter may be designed in various forms, for example, it may be a horizontal type converter. In one embodiment of the present invention, the converter is in a vertical form, and specifically, the converter includes a converter housing 601 defining a first conversion chamber 101 and a second conversion chamber 102, the first conversion gas inlet 301 is disposed at the bottom of the converter housing 601, and the second conversion gas outlet 402 is disposed at the top of the converter housing 601. The advantage of setting up like this is that save area more, reduces the treatment cost of sulphur waste effectively.
In order to make each catalyst layer can set up in the conversion cavity more firmly in the utility model discloses an in the embodiment, the converter include with first catalyst layer 201, second catalyst layer 202, third catalyst layer 203 and fourth catalyst layer 204 one-to-one a plurality of supporting components, supporting component includes grate plate 701, and the border of grate plate 701 is connected in order to provide the support to the catalyst layer with the inner wall of converter casing 601.
Further, the support member includes heat-resistant porcelain balls 702 disposed between the grate plate 701 and the catalyst layer. The heat-resistant ceramic balls 702 can exchange heat with the process gas passing through, so that the temperature of the process gas is reduced to a temperature suitable for reacting with the catalyst layer, and can absorb impurity particles in the process gas to play a purifying role.
In order to effectively monitor the temperature of the process gas in the conversion chamber, in an embodiment of the present invention, the converter includes a plurality of thermocouple connection pipes 801 disposed on the inner wall of the converter housing 601, the plurality of thermocouple connection pipes 801 are disposed at intervals along the flow direction of the process gas, and the thermocouple connection pipes 801 can sense the temperature of the process gas and transmit the temperature signal to an external monitoring unit.
To better monitor the pressure inside the converter and more conveniently inspect the converter at the same time, an embodiment of the present invention provides that the bottom of the converter housing 601 is provided with a pressure gauge connection 802 and a manhole 803.
The utility model also provides a contain sulphur waste disposal system, this contain sulphur waste disposal system includes foretell converter.
The sulfur-containing waste treatment system has the same advantages as the above converter over the prior art and will not be described herein.
The preferred embodiments of the present invention have been described in detail with reference to the accompanying drawings, but the present invention is not limited thereto. In the technical idea scope of the present invention, it is possible to provide a solution of the present invention with a plurality of simple modifications to avoid unnecessary repetition, and the present invention is not described separately for various possible combinations. These simple variations and combinations should also be considered as disclosed in the present invention, all falling within the scope of protection of the present invention.

Claims (10)

1. A reformer, characterized in that it comprises a first reforming chamber (101), a second reforming chamber (102), a first catalyst layer (201), a second catalyst layer (202), a third catalyst layer (203), a fourth catalyst layer (204), a first reformed gas inlet (301), a second reformed gas inlet (302), a first reformed gas outlet (401) and a second reformed gas outlet (402);
-the first conversion gas inlet (301) and the first conversion gas outlet (401) are both in communication with the first conversion chamber (101) to enable a process gas to flow from the first conversion gas inlet (301) to the first conversion gas outlet (401);
the second conversion gas inlet (302) and the second conversion gas outlet (402) are both in communication with the second conversion chamber (102) to enable process gas to flow from the second conversion gas inlet (302) to the second conversion gas outlet (402);
the first catalyst layer (201) and the second catalyst layer (202) are both arranged in the first conversion chamber (101) and are arranged at intervals along the flow direction of the process gas;
the fourth catalyst layer (204) is disposed in the second conversion chamber (102);
the third catalyst layer (203) is arranged in the first conversion chamber (101) or the second conversion chamber (102) and is spaced apart from the other catalyst layers in the flow direction of the process gas.
2. The converter according to claim 1, characterized in that it comprises a first heat exchanger (501) and a second heat exchanger (502), said first heat exchanger (501) and said second heat exchanger (502) being respectively arranged between two adjacent catalyst layers.
3. The converter according to claim 2, characterized in that the third catalyst layer (203) is arranged in the first conversion chamber (101) downstream of the second catalyst layer (202), the first heat exchanger (501) being arranged between the first catalyst layer (201) and the second catalyst layer (202), the second heat exchanger (502) being arranged between the second catalyst layer (202) and the third catalyst layer (203).
4. The converter according to claim 2, characterized in that the third catalyst layer (203) is arranged in the second conversion chamber (102) upstream of the fourth catalyst layer (204), the first heat exchanger (501) being arranged between the first catalyst layer (201) and the second catalyst layer (202), the second heat exchanger (502) being arranged between the third catalyst layer (203) and the fourth catalyst layer (204).
5. The converter according to any of claims 2-4, characterized in that the converter comprises a converter housing (601) defining the first (101) and second (102) conversion chambers, the first conversion gas inlet (301) being arranged at the bottom of the converter housing (601) and the second conversion gas outlet (402) being arranged at the top of the converter housing (601).
6. The reformer according to claim 5, characterized in that it comprises a plurality of support members in one-to-one correspondence with the first catalyst layer (201), the second catalyst layer (202), the third catalyst layer (203) and the fourth catalyst layer (204), the support members comprising a grate plate (701), the edges of the grate plate (701) being connected with the inner wall of the reformer housing (601) to provide support to the catalyst layers.
7. The converter according to claim 6, characterized in that said support means comprise heat-resistant ceramic balls (702) arranged between said grate plate (701) and the catalytic layer.
8. The converter according to claim 5, characterized in that it comprises a plurality of thermowells (801) arranged on the inner wall of the converter housing (601), a plurality of said thermowells (801) being arranged at intervals in the flow direction of the process gas.
9. Converter according to claim 5, characterized in that the bottom of the converter housing (601) is provided with a pressure tap (802) and/or a manhole (803).
10. A sulfur-containing waste treatment system comprising the converter of any one of claims 1-9.
CN202121478711.1U 2020-08-20 2021-06-30 Converter and sulfur-containing waste treatment system Active CN215233316U (en)

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Application Number Priority Date Filing Date Title
CN2020108418745 2020-08-20
CN202010841874 2020-08-20

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CN215233316U true CN215233316U (en) 2021-12-21

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Application Number Title Priority Date Filing Date
CN202110739603.3A Active CN114074926B (en) 2020-08-20 2021-06-30 Converter and sulfur-containing waste treatment system
CN202110739640.4A Pending CN114076320A (en) 2020-08-20 2021-06-30 Control method and device for sulfur-containing waste treatment system and readable storage medium
CN202110739636.8A Pending CN114076523A (en) 2020-08-20 2021-06-30 Reaction furnace assembly and sulfur-containing waste treatment system
CN202110736751.XA Pending CN114074924A (en) 2020-08-20 2021-06-30 System and method for preparing sulfuric acid by regenerating sulfur-containing waste
CN202110736744.XA Pending CN114076317A (en) 2020-08-20 2021-06-30 Sulfur-containing waste system, reaction furnace combustion control method and device and storage medium
CN202110736752.4A Pending CN114074925A (en) 2020-08-20 2021-06-30 Method for burning sulfur-containing waste and method for preparing sulfuric acid from sulfur-containing waste
CN202110736743.5A Pending CN114162790A (en) 2020-08-20 2021-06-30 Dust-removing heat-exchanging device, dust-removing heat-exchanging method of dust-containing high-temperature flue gas and method for preparing sulfuric acid from sulfur-containing waste
CN202110736754.3A Pending CN114076318A (en) 2020-08-20 2021-06-30 Sulfur-containing waste treatment system, start-up temperature rise method, device and storage medium
CN202121478711.1U Active CN215233316U (en) 2020-08-20 2021-06-30 Converter and sulfur-containing waste treatment system
CN202121483021.5U Active CN215962868U (en) 2020-08-20 2021-06-30 Cooling absorption tower and sulfur-containing waste treatment system

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CN202110739603.3A Active CN114074926B (en) 2020-08-20 2021-06-30 Converter and sulfur-containing waste treatment system
CN202110739640.4A Pending CN114076320A (en) 2020-08-20 2021-06-30 Control method and device for sulfur-containing waste treatment system and readable storage medium
CN202110739636.8A Pending CN114076523A (en) 2020-08-20 2021-06-30 Reaction furnace assembly and sulfur-containing waste treatment system
CN202110736751.XA Pending CN114074924A (en) 2020-08-20 2021-06-30 System and method for preparing sulfuric acid by regenerating sulfur-containing waste
CN202110736744.XA Pending CN114076317A (en) 2020-08-20 2021-06-30 Sulfur-containing waste system, reaction furnace combustion control method and device and storage medium
CN202110736752.4A Pending CN114074925A (en) 2020-08-20 2021-06-30 Method for burning sulfur-containing waste and method for preparing sulfuric acid from sulfur-containing waste
CN202110736743.5A Pending CN114162790A (en) 2020-08-20 2021-06-30 Dust-removing heat-exchanging device, dust-removing heat-exchanging method of dust-containing high-temperature flue gas and method for preparing sulfuric acid from sulfur-containing waste
CN202110736754.3A Pending CN114076318A (en) 2020-08-20 2021-06-30 Sulfur-containing waste treatment system, start-up temperature rise method, device and storage medium

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CN202121483021.5U Active CN215962868U (en) 2020-08-20 2021-06-30 Cooling absorption tower and sulfur-containing waste treatment system

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