CN108394902B - Carbon disulfide production system and method - Google Patents
Carbon disulfide production system and method Download PDFInfo
- Publication number
- CN108394902B CN108394902B CN201810401491.9A CN201810401491A CN108394902B CN 108394902 B CN108394902 B CN 108394902B CN 201810401491 A CN201810401491 A CN 201810401491A CN 108394902 B CN108394902 B CN 108394902B
- Authority
- CN
- China
- Prior art keywords
- reaction
- chamber
- gas
- temperature
- reaction chamber
- 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.)
- Active
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
- C01B32/70—Compounds containing carbon and sulfur, e.g. thiophosgene
- C01B32/72—Carbon disulfide
- C01B32/75—Preparation by reacting sulfur or sulfur compounds with hydrocarbons
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
The invention provides a carbon disulfide production system and a method, wherein the reaction system comprises a carbon disulfide reaction furnace, an electric heater, a flue gas heat exchanger, a product heat exchanger and a compressor, wherein the carbon disulfide reaction furnace is divided into a first reaction chamber, a mixing distribution chamber and a second reaction chamber, and natural gas is divided into two parts which enter different parts of the reaction furnace to react with sulfur to generate carbon disulfide. The reaction temperature of the reaction zone is controlled by controlling the amount of the natural gas entering the reaction furnace and the temperature of the nitrogen entering the second reaction chamber in the reaction process, so that the heating uniformity of the reaction zone is improved, the controllability of the temperature of the reaction zone is realized, the reduction of the service life of the reaction furnace caused by frequent temperature change is avoided, and meanwhile, the heat energy utilization efficiency is improved by recovering the heat in the flue gas and the product gas.
Description
Technical Field
The invention belongs to the technical field of carbon disulfide production, and particularly relates to a carbon disulfide production system and a method for producing carbon disulfide by using the production system.
Background
Carbon disulfide is used as an important chemical raw material, is mainly used as a raw material for manufacturing viscose fiber and cellophane, and is used as a raw material for producing rayon, cellophane, carbon tetrachloride, pesticide bactericide and rubber auxiliary agent; carbon disulfide is an excellent solvent in the production of products such as grease, wax, resin, rubber, sulfur and the like; can be used as wool degreasing agent, clothes detergent, metal flotation agent, parting agent of paint and varnish, aviation kerosene additive, etc. At present, the method for preparing carbon disulfide mainly comprises three methods, wherein one method is prepared by reacting charcoal and sulfur, and the method can be simply divided into an external furnace method and an internal heat method according to different heat sources, and the method consumes a large amount of wood, so that the application of the method is limited; secondly, charcoal substitutes such as coke are used as raw materials to prepare carbon disulfide, but the pollution caused by the method is serious; thirdly, the carbon disulfide is produced by the reaction of natural gas and sulfur, and the method is widely applied at present.
In the process of preparing carbon disulfide by a natural gas method, the sulfur is usually carried out under the condition of excess sulfur, and solid sulfur is gasified and then reacts with methane under the condition of high temperature. For preparing carbon disulfide by a natural gas method, a reaction furnace is a key device of the process, and a research hotspot in the field is to extend the service life of the furnace and improve the production efficiency of carbon disulfide.
Chinese patent CN100503437C discloses a reaction furnace for manufacturing carbon disulfide by a high-pressure non-catalytic natural gas method, the reaction furnace has a radiation section and an impulse section, raw materials enter a furnace tube by the impulse section to be preheated, and then are heated in the radiation section, the furnace is led out from the bottom of the radiation section, the radiation section is provided with a refractory furnace lining, a plurality of burners are arranged in the side walls of the furnace body and the furnace lining of the radiation section, the furnace tube in the hearth is mainly heated by the thermal radiation of the heated furnace lining and the convection and heat conduction of flue gas, the flue gas generated by the burners is led into the impulse section by negative pressure, and is subjected to impact heat exchange with a feeding furnace tube in the impulse section, and the convection section is selected to be arranged after the impulse section to recover the waste heat in the flue gas.
Chinese patent CN107151018A discloses a reaction furnace for producing carbon disulfide by a natural gas sulfur method, which comprises a furnace body shell, wherein the top of the furnace body shell is connected with a chimney, a cylindrical coil pipe is arranged in the furnace body shell, the top of the rotary coil pipe is provided with a third inlet, and the bottom of the rotary coil pipe is provided with a third outlet; the bottom in the furnace body shell is provided with a burner, and the center of the burner is positioned on the axis of the rotary coil pipe.
However, the existing furnaces have the problems of easy coking, short service life and the like to a certain extent, so the invention provides a novel carbon disulfide production system and inhibits the coking problem in the reaction process to a certain extent.
Disclosure of Invention
The invention aims to provide a carbon disulfide production system and a method, which fundamentally solve the problems of short service life of a reaction furnace, easy coking of a reaction tube and easy abrasion in the prior art. The reaction system provided by the invention realizes constant temperature in the reaction process through nitrogen temperature control, thereby inhibiting the occurrence of coking in the reaction process, recycling the flue gas generated in the reaction process and the heat attached by the product gas carbon disulfide, and improving the energy utilization efficiency.
The technical scheme adopted by the invention is as follows:
a carbon disulfide production system which characterized in that: comprises a carbon disulfide reaction furnace, an electric heater, a flue gas heat exchanger, a product heat exchanger and a compressor; the carbon disulfide reaction furnace is divided into three parts, namely a first reaction chamber, a mixing distribution chamber and a second reaction chamber, wherein the first reaction chamber is of a double-layer cylinder structure, the inner layer is a heating chamber, the upper part of the heating chamber is provided with a flue gas outlet, the lower part of the heating chamber is provided with a combustion gas inlet and a burner, the burner is of a cylindrical structure, the upper part of the outer layer of the first reaction chamber is provided with a sulfur gasification chamber, the middle part of the outer layer of the first reaction chamber is provided with a mixing chamber, the lower part of the outer layer of the first reaction chamber is provided with a reaction chamber, the upper part of the sulfur gasification chamber is provided with a sulfur charging port, and the side surface of the mixing chamber is provided with a first natural gas inlet; the upper part of the mixing distribution chamber is communicated with the first gas reaction chamber, the lower part of the mixing distribution chamber is provided with a gas distribution plate and is communicated with the second reaction chamber, and the side surface of the mixing distribution chamber is provided with a second natural gas inlet; the second reaction chamber is divided into a tube side and a shell side, wherein the tube side is a reaction tube, the reaction tube is communicated with the gas distribution plate through a communicating vessel, the reaction tube is of a spiral structure, the side surface of the shell side is provided with a high-temperature nitrogen inlet and a high-temperature nitrogen outlet, the lower part of the second reaction chamber is provided with a high-temperature product outlet, and the high-temperature product outlet is connected with the product heat exchanger through a pipeline;
the electric heater is of a cylindrical structure, the outer layer is provided with a silicon carbide rod heating device, the inner layer is a gas circulation pipe, and the gas circulation pipe is communicated with the high-temperature nitrogen inlet;
the flue gas heat exchanger is of a shell-and-tube structure, a shell pass is communicated with a flue gas outlet of the reaction furnace, and a tube pass is communicated with a raw gas natural gas pipeline;
the product heat exchanger is of a shell-and-tube structure, wherein the tube pass is of a spiral tube structure, the carbon disulfide product flows through the spiral tube, and the inlet of the spiral tube is communicated with the product gas outlet.
Furthermore, a fuel gas and oxygen mixing chamber is arranged at the inlet of the burner, and fuel gas nozzles are arranged on the burner, wherein the number of the nozzles is 4, and the horizontal included angle of the nozzles is 40 degrees.
Further, ceramic balls are filled in the mixing chamber, and the particle size of the ceramic balls is 5-8 mm.
Further, the inner layer and the outer layer of the first reaction chamber of the reaction furnace are separated by a high-temperature heat-conducting brick, wherein the main component of the high-temperature heat-conducting brick is SiO2、Al2O3、Fe2O3And CaO.
Further, the sulfur feed inlet is provided with a micro pyrolysis device and a liquid sulfur conduit, wherein the heating temperature is 100-120 ℃.
Further, the communicating vessel is of a circular truncated cone structure, the diameter of the upper table top is the same as that of the gas distribution plate, the diameter of the upper table top is 15-19 cm, the diameter of the lower table top is the same as that of the reaction tube of the second reaction chamber, and the diameter of the lower table top is 3-4 cm.
Further, a temperature measuring device is arranged in the second reaction chamber.
The invention provides a carbon disulfide production method, which adopts the device and is characterized in that: the method comprises the following steps:
(1) adding sulfur into a sulfur gasification chamber from a sulfur feed port, spraying a mixture of natural gas and oxygen through a fuel gas inlet, and combusting in a combustor to raise the temperature of a heating chamber, and simultaneously raising the temperature of the sulfur gasification chamber to 500-600 ℃ to gasify sulfur in the gasification chamber;
(2) flue gas from the heating chamber enters a shell pass of the flue gas heat exchanger through a flue gas outlet to exchange heat with raw material gas of a tube pass, the temperature of the raw material gas rises to 400-500 ℃, the raw material gas is divided into two parts, one part of the heated natural gas enters a mixing chamber to be uniformly mixed with gasified sulfur, and then enters a reaction chamber to react to generate carbon disulfide, and meanwhile, the temperature of the reaction chamber is controlled to be 500-900 ℃, and the pressure is controlled to be 1.2-1.5 MPa; the other part of the heated natural gas enters the mixing distribution chamber to be mixed with the carbon disulfide and the gasified sulfur from the first gas reaction chamber, then enters the tube pass of the second reaction chamber through the gas distribution plate, and is discharged from the high-temperature product outlet after reaction;
(3) in the reaction process, the nitrogen is compressed by a compressor, then the nitrogen and the product gas exchange heat in a product heat exchanger, the nitrogen enters an electric heater to be heated to 600-800 ℃, then enters the shell pass of a second reaction chamber, and the reaction temperature of the carbon disulfide in the second reaction chamber is controlled by controlling the temperature of the nitrogen.
Further, the fuel gas in the step (1) is any one of coke oven gas, natural gas, coal bed gas and liquefied petroleum gas.
Further, the molar ratio of the natural gas entering the reaction system in the steps (1) and (2) to the sulfur is 1: 2-3, and the raw material natural gas is divided into two parts after being heated, and the two parts enter the mixing chamber and the mixing distribution chamber respectively in a volume ratio of 1: 2.
the process for producing the carbon disulfide by adopting the production system comprises the following steps: the sulfur solid enters the gasification chamber through a sulfur feed inlet, and part of sulfur reacts as follows:
S8→S6→S2
after the gasified sulfur coming out of the gasification chamber and the heated natural gas are uniformly mixed in the mixing chamber, the mixture enters the reaction chamber for reaction as follows:
CH4+S2→CS2+H2S
the other part of natural gas is mixed with carbon disulfide and gasified sulfur from the first reaction chamber and then enters the tube pass of the second reaction chamber through the gas distribution plate, the gasified sulfur which is completely reacted in the first reaction chamber further reacts with methane to generate carbon disulfide, and the reaction temperature of the second reaction chamber is controlled by adding nitrogen in the process.
In the reaction process, as the change process of the sulfur is endothermic reaction, more heat is needed, and therefore, heat is provided for the change process by arranging the combustion chamber.
In the reaction process, on one hand, the progress of the reaction is controlled by controlling the amount of natural gas entering the first reaction chamber and the second reaction chamber, the reaction of methane and sulfur is an exothermic reaction, the temperature of the reaction chambers is rapidly increased due to the excessively fast reaction, the heat load of the reaction tubes is easily increased, and the service life of the reaction tubes is reduced; on one hand, the temperature of the second reaction chamber is controlled by adding nitrogen, so that the constant temperature state of the reaction process can be ensured, the heating uniformity of the reaction tube can be improved, the service life of the furnace tube can be prolonged, and the coking can be reduced.
Compared with the prior art, the device and the method provided by the invention have the following beneficial effects:
(1) the progress of the reaction process is controlled in various ways, so that the purpose of controlling the temperature of the reaction zone is achieved.
(2) The internal combustion heating and the external nitrogen heat control are combined, so that the reaction zone is heated uniformly, the temperature of the reaction zone is controllable, and the reduction of the service life of the reaction furnace tube caused by temperature jump is avoided.
(3) This reaction system has realized thermal recycle, and the flue gas that produces the reacting furnace burning is used for heating raw materials natural gas on the one hand, and on the other hand utilizes the heat that product gas carried to preheat nitrogen gas.
(4) The reaction furnace is provided with a mixing chamber, and ceramic balls are filled in the mixing chamber, so that unvaporized sulfur can be prevented from entering the reaction chamber.
(5) The second reaction zone adopts a spiral pipe, so that the residence time of reactants in the reaction pipe can be increased, and the yield of reaction products is improved.
Drawings
Figure 1 is a carbon disulfide production system;
FIG. 2 is a burner;
FIG. 3 is a communicator;
1 is a first reaction chamber, 2 is a mixing distribution chamber, 3 is a second reaction chamber, 101 is a heating chamber, 102 is a flue gas outlet, 103 is a burner, 104 is a sulfur gasification chamber, 105 is a mixing chamber, 106 is a reaction chamber, 107 is a sulfur charging port, 108 is a natural gas first air inlet, 103-1 is a spray head, 103-2 is a mixing chamber, 103-3 is a combustion gas mixture conduit, 201 is a gas distribution plate, 202 is a natural gas second air inlet, 301 is a tube pass, 302 is a shell pass, 303 is a high-temperature nitrogen inlet, 304 is a nitrogen outlet, 305 is a high-temperature product outlet, 306 is a communicating vessel, 307 is an upper table top, 308 is a lower table top, 4 is an electric heater, 5 is a flue gas heat exchanger, 501 is a flue gas outlet, 502 is a natural gas inlet, 6 is a product heat exchanger, 601 is a low-temperature product outlet, 7 is a compressor, 701 a nitrogen inlet, and 8 is a temperature measuring device.
Detailed Description
The following further describes the embodiments of the present invention.
Examples
A carbon disulfide production system which characterized in that: comprises a carbon disulfide reaction furnace, an electric heater, a flue gas heat exchanger, a product heat exchanger and a compressor; the carbon disulfide reaction furnace is divided into three parts, namely a first reaction chamber, a mixing distribution chamber and a second reaction chamber, wherein the first reaction chamber is of a double-layer cylinder structure, the inner layer is a heating chamber, the upper part of the heating chamber is provided with a flue gas outlet, the lower part of the heating chamber is provided with a combustion gas inlet and a burner, the burner is of a cylindrical structure, the upper part of the outer layer of the first reaction chamber is provided with a sulfur gasification chamber, the middle part of the outer layer of the first reaction chamber is provided with a mixing chamber, the lower part of the outer layer of the first reaction chamber is provided with a reaction chamber, the upper part of the sulfur gasification chamber is provided with a sulfur charging port, and the side surface of the mixing chamber is provided with a first natural gas inlet; the upper part of the mixing distribution chamber is communicated with the first gas reaction chamber, the lower part of the mixing distribution chamber is provided with a gas distribution plate and is communicated with the second reaction chamber, and the side surface of the mixing distribution chamber is provided with a second natural gas inlet; the second reaction chamber is divided into a tube side and a shell side, wherein the tube side is a reaction tube, the reaction tube is communicated with the gas distribution plate through a communicating vessel, the reaction tube is of a spiral structure, the side surface of the shell side is provided with a high-temperature nitrogen inlet and a high-temperature nitrogen outlet, the lower part of the second reaction chamber is provided with a high-temperature product outlet, and the high-temperature product outlet is connected with the product heat exchanger through a pipeline;
the electric heater is of a cylindrical structure, the outer layer is provided with a silicon carbide rod heating device, the inner layer is a gas circulation pipe, and the gas circulation pipe is communicated with the high-temperature nitrogen inlet;
the flue gas heat exchanger is of a shell-and-tube structure, a shell pass is communicated with a flue gas outlet of the reaction furnace, and a tube pass is communicated with a raw gas natural gas pipeline;
the product heat exchanger is of a shell-and-tube structure, wherein the tube pass is of a spiral tube structure, the carbon disulfide product flows through the spiral tube, and the inlet of the spiral tube is communicated with the product gas outlet.
The combustor inlet is provided with a fuel gas and oxygen mixing chamber, and the combustor is provided with fuel gas nozzles, wherein the number of the nozzles is 4, and the horizontal included angle of the nozzles is 40 degrees.
In the system, the mixing chamber is filled with ceramic balls, and the particle size of the ceramic balls is 5-8 mm.
In the system, the inner layer and the outer layer of the first reaction chamber of the reaction furnace are separated by the high-temperature heat-conducting brick, wherein the main component of the high-temperature heat-conducting brick is SiO2、Al2O3、Fe2O3And CaO.
In the system, the sulfur feed inlet is provided with a micro pyrolysis device and a liquid sulfur conduit, wherein the heating temperature is 100-120 ℃.
In the system, the communicating vessel is of a circular truncated cone structure, the diameter of the upper table top is the same as that of the gas distribution plate, and the diameter is 15-19 cm; the diameter of the lower table surface is the same as that of the reaction tube of the second reaction chamber, and the diameter is 3-4 cm.
In the system, a temperature measuring device is arranged in the second reaction chamber.
The concrete implementation method of the carbon disulfide production system provided by the invention comprises the following steps:
firstly, adding sulfur into a sulfur gasification chamber through a sulfur feed port, spraying a mixture of natural gas and oxygen through a fuel gas inlet, and combusting in a combustor to raise the temperature of a heating chamber, and simultaneously raising the temperature of the sulfur gasification chamber to 500-600 ℃ to gasify sulfur in the gasification chamber;
then, flue gas from the heating chamber enters a shell pass of the flue gas heat exchanger through a flue gas outlet to exchange heat with raw material gas of a tube pass, the temperature of the raw material gas rises to 500 ℃, the raw material gas is divided into two parts, the two parts are divided into 1:2 according to the volume, the temperature-rising natural gas with a small volume enters a mixing chamber to be uniformly mixed with gasified sulfur, and then enters a reaction chamber to react to generate carbon disulfide, and meanwhile, the temperature of the reaction chamber is controlled to be 500 ℃ and the pressure is controlled to be 1.2 MPa; the other part of the heated natural gas enters a mixing distribution chamber to be mixed with the carbon disulfide and the gasified sulfur from the first gas reaction chamber, then enters a tube pass of a second reaction chamber through a gas distribution plate, the temperature in the reaction process is controlled to be 800 ℃, and the reaction product is discharged from a high-temperature product outlet after reaction;
during the reaction process, nitrogen is compressed by a compressor, then the nitrogen and product gas exchange heat in a product heat exchanger, the nitrogen enters an electric heater to be heated to 800 ℃, then enters the shell pass of a second reaction chamber, and the reaction temperature of carbon disulfide in the second reaction chamber is controlled by controlling the temperature of the nitrogen.
And purifying the product gas from the product heat exchanger to obtain the product carbon disulfide.
Claims (9)
1. A carbon disulfide production system which characterized in that: comprises a carbon disulfide reaction furnace, an electric heater, a flue gas heat exchanger, a product heat exchanger and a compressor; the carbon disulfide reaction furnace is divided into three parts, namely a first reaction chamber, a mixing distribution chamber and a second reaction chamber, wherein the first reaction chamber is of a double-layer cylinder structure, the inner layer is a heating chamber, the upper part of the heating chamber is provided with a flue gas outlet, the lower part of the heating chamber is provided with a combustion gas inlet and a burner, the burner is of a cylindrical structure, the upper part of the outer layer of the first reaction chamber is provided with a sulfur gasification chamber, the middle part of the outer layer of the first reaction chamber is provided with a mixing chamber, the lower part of the outer layer of the first reaction chamber is provided with a reaction chamber, the upper part of the sulfur gasification chamber is provided with a sulfur charging port, and the side surface of the mixing chamber is provided with a first natural gas inlet; the upper part of the mixing distribution chamber is communicated with the first reaction chamber, the lower part of the mixing distribution chamber is provided with a gas distribution plate and is communicated with the second reaction chamber, and the side surface of the mixing distribution chamber is provided with a second natural gas inlet; the second reaction chamber is divided into a tube side and a shell side, wherein the tube side is a reaction tube, the reaction tube is communicated with the gas distribution plate through a communicating vessel, the reaction tube is of a spiral structure, the side surface of the shell side is provided with a high-temperature nitrogen inlet and a high-temperature nitrogen outlet, the lower part of the second reaction chamber is provided with a high-temperature product outlet, and the high-temperature product outlet is connected with the product heat exchanger through a pipeline;
one end of the product heat exchanger is communicated with the compressor through a pipeline, and the other end of the product heat exchanger is communicated with the electric heater through a pipeline;
the electric heater is of a cylindrical structure, the outer layer is provided with a silicon carbide rod heating device, the inner layer is a gas circulation pipe, and the gas circulation pipe is communicated with the high-temperature nitrogen inlet;
the flue gas heat exchanger is of a shell-and-tube structure, a shell pass is communicated with a flue gas outlet of the reaction furnace, and a tube pass is communicated with a raw gas natural gas pipeline;
the product heat exchanger is of a shell-and-tube structure, wherein the tube pass is of a spiral tube structure, the carbon disulfide product flows through the spiral tube, and the inlet of the spiral tube is communicated with the product gas outlet.
2. A carbon disulphide production system according to claim 1, wherein: the combustor inlet is provided with a fuel gas and oxygen mixing chamber, and the combustor is provided with fuel gas nozzles, wherein the number of the nozzles is 4, and the horizontal included angle of the nozzles is 40 degrees.
3. A carbon disulphide production system according to claim 1, wherein: and ceramic balls are filled in the mixing chamber, and the particle size of the ceramic balls is 5-8 mm.
4. A carbon disulphide production system according to claim 1, wherein: the inner layer and the outer layer of the first reaction chamber of the carbon disulfide reaction furnace are separated by a high-temperature heat-conducting brick, wherein the main component of the high-temperature heat-conducting brick is SiO2、Al2O3、Fe2O3And CaO.
5. A carbon disulphide production system according to claim 1, wherein: the sulfur feed inlet is provided with a micro pyrolysis device and a liquid sulfur conduit, wherein the heating temperature is 100-120 ℃.
6. A carbon disulphide production system according to claim 1, wherein: the communicating vessel is of a circular truncated cone structure, the diameter of the upper table top is the same as that of the gas distribution plate, and the diameter of the upper table top is 15-19 cm; the diameter of the lower table surface is the same as that of the reaction tube of the second reaction chamber, and the diameter is 3-4 cm.
7. A carbon disulphide production system according to claim 1, wherein: and a temperature measuring device is arranged in the second reaction chamber.
8. A carbon disulfide production method, using the production system of claim 1, characterized in that: the method comprises the following steps:
adding sulfur into a sulfur gasification chamber from a sulfur feed port, spraying a mixture of fuel gas and oxygen through a combustion gas inlet, and combusting in a combustor to raise the temperature of a heating chamber, and simultaneously raising the temperature of the sulfur gasification chamber to 500-600 ℃ to gasify sulfur in the gasification chamber;
flue gas from the heating chamber enters a shell pass of the flue gas heat exchanger through a flue gas outlet to exchange heat with raw material gas of a tube pass, the temperature of the raw material gas rises to 400-500 ℃, the raw material gas is divided into two parts, one part of the heated natural gas enters a mixing chamber to be uniformly mixed with gasified sulfur, and then enters a reaction chamber to react to generate carbon disulfide, and meanwhile, the temperature of the reaction chamber is controlled to be 500-900 ℃, and the pressure is controlled to be 1.2-1.5 MPa; the other part of the heated natural gas enters the mixing distribution chamber to be mixed with the carbon disulfide and the gasified sulfur from the first reaction chamber, then enters the tube pass of the second reaction chamber through the gas distribution plate, and is discharged from the high-temperature product outlet after reaction;
in the reaction process, the nitrogen is compressed by a compressor, then the nitrogen and the product gas exchange heat in a product heat exchanger, the nitrogen enters an electric heater to be heated to 600-800 ℃, then enters the shell pass of a second reaction chamber, and the reaction temperature of the carbon disulfide in the second reaction chamber is controlled by controlling the temperature of the nitrogen.
9. A carbon disulphide production process according to claim 8, wherein: the fuel gas is any one of coke oven gas, natural gas, coal bed gas and liquefied petroleum gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810401491.9A CN108394902B (en) | 2018-04-28 | 2018-04-28 | Carbon disulfide production system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810401491.9A CN108394902B (en) | 2018-04-28 | 2018-04-28 | Carbon disulfide production system and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108394902A CN108394902A (en) | 2018-08-14 |
| CN108394902B true CN108394902B (en) | 2021-07-27 |
Family
ID=63100775
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810401491.9A Active CN108394902B (en) | 2018-04-28 | 2018-04-28 | Carbon disulfide production system and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108394902B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112374499B (en) * | 2020-12-02 | 2022-07-12 | 河南省化工研究所有限责任公司 | Carbon disulfide production equipment and production method |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102004013283A1 (en) * | 2004-03-18 | 2005-10-13 | Guennadi, Berner | Combined production of carbon disulfide and sulfuric acid from sulfur, without use of natural gas fuel, by using heat from oxidation of sulfur to drive the endothermic carbon disulfide production reaction |
| CN1919731A (en) * | 2006-09-18 | 2007-02-28 | 孔庆然 | Preparation method for carbon bisulfide |
| CN104671243A (en) * | 2015-03-26 | 2015-06-03 | 张贯彪 | Carbon disulfide reacting furnace |
| CN204429254U (en) * | 2015-01-06 | 2015-07-01 | 张自杰 | A kind of totally-enclosed fluid bed carbon disulphide production device continuously |
| CN107244674A (en) * | 2017-06-21 | 2017-10-13 | 阳城县绿色铸造研发中心 | Carbon disulfide gasification reacting furnace heater and heating means |
| CN107673353A (en) * | 2017-10-10 | 2018-02-09 | 重庆兴发金冠化工有限公司 | A kind of raw material heating system and technique for producing carbon disulfide |
-
2018
- 2018-04-28 CN CN201810401491.9A patent/CN108394902B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102004013283A1 (en) * | 2004-03-18 | 2005-10-13 | Guennadi, Berner | Combined production of carbon disulfide and sulfuric acid from sulfur, without use of natural gas fuel, by using heat from oxidation of sulfur to drive the endothermic carbon disulfide production reaction |
| CN1919731A (en) * | 2006-09-18 | 2007-02-28 | 孔庆然 | Preparation method for carbon bisulfide |
| CN204429254U (en) * | 2015-01-06 | 2015-07-01 | 张自杰 | A kind of totally-enclosed fluid bed carbon disulphide production device continuously |
| CN104671243A (en) * | 2015-03-26 | 2015-06-03 | 张贯彪 | Carbon disulfide reacting furnace |
| CN107244674A (en) * | 2017-06-21 | 2017-10-13 | 阳城县绿色铸造研发中心 | Carbon disulfide gasification reacting furnace heater and heating means |
| CN107673353A (en) * | 2017-10-10 | 2018-02-09 | 重庆兴发金冠化工有限公司 | A kind of raw material heating system and technique for producing carbon disulfide |
Non-Patent Citations (1)
| Title |
|---|
| "由天然气与硫磺制备CS2初探";天春云 等;《大庆石油学院学报》;19851231(第3期，总第27期);第93-97页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108394902A (en) | 2018-08-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102115675B (en) | Heavy oil lightening method and device | |
| CN102492478B (en) | Novel two-stage multi-nozzle pressurized gasifier and its gasification method | |
| KR101955740B1 (en) | Method for the parallel production of hydrogen and carbon-containing products | |
| CN103998580A (en) | Method and device for the entrained flow gasification of solid fuels under pressure | |
| CN201195718Y (en) | Novel gasification furnace propitious to recycle heat | |
| CN1021730C (en) | Process and apparatus for hydrocarbons conversion | |
| CN109628157B (en) | Continuous biomass pyrolysis gasification device and method | |
| CN107083249A (en) | A kind of fine coal prepares air flow bed pyrolysis oven, the system and method vented one's spleen rich in methane thermal | |
| CN101144022A (en) | Three-section type biomass gasifying furnace | |
| CN101230281A (en) | Solid biomass semi-water coal-gas producer | |
| CN102234522A (en) | Processing method and apparatus for converting heavy oil to light fractions | |
| CN100362084C (en) | Internal and external circulation coal gasification method and device | |
| CN105084361B (en) | A kind of gas heating multistage calcium carbide reactor and its technique | |
| CN102796568B (en) | Device and technology for producing blau-gas and carbon monoxide | |
| CN114045373A (en) | Gas-based shaft furnace direct reduction method | |
| CN108394902B (en) | Carbon disulfide production system and method | |
| CN101880550B (en) | High-temperature solid fuel gasification device | |
| CN114182052A (en) | Direct reduction method and reduction system for hydrocarbon-rich gas-based shaft furnace | |
| CN113652508A (en) | Electromagnetic induction heating reforming furnace and using method thereof | |
| CN116143425B (en) | Central burner type lime kiln | |
| JP5860469B2 (en) | Method and equipment for producing coke during indirect heating gasification | |
| CN218879751U (en) | Central burner type lime kiln | |
| CN202214340U (en) | Continuous gasification and tar removing device for biomass moving bed | |
| CN206902071U (en) | It is a kind of to prepare the air flow bed pyrolysis oven vented one's spleen rich in methane thermal and system | |
| CN100503437C (en) | Reaction furnace for manufacturing carbon disulfide using high pressure non catalytic natural gas method |
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 | ||
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20210709 Address after: 014000 1-1112, Kunlun square, west of linyinzhong road and south of Youyi street, Kundulun District, Baotou City, Inner Mongolia Autonomous Region Applicant after: Inner Mongolia Xiangtai Environmental Technology Co.,Ltd. Address before: 277000 Fuyuan community, Taishan Road, Xuecheng District, Zaozhuang City, Shandong Province Applicant before: Meng Tao |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |