CN214810706U - Tube type fixed bed reactor for producing carbonyl sulfide - Google Patents
Tube type fixed bed reactor for producing carbonyl sulfide Download PDFInfo
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- CN214810706U CN214810706U CN202023243537.0U CN202023243537U CN214810706U CN 214810706 U CN214810706 U CN 214810706U CN 202023243537 U CN202023243537 U CN 202023243537U CN 214810706 U CN214810706 U CN 214810706U
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Abstract
The utility model provides a tubular fixed bed reactor for producing carbonyl sulfide, which comprises a shell, wherein liquid sulfur is injected into the shell; an upper air inlet pipe fitting and a lower air inlet pipe fitting are arranged in the shell, the outlet end of the upper air inlet pipe fitting is positioned above the liquid sulfur liquid level, and CO is introduced above the liquid sulfur liquid level through the upper air inlet pipe fitting and is mixed with sulfur vapor; the outlet end of the lower air inlet pipe extends below the liquid sulfur level, and CO is introduced into the liquid sulfur through the lower air inlet pipe to bubble and sublimate part of the liquid sulfur; and a catalyst tube array penetrating through the liquid sulfur layer is also arranged in the shell. The whole course of the reaction is carried out in a closed manner, sulfur vapor can be fully mixed with CO through the upper air inlet pipe fitting and the lower air inlet pipe fitting, the gasification amount of liquid sulfur can be accurately adjusted, the production cost is greatly saved, the raw material utilization rate is improved, the process and the control are simple, the reaction is complete, the yield is high, and the continuous production can be realized.
Description
Technical Field
The utility model belongs to the technical field of the production of carbonyl sulfide, a shell and tube fixed bed reactor for producing carbonyl sulfide is related to.
Background
Carbonyl sulfide (COS), also known as carbonyl sulfide, is a gas widely used in the production of medicines, pesticides and other chemical products, has been used as a fumigant for grains, has the characteristics of moderate toxicity, easy degradation and the like, and is also an important raw material for synthesizing thiocarbamate pesticides and insecticides. In recent years, high purity carbon oxysulfide has been used in integrated circuit etching processes, and the trend is strong.
At present, the method for preparing the carbonyl sulfide is divided into a dry method and a wet method, the representative process for producing the carbonyl sulfide by the wet method is an ammonium thiocyanate method, the reaction condition of the method is mild, and the risk factors in the reaction process are few. The dry method is mainly characterized in that CO and high-temperature sulfur are reacted to generate carbonyl sulfide under the condition of no solvent, the method has simple flow, high yield and environment friendliness, and has the defects that the reaction process needs to be carried out under the high-temperature condition by a catalyst, and H is easily formed when the reaction is not good2S、CS2、SO2、CO2And the like, and carbon monoxide is a combustible toxic gas, so the production process is dangerous. Under the background, a carbon oxysulfide fixed bed reactor with reasonable process, safety, reliability and strong controllability needs to be developed.
CN205653172U discloses a carbonyl sulfide apparatus for producing, including carbonyl sulfide reation kettle, calcium chloride reaction column and storage tank, the storage tank passes through the calcium chloride reaction column and is connected with carbonyl sulfide reation kettle, forms the air flue that supplies carbonyl sulfide to pass in the calcium chloride reaction column, and calcium chloride reaction column one end is inserted in the carbonyl sulfide reation kettle and is opened there is the hand-hole that supplies carbonyl sulfide to get into the air flue.
CN110127702A discloses a method and a device for preparing carbonyl sulfide gas, the method comprises the steps of simultaneously dripping ammonium thiocyanate solution and concentrated sulfuric acid into sulfuric acid solution with a certain concentration for reaction, and filling the generated carbonyl sulfide gas after condensation, drying and compression; the device is formed by connecting a reaction kettle, a raw material dripping tank A, a raw material dripping tank B, a condenser, a dryer, a compressor and a product bottle through pipelines.
CN205683986U discloses a carbon oxysulfide reation kettle, including the reation kettle body, be equipped with feed inlet and discharge gate on the reaction housing, discharge gate department is equipped with ejection of compact pipeline, is equipped with solid sulphur device between discharge gate and ejection of compact pipeline, and solid sulphur device includes the casing and realizes the sulphur pipe that advances that casing and discharge gate are connected, sets up the solid sulphur board that has the mesh in the casing, and ejection of compact pipe connection is on the casing, the casing is equipped with annular sealed pad and can dismantle fixed connection through the connecting piece that sets up on first boss and second boss including the left casing that has first boss and the right casing that has the second boss between the two.
However, the yield of the existing fixed bed reactor is low, and the waste of raw materials is serious, so that improvement on the existing reactor is urgently needed to improve the utilization rate of raw materials and the yield of products.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a not enough to prior art exists, the utility model provides a shell and tube fixed bed reactor for producing carbonyl sulfide, the utility model provides a shell and tube fixed bed reactor's rational in infrastructure, the whole inclosed of reaction goes on, not only makes sulphur vapour can fully mix with CO through setting up the pipe fitting that admits air and the pipe fitting that admits air down, also can accurate regulation liquid sulphur gasification volume, has greatly practiced thrift manufacturing cost, has improved raw materials utilization ratio, and technology and control are simple, and the reaction is complete, and the yield is high, can realize serialization production.
To achieve the purpose, the utility model adopts the following technical proposal:
the utility model provides a tubular fixed bed reactor for producing carbonyl sulfide, which comprises a shell, wherein liquid sulfur is injected into the shell; an upper air inlet pipe fitting and a lower air inlet pipe fitting are arranged in the shell, the outlet end of the upper air inlet pipe fitting is positioned above the liquid sulfur liquid level, and CO is introduced above the liquid sulfur liquid level through the upper air inlet pipe fitting and is mixed with sulfur vapor; the outlet end of the lower air inlet pipe extends below the liquid sulfur level, and CO is introduced into the liquid sulfur through the lower air inlet pipe to bubble and sublimate part of the liquid sulfur; and a catalyst tube array penetrating through the liquid sulfur layer is also arranged in the shell.
The utility model provides a shell and tube fixed bed reactor's rational in infrastructure, the whole inclosed of reaction goes on, through set up admit air pipe fitting and admit air pipe fitting down not only make sulphur vapour can fully mix with CO, also can accurate regulation liquid sulphur evaporation capacity, has greatly practiced thrift manufacturing cost, has improved utilization of raw materials rate, and technology and control are simple, and the reaction is complete, and the yield is high, can realize serialization production.
As an optimized technical scheme of the utility model, the inside top of casing be provided with the tube sheet, the inside below of casing be provided with down the tube sheet, catalyst pipe array be fixed in between tube sheet and the lower tube sheet.
The catalyst tube array comprises at least 2 catalyst tubes, catalysts are filled in the catalyst tubes, two ends of each catalyst tube penetrate through the upper tube plate and the lower tube plate respectively, and the catalyst tubes are arranged in the shell in a matrix manner.
The upper tube plate is provided with holes, so that the mixed gas of CO and sulfur vapor passes through the upper tube plate.
The bottom surface of the lower tube plate is sequentially stacked with a screen and a packing support plate, and the packing support plate is used for supporting the screen and the catalyst packing.
In a preferred embodiment of the present invention, the number of the catalyst tubes is 2 to 400, and may be, for example, 2, 50, 100, 150, 200, 250, 300, 350 or 400, but is not limited to the above-mentioned values, and other values not listed in the above-mentioned range are also applicable.
As a preferred technical scheme of the utility model, the lower air inlet pipe fitting comprises at least two mutually independent distribution pipes extending into the liquid sulfur, and one end of each distribution pipe is connected with one end of the lower air inlet pipe; the lower air inlet pipe partially extends out of the shell, CO is introduced into the shell through the lower air inlet pipe, and a lower air inlet regulating valve is arranged on the part of the lower air inlet pipe extending into the shell.
The tail end of the distribution pipe is provided with a gas distribution pipe, the gas distribution pipe is provided with a through hole, CO introduced from the upper gas inlet pipe flows through the distribution pipe, liquid sulfur is sprayed into the distribution pipe through the gas distribution pipe, bubbles are formed in the liquid sulfur layer, and part of the liquid sulfur is sublimated.
The upper air inlet pipe piece comprises an upper air inlet pipe, part of the upper air inlet pipe extends out of the shell, and an upper air adjusting valve is arranged on the part of the upper air inlet pipe, which extends out of the shell.
As an optimized technical scheme of the utility model, the quantity of distributing pipe be 2 ~ 4.
In a preferred embodiment of the present invention, the vertical distance between the lower end of the air distribution pipe and the lower pipe plate is 100 to 500mm, for example, 100mm, 150mm, 200mm, 250mm, 300mm, 350mm, 400mm, 450mm or 500mm, but the present invention is not limited to the above-mentioned values, and other values not listed in the above-mentioned value range are also applicable.
As a preferred technical scheme of the utility model, the catalyst intraductal catalyst thermodetector that inserts.
The liquid sulfur thermometer is inserted into the liquid sulfur, and a thermometer sleeve is sleeved on the periphery of the liquid sulfur thermometer.
As an optimal technical scheme, the casing lateral wall that liquid sulphur was located on be provided with liquid phase heating device, liquid phase heating device heat liquid sulphur.
And the gas-phase heating device is arranged on the outer side wall of the shell above the liquid sulfur liquid level and is used for heating sulfur steam above the liquid sulfur liquid level.
As an optimal technical scheme of the utility model, the casing dock in proper order by upper cover, barrel and low head and form.
The upper end socket is an elliptical end socket, the lower end socket is a conical end socket, a discharge hole is formed in the bottom of the conical end socket, the conical angle of the conical end socket is 60-120 degrees, and can be 60 degrees, 65 degrees, 70 degrees, 75 degrees, 80 degrees, 85 degrees, 90 degrees, 95 degrees, 100 degrees, 105 degrees, 110 degrees, 115 degrees or 120 degrees, but the conical angle is not limited to the enumerated numerical values, and other numerical values which are not enumerated in the numerical value range are also applicable.
The top of the shell is provided with a pressure measuring port, and a pressure transmitter is arranged at the position of the pressure measuring port.
And the top of the shell is also provided with a vent.
The lower part of the outer side wall of the shell is provided with a liquid sulfur inlet and a discharge port, and the liquid sulfur inlet is provided with a liquid sulfur feeding regulating valve.
The utility model discloses in, the periphery of liquid sulphur import is provided with jacket pipe optionally and keeps warm to prevent that sulphur from blockking up the pipeline.
An overflow port is arranged above the outer side wall of the shell and is positioned below the upper tube plate.
The outer side wall of the cylinder body is provided with four mutually symmetrical lug seats.
As an optimized technical scheme, shell and tube fixed bed reactor still include the controller, the controller respectively independent ground electric connection liquid sulphur thermoscope and catalyst thermoscope, the controller respectively independent feedback control liquid phase heating device's power, gaseous phase heating device's power and the aperture of liquid sulphur feeding governing valve.
And the liquid sulfur thermometer outputs a feedback signal to the controller, the controller receives the feedback signal and then compares the feedback signal with the preset liquid sulfur temperature, and the power of the liquid phase heating device and the opening of the liquid sulfur feeding regulating valve are fed back and controlled according to a comparison result.
The catalyst temperature detector outputs a feedback signal to the controller, the controller receives the feedback signal and compares the feedback signal with a preset reaction temperature, and the power of the gas-phase heating device is fed back and controlled according to a comparison result.
The utility model discloses set up the controller, realized the real time control to reaction temperature and liquid sulphur temperature. Specifically, the liquid phase heating device can be selected as a liquid phase far infrared heater, the gas phase heating device can be selected as a gas phase far infrared heater, and the liquid phase far infrared heater and the gas phase far infrared heater respectively heat the liquid sulfur and the mixed gas phase. The controller adjusts the carbon monoxide air inflow of the lower air inlet pipe fitting by controlling the opening degrees of the upper air inlet adjusting valve and the lower air inlet adjusting valve, thereby controlling the gasification amount of the liquid sulfur and adjusting the reactant proportion. The controller adjusts the power of the liquid-phase far infrared heater or the opening of the liquid sulfur feeding adjusting valve through the temperature fed back by the liquid sulfur thermometer, so that the temperature of the liquid sulfur is maintained in a certain range. The controller adjusts the power of the gas-phase far-infrared heater through the temperature fed back by the catalyst temperature detector, so that the reaction temperature is maintained in a certain range.
Exemplarily, the utility model provides a shell and tube fixed bed reactor's theory of operation as follows:
during production, liquid sulfur continuously enters the reactor through the liquid sulfur inlet, fills the space between the shell and the catalyst pipe, and discharges redundant liquid sulfur through the overflow port; part of CO gas is introduced into the shell through the gas inlet pipe, and liquid sulfur is sprayed into the shell through the gas distribution pipe through the distribution pipe, so that bubbles are formed in the liquid sulfur layer; in the bubbling process, partial liquid sulfur is sublimated to form sulfur vapor; introducing the residual CO gas above the liquid sulfur liquid level through an upper gas inlet pipe and mixing the residual CO gas with sulfur vapor to form mixed gas; the mixed gas passes through the upper tube plate and the catalyst tube, reacts under the action of the catalyst to generate carbonyl sulfide, and the generated carbonyl sulfide is discharged from a discharge port and processed in the next working procedure.
In the production process, the reaction temperature and the liquid sulfur temperature are monitored in real time through a liquid sulfur thermometer and a catalyst thermometer, the liquid sulfur thermometer continuously outputs a feedback signal to a controller, the controller receives the feedback signal and then compares the feedback signal with the preset liquid sulfur temperature, and the power of a liquid phase heating device and the opening of a liquid sulfur feeding regulating valve are fed back and controlled according to the comparison result; meanwhile, the catalyst temperature detector outputs a feedback signal to the controller, the controller receives the feedback signal and then compares the feedback signal with a preset reaction temperature, and the power of the gas-phase heating device is fed back and controlled according to a comparison result.
Compared with the prior art, the beneficial effects of the utility model are that:
the utility model provides a shell and tube fixed bed reactor's rational in infrastructure, the whole inclosed of reaction goes on, through set up admit air the pipe fitting and admit air the pipe fitting down not only make sulphur vapour can fully mix with CO, also can accurate regulation liquid sulphur gasification volume, has greatly practiced thrift manufacturing cost, and technology and control are simple, and the reaction is the yield height completely, can realize serialization production.
Drawings
FIG. 1 is a schematic structural diagram of a tubular fixed bed reactor according to an embodiment of the present invention;
fig. 2 is a schematic structural view of a lower air inlet pipe fitting according to an embodiment of the present invention;
fig. 3 is a partially enlarged view of the area a in fig. 1.
Wherein, 1-lower end enclosure; 2-a filler pallet; 3-screening a screen; 4-lower tube plate; 5-a cylinder body; 6-ear seat; 7-a catalyst tube; 8-sleeve of the thermodetector; 9-upper tube plate; 10-a vent; 11-lower air inlet pipe fitting; 12-upper air inlet pipe fitting; 13-upper end enclosure; 14-liquid phase heating means; 15-a pressure transmitter; 16-liquid sulfur thermometers; 17-catalyst thermometers; 18-upper air regulating valve; 19-lower inlet regulating valve; 20-liquid sulfur feed regulating valve; 21-a gas phase heating device; 22-an overflow port; 23-a discharge outlet; 24-a drain port; 25-lower air inlet pipe; 26-a distribution pipe; 27-gas distribution pipe.
Detailed Description
It is to be understood that in the description of the present invention, the terms "central," "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in the orientation or positional relationship indicated in the drawings for the purpose of convenience and simplicity of description, and are not intended to indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are not to be construed as limiting the present invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
It should be noted that, unless explicitly stated or limited otherwise, the terms "disposed," "connected" and "connected" in the description of the present invention are to be construed broadly, and may for example be fixedly connected, detachably connected or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
The technical solution of the present invention is further explained by the following embodiments with reference to the accompanying drawings.
In a specific embodiment, the utility model provides a shell and tube fixed bed reactor for producing carbonyl sulfide, shell and tube fixed bed reactor as shown in figure 1, including the casing, pour into liquid sulphur into in the casing, insert liquid sulphur thermodetector 16 in the liquid sulphur, 16 periphery covers of liquid sulphur thermodetector are equipped with thermodetector sleeve pipe 8. An upper air inlet pipe fitting 12 and a lower air inlet pipe fitting 11 are arranged in the shell, the outlet end of the upper air inlet pipe fitting 12 is positioned above the liquid sulfur liquid level, and CO is introduced from the upper air inlet pipe fitting 12 to the liquid sulfur liquid level and is mixed with sulfur vapor; the outlet end of the lower air inlet pipe fitting 11 extends below the liquid sulfur level, and CO is introduced into the liquid sulfur through the lower air inlet pipe fitting 11, so that bubbles are formed in the liquid sulfur layer and part of the liquid sulfur is sublimated; an array of catalyst tubes 7 is also provided inside the housing, passing through the liquid sulphur layer.
An upper tube plate 9 is arranged above the inside of the shell, a lower tube plate 4 is arranged below the inside of the shell, and the catalyst tubes 7 are fixed between the upper tube plate 9 and the lower tube plate 4 in an array. The catalyst tube 7 array comprises at least 2 catalyst tubes 7, and further the number of the catalyst tubes 7 is 2-400. Catalyst is filled in the catalyst tube 7, a catalyst thermometer 17 is inserted in the catalyst tube 7, two ends of the catalyst tube 7 respectively penetrate the upper tube plate 9 and the lower tube plate 4, and the catalyst tubes 7 are arranged in a matrix in the shell. The bottom surface of the lower tube plate 4 is sequentially laminated with a screen 3 and a packing pallet 2 (as shown in fig. 3), and the packing pallet 2 is used for supporting the screen 3 and the catalyst packing.
As shown in fig. 2, the lower air inlet pipe 11 includes at least two independent distribution pipes 26 extending into the liquid sulfur, and further, the number of the distribution pipes 26 is 2 to 4. One end of the distribution pipe 26 is connected and communicated with one end of the lower air inlet pipe 25; the lower air inlet pipe 25 partially extends out of the shell, CO is introduced into the shell through the lower air inlet pipe 25, and the lower air inlet regulating valve 19 is arranged on the part, extending into the shell, of the lower air inlet pipe 25. The tail end of the distribution pipe 26 is provided with a gas distribution pipe 27, the gas distribution pipe 27 is provided with a through hole, and the vertical distance between the lower end of the gas distribution pipe 27 and the lower pipe plate 4 is 100-500 mm. The CO introduced through the lower inlet pipe 25 flows through the distribution pipe 26 and is sprayed into the liquid sulfur layer through the gas distribution pipe 27, so that bubbles are formed in the liquid sulfur layer and a part of the liquid sulfur is sublimated. The upper inlet pipe member 12 includes an upper inlet pipe partially extending from the housing, and an upper inlet regulating valve 18 is provided on a portion of the upper inlet pipe extending from the housing.
And a liquid phase heating device 14 is arranged on the outer side wall of the shell where the liquid sulfur is located, and the liquid phase heating device 14 heats the liquid sulfur. And the gas phase heating device 21 is arranged on the outer side wall of the shell above the liquid sulfur liquid level, and the gas phase heating device 21 heats sulfur steam above the liquid sulfur liquid level.
The casing is by upper cover 13, barrel 5 and lower head 1 butt joint formation in proper order, and upper cover 13 is oval head, and lower head 1 is the toper head, and bin outlet 23 has been seted up to the bottom of toper head, and the cone angle of toper head is 60 ~ 120. The top of the shell is provided with a pressure measuring port, the pressure measuring port is provided with a pressure transmitter 15, and the top of the shell is also provided with a vent 10. The lower part of the outer side wall of the shell is provided with a liquid sulfur inlet and a discharge port 24, and the liquid sulfur inlet is provided with a liquid sulfur feeding regulating valve 20. An overflow port 22 is arranged above the outer side wall of the shell, and the overflow port 22 is positioned below the upper tube plate 9. Four mutually symmetrical lug seats 6 are arranged on the outer side wall of the cylinder 5.
The tubular fixed bed reactor also comprises a controller, the controller is respectively and independently electrically connected with the liquid sulfur temperature detector 16 and the catalyst temperature detector 17, and the controller respectively and independently controls the power of the liquid phase heating device 14, the power of the gas phase heating device 21 and the opening degree of the liquid sulfur feeding regulating valve 20 in a feedback mode. The specific control logic is as follows: the liquid sulfur thermometer 16 outputs a feedback signal to the controller, the controller receives the feedback signal and compares the feedback signal with a preset liquid sulfur temperature, and the power of the liquid phase heating device 14 and the opening of the liquid sulfur feeding regulating valve 20 are feedback-controlled according to a comparison result. The catalyst temperature detector 17 outputs a feedback signal to the controller, the controller compares the feedback signal with a preset reaction temperature after receiving the feedback signal, and the power of the gas phase heating device 21 is feedback-controlled according to the comparison result.
In another embodiment, the present invention provides a method for producing carbonyl sulfide by using the tubular fixed bed reactor provided in the above embodiment, the method specifically comprises the following steps:
during production, liquid sulfur continuously enters the reactor through the liquid sulfur inlet, fills the space between the shell and the catalyst pipe 7, and discharges redundant liquid sulfur through the overflow port 22; part of CO gas is introduced into the shell through a lower gas inlet pipe 25, and is sprayed into the liquid sulfur through a distribution pipe 26 and a gas distribution pipe 27, so that bubbles are formed in the liquid sulfur layer, and in the bubbling process, part of the liquid sulfur is sublimated to form sulfur vapor; introducing the residual CO gas above the liquid sulfur liquid level through an upper gas inlet pipe and mixing the residual CO gas with sulfur vapor to form mixed gas; the mixed gas passes through the upper tube plate 9 and the catalyst tube 7 and reacts under the action of the catalyst to generate carbonyl sulfide, and the generated carbonyl sulfide is discharged from the discharge opening 23 and is processed in the next procedure.
In the production process, the reaction temperature and the liquid sulfur temperature are monitored in real time through the liquid sulfur temperature detector 16 and the catalyst temperature detector 17, the liquid sulfur temperature detector 16 continuously outputs a feedback signal to the controller, the controller receives the feedback signal and then compares the feedback signal with the preset liquid sulfur temperature, and the power of the liquid phase heating device 14 and the opening of the liquid sulfur feeding regulating valve 20 are controlled in a feedback mode according to the comparison result; meanwhile, the catalyst temperature detector 17 outputs a feedback signal to the controller, the controller compares the feedback signal with a preset reaction temperature after receiving the feedback signal, and the power of the gas phase heating device 21 is feedback-controlled according to the comparison result.
The applicant states that the above description is only a specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and those skilled in the art should understand that any changes or substitutions easily conceivable by those skilled in the art within the technical scope of the present invention are within the protection scope and the disclosure scope of the present invention.
Claims (10)
1. A tubular fixed bed reactor for producing carbonyl sulfide is characterized in that the tubular fixed bed reactor comprises a shell, wherein liquid sulfur is injected into the shell; an upper air inlet pipe fitting and a lower air inlet pipe fitting are arranged in the shell, the outlet end of the upper air inlet pipe fitting is positioned above the liquid sulfur liquid level, and CO is introduced above the liquid sulfur liquid level through the upper air inlet pipe fitting and is mixed with sulfur vapor; the outlet end of the lower air inlet pipe extends below the liquid sulfur level, and CO is introduced into the liquid sulfur through the lower air inlet pipe to bubble and sublimate part of the liquid sulfur; and a catalyst tube array penetrating through the liquid sulfur layer is also arranged in the shell.
2. The tubular fixed bed reactor of claim 1 wherein an upper tube sheet is disposed above the interior of said shell and a lower tube sheet is disposed below the interior of said shell, said array of catalyst tubes being secured between said upper and lower tube sheets;
the catalyst tube array comprises at least 2 catalyst tubes, catalysts are filled in the catalyst tubes, two ends of each catalyst tube respectively penetrate through the upper tube plate and the lower tube plate, and the catalyst tubes are arranged in a matrix manner in the shell;
the upper tube plate is provided with holes, so that the mixed gas of CO and sulfur vapor passes through the upper tube plate;
the bottom surface of the lower tube plate is sequentially stacked with a screen and a packing support plate, and the packing support plate is used for supporting the screen and the catalyst packing.
3. The shell and tube fixed bed reactor according to claim 2, wherein the number of the catalyst tubes is 2 to 400.
4. The tubular fixed bed reactor according to claim 2, wherein said lower inlet tube member comprises at least two separate distribution tubes extending into the liquid sulfur, one end of said distribution tubes being connected to and communicating with one end of the lower inlet tube; the lower air inlet pipe partially extends out of the shell, CO is introduced into the shell through the lower air inlet pipe, and a lower air inlet regulating valve is arranged at the part of the lower air inlet pipe extending into the shell;
the tail end of the distribution pipe is provided with a gas distribution pipe, the gas distribution pipe is provided with a through hole, CO introduced from the upper gas inlet pipe flows through the distribution pipe, liquid sulfur is sprayed from the gas distribution pipe, bubbles are formed in the liquid sulfur layer, and part of the liquid sulfur is sublimated;
the upper air inlet pipe piece comprises an upper air inlet pipe, part of the upper air inlet pipe extends out of the shell, and an upper air adjusting valve is arranged on the part of the upper air inlet pipe, which extends out of the shell.
5. The tube type fixed bed reactor according to claim 4, wherein the number of the distribution tubes is 2-4.
6. The tubular fixed bed reactor according to claim 4, wherein the vertical distance between the lower end of the gas distribution tube and the lower tube plate is 100 to 500 mm.
7. The shell and tube fixed bed reactor of claim 2, wherein a catalyst thermometer is inserted into the catalyst tube;
the liquid sulfur thermometer is inserted into the liquid sulfur, and a thermometer sleeve is sleeved on the periphery of the liquid sulfur thermometer.
8. The tubular fixed bed reactor according to claim 7, characterized in that a liquid phase heating device is arranged on the outer side wall of the shell where the liquid sulfur is located, and the liquid phase heating device heats the liquid sulfur;
and the gas-phase heating device is arranged on the outer side wall of the shell above the liquid sulfur liquid level and is used for heating sulfur steam above the liquid sulfur liquid level.
9. The tube array type fixed bed reactor according to claim 1, wherein the shell is formed by sequentially butting an upper end enclosure, a cylinder body and a lower end enclosure;
the upper end socket is an elliptical end socket, the lower end socket is a conical end socket, a discharge hole is formed in the bottom of the conical end socket, and the cone angle of the conical end socket is 60-120 degrees;
the top of the shell is provided with a pressure measuring port, and a pressure transmitter is arranged at the pressure measuring port;
the top of the shell is also provided with a vent;
a liquid sulfur inlet and a liquid sulfur exhaust port are arranged below the outer side wall of the shell, and a liquid sulfur feeding regulating valve is arranged at the liquid sulfur inlet;
an overflow port is arranged above the outer side wall of the shell and is positioned below the upper tube plate;
the outer side wall of the cylinder body is provided with four mutually symmetrical lug seats.
10. The tubular fixed bed reactor according to claim 8, characterized in that the tubular fixed bed reactor further comprises a controller, the controller is respectively and independently electrically connected with the liquid sulfur thermometer and the catalyst thermometer, and the controller respectively and independently controls the power of the liquid phase heating device, the power of the gas phase heating device and the opening degree of the liquid sulfur feeding regulating valve in a feedback manner;
the liquid sulfur temperature detector outputs a feedback signal to the controller, the controller receives the feedback signal and compares the feedback signal with a preset liquid sulfur temperature, and the power of the liquid phase heating device and the opening of the liquid sulfur feeding regulating valve are controlled in a feedback mode according to a comparison result;
the catalyst temperature detector outputs a feedback signal to the controller, the controller receives the feedback signal and compares the feedback signal with a preset reaction temperature, and the power of the gas-phase heating device is fed back and controlled according to a comparison result.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114682171A (en) * | 2022-04-15 | 2022-07-01 | 北京海望氢能科技有限公司 | High-efficiency dehydrogenation or hydrogenation reactor and dehydrogenation or hydrogenation process system for organic liquid |
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2020
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114682171A (en) * | 2022-04-15 | 2022-07-01 | 北京海望氢能科技有限公司 | High-efficiency dehydrogenation or hydrogenation reactor and dehydrogenation or hydrogenation process system for organic liquid |
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