CN115715959A - Unloading equipment and method for coal-to-ethylene glycol hydrogenation catalyst - Google Patents
Unloading equipment and method for coal-to-ethylene glycol hydrogenation catalyst Download PDFInfo
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- CN115715959A CN115715959A CN202110973715.5A CN202110973715A CN115715959A CN 115715959 A CN115715959 A CN 115715959A CN 202110973715 A CN202110973715 A CN 202110973715A CN 115715959 A CN115715959 A CN 115715959A
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Abstract
The invention provides a device and a method for unloading a coal-to-ethylene glycol hydrogenation catalyst, wherein the device comprises a catalyst unloading device and a vacuum pump which are connected with each other; the catalyst remover comprises a barrel and a support frame, wherein the barrel is welded on the support frame, and the barrel comprises an air extraction area, a material storage area and a material discharging area which are connected from top to bottom. According to the invention, the catalyst is removed in a nitrogen environment, so that passivation before catalyst removal is not needed, personnel and catalyst powder are in close contact during removal, the damage to equipment and personnel is reduced, the operation time is shortened, and only 2-3 days are needed.
Description
Technical Field
The invention relates to the technical field of coal chemical industry, in particular to a coal-to-ethylene glycol hydrogenation catalyst unloading device and method.
Background
The technology for preparing glycol from coal refers to the coupling generation of high-purity carbon monoxide, hydrogen and carbon monoxide by gasifying and purifying coalAnd the oxalic ester is subjected to hydrogenation to generate ethylene glycol. The oxalate hydrogenation reaction needs a catalyst which is a copper catalyst, and the catalyst reduces CUO in the catalyst component into CU when in use + Or metallic copper, and SiO in the composition 2 Dissolving and solidifying together, and has activity. Once the copper in this phase is sufficiently contacted with air, it will burn violently and generate a large amount of heat of reaction, so that the catalyst needs to be passivated by slowly adding air before the removal of the deactivated hydrogenation catalyst. However, in the passivation process, the medium during the normal operation of the hydrogenation circulator is mainly hydrogen with low density, while the medium during the passivation is nitrogen, oxygen and high density, so that the circulation gas amount is less than one tenth of the normal operation gas amount, the local temperature accumulation or temperature runaway phenomenon of the reactor is easily caused, the catalyst is also incompletely passivated, and the catalyst is violently combusted when meeting oxygen in the process of contact with air during the removal, so that the damage of a reactor tube is caused, and the personal safety of a discharging person is also endangered. And organic matters such as methanol, methyl glycolate, diethylene glycol and the like adsorbed on the surface of the catalyst in the normal operation process are coked on the surface of the reactor tube array due to high temperature, the coked matters have strong adsorption capacity on the surface of the tube array and need to be cleaned by a high-pressure water gun, and the damage of the reactor tube array is easily caused by high-temperature and high-pressure cleaning, so that the service life of the reactor is influenced. Meanwhile, the catalyst is pulverized, so that the particles of the catalyst are very fine, and the operator is difficult to completely protect and avoid the injury to the human body in the process of removing the catalyst.
The conventional coal-to-ethylene glycol hydrogenation catalyst removal method needs passivation, removal and pipe arrangement cleaning, and both equipment and personnel are at great risk. Moreover, the time for using is long, and generally about 15 to 20 days are needed.
Disclosure of Invention
In view of the above, the main objective of the present invention is to provide a device and a method for removing a coal-derived ethylene glycol hydrogenation catalyst, wherein the catalyst is removed without passivation, so that the damage to equipment and personnel during the conventional catalyst removal process is reduced, and the operation time is shortened.
In order to achieve the above object, the present invention provides a coal-to-ethylene glycol hydrogenation catalyst unloading device, comprising a catalyst unloader and a vacuum pump connected to each other; the catalyst remover comprises a barrel and a support frame, wherein the barrel is welded on the support frame, and the barrel comprises an air extraction area, a material storage area and a material discharging area which are connected from top to bottom.
Further, the catalyst remover is connected with a vacuum pump through an inlet hose.
Further, the upper middle part of the storage area is of a cylindrical structure, and a short pipe connected with a catalyst extraction hose is arranged on one side of the top of the cylindrical structure.
Further, the air exhaust area is arranged at the top of the material storage area, a filter rod is arranged in the air exhaust area, a wire mesh is wound outside the filter rod, and a flange cover is detachably arranged at the top of the air exhaust area; and the flange cover is provided with a short pipe connected with an inlet hose of the vacuum pump.
Further, the mesh number of the screen is set to be 200-500 meshes according to the pulverization degree of the catalyst.
Further, wherein the support frame includes the base and with four pillars that the base welding is as an organic whole, the base is the square recess that four channel-section steels are constituteed, the square recess orientation deviates from the direction that the ware was unloaded to the catalyst.
Further, the material of the catalyst remover barrel is stainless steel or carbon steel.
Further, wherein the diameter of the catalyst withdrawal hose is matched to the inner diameter of the catalyst tube and extends into the reactor at that end, a marked mark is made at a distance from the top, measured for the length of the reactor tube.
Further, the vacuum pump inlet hose is matched with the inlet caliber of the vacuum pump.
Furthermore, the catalyst extraction hose and the vacuum pump inlet hose are metal hoses, rubber hoses or flexible hoses, and the connection mode is flange or spigot-and-socket.
In order to achieve the above object, the present invention provides a method for removing a catalyst used in hydrogenation of ethylene glycol from coal, comprising the following steps:
s1, processing and preparing before unloading: stopping feeding a reactor of the catalyst to be unloaded, cooling, depressurizing, replacing with nitrogen, isolating, keeping nitrogen micro-positive pressure, and opening a top manhole;
s2, discharging the catalyst: the catalyst in the reactor was withdrawn under nitrogen atmosphere using the above-described take-off device.
Further, in the process treatment and preparation before the removal in the step S1, the reactor to be subjected to catalyst removal is stopped from feeding the raw material of the grass ester, the amount of circulating hydrogen and the addition of fresh hydrogen are continuously kept, and the temperature and the pressure of the reactor are maintained within the temperature and the pressure range of the reaction; when the fresh hydrogen addition is less than 100NM 3 When the reaction time is/h, the reactor starts to alternately reduce the pressure and the temperature; when the pressure of the reactor is reduced to micro positive pressure of 0.01-0.03MPa and the temperature is reduced to below 50 ℃, nitrogen replacement is carried out; when the nitrogen in the reactor is replaced until the hydrogen content in the reactor is less than 0.5 percent (v/v), discharging to the micro-positive pressure of 0.01-0.03MPa, and adding a blind plate to isolate inlet and outlet pipelines of the reactor; then 0.1-0.4MPa nitrogen is added from the bottom of the reactor and the top manhole is opened.
Further wherein the temperature and pressure ranges of the reaction are: the temperature is 170-200 ℃, and the pressure is 2.5-35MPa.
Further, in the catalyst removal in the step S2, under the condition that the reactor keeps continuously introducing nitrogen of 0.1-0.4MPa, inserting a catalyst extraction hose with one end connected with one of the connection ports at the top end of the catalyst remover into the tube array of the reactor, wherein the catalyst remover keeps sealed, connecting the other connection port at the top end of the catalyst remover with an inlet hose of a vacuum pump, and after the vacuum pump is started, extracting the waste catalyst in the tube array of the reactor into the catalyst remover; after the catalyst remover is filled, two connecting ports at the top end of the catalyst remover are respectively disconnected with the inlet hose and the catalyst extraction hose, and then sealing is carried out; then the vacuum pump inlet hose and the catalyst extraction hose are connected with two connecting ports at the top end of another catalyst remover.
Further wherein the method further comprises storage and transport of the unloaded catalyst after step S2: and carrying out sealed caching and transportation by utilizing the unloading equipment.
By the technical scheme, the unloading equipment and the method for the coal-to-ethylene glycol hydrogenation catalyst provided by the invention at least have the following advantages:
according to the invention, the catalyst is removed in a nitrogen environment, so that passivation before catalyst removal is not needed, personnel and catalyst powder are in close contact during removal, the damage to equipment and personnel is reduced, the operation time is shortened, and only 2-3 days are needed.
The foregoing is a summary of the present invention, and the following is a detailed description of the preferred embodiments of the present invention in order to provide a clear understanding of the technical features of the present invention.
Drawings
FIG. 1 is a schematic structural diagram of a coal-to-ethylene glycol hydrogenation catalyst dump unit according to the present invention;
FIG. 2 is a schematic diagram of the coal to ethylene glycol hydrogenation catalyst removal process of the present invention.
Description of reference numerals:
1-a reactor; 11-reactor inlet line; 12-reactor outlet line; 13-fresh hydrogen line; 14-oxalate is added into a pipeline; 15-recycle gas addition line; 16-top manhole; 17-nitrogen addition line; 18-a blow-down line;
2-catalyst remover; 21-catalyst extraction hose; 21 a-a discharge opening; 22-vacuum pump inlet hose; 22 a-short tube; 23-an air extraction area; 23 a-short tube; 23 b-a filter rod; 24-a support frame; 25-a storage area; 26-a discharge zone; 3-vacuum pump.
Detailed Description
To further illustrate the technical means and effects of the present invention adopted to achieve the predetermined objects, the following detailed description will be given to the specific implementation, features and properties of the coal-to-ethylene glycol hydrogenation catalyst unloading apparatus and method according to the present invention with reference to the preferred embodiments. In the following description, different "one embodiment" or "an embodiment" refers to not necessarily the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.
As shown in FIG. 1, the invention provides a coal-to-ethylene glycol hydrogenation catalyst removal device, which comprises a catalyst remover 2 and a vacuum pump 3 which are connected with each other; the catalyst remover 2 comprises a barrel body and a support frame 24, the barrel body is welded on the support frame 24, so that the catalyst remover can be conveniently and stably placed and transported, and the barrel body comprises an air extraction area 23, a storage area 25 and a discharging area 26 which are connected from top to bottom; the lower end of the discharge area 26 is provided with a discharge opening 21a. During the operation of the catalyst remover 2, the vacuum pump 3 pumps out gas from the suction area 23 to maintain the negative pressure state in the catalyst remover 2, and the spent catalyst extracted from the reactor 1 is stored in the storage area 25, after which the catalyst remover 2 is transported to a spent catalyst treatment unit and discharged through the discharge opening of the discharge area 26.
The catalyst remover 2 is connected to the vacuum pump 3 through a vacuum pump inlet hose 22. After the vacuum pump 3 is thus turned on, the air in the ejector 2 is evacuated through the vacuum pump inlet hose 22, so that a vacuum state is formed in the ejector 2, the pressure is controlled to 10 to 60kpa (absolute), preferably 20 to 40kpa (absolute), and the spent catalyst side is in a normal pressure state, thereby providing a sufficient suction force to suck the spent catalyst into the ejector 2.
The upper middle part of the material storage area 25 is of a cylindrical structure and is used for temporarily storing the extracted waste catalyst. A short pipe 22a connected to the catalyst withdrawal hose 21 is provided at one side of the top of the cylindrical structure. This facilitates the fixed connection of the extraction hose 21 to the short pipe 22a and then the spent catalyst is extracted into the discharger 2 through the extraction hose 21.
The top of storing area 25 is located to the exhaust area 23, install filter rod 23b in the exhaust area 23, filter rod 23b has twined the silk screen outward, and the purpose that sets up the silk screen prevents that useless catalyst powder from passing through vacuum pump import pipe and getting into the vacuum pump, influencing the normal operating of vacuum pump. The mesh number of the screen is set to be 200-500 meshes according to the pulverization degree of the catalyst. In addition, the top of the air exhaust area 23 is provided with a detachable flange cover, so that the filter rod 23b can be detached and cleaned after the flange cover is opened. The flange cover is provided with a short pipe 23a connected with the vacuum pump inlet hose 22, so that the vacuum pump inlet hose 22 is conveniently and fixedly connected to the short pipe 23a, and the vacuum pump 3 is communicated with the remover 2.
The support frame 24 includes the base and with four pillars that the base welding is as an organic whole, the base is the square groove that four channel-section steels are constituteed, the square groove orientation deviates from the direction that the catalyst unloads the ware 2, like this, when removing the catalyst with fork truck and unloading the ware 2, both made things convenient for the fork handle to insert, also can guarantee that the catalyst unloads the stability of ware 2 at the removal in-process.
The cylinder material of the catalyst remover 2 can be stainless steel or metal material such as carbon steel. Stainless steel is preferably used to prevent the carbon steel from generating rust in the process of reusing the catalyst remover 2, polluting the waste catalyst and influencing the recovery treatment of the waste catalyst.
The diameter of the catalyst extraction hose 21 is matched with the inner diameter of the catalyst tube array, so that the catalyst extraction hose is ensured to be smoothly inserted into the catalyst tube array and extend into the end of the reactor 1, and obvious marks are made at a distance which is as long as the tube array of the reactor 2 and measured from the top end. When the exhaust hose is used for exhausting, the exhaust hose is inserted into the tube array to the marked position, and the waste catalyst in the tube array can be completely exhausted.
The inlet hose 22 of the vacuum pump is matched with the inlet caliber of the vacuum pump 3; this ensures that the vacuum pump 3 and the catalyst remover 2 can be reliably and hermetically connected, thereby allowing the catalyst remover to quickly and stably reach a vacuum state therein.
The catalyst extraction hose 21 and the vacuum pump inlet hose 22 can be in various forms such as metal hoses, rubber hoses and flexible hoses, and the connection mode can be in various modes such as flanges and socket joints. The preferred snakeskin pipe is connected in a socket mode, so that the length of the hose can be adjusted in time according to the actual situation on site, and the catalyst remover can be replaced.
As shown in fig. 2, the invention also provides a method for removing the coal-to-ethylene glycol hydrogenation catalyst, which comprises the following steps:
s1, processing and preparation before removal: stopping feeding the reactor 1 of the catalyst to be unloaded, cooling, depressurizing, replacing with nitrogen, isolating, keeping nitrogen micro-positive pressure, and opening a top manhole;
s2, discharging the catalyst: the catalyst in the reactor 1 was evacuated under nitrogen atmosphere using the above-described take-off device.
In the process treatment and preparation before the removal in the step S1, the feeding of the reactor 1 to be subjected to catalyst removal through the oxalate feeding line 14 is stopped, and the feeding of circulating hydrogen is kept through the circulating gas feeding line 15; in this embodiment, the amount of circulating hydrogen may be 15 ten thousand NM 3 H-30 ten thousand NM 3 H, preferably 18 ten thousand NM 3 H-25 ten thousand NM 3 H, so that the ideal catalyst bed temperature can be maintained.
The raw material oxalate possibly remaining in the catalyst layer is consumed by the addition of fresh hydrogen through a fresh hydrogen line 13, which may be 300-2000NM in this example 3 H, preferably from 1000 to 2000NM 3 The residual raw material oxalate in the catalyst bed layer can be consumed as soon as possible, and the temperature and the pressure of the reactor 1 can be maintained within the temperature and the pressure range of the reaction. In this embodiment, the temperature of the reactor 1 is maintained between 150 and 200 ℃, preferably between 170 and 190 ℃; the pressure is between 2.5 and 3.5MPa, preferably between 2.7 and 3.2MPa; therefore, the residual raw material grass ester in the catalyst bed can be fully reacted within the preferable temperature and pressure range, the residual quantity is greatly reduced, and the treatment time is shortened.
The consumption of fresh hydrogen is gradually reduced with decreasing residual feed, when it is observed that the amount of fresh hydrogen added through the fresh hydrogen line 13 is less than 100NM 3 At the end of the reaction, the residual grass ester material in the catalyst layer is consumed and no hydrogen is consumed, and the reactionThe device starts to alternately reduce the pressure and the temperature. At this time, the fresh hydrogen line 13 is closed to stop the addition of fresh hydrogen, and the continuous addition of the circulating hydrogen amount in normal production is maintained, and in this embodiment, the circulating hydrogen amount may be 15 ten thousand NM 3 H-30 ten thousand NM 3 H, preferably 25 ten thousand NM 3 H-30 ten thousand NM 3 The heat in the reactor 1 can be taken away more quickly, which is beneficial to the bed layer cooling of the reactor; the vent line 18 is opened to depressurize so that the reactor 1 begins to depressurize and lower the temperature.
When the pressure of the reactor 1 is reduced to the micro-positive pressure of 0.01-0.03MPa and the temperature is reduced to below 50 ℃, nitrogen replacement is carried out, nitrogen is added through a nitrogen pipeline, and the adding speed of the nitrogen is less than 20m/s, preferably 15-19m/s, so that the replacement progress can be ensured, and the safety can be ensured. The reactor was purged with nitrogen by venting through a vent line.
When the nitrogen is replaced until the hydrogen content in the reactor 1 is less than 0.5 percent (v/v), the nitrogen is discharged to the micro-positive pressure of 0.005-0.02MPa, preferably 0.005-0.01MPa, so that when the opening of the isolation blind plate is opened in the next step of the reactor, a large amount of nitrogen is not discharged, and air can be prevented from entering the reactor through the opening. The reactor 1 is isolated by adding a blind plate to the reactor inlet line 11 and the reactor outlet line 12.
Subsequently, a nitrogen gas introducing line 17 is opened from the bottom of the reactor 1, and the pressure of the introduced nitrogen gas is 0.1 to 0.4MPa, preferably 0.1 to 0.2MPa, to prevent the pressure from being excessively high, blowing up the spent catalyst powder to raise dust, and deteriorating the working environment in the reactor. The top manhole 16 is opened. The nitrogen gas feed line 17 is provided on the reactor outlet line 12, so that the nitrogen gas can be conveniently fed into the reactor from the bottom thereof.
Wherein the catalyst unloading step S2 specifically comprises: under the condition that the reactor 1 is continuously filled with 0.1-0.4MPa of nitrogen, an operator wears an isolation respirator to enter the reactor, a catalyst extraction hose 21 with one end connected with one connecting port at the top end of a catalyst remover 2 is inserted into a tube array of the reactor 1, the catalyst remover 2 keeps sealed at the moment, the other connecting port at the top end of the catalyst remover 2 is connected with a vacuum pump inlet hose 22, and after the vacuum pump 3 is started, the waste catalyst in the tube array of the reactor 1 is extracted into the catalyst remover 2.
After the catalyst remover 2 is filled, two connecting ports at the top end of the catalyst remover 2 are respectively disconnected with a vacuum pump inlet hose 22 and a catalyst extraction hose 21, and then are sealed to prevent air from entering; the vacuum pump inlet hose 22 and the catalyst extraction hose 21 are then connected to the two connection ports at the top end of the other catalyst remover 2.
Wherein the method further comprises, after step S2, storage and transport of the unloaded catalyst: and carrying out sealed caching and transportation by utilizing the unloading equipment.
Specifically, the catalyst storage and transportation includes buffering the catalyst remover 2 as a container, transporting to a waste catalyst treatment unit such as a dedicated waste catalyst recovery plant, and discharging the waste catalyst in the catalyst remover 2 through a discharge opening of the discharge area 26 to recycle the catalyst remover 2 for reuse.
The reactor 1 is connected with a catalyst remover 2 through a catalyst extraction hose 21; the catalyst remover 2 is connected to a vacuum pump 3 through a vacuum pump inlet hose 22. The reactor 1, the catalyst remover 2 and the vacuum pump 3 can be kept communicated, the vacuum pump 3 is started to pump out the gas in the catalyst remover 2, so that the catalyst remover 2 forms negative pressure, and the waste catalyst in the reactor 1 is pumped out to the storage area 25 of the catalyst remover 2.
A top manhole 16 is arranged on one side of the top of the reactor 1; the top manhole 16 is used for the access of personnel, working in the equipment.
The top of the reactor 1 is connected with a vent pipeline 18; this vent line 18 is used for venting the reactor during depressurization and replacement.
The top of the reactor 1 is provided with a reactor inlet, and the reactor inlet is connected with a reactor inlet pipeline 11 for the raw materials to enter when the reactor 1 is in normal production.
Wherein the reactor inlet pipeline 11 is further provided with a fresh hydrogen pipeline 13, an oxalate adding pipeline 14 and a recycle gas adding pipeline 15, and the fresh hydrogen pipeline 13, the oxalate adding pipeline 14 and the recycle gas adding pipeline 15 are connected with the reactor inlet through the reactor inlet pipeline 11. In the normal use process of the catalyst, the raw materials are as follows: oxalate, fresh hydrogen, and recycle hydrogen were added through these lines.
The above embodiments are only used for the technical solution of the present invention, and not for limitation thereof; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those skilled in the art; the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (10)
1. The unloading equipment for the coal-to-ethylene glycol hydrogenation catalyst is characterized by comprising a catalyst unloading device and a vacuum pump which are connected with each other; the catalyst remover comprises a barrel and a support frame, wherein the barrel is welded on the support frame, and the barrel comprises an air extraction area, a material storage area and a material discharging area which are connected from top to bottom.
2. The coal-to-ethylene-glycol hydrogenation catalyst removal apparatus as claimed in claim 1, wherein the catalyst remover is connected to the vacuum pump through an inlet hose.
3. The apparatus for discharging a catalyst used in hydrogenation of ethylene glycol produced from coal as set forth in claim 2, wherein the storage area has a cylindrical shape at the upper middle portion thereof, and a short pipe connected to a catalyst extraction hose is provided at one side of the top of the cylindrical shape.
4. The coal-to-ethylene-glycol hydrogenation catalyst unloading device as defined in claim 3, wherein the air extraction area is arranged at the top of the storage area, a filter rod is arranged in the air extraction area, a wire mesh is wound outside the filter rod, and a flange cover is detachably arranged at the top of the air extraction area; and the flange cover is provided with a short pipe connected with an inlet hose of the vacuum pump.
5. The coal-to-ethylene-glycol hydrogenation catalyst removal equipment as claimed in claim 4, wherein the support frame comprises a base and four pillars welded to the base into a whole, the base is a square groove formed by four steel channels, and the square groove faces a direction away from the catalyst remover.
6. A method for unloading a coal-to-ethylene glycol hydrogenation catalyst is characterized by comprising the following steps:
s1, processing and preparing before unloading: stopping feeding a reactor of the catalyst to be unloaded, cooling, depressurizing, replacing with nitrogen, isolating, keeping the micro-positive pressure of the nitrogen, and opening a manhole at the top;
s2, discharging the catalyst: the catalyst in the reactor is pumped out under nitrogen atmosphere using the unloading device according to any of claims 1 to 5.
7. The method for unloading the catalyst used in the hydrogenation of coal glycol according to claim 6, wherein in the process treatment and preparation before unloading in step S1, the reactor to be unloaded is stopped from feeding the raw material of straw ester, the amount of recycle hydrogen and the addition of fresh hydrogen are continuously maintained, and the temperature and pressure of the reactor are maintained within the temperature and pressure range of the reaction; when the fresh hydrogen addition is less than 100NM 3 When the reaction time is/h, the reactor starts to alternately reduce the pressure and the temperature; when the pressure of the reactor is reduced to micro positive pressure of 0.01-0.03MPa and the temperature is reduced to below 50 ℃, nitrogen replacement is carried out; when the nitrogen in the reactor is replaced until the hydrogen content in the reactor is less than 0.5 percent (v/v), discharging to the micro-positive pressure of 0.01-0.03MPa, and adding a blind plate to isolate inlet and outlet pipelines of the reactor; then 0.1-0.4MPa nitrogen is added from the bottom of the reactor and the top manhole is opened.
8. The method for removing the catalyst for hydrogenation of coal-derived ethylene glycol according to claim 7, wherein the reaction temperature and pressure ranges are as follows: the temperature is 170-200 ℃, and the pressure is 2.5-35MPa.
9. The method for removing the catalyst used in the hydrogenation of coal-derived ethylene glycol according to claim 8, wherein in the step S2, the catalyst removal hose having one end connected to one of the connection ports at the top end of the catalyst remover is inserted into the tube nest of the reactor while the reactor is kept continuously filled with 0.1 to 0.4MPa of nitrogen gas, the catalyst remover is kept sealed, the other connection port at the top end of the catalyst remover is connected to the inlet hose of the vacuum pump, and the waste catalyst in the tube nest of the reactor is pumped into the catalyst remover after the vacuum pump is started; after the catalyst remover is filled, two connectors at the top end of the catalyst remover are respectively disconnected with the inlet hose and the catalyst extraction hose, and then sealing is carried out; then the vacuum pump inlet hose and the catalyst extraction hose are connected with two connecting ports at the top end of another catalyst remover.
10. The method for unloading the catalyst used in the hydrogenation of coal glycol according to claim 6, wherein the method further comprises the following steps of storing and transporting the unloaded catalyst after step S2: and carrying out sealed caching and transportation by utilizing the unloading equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202110973715.5A CN115715959A (en) | 2021-08-24 | 2021-08-24 | Unloading equipment and method for coal-to-ethylene glycol hydrogenation catalyst |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202110973715.5A CN115715959A (en) | 2021-08-24 | 2021-08-24 | Unloading equipment and method for coal-to-ethylene glycol hydrogenation catalyst |
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| CN115715959A true CN115715959A (en) | 2023-02-28 |
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| CN202110973715.5A Pending CN115715959A (en) | 2021-08-24 | 2021-08-24 | Unloading equipment and method for coal-to-ethylene glycol hydrogenation catalyst |
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