CN109603687B - Methanol oxidizer in efficient silver-process formaldehyde device - Google Patents
Methanol oxidizer in efficient silver-process formaldehyde device Download PDFInfo
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- CN109603687B CN109603687B CN201811378889.1A CN201811378889A CN109603687B CN 109603687 B CN109603687 B CN 109603687B CN 201811378889 A CN201811378889 A CN 201811378889A CN 109603687 B CN109603687 B CN 109603687B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
- C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
- C07C45/37—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups
- C07C45/38—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups being a primary hydroxyl group
Abstract
The invention discloses a methanol oxidizer in a high-efficiency silver-process formaldehyde device, which comprises a tank body (1), a silver catalyst layer (2) and a cooling pipe (3), wherein the cooling pipe (3) is arranged in the tank body (1), the bottom of the tank body (1) is provided with a truncated cone-shaped structure, the side surface of the truncated cone-shaped structure is provided with a feeding hole, the feeding hole is provided with the silver catalyst layer (2), the upper part of the tank body (1) is provided with a formaldehyde outlet (4), and the feeding hole and the formaldehyde outlet (4) are both communicated with the tank body (1). The methanol oxidizer in the high-efficiency silver-process formaldehyde device has the advantages that the feed inlet is changed from the top of the methanol oxidizer to the side surface of the round table structure at the bottom of the tank body of the methanol oxidizer, so that the reaction area of methanol and a silver catalyst can be greatly increased, the reaction efficiency is improved, and the volume of the methanol oxidizer can be reduced.
Description
Technical Field
The invention relates to a methanol oxidizer in a high-efficiency silver-process formaldehyde device.
Background
In the production process of formaldehyde by a silver method, the chemical reaction in the methanol mixed gas reoxidator is mainly as follows:
oxidation reaction
CH3OH+1/2O2→CH2O+H2O (1)
Dehydrogenation reaction
CH3OH→CH2O+H2 (2)
Chemical equation of side reaction in the reaction process:
CH3OH+3/2O2→CO2+2H2O (3)
CH3OH→CO+2H2O……… (4)
CH3OH+H2→CH4+H2O……… (5)
CH3OH+O2→HCOOH+H2O (6)
at present, the appearance of the traditional oxidizer in the formaldehyde industry is vertical cylindrical equipment, and the traditional oxidizer can be generally divided into three sections from top to bottom: the upper section is an oxidizer top cover; the middle section is a combination of a catalyst chamber and a quenching section; the lower section can be provided with a cooling section (according to the requirement). Technical drawbacks of using conventional oxidizers:
a. because the quick cooling section of the oxidizer adopts a tubular heat exchanger form, the temperature of a catalyst layer on an upper tube plate is 630-650 ℃, and because the upper tube plate and the heat exchange tube are welded by austenitic stainless steel, the austenitic stainless steel is at the sensitization temperature which is most easily damaged at the temperature, the crystal lattice is thick, particularly, intergranular corrosion is easily generated in a welded heat affected zone, and the heat affected zone of the upper tube plate can generate heat cracks and water leakage after long time. In the water leakage part of the oxidizer, the local temperature is low, the oxidation reaction of methanol is insufficient, the unit consumption is high, and water leakage continues due to the change of the material of the welding heat affected zone after repair welding. Therefore, the number of water leakage pipelines of the oxidizer reaches about 5-10% of that of the heat exchange pipe, and the oxidizer needs to be replaced when the unit consumption is 450kg formaldehyde/t formaldehyde (37%). The oxidizer is replaced typically about 3 years. The cost of the oxidizer in a formaldehyde plant is generally about 20%.
b. The tube plate of the heat exchange tube of the oxidizer is made of stainless steel, and the shell pass is made of carbon steel in order to reduce the manufacturing cost. In a tube side, the gas phase temperature after reaction is higher, and the thermal expansion coefficient (17.9) of stainless steel of the heat exchange tube is far greater than that (11.3-13) of shell side carbon steel, so that the stress of the heat exchange tube for jacking a tube plate is very large, and through calculation, the thermal stress of a 5 ten thousand ton oxidizer in operation reaches about 48 tons, although an expansion joint is adopted to offset partial thermal stress, the thermal stress exists, and particularly, the heat affected zone of the tube plate and the heat exchange tube is fatally damaged at high temperature.
c. For formaldehyde devices with the volume of 10 ten thousand tons and more, the effective diameter of an oxidizer is larger than phi 2600, the heat in the middle part is difficult to take away, in order to reduce the defect that the heat cannot be brought out in the middle shell pass of a tube plate, only a mode of increasing the tube spacing is adopted, but at the moment, the effective area of mixed gas passing through a catalyst is reduced, the oxidizer has to be made large, and the result is high unit consumption and low productivity.
d. For a formaldehyde device with 12 ten thousand tons, the effective diameter phi 2800 of an oxidizer, the diameter phi 2900 of a catalyst chamber of the oxidizer, the outer diameter phi 4000 of a shell side of the oxidizer, and an extended connecting pipe are added, the maximum transport outer diameter of the oxidizer reaches phi 4600, which is the limit value of transport height, so the limit capacity of the formaldehyde device by the silver method is 12 ten thousand tons.
e. Fatal defect of the conventional oxidizer: 1. the oxidizer is a vulnerable part and needs to be replaced about 3 years, so that the cost is high; 2. the maximum capacity of the oxidizer can only reach 12 ten thousand tons, and the large-scale formaldehyde device is limited by fatality; 3. the transportation process is limited, and the design of a 12 ten thousand ton formaldehyde device is almost the largest; 4. the large-scale oxidizer has high unit consumption and difficult operation.
Therefore, there is a need for a high efficiency methanol oxidizer in a silver process formaldehyde plant to solve the above problems.
Disclosure of Invention
The purpose of the invention is as follows: aiming at the defects of the prior art, the invention provides a methanol oxidizer in a silver method formaldehyde device with high efficiency.
The technical scheme is as follows: in order to solve the technical problems, the methanol oxidizer in the high-efficiency silver method formaldehyde device adopts the following technical scheme:
the utility model provides a methanol oxidation ware in efficient silver-process formaldehyde device, includes a jar body, silver catalyst layer and cooling tube, the cooling tube sets up the jar is internal, the bottom of the jar body is provided with round platform shape structure, the side of round platform shape structure is provided with the feed inlet, feed inlet department is provided with silver catalyst layer, the upper portion of the jar body is provided with the formaldehyde export, feed inlet and formaldehyde export all with jar body intercommunication.
Furthermore, a circle of feed inlets are formed in the side face of the circular truncated cone-shaped structure. The side of the lower part of the tank body is provided with a circle of feed inlet, so that the feeding area can be effectively increased.
Furthermore, a circle of silver catalyst layer is arranged on the side surface of the truncated cone-shaped structure. The silver catalyst layer is arranged corresponding to the feed inlet. The side of the round platform-shaped structure is provided with a circle of silver catalyst layer, so that the reaction area of the methanol and the catalyst can be greatly increased, and the oxidation efficiency is improved.
Further, the silver catalyst layer is divided into a plurality of silver catalyst blocks in the circumferential direction. Divide into the polylith with jar body silver catalyst layer all around along circumference, can conveniently divide the piece to change silver catalyst.
Furthermore, a first closed chamber and a second closed chamber are respectively arranged below and above each silver catalyst block, a second silver catalyst block is arranged in the first closed chamber, one end of the second silver catalyst block is in contact with the silver catalyst block, and a pushing device is arranged at the other end of the second silver catalyst block.
Furthermore, the first closed chamber and/or the second closed chamber are filled with inert gas. And filling inert gas into the first closed chamber and/or the second closed chamber to prevent the gas in the feed inlet from leaking into the first closed chamber and/or the second closed chamber.
Further, the pressure of the gas in the first closed chamber and/or the second closed chamber is higher than the pressure of the gas in the feed port. The air pressure in the first closed chamber and/or the second closed chamber is higher than that of the feeding hole, so that the leakage prevention effect of the first closed chamber and/or the second closed chamber is better.
Still further, still include the feed chamber, the feed chamber through the feed inlet with jar body intercommunication, silver catalyst layer sets up in the feed chamber. Conveniently utilize the feed chamber, through reinforced to the jar internal because of catalyst and feed inlet.
Further, the cooling pipes are wound around each other. The cooling area of the cooling pipe can be greatly increased, the stress at two ends of the cooling pipe can be effectively reduced, and the service life of the oxidation device is prolonged.
Furthermore, the top of the tank body is provided with a convex top, and the formaldehyde outlet is arranged at the highest position of the convex top. Make things convenient for formaldehyde to discharge from jar body top, and can not form the siltation in jar body.
Has the advantages that: the methanol oxidizer in the high-efficiency silver-process formaldehyde device has the advantages that the feed inlet is changed from the top of the methanol oxidizer to the side surface of the round table structure at the bottom of the tank body of the methanol oxidizer, so that the reaction area of methanol and a silver catalyst can be greatly increased, the reaction efficiency is improved, and the volume of the methanol oxidizer can be reduced.
Drawings
FIG. 1 is a schematic diagram of the structure of a methanol oxidizer in a high efficiency silver-process formaldehyde plant of the present invention;
fig. 2 is a cross-sectional view at the silver catalyst layer of the methanol oxidizer in the high efficiency silver-process formaldehyde unit of the present invention.
Detailed Description
The present invention is further illustrated by the following figures and specific examples, which are to be understood as illustrative only and not as limiting the scope of the invention, which is to be given the full breadth of the appended claims and any and all equivalent modifications thereof which may occur to those skilled in the art upon reading the present specification.
Referring to fig. 1, the methanol oxidizer in the high-efficiency silver-process formaldehyde device of the invention comprises a tank body 1, a silver catalyst layer 2 and a cooling pipe 3, wherein the cooling pipe 3 is arranged in the tank body 1, the bottom of the tank body 1 is provided with a truncated cone-shaped structure, the side surface of the truncated cone-shaped structure is provided with a feed inlet, the silver catalyst layer 2 is arranged at the feed inlet, the upper part of the tank body 1 is provided with a formaldehyde outlet 4, and the feed inlet and the formaldehyde outlet 4 are both communicated with the tank body 1. The tank body 1 is externally provided with a cooling liquid inlet and a cooling liquid outlet which are respectively connected with two ends of the cooling pipe 3. Cooling liquid is circularly flushed into the cooling pipe in the tank body through the cooling liquid inlet and the cooling liquid outlet.
Wherein, preferably, the side of round platform shape structure is provided with round feed inlet. The side of the lower part of the tank body is provided with a circle of feed inlet, so that the feeding area can be effectively increased. Preferably, the sides of the truncated cone-shaped structure are provided with a ring of silver catalyst layer 2. The silver catalyst layer is arranged corresponding to the feed inlet. The side of the round platform-shaped structure is provided with a circle of silver catalyst layer, so that the reaction area of the methanol and the catalyst can be greatly increased, and the oxidation efficiency is improved.
Preferably, the silver catalyst layer 2 is divided into a plurality of silver catalyst blocks in the circumferential direction. Divide into the polylith with jar body silver catalyst layer all around along circumference, can conveniently divide the piece to change silver catalyst. Preferably, a first closed chamber 22 and a second closed chamber 23 are respectively arranged below and above each silver catalyst block, a second silver catalyst block 21 is arranged in the first closed chamber 22, one end of the second silver catalyst block 21 is in contact with the silver catalyst block, and the other end is provided with a pushing device 24. Wherein, the one end that first airtight chamber 22 and second airtight chamber 23 contacted with silver catalyst layer is provided with the opening with silver catalyst layer complex, conveniently changes silver catalyst layer. The second silver catalyst block 21 is pushed upwards by the pushing device 24, the original silver catalyst block is replaced slowly, and automatic replacement is conveniently realized by adopting the mode. The pushing device 24 can be implemented by various means in the prior art, such as a linear motor, and can directly push the second silver catalyst block by using the output end thereof, and the second silver catalyst block pushes the original silver catalyst block until the second silver catalyst block is replaced by the original silver catalyst block, so as to implement the replacement of the silver catalyst. The output end of the stepping motor can be changed into linear output by adopting the existing transmission mechanism, so that the second silver catalyst block can be pushed. Wherein, the ejector 24 is arranged in the first closed chamber 22 below the silver catalyst layer, so that the influence of the heated tank on the ejector 24 can be effectively avoided.
Preferably, the first closed chamber 22 and/or the second closed chamber 23 are filled with inert gas. The gas in the feed port is prevented from leaking to the first closed chamber 22 and/or the second closed chamber 23 by filling the first closed chamber 22 and/or the second closed chamber 23 with the inert gas. Preferably, the gas pressure in the first closed chamber 22 and/or the second closed chamber 23 is higher than the gas pressure in the feed opening. The air pressure in the first closed chamber 22 and/or the second closed chamber 23 is higher than that of the feed inlet, so that the leakage prevention effect of the first closed chamber 22 and/or the second closed chamber 23 can be better.
Preferably, the silver catalyst material further comprises a feeding chamber 25, wherein the feeding chamber 25 is communicated with the tank body 1 through a feeding hole, and the silver catalyst layer 2 is arranged in the feeding chamber 25. Conveniently utilize the feed chamber, through reinforced to the jar internal because of catalyst and feed inlet. Preferably, the cooling tubes 3 are intertwined. The cooling area of the cooling pipe can be greatly increased, the stress at two ends of the cooling pipe can be effectively reduced, and the service life of the oxidation device is prolonged. Preferably, the top of the tank body 1 is provided with a convex top, and the formaldehyde outlet 4 is arranged at the highest position of the convex top. Make things convenient for formaldehyde to discharge from jar body top, and can not form the siltation in jar body.
The methanol oxidizer in the high-efficiency silver-process formaldehyde device has the advantages that the feed inlet is changed from the top of the methanol oxidizer to the side surface of the tank body of the methanol oxidizer, so that the reaction area of methanol and a silver catalyst can be greatly increased, the reaction efficiency is improved, and the volume of the methanol oxidizer can be reduced.
Claims (6)
1. The methanol oxidizer in the high-efficiency silver-process formaldehyde device is characterized by comprising a tank body (1), a silver catalyst layer (2) and a cooling pipe (3), wherein the cooling pipe (3) is arranged in the tank body (1), the bottom of the tank body (1) is provided with a truncated cone-shaped structure, the side surface of the truncated cone-shaped structure is provided with a feeding hole, the silver catalyst layer (2) is arranged at the feeding hole, the upper part of the tank body (1) is provided with a formaldehyde outlet (4), and the feeding hole and the formaldehyde outlet (4) are communicated with the tank body (1);
a circle of feeding holes are formed in the side face of the circular truncated cone-shaped structure;
a circle of silver catalyst layer (2) is arranged on the side surface of the truncated cone-shaped structure;
the silver catalyst layer (2) is divided into a plurality of silver catalyst blocks along the circumferential direction;
a first closed chamber (22) and a second closed chamber (23) are respectively arranged below and above each silver catalyst block, a second silver catalyst block (21) is arranged in the first closed chamber (22), one end of the second silver catalyst block (21) is in contact with the silver catalyst block, and a pushing device (24) is arranged at the other end of the second silver catalyst block;
the feed inlet and the silver catalyst layer (2) are arranged on the outer side of the tank body (1);
the ejector (24) is arranged in the first closed chamber (22) below the silver catalyst layer.
2. The methanol oxidizer of a high-efficiency silver-process formaldehyde plant as recited in claim 1, wherein the first closed chamber (22) and/or the second closed chamber (23) is filled with an inert gas.
3. The high efficiency methanol oxidizer of a silver-process formaldehyde plant as recited in claim 2, wherein the gas pressure in the first closed chamber (22) and/or the second closed chamber (23) is higher than the gas pressure at the feed inlet.
4. The methanol oxidizer in a high-efficiency silver-process formaldehyde plant according to claim 1, further comprising a feeding chamber (25), wherein the feeding chamber (25) is communicated with the tank body (1) through a feeding port, and the silver catalyst layer (2) is disposed in the feeding chamber (25).
5. The high efficiency methanol oxidizer of a silver-process formaldehyde plant as recited in claim 1, wherein the cooling tubes (3) are intertwined.
6. The methanol oxidizer in a high-efficiency silver-process formaldehyde plant as set forth in claim 1, characterized in that the top of the tank (1) is provided with a convex top, and the formaldehyde outlet (4) is disposed at the highest position of the convex top.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201811378889.1A CN109603687B (en) | 2018-11-19 | 2018-11-19 | Methanol oxidizer in efficient silver-process formaldehyde device |
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| CN201811378889.1A CN109603687B (en) | 2018-11-19 | 2018-11-19 | Methanol oxidizer in efficient silver-process formaldehyde device |
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| CN109603687A CN109603687A (en) | 2019-04-12 |
| CN109603687B true CN109603687B (en) | 2021-08-24 |
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| US7842251B2 (en) * | 2007-09-07 | 2010-11-30 | Babcock & Wilcox Power Generation Group, Inc. | Catalyst particulate diverter |
| CN204799235U (en) * | 2015-06-29 | 2015-11-25 | 天津市先权工贸发展有限公司 | Chemistry catalytic converter |
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|---|---|---|---|---|
| WO2011093749A3 (en) * | 2010-02-01 | 2011-12-29 | Infra Technologies Ltd | Process for producing synthetic liquid hydrocarbons and reactor for fischer-tropsch synthesis |
| CN102091572A (en) * | 2011-01-20 | 2011-06-15 | 宋晓轩 | Polymer reactor for synthesizing rubber |
| CN202028401U (en) * | 2011-03-10 | 2011-11-09 | 青岛华拓电力环保有限公司 | Automatic screen replacing device for filtering denitration catalyst |
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