CN1436586A - Catalytic distillation tower member and its manufacture - Google Patents
Catalytic distillation tower member and its manufacture Download PDFInfo
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- CN1436586A CN1436586A CN 02104203 CN02104203A CN1436586A CN 1436586 A CN1436586 A CN 1436586A CN 02104203 CN02104203 CN 02104203 CN 02104203 A CN02104203 A CN 02104203A CN 1436586 A CN1436586 A CN 1436586A
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- catalytic distillation
- distillation tower
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Abstract
The catalytic distillation tower member consists of base body, modified layer and activating layer and features the base body made of regular porous ceramic stuffing, the modified layer being coating formed through surface treatment of the base body with alpha-alumina, and the activating layer comprising active catalyst component coated to the modified layer. The catalyst distillation tower member integrates the distilling stuffing and catalyst; has high efficiency, enough gas-liquid contact area, efficient mass transfer between the gas phase and the liquid phase, and excellent reaction and separation effect; and is convenient in assembling and disassembling and suitable for industrial application.
Description
Technical field
The present invention relates to a kind of catalytic distillation tower member that is used for petrochemical industry, specifically, relate to structure of the catalytic distillation tower inner member in a kind of catalytic distillation technology and preparation method thereof.
Background technology
Catalytic distillation technology is a kind of new Chemical Engineering method that development in recent years is got up, and this technology collection catalytic process and still-process are one, and reaction is carried out in same tower simultaneously with the operating process that separates.This process can constantly be removed product from each reaction member separation, also can utilize reaction heat as the required heat of vaporization of still-process simultaneously.Therefore series of advantages such as catalytic distillation technology has the conversion ratio height, selectivity is good, energy consumption is low, product purity is high, easy to operate, reduced investment have just obtained extensive studies and have developed rapidly in the eighties.Catalytic distillation technology is application success in the production of methyl tertiary butyl ether(MTBE) (MTBE) at first, and has been applied to other many fields.
The key of catalytic distillation technology is the type of feed of reacting section catalyst in the catalytic distillation tower.Catalyst be filled with a lot of forms, usually can be divided into two classes: a class is catalyst and the processing and manufacturing respectively of distillation filler, be about to catalyst and directly make the particle of different shape size, and in different ways with the distillation filler combination together, fill in the catalytic distillation tower then; Another kind of is that catalyst is made of one with the distillation filler, is put in catalytic distillation tower again behind the even unified element of formation.
US4443559 discloses in a kind of tiny pocket that catalyst granules is seated on the cloth bag made from glass cloth, cover to support with the stainless steel cloth that the certain opening space is arranged, be rolled into again have the layer of steel wire net, the harness shape cylinder catalyst structure of one deck cloth bag.This member is packed in the tower, and make its spatial distribution even, liquid phase can fully be contacted with catalyst, and leave enough gas-liquid phase flow channel and contact area.In order to prevent the steam short circuit of rising, adjacent two layers member silk screen is staggeredly placed.This patented technology is adopted by the catalytic distillation of synthetic MTBE, has realized industrialization.This scheme makes the catalytic distillation tower conversion zone into the voidage general little particular fillers tower of packed tower, and the above and below of conversion zone then is still common filler or column plate.Thereby the design of whole catalytic distillation tower, make with regard to more complicated, specification requirement is higher, and the filler loading and unloading are cumbersome.
US5262012 proposes catalyst is pressed the filling of dumped packing form.For example, granular catalyst is mixed in the tower of packing into inertia filled media such as porcelain ball, bead, hollow porous spheroid or cylinder etc.But this kind structural tower internal pore rate is not high, and operating flexibility is poor, and is not easy to industrial loading and unloading, does not therefore see and uses report.
CN1060228 has described a kind of catalytic rectifying tower, and column plate wherein or filler have solved the packing and the Packing Problems of catalytic rectifying tower catalyst with containing activity of such catalysts materials processing moulding.Catalytic rectifying tower can be a packed tower, also can be plate column, bubble column or its any combination, wherein be used for dumped packing or corrugated plate shape such as the Raschig ring, Bao Erhuan, wheel shape, rectangular saddle ring of packed tower, spherical, column, cellular structured packing can be with containing activity of such catalysts materials processing moulding.Sieve plate, corrugated plating, bubble cap plate, the valve plate of same plate column also can be with containing activity of such catalysts materials processing moulding.This patent has only proposed column plate or filler usefulness contains the imagination of activity of such catalysts materials processing moulding, and does not provide the specific implementation method.This imagination implements very difficulty on the practical work, just there is strength problem because contain activity of such catalysts material itself, and when being processed into column plate or filler various factors such as Yin Gaowen and make the catalyst activity forfeiture often, thereby do not have the effect of catalytic reaction.
CN1167009 has prepared a kind of mordenite/metal or ceramic composite, is made up of the pre-designed shape with dumped packing, structured packing, static mixer, special-shaped catalyst and integral catalyzer of mordenite molecular sieve and this molecular sieve of load and the metal or the ceramic base material of size or shape similarly and size.It has kept the characteristic of mordenite molecular sieve on catalytic performance, and can satisfy the needs of differential responses by modification; On engineering properties, can be used as catalytic distillation structure, also can be used as irregular shape catalyst by changing the metal or the shape of ceramic base material, the requirement that size satisfies different process.Yet this composite only limits to mordenite molecular sieve is compounded on metal or the ceramic base material, only effective to the reaction of modenite useful as catalysts, reaction applicatory field is more limited, and composite methods only adopted the crystallization method of immersing, and compound means are also very limited.
US5780688 has described a kind of loaded catalyst with random packing shape, and this catalyst is made of porous materials, and adopts machinery or chemical method that macroporous ion exchange resin is adhered on the surfaces externally and internally of porous material.This catalyst only relates to spent ion exchange resin as active ingredient, and its adhesion method has only been narrated the method for immersing, and this catalyst only is applicable to dumped packing, and application and preparation method are limited.
CN1228032 has described a kind of catalyst filling that uses in catalytic distillation technology, it is by gas deposition and/or be ejected on yarn fabric, knit goods or the flake stuffing as matrix and make with at least a active material as catalyst and/or promoter.Wherein a kind of heterogeneous catalytic reaction is to combine with distillation or the rectifying carried out simultaneously on the catalyst filling.The catalyst matrix that this patent is selected for use is yarn fabric, knit goods or flake stuffing, but these materials and be not suitable for all chemical reaction processes, if as fractional distillation filling-material, is subjected to the separation requirement restriction also may not be suitable fully.This patent is overlying on catalyst on the matrix by gas deposition and/or injection in addition, and some catalyst and be not suitable for the employing vapour phase processes, can only adopt liquid phase to immerse method and finish and cover attachedly, so this patent still fails to solve the practical problem that exists in the catalytic distillation process.
DE29609079 U1 has described a kind of catalyst that is used for exhaust-gas treatment, and this catalyst is coated with and invests on the ceramic body, the outsourcing steel bushing.Steel bushing can have side opening, also can be made up of the parts of some mechanical connections.This kind structure is easy to dismounting, and convenient test can be reclaimed noble metal and reused, and can be used for the catalyst of Any shape, comprises ball-type.But this structure only limits the use of in exhaust-gas treatment, and is surrounded by steel bushing outside the ceramic substrate catalyst, and structure is too complicated, is unwell to be used as the catalytic distillation tower packing.
CN1046473 has described a kind of purification catalyst for automobile exhaust, this catalyst is a complex carrier by ceramic honeycomb material and aluminum oxide coating layer, the oxide of base metal element and thulium is that active constituent is formed, and wherein the aluminum oxide coating layer as carrier is the modified aluminas with the double-deck pore structure of two coatings.But this catalyst is not suitable for being used as the catalytic distillation tower packing.
US5235102 has narrated the technology that a kind of method that adopts catalytic distillation is converted into gas phase or liquid-phase feed stream required product, the rigidity honeycomb block that this technology catalytic distillation tower adopts rigidity honeycomb block or is coated with the catalyst activity component is as filler, the preferably ceramic honeycomb block.But the ceramic honeycomb piece that this technology is selected for use is the rigidity alveolate texture with some upright openings that are parallel to each other, and is separate between each duct, is unfavorable for the mass transfer between gas-liquid, and the usefulness of catalytic distillation can not get effective performance.In addition, this filler has been adopted the rigidity honeycomb block, is not easy to the coated catalysts active component.
Summary of the invention
The object of the present invention is to provide a kind of new catalytic destilling tower member simple, that be easy to realize of making.This new structure can be given full play to the efficient of catalyst, and enough gas-liquid contacts area are provided, and helps the mass transfer between gas-liquid two-phase, and reaction and separating effect are all good, and easy to loading and unloading, are easy to commercial Application.
Catalytic distillation tower member of the present invention is made of matrix, modified layer and active layer, it is characterized in that with the porous ceramics structured packing with microcellular structure be matrix, with through α-Al
2O
3The alumina layer that matrix is carried out forming after the surface treatment is a modified layer, is active layer to cover the catalyst activity component that invests on the modified layer, forms the catalytic distillation tower structured packing with reaction and separation of double effect of homogeneous.
Structured packing of the present invention is made by porous ceramics.The base material that porous ceramics is selected for use can be various types of clays, preferred aluminium-silicate, high attaclay or diatomite etc., can adopt conventional preparation method to obtain, the preferred following steps that adopt prepare: mix the base material of 60%～80% weight fraction (1) with the distilled water of 20%～40% weight fraction, add 10%～20% weight fraction binding agent and pore creating material, after 5～20 hours, obtain homodisperse mud through mixing and ball milling, adjust its pH value to 5.0～7.0 again; (2) under certain mould with the extrusion modling of step (1) gained slurry, for preferred porous ceramics corrugated plating, mould should have satisfactory crest height of wave, the pitch of waves and inclination angle; The blank of moulding is carried out integer, make the smooth zero defect of filling surface, at room temperature dry then, and on blank, open several apertures; (3) dried each sheet blank is assembled, the ripple of adjacent two fillers intersects 90 ° during assembling, connects each sheet assembling back one-tenth dish between the crest of adjacent two fillers with binding agent; (4) the cellar for storing things roasting is put in the structured packing that will be assembled into dish, obtains the porous ceramics structured packing at 800～1000 ℃ of following sintering.Wherein the preferred starch that uses preferably uses hydrochloric acid or TMAH to regulate the pH value of mud as binding agent and pore creating material in the step (1); The preferred waterglass that uses is made binding agent in the step (3).Preferably whole dish type is made in described porous ceramics structured packing below diameter 500mm, made six below the diameter 800mm and piece together system shape, be nine or more assembly system shapes more than the 800mm.
The porous ceramics structured packing that described matrix adopting makes as stated above for porous ceramics corrugated plating, porous ceramics silk screen or porous ceramics fin, is preferably the porous ceramics corrugated plating.
Described porous ceramics corrugated plating has microcellular structure, and its porosity is 30～60%, and the aperture is 10～18 μ m; Described corrugated plating wall thickness 0.8～1.2mm, 30 °～45 ° at ripple inclination angle, the crest height of wave and the pitch of waves are 5～30mm, have the hole of 3～6mm on the corrugated siding, purpose is in order to strengthen mass transfer.
The specific area of described matrix generally should be greater than 400m
2/ m
3, can choose 400～800m
2/ m
3, voidage generally should can choose 72～95% greater than 72%, and number of theoretical plate is greater than 4 plates/m.
For making the catalyst activity component can be effectively and cover securely and invest in the porous ceramics structured packing, the porous ceramics structured packing that makes as stated above need be carried out modification as matrix, be about to surfaces externally and internally coating one deck Alpha-alumina film of matrix, form modified layer.Preferred manufacturing procedure is at first described matrix to be immersed in the aluminium hydroxide suspension, takes out after 12～24 hours, then 1000～1200 ℃ of roastings 8～12 hours; In roasting process, the aluminium hydroxide of coating undergoes phase transition, and obtains the Alpha-alumina modified layer at last.
Proposed by the invention with α-Al
2O
3The method of carrying out surface modification is a kind of peculiar methods that is different from other method.Aluminium oxide has multiple variant, wherein γ-Al
2O
3And η-Al
2O
3Have higher chemism, the spy is called activated alumina; α-Al
2O
3Structure is the most stable, and other variant of aluminium oxide is heated to more than 1100 ℃ and all can changes α-Al into
2O
3, be the low surperficial high-intensity carrier of a kind of high temperature.For catalytic distillation tower member proposed by the invention, the carrier of catalyst is the porous ceramics structured packing, has possessed enough carrier surfaces, and what need is catalyst activity component to be covered thereon attached, does not need to have chemically active Al
2O
3And γ-Al
2O
3And η-Al
2O
3All has bigger specific surface, if with γ-Al
2O
3And η-Al
2O
3Surface modification is carried out in the porous ceramics structured packing, and it is more then to cover attached catalyst activity component, then is easy to assemble for metal component, though the catalytic distillation tower member that so makes has advantages of high catalytic activity, but selectivity is not high, and accessory substance is many, is unfavorable for the carrying out of catalytic reaction.And with α-Al
2O
3Carry out surface modification and just can avoid these shortcomings.α-Al
2O
3Specific surface less relatively, but intensity is high, covers attached catalyst activity component more evenly and comparatively firm, can satisfy conversion ratio and optionally requirement simultaneously.Usually sintering temperature is determining Al
2O
3Kenel, generally obtain γ-Al 400-600 ℃ of following roasting
2O
3, and generally obtain α-Al 1000-1200 ℃ of following roasting
2O
3
Described active layer is catalyst activity component to be covered to invest on the matrix that forms modified layer equably form.The porous ceramics structured packing is after modification, catalyst activity component can cover equably, securely to invest on the porous ceramics structured packing modified layer that designs as required in advance and forms active layer by immersing method or spraying process, thereby makes catalytic distillation tower member.
The method of formation active layer provided by the present invention can have two kinds, and a kind of is that liquid phase is immersed method, and another kind is a spraying process.
It is that the matrix that will form modified layer is immersed in the solution that contains catalyst activity component that described liquid phase is immersed method, after 24～48 hours crystallization, take out washing, drying, so repeatedly for several times, 400～600 ℃ of roastings 8～12 hours, make catalytic distillation tower member then with reaction and separation of double effect.
Described spraying process is to select suitable sprayer for use, with the solution spraying that contains catalyst activity component for preparing on the matrix that forms modified layer, then 50～150 ℃ of dryings, 400～600 ℃ of roastings 8～20 hours, after 10～20 hours, make described catalytic distillation tower member through reducing gas such as H2 reduction again.
Described catalyst activity component can be VIII family or IB family metal and composition thereof, also can be acid cation exchange resin or Y type, X type, β type and various modified zeolite molecular sieve.Have as the metal of catalyst activity component according to the present invention: the mixture of element such as copper, silver, gold, ruthenium, cobalt, rhodium, nickel, palladium, platinum and these elements.
The adaptable field of catalytic distillation tower member of the present invention has the cracking gas catalytic distillation to select acetylene hydrogenation and alkadienes process, and the chemical process of multiple applied catalysis distillation techniques such as etherificate, ether decomposition, esterification, dimerization, alkylation, isomerization, dehydration, hydrolysis.
Catalytic distillation tower member provided by the present invention has following advantage:
1) member is made of matrix, modified layer and active layer, integrate distillation filler and catalyst, both had higher separating property, have good reactivity worth again, can make the catalytic distillation process be able to efficiently successfully carry out, improve the conversion ratio and the selectivity of catalytic reaction;
2) the member matrix is through α-Al
2O
3Carry out forming modified layer after the surface treatment, catalyst activity component can cover thereon attached securely, has avoided the loss of active constituent;
3) catalyst activity component evenly distributes in member, has improved the geometrical surface of catalyst, makes catalyst have higher utilization rate;
4) member shape and big I are flexible and changeable as required, but also flexible modulation of active constituent and content;
5) member has bigger voidage and specific area, and pressure drop reduces, and mass-and heat-transfer efficient is improved.
The specific embodiment
Embodiment 1
Get mass fraction and be 70% Al
2O
3Mix with 20% distilled water, add 10% starch again, after 6 hours, obtain homodisperse mud through mixing and ball milling, adjusting its pH value with hydrochloric acid again is 6; Select for use the mould that designs with the mud blank extrusion modling that makes, obtain crest height of wave 6mm, pitch of waves 12mm, 45 ° at ripple inclination angle, the corrugated plating blank of wall thickness 0.8mm has the hole of φ 4mm on corrugated siding.The blank of moulding is at room temperature dry after integer, then dried each sheet blank is assembled, the ripple of adjacent two fillers intersects 90 ° during assembling, connects with waterglass between the crest of adjacent two fillers, and each sheet assembling back forms φ 100 * 100mm structured packing dish; The cellar for storing things roasting is put in the structured packing that will be assembled into dish at last, obtains porous ceramics structured packing as matrix at 800～900 ℃ of following sintering.
Embodiment 2
The porous ceramics structured packing that embodiment 1 is made is carried out surface modification as matrix to it.φ 100 * 100mm porous ceramics structured packing dish is immersed in the aluminium hydroxide suspension, after 20 hours, take out, again 1100 ℃ of roastings 12 hours.In roasting process, the aluminium hydroxide of coating undergoes phase transition, and obtains α-type aluminium oxide at last.Through α-Al
2O
3Its specific area of matrix of carrying out surface modification is 550m
2/ m
3
Embodiment 3
The metallizing palladium is with the preparation hydrogenation catalyst on the matrix of the formation modified layer that embodiment 2 is obtained.Press palladium content 0.5% (weight) preparation palladium bichloride or palladium nitrate aqueous solution, adjust pH to 5.0～6.5 are sprayed on the modified matrix that is preheating to 40～60 ℃ with suitable sprayer, then 120 ℃ of dryings.The filler that carries palladium preferably is no more than 500 ℃ 350～500 ℃ of roastings.General roasting time 10 hours.Make catalyst reduction 12 hours with hydrogen-containing gas suitable pressure and 60～120 ℃ then, make the filler that contains catalyst activity component.
Embodiment 4
Catalytic distillation tower member with embodiment 3 makes in its φ 100mm catalytic distillation tower conversion zone of packing into, carries out carbon three hydrogenation catalyst distillation tests, promptly by selecting hydrogenation, removes propine contained in the propylene and allene.Catalytic distillation tower height 6m divides rectifying section, conversion zone and stripping section, the high 5m of rectifying section and stripping section, the random packing of filling φ 6 * 6mm stainless steel cannon ring; The high 1m of conversion zone, 10 on the φ 100 * 100mm porous ceramics structured packing dish of packing into altogether.Raw material feeds from the conversion zone bottom, and cat head obtains product.Result of the test is as shown in table 1:
Table 1
| The position | Charging | Cat head | The tower still | |
| Form mol% | ?C 2 0 | ????0.02 | ????0.02 | |
| ?C 3 0 | ????2.50 | ????4.11 | ????1.46 | |
| ?C 3 ＝ | ????72.14 | ????95.87 | ????11.29 | |
| ?C 3 ＝ | ????1.08 | ????4ppm | ????2.47 | |
| ?C 3 ≡ | ????2.09 | ????3ppm | ????4.72 | |
| ?C 4 | ????19.43 | ????74.05 | ||
| ?C 5 | ????2.72 | ????6.02 | ||
| Flow (l/h) | ????10 | ????7.4 | ????2.6 | |
| Temperature (℃) | ????25 | ????42 | ????98 | |
| Pressure (MPa) | ????2.3 | ????1.75 | ????1.78 | |
| Hydrogen alkynes ratio | ??????????????????0.9 | |||
| Propene yield (%) | ??????????????????101.9 | |||
As seen from the experiment, this catalytic distillation structure has good reaction and separating property, and by catalytic distillation, propine and allene content are reduced to below the 10ppm in the cat head discharging.
Embodiment 5
Contrast is through different al
2O
3The performance of catalytic distillation tower member after the surface modification.Make the structured packing of a plurality of φ 100 * 100mm porous ceramics by embodiment 1, it is immersed in aluminium hydroxide suspension, took out after 20 hours, divide two groups respectively 500 ℃ and 1100 ℃ of following roastings 12 hours, then filling surface is respectively by γ-Al
2O
3And α-Al
2O
3Modification.Press embodiment 3 metallizing palladium in the porous ceramics structured packing after the modification again, by embodiment 4 two groups of catalytic distillation tower members are packed in the catalytic distillation tower conversion zone then, and carrying out carbon three hydrogenation catalyst distillation tests by the reaction condition that embodiment 4 provides, the result is as shown in table 2.
Table 2
| Catalytic distillation tower member | Through γ-Al 2O 3Modification | Through α-Al 2O 3Modification |
| Specific area (m 2/g) | ????50 | ????10 |
| Conversion ratio (%) | ????99.98 | ????99.96 |
| Selectivity (%) | ????46.38 | ????82.44 |
As seen from the experiment, through γ-Al
2O
3Though the catalytic distillation tower member of modification has higher conversion ratio, selectivity is relatively poor; And through α-Al
2O
3The catalytic distillation tower member of modification has higher conversion ratio and good selectivity simultaneously.Therefore, catalytic distillation tower member of the present invention adopts α-Al
2O
3Surface modification is carried out in the porous ceramics structured packing.
Claims (12)
1. catalytic distillation tower member that constitutes by matrix, modified layer and active layer, it is characterized in that with the porous ceramics structured packing with microcellular structure be matrix, with the coating of matrix being carried out forming after the surface treatment through Alpha-alumina is modified layer, is active layer to cover the catalyst activity component that invests on the modified layer.
2. according to the described catalytic distillation tower member of claim 1, the specific area of wherein said matrix is 400～800m
2/ m
3, voidage is 72～95%.
3. according to the described catalytic distillation tower member of claim 1, wherein said catalyst activity component can be VIII family or IB family metal and composition thereof, also can be acid cation exchange resin or Y type, X type, β type and various modified zeolite molecular sieve.
4. according to the described catalytic distillation tower member of claim 1, wherein said matrix is porous ceramics corrugated plating, porous ceramics silk screen or porous ceramics fin.
5. according to the described catalytic distillation tower member of claim 4, wherein said matrix is the porous ceramics corrugated plating, and its porosity is 30～60%, and the aperture is 10～18 μ m.
6. according to the described catalytic distillation tower member of claim 5, wherein said porous ceramics corrugated plating wall thickness 0.8～1.2mm, 30 °～45 ° at ripple inclination angle, the crest height of wave and the pitch of waves are 5～30mm, have the hole of 3～6mm on the corrugated siding.
7. the preparation method of the described catalytic distillation tower member of claim 5, wherein said matrix prepares according to the following steps: mix as base material aluminium-silicate, high attaclay or diatomite (1) with distilled water, outer adding additives and pore creating material, with its mixing and ball milling 5～20 hours, the pH value of gained mud is adjusted to 5.0～7.0; (2) step (1) gained slurry is squeezed into corrugated plate type, the blank of moulding carries out after the integer at room temperature dry, and opens several apertures on blank; (3) dried each sheet blank is assembled, the ripple of adjacent two corrugated platings intersects 90 ° during assembling, connects each sheet assembling back one-tenth dish between adjacent two crest with binding agent; (4) the cellar for storing things roasting is put in the structured packing that will be assembled into dish, at 800～1000 ℃ of following sintering.
8. according to the described preparation method of claim 7, the binding agent and the pore creating material that use in the wherein said step (1) are starch, use hydrochloric acid or TMAH to regulate the pH value of mud; The binding agent that uses in the described step (3) is waterglass.
9. the preparation method of the described catalytic distillation tower member of claim 1, wherein said modified layer is carried out modification by the following method with matrix and is obtained: at first matrix is immersed in the aluminium hydroxide suspension, after 12～24 hours, take out, then 1000～1200 ℃ of roastings 8～12 hours, in roasting process, the aluminium hydroxide of coating undergoes phase transition, and changes the Alpha-alumina modified layer at last into.
10. the preparation method of claim 1 or 3 described catalytic distillation tower members, wherein said active layer is to adopt the method for immersing or spraying process that catalyst activity component is covered equably to invest on the matrix that forms modified layer and form.
11. according to the described preparation method of claim 10, the wherein said method of immersing comprises that the matrix that will form modified layer is immersed in crystallization in the solution that contains catalyst activity component, takes out washing, dry, roasting then.
12. according to the described preparation method of claim 10, wherein said spraying process comprises uses sprayer, and the solution spraying that contains catalyst activity component for preparing on the matrix that forms modified layer, is carried out drying, roasting, reduction then.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02104203 CN1193820C (en) | 2002-02-07 | 2002-02-07 | Catalytic distillation tower member and its manufacture |
| US10/361,084 US7226884B2 (en) | 2002-02-07 | 2003-02-06 | Composite for catalytic distillation and its preparation |
| US11/741,395 US7642388B2 (en) | 2002-02-07 | 2007-04-27 | Composite for catalytic distillation and its preparation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02104203 CN1193820C (en) | 2002-02-07 | 2002-02-07 | Catalytic distillation tower member and its manufacture |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1436586A true CN1436586A (en) | 2003-08-20 |
| CN1193820C CN1193820C (en) | 2005-03-23 |
Family
ID=27627954
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02104203 Expired - Lifetime CN1193820C (en) | 2002-02-07 | 2002-02-07 | Catalytic distillation tower member and its manufacture |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1193820C (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012075675A1 (en) * | 2010-12-10 | 2012-06-14 | 中国石油天然气股份有限公司 | Method for preparing catalyst coating on metal base plate |
| CN103822937A (en) * | 2012-11-16 | 2014-05-28 | 哈尔滨飞机工业集团有限责任公司 | Boiling point testing method for trichloroethylene bath solution |
| CN105597357A (en) * | 2016-02-29 | 2016-05-25 | 中石化炼化工程（集团）股份有限公司 | Composite regular packing and manufacturing method thereof |
| CN109349681A (en) * | 2018-11-15 | 2019-02-19 | 深圳市合元科技有限公司 | Porous heater, the atomizer comprising porous heater and porous preparation |
| CN113198535A (en) * | 2021-05-17 | 2021-08-03 | 厦门大学 | Preparation method of ceramic surface supported catalytic filler |
-
2002
- 2002-02-07 CN CN 02104203 patent/CN1193820C/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012075675A1 (en) * | 2010-12-10 | 2012-06-14 | 中国石油天然气股份有限公司 | Method for preparing catalyst coating on metal base plate |
| US9440227B2 (en) | 2010-12-10 | 2016-09-13 | Petrochina Company Limited | Method for preparing catalyst coating on metal base plate |
| CN103822937A (en) * | 2012-11-16 | 2014-05-28 | 哈尔滨飞机工业集团有限责任公司 | Boiling point testing method for trichloroethylene bath solution |
| CN105597357A (en) * | 2016-02-29 | 2016-05-25 | 中石化炼化工程（集团）股份有限公司 | Composite regular packing and manufacturing method thereof |
| CN105597357B (en) * | 2016-02-29 | 2018-08-24 | 中石化炼化工程（集团）股份有限公司 | A kind of compound regular packing and preparation method thereof |
| CN109349681A (en) * | 2018-11-15 | 2019-02-19 | 深圳市合元科技有限公司 | Porous heater, the atomizer comprising porous heater and porous preparation |
| CN109349681B (en) * | 2018-11-15 | 2021-09-03 | 深圳市合元科技有限公司 | Porous heating element, atomizer containing porous heating element and porous body preparation method |
| CN113198535A (en) * | 2021-05-17 | 2021-08-03 | 厦门大学 | Preparation method of ceramic surface supported catalytic filler |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1193820C (en) | 2005-03-23 |
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