CN105833803A - Gas foam remover for acetylene hydrogenation type ethylene preparation packing bubbling bed - Google Patents
Gas foam remover for acetylene hydrogenation type ethylene preparation packing bubbling bed Download PDFInfo
- Publication number
- CN105833803A CN105833803A CN201610366015.9A CN201610366015A CN105833803A CN 105833803 A CN105833803 A CN 105833803A CN 201610366015 A CN201610366015 A CN 201610366015A CN 105833803 A CN105833803 A CN 105833803A
- Authority
- CN
- China
- Prior art keywords
- silk screen
- catalyst
- bubbling bed
- gas
- gas demister
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/04—Ethylene
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
- C07C5/05—Partial hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
- C07C2523/44—Palladium
Abstract
The invention discloses a gas foam remover for an acetylene hydrogenation type ethylene preparation packing bubbling bed. The gas foam remover comprises a 15-25-mesh screen mesh and a screen mesh mounting part, the screen mesh mounting part is fixed to the inner wall of the upper middle portion of the packing bubbling bed, and the screen mesh is coated with a catalyst and fixed to the screen mesh mounting part. Since the screen mesh coated with the catalyst is arranged on the gas foam remover, escape of solvent volatile components is prevented while trace acetylene in reaction products can be converted completely, and structural simplicity and easiness in mounting are realized.
Description
Technical field
The invention belongs to chemical industry equipment equipment manufacturing field, fill out particularly to a kind of producing ethylene with acetylene hydrogenation
The gas demister of material bubbling bed.
Background technology
Along with petroleum resources are the most exhausted, Development of Coal chemical industry is that the chemical process of raw material becomes petroleum replacing
The significant process of chemical industry route, obtains extensive concern, and obtains fast development.
In coal chemical technology, produce acetylene for raw material by calcium carbide technique with coal, have been widely used,
With acetylene as raw material, under selective hydrocatalyst effect, by Hydrogenation for ethylene product, can
Expand Coal Chemical Industry Route further.And the downstream product polyvinyl chloride (PVC) that acetylene is main in the last few years
Supply exceed demand, and PVC industrial profit is the highest, is badly in need of expanding acetylene downstream product industrial chain.
Ethene is most important basic material in petrochemical industry, is referred to as " mother of petrochemical industry ".Extensively
For plastics, lubricating oil, polymer and some intermediates, currently mainly by oil or low-carbon alkanes
Pass through cracking.Ethene downstream product such as ethylene glycol, butanediol, acrylic acid, polyvinyl alcohol etc. are also
There is good economic worth.Therefore, the novel technique of exploitation producing ethylene with acetylene hydrogenation can be ethene
Industry provides a kind of new raw material source, and reduces ethene to the degree of dependence of petroleum resources and ethylene production
Cost, has broad application prospects.
Preparation of ethylene through selective hydrogenation of acetylene technique nucleus equipment is filler bubbling bed hydrogenation reactor, because second
Alkynes hydrogenation be the catalytic reaction process that exothermic heat of reaction amount is the biggest, reaction generate gas temperature higher, from
Meeting entrained liquids mist when holding filler bubbling bed, and in this filler bubbling bed, the conversion ratio of acetylene is the highest
Can only achieve 96%, have a large amount of ethene, a small amount of ethane and trace acetylene in the reaction product, these are three years old
Plant acetylene in gaseous material to be difficult to separate with ethane, ethene, the purity of purpose product can be affected, impact
Products application scope.Industrial typically take front-end hydrogenation technique, reset a selective acetylene
Hydrogenation fixed bed device eliminates the acetylene of trace, meets industrial polymer grade ethylene ingredient requirement.
In filler bubbling bed hydrogenation reactor, gas demister is to leave after reacting gas hydrogenation reaction
Last one barrier of filler bubbling bed.In prior art, there is a kind of wire mesh demister, mainly by silk
The waveform silk screen block composition that net barrier, silk screen are combined into after molding, demister mainly applies silk screen to remove
Foam, function singleness, only there is foam removal function, and structure is complicated.
Summary of the invention
In order to solve the problems referred to above, the present invention provides a kind of for producing ethylene with acetylene hydrogenation filler bubbling bed
Gas demister, this gas demister arrange be similar to fixed bed effect containing having catalysis efficiency
Silk screen, not only prevents the effusion of solvent volatile component, again can be by complete for the acetylene of trace in reactor product
Full conversion, and simple in construction, it is easy to install.
A kind of gas demister for producing ethylene with acetylene hydrogenation filler bubbling bed, including: silk screen and silk
Net installed part,
On the middle part inwall of the upper space that described silk screen installed part is fixed on filler bubbling bed；Described silk
The mesh number of net is 15～25 mesh, and described silk screen is coated with catalyst；Described silk screen is fixed on described silk
On net installed part.
Described gas demister installation site is positioned at the middle part of the upper space of filler bubbling bed, and this is
Depending on reaction mechanism according to filler bubbling bed.Because in filler bubbling bed, liquid phase is from end socket bottom
Removal recycles, and product gas is discharged from top, and the droplet distribution carried secretly is few and ratio is more uniform,
Body demister installation site is positioned at the middle part of the upper space of filler bubbling bed, can effectively capture liquid
Drip and separate.
Experimentally determined, under the conditions of meshcount is 15～25 purposes, the mist of rising touches silk
During net, easily forming water film, the solvent of gasification can be condensed into drop.
Specifically, described silk screen installed part includes bracer and a securing member, and described bracer is fixed on and fills out
On the middle part inwall of the upper space of material bubbling bed, described silk screen is fixed on described by described securing member
Prop up on bracer.
In the present invention, described catalyst is the catalyst of palladium catalyst, and active ingredient is Metal Palladium, gold
Belong to nickel, metallic cobalt, metal molybdenum, tungsten or manganese metal.
The active ingredient of described catalyst percentage by weight in the catalyst be 0.01wt%～
0.08wt%.
Preferably, the carrier of described catalyst can be α-Al2O3、γ-Al2O3、TiO2
Or SiO2。
Concrete, described catalyst is prepared by infusion process, the granular size of ground catalyst be 50～
100nm, is heated to 200-280 DEG C by spray gun, preferably 280 DEG C, after spray to silk screen surface.
Understand through experiment, when the thickness of described catalyst is 0.5 μm-20 μm, just can be catalyzed
Unreacted residual gas.
In the present invention, the material of described silk screen is the polytetrafluoroethylene (PTFE) (PTFE) of high intensity, wear resistant nylon
66 (POLIBLEND) or polypropylene (PP), make silk screen corrosion-proof high-temp, increase the service life,
Cost-effective.
In order to fabricate, and producing the facility keeped in repair, the silk screen of the present invention can design with split,
Described silk screen includes one or more silk screen module.
In the present invention, described support block welding or be bolted on the top of described filler bubbling bed
On the middle part inwall in space.
The gas demister simple in construction for filler bubbling bed that the present invention provides, it is easy to install, grasp
Make, keep in repair and clean；Nano level palladium catalyst catalyst is sprayed on silk screen, can be by micro-in product gas
Amount acetylene is under the effect of catalyst, and the hydrogen generation selective hydrogenation in gas, by trace
Acetylene is fully converted to ethene；Solve the difficult problem that trace acetylene in purpose product is difficult to separate, it is to avoid
The problem that have impact on ethylene product range of application due to the purity of purpose product.
Accompanying drawing explanation
Fig. 1 is the gas demister scheme of installation of filler bubbling bed；
Fig. 2 is the gas demister scheme of installation of filler bubbling bed.
In figure: a bracer 1, securing member 2, silk screen 3, product gas outlet 4, filler bubbling bed inwall 5,
Filler bubbling bed solvent liquid level 6.
Detailed description of the invention
Below in conjunction with drawings and Examples, the detailed description of the invention of the present invention is carried out more detailed theory
Bright, so as to the advantage being more fully understood that the solution of the present invention and various aspects thereof.But, below
The detailed description of the invention and the embodiment that describe are only descriptive purpose rather than limitation of the present invention.
A kind of gas demister for producing ethylene with acetylene hydrogenation filler bubbling bed that the present invention provides, as
Shown in Fig. 1, including: silk screen 3 and silk screen installed part.
Gas demister installation site is positioned at the middle part of the upper space of filler bubbling bed, silk screen installed part
On the middle part inwall 5 of the upper space being fixed on filler bubbling bed, silk screen 3 is fixed on silk screen installed part
On.Depending on this is the reaction mechanism according to filler bubbling bed.Because in filler bubbling bed, liquid phase from
The removal of end socket bottom recycles, and product gas is discharged from top, and the droplet distribution carried secretly is few and compares
More uniform, silk screen module mounting location is positioned at the middle part of the upper space of filler bubbling bed, can be effective
Ground capture drop and separation.
The mesh number of silk screen 3 is 15～25 mesh, and silk screen 3 is coated with catalyst, and catalyst is palladium catalyst
Catalyst granules.Experimentally determined, under the conditions of meshcount is 15～25 purposes, the mist of rising
When foam touches silk screen, easily forming water film, the solvent of gasification can be condensed into drop.When with mist
The gas of foam when filler bubbling bed solvent liquid level 6 rises through silk screen 3 with certain speed, due to
The effect of inertia that mist rises, mist and silk screen 3 collide and are attached on the surface of silk screen 3.
The diffusion of mist on silk screen 3 surface, the gravitational settling of mist, make mist formed bigger drop along
Silk screen 3 flow to the interface point of two silks.The mixtures such as acetylene, ethene, hydrogen pass catalyst silk screen 3
Time, under the palladium catalysis of the trace acetylene therein coating outside silk screen 3, with the hydrogen in gas
Gas generation selective hydrogenation, trace acetylene is fully converted to ethene, follows gas and goes out from product gas
Mouth 4 effusion.
Silk screen 3 itself has wettability, at the surface tension of liquid and the work of the capillary of silk screen
Under with so that drop is increasing, until the drop assembled arrives greatly the gravity himself produced and exceedes gas
The climbing power of body and when making a concerted effort of surface tension of liquid, drop just separates from silk screen, is returned to
In dicyandiamide solution, and the gas through filtering is discharged from product gas outlet 4.
Silk screen installed part includes bracer 1 and a securing member 2, and a bracer 1 is fixed on the upper of filler bubbling bed
On the middle part inwall 5 in space, portion, described silk screen 3 is fixed on a bracer 1 by securing member 2.?
Bracer 1 welds or is bolted on the inwall 5 of filler bubbling.
Polytetrafluoroethylene (PTFE) (PTFE) that silk screen 3 uses material to be high intensity, wear resistant nylon 66
Or polypropylene (PP) (POLIBLEND), make silk screen corrosion-proof high-temp, extend the use time, joint
About cost.Silk screen 3 can include one or more silk screen module, silk screen 3 is divided into multiple module, makes
Obtain installation, maintenance more convenient, it is easy to processing and manufacturing.
The active ingredient of catalyst is Metal Palladium, metallic nickel, metallic cobalt, metal molybdenum, tungsten or gold
Belong to manganese etc..The active ingredient of catalyst percentage by weight in the catalyst be 0.01wt%～
0.08wt%.The carrier of catalyst is α-Al2O3、γ-Al2O3、TiO2Or SiO2Deng.Catalyst
Granular size is 50-100nm.The thickness of catalyst is 0.5 μm-20 μm.
Catalyst is prepared by infusion process, and the granular size of ground catalyst is 50～100nm, logical
Cross and after spray gun is heated to 200-280 DEG C, spray to silk screen 3 surface.When being heated to 280 DEG C, catalyst
Adhesion effect more preferable.
In the present invention, filler bubbling bed has the feature of efficient mass transfer, heat transfer, owing to there being filler to urge
Agent liquid layer is uniformly distributed, and reacting gas enters from the aperture bubbling of distributor at the bottom of tower, divides through air-liquid
Fabric swatch enters filler bubbling bed and is fully contacted with liquid phase and solid phase, and reacted product gas rises reaction
Behind device top, from end socket bottom, removal recycles liquid phase, and product gas is discharged from top.At this
Under the mesh said conditions of bright silk screen, when mist is stained with on silk screen, easily form water film, and water film
Time under the area of this size, tension force is easily damaged, and causes it to turn to rapidly water droplet, and mist is disappeared
Remove, the best results of demister.
Embodiment
The gas demister structure of the present embodiment as depicted in figs. 1 and 2,
The mesh number of silk screen 3 is 20 mesh, and employing material is high-strength polytetrafluoroethyl-ne, silk screen module number
It it is 3 pieces；
The surface spraying thickness of silk screen is 0.5 μm～the catalyst of 20 μm；
Catalyst active ingredient is Metal Palladium particle；
The granular size that catalyst divides is 50～100nm；
Catalyst active ingredient percentage by weight in catalyst layer is 0.01wt%～0.08wt%；
The carrier of catalyst active ingredient is α-Al2O3。
Propping up bracer 1 to be welded on the middle part inwall 5 of filler bubbling upper space, 3 pieces of silk screen modules are respectively
Being fixed on a bracer 1 by securing member 2, securing member 2 is the stainless steel stud of Φ 12.
The filler bubbling bed gas demister simple in construction that the present invention provides, it is easy to install, operate, tie up
Repair and clean.Spray nano level palladium catalyst catalyst on silk screen, not only prevent solvent volatile component
Effusion, also can be by trace acetylene in product gas under the effect of catalyst, with the hydrogen in gas
There is selective hydrogenation, trace acetylene is fully converted to ethene, is greatly improved catalytic reaction
Conversion ratio.
It should be noted that each embodiment above by reference to described by accompanying drawing is only in order to illustrate the present invention
And unrestricted the scope of the present invention, it will be understood by those within the art that, without departing from this
The amendment on the premise of bright spirit and scope carried out the present invention or equivalent, all should contain
Within the scope of the present invention.Additionally, unless the context outside indication, the word bag occurred in the singular
Including plural form, vice versa.It addition, unless stated otherwise, then any embodiment whole or
A part can use in conjunction with all or part of of any other embodiments.
Claims (10)
1. for the gas demister of producing ethylene with acetylene hydrogenation filler bubbling bed, including: silk screen and
Silk screen installed part, it is characterised in that
On the middle part inwall of the upper space that described silk screen installed part is fixed on filler bubbling bed；
The mesh number of described silk screen is 15～25 mesh, and described silk screen is coated with catalyst；
Described silk screen is fixed on described silk screen installed part.
Gas demister the most according to claim 1, it is characterised in that described silk screen installed part
Including bracer and a securing member, in the middle part of the upper space that described bracer is fixed on filler bubbling bed
On wall, described silk screen is fixed on described bracer by described securing member.
Gas demister the most according to claim 1, it is characterised in that having of described catalyst
Effect composition is Metal Palladium, metallic nickel, metallic cobalt, metal molybdenum, tungsten or manganese metal.
Gas demister the most according to claim 3, it is characterised in that having of described catalyst
Effect composition percentage by weight in the catalyst is 0.01wt%～0.08wt%.
Gas demister the most according to claim 1, it is characterised in that the load of described catalyst
Body is α-Al2O3、γ-Al2O3、TiO2Or SiO2。
Gas demister the most according to claim 1, it is characterised in that described catalyst
Grain size is 50-100nm.
Gas demister the most according to claim 1, it is characterised in that the thickness of described catalyst
Spend 0.5 μm-20 μm.
Gas demister the most according to claim 1, it is characterised in that the material of described silk screen
For polytetrafluoroethylene (PTFE) (PTFE), wear resistant nylon 66 (POLIBLEND) or polypropylene (PP).
Gas demister the most according to claim 1, it is characterised in that described silk screen includes one
Individual or multiple silk screen modules.
Gas demister the most according to claim 2, it is characterised in that described bracer weldering
Connect or be bolted on described filler bubbling bed inwall.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610366015.9A CN105833803A (en) | 2016-05-27 | 2016-05-27 | Gas foam remover for acetylene hydrogenation type ethylene preparation packing bubbling bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610366015.9A CN105833803A (en) | 2016-05-27 | 2016-05-27 | Gas foam remover for acetylene hydrogenation type ethylene preparation packing bubbling bed |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105833803A true CN105833803A (en) | 2016-08-10 |
Family
ID=56594949
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610366015.9A Pending CN105833803A (en) | 2016-05-27 | 2016-05-27 | Gas foam remover for acetylene hydrogenation type ethylene preparation packing bubbling bed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105833803A (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06262037A (en) * | 1993-03-10 | 1994-09-20 | Asahi Glass Co Ltd | Method for denitrification of exhaust gas from glass kiln |
| CN1203595A (en) * | 1995-11-29 | 1998-12-30 | 巴斯福股份公司 | Process for hydrogenating dihydrofuranes to tetrahydrofuranes |
| CN1600412A (en) * | 2003-09-22 | 2005-03-30 | 上海兖矿能源科技研发有限公司 | Contiuous industrial reactor of slurry state bed in gas, liquid and solid three phases |
| CN101151227A (en) * | 2005-04-06 | 2008-03-26 | 沙特基础工业公司 | Method for selective hydrogenation of acetylene to ethylene |
| CN203862132U (en) * | 2014-01-26 | 2014-10-08 | 北京诺曼斯佰环保科技有限公司 | Wet flue gas desulfurization tower and deep flue gas purification system |
| CN104128050A (en) * | 2014-07-17 | 2014-11-05 | 广西新天德能源有限公司 | Demister |
| CN204973827U (en) * | 2015-08-07 | 2016-01-20 | 北京神雾环境能源科技集团股份有限公司 | A reaction tower for acetylene hydrogenation makes ethylene |
| CN206404746U (en) * | 2016-05-27 | 2017-08-15 | 北京华福工程有限公司 | A kind of gas demister for producing ethylene with acetylene hydrogenation filler bubbling bed |
-
2016
- 2016-05-27 CN CN201610366015.9A patent/CN105833803A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06262037A (en) * | 1993-03-10 | 1994-09-20 | Asahi Glass Co Ltd | Method for denitrification of exhaust gas from glass kiln |
| CN1203595A (en) * | 1995-11-29 | 1998-12-30 | 巴斯福股份公司 | Process for hydrogenating dihydrofuranes to tetrahydrofuranes |
| CN1600412A (en) * | 2003-09-22 | 2005-03-30 | 上海兖矿能源科技研发有限公司 | Contiuous industrial reactor of slurry state bed in gas, liquid and solid three phases |
| CN101151227A (en) * | 2005-04-06 | 2008-03-26 | 沙特基础工业公司 | Method for selective hydrogenation of acetylene to ethylene |
| CN203862132U (en) * | 2014-01-26 | 2014-10-08 | 北京诺曼斯佰环保科技有限公司 | Wet flue gas desulfurization tower and deep flue gas purification system |
| CN104128050A (en) * | 2014-07-17 | 2014-11-05 | 广西新天德能源有限公司 | Demister |
| CN204973827U (en) * | 2015-08-07 | 2016-01-20 | 北京神雾环境能源科技集团股份有限公司 | A reaction tower for acetylene hydrogenation makes ethylene |
| CN206404746U (en) * | 2016-05-27 | 2017-08-15 | 北京华福工程有限公司 | A kind of gas demister for producing ethylene with acetylene hydrogenation filler bubbling bed |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102272092A (en) | Method for producing toluylenediamine by hydrogenating dinitrotoluene | |
| CN201154303Y (en) | Gas feed distributor | |
| KR102008423B1 (en) | Methane pyrolysis solar reactor and method for producing hydrogen and carbon black using the same | |
| CN206404746U (en) | A kind of gas demister for producing ethylene with acetylene hydrogenation filler bubbling bed | |
| CN102410518B (en) | Low-grade heat energy recycling method for liquid urea washing tower | |
| NZ212224A (en) | Vertical tube reactor for carrying out non-isothermal reactions | |
| CN100551478C (en) | Catalyze rectification packing tower | |
| CN201482591U (en) | Gas distributor | |
| CN205095760U (en) | A reactor and device for inciting somebody to action methyl alcohol or dimethyl ether turn into propylene | |
| CN201710990U (en) | Variable aperture dual-flow sieve-plate tower | |
| CN202191810U (en) | Wet dust-extraction washing tower for synthesis gas in trichlorosilane production | |
| CN204051632U (en) | A kind of Venturi tube-type spreader gas-liquid allotter of high-efficient atomizing | |
| CN206404748U (en) | A kind of gas demister for producing ethylene with acetylene hydrogenation three phase fluidized bed | |
| CN206404744U (en) | A kind of gas demister for producing ethylene with acetylene hydrogenation trickle bed | |
| CN102274707A (en) | Slurry reactor used for producing liquid fuel | |
| CN105833803A (en) | Gas foam remover for acetylene hydrogenation type ethylene preparation packing bubbling bed | |
| CN108854929A (en) | A kind of falling film reactor of the dehydrogenation reaction suitable for liquid hydrogen source material | |
| CN105833801A (en) | Gas foam remover for acetylene hydrogenation type ethylene preparation trickle bed | |
| CN105833806A (en) | Gas foam remover for acetylene hydrogenation type ethylene preparation three-phase fluidized bed | |
| CN206045984U (en) | A kind of gas demister for producing ethylene with acetylene hydrogenation slurry bed system | |
| CN211814294U (en) | Ultra-deep removing device for organic sulfur in coke oven gas | |
| CN100390132C (en) | Gas distributor in fluidized bed of aniline synthesis and aniline synthesis method | |
| CN102350162A (en) | Tower top dust recovery device for urea granulation tower and recovery method for dust on top of urea granulation tower | |
| CN105060297B (en) | A kind of method and device for producing silicochloroform | |
| CN102309948A (en) | Method for charging boiling bed catalyst on line |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20160922 Address after: 102200 Beijing City, Changping District science and Technology Park Fukang Road No. 18 Applicant after: Beijing Huafu Engineering Co., Ltd. Address before: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Applicant before: Beijing Shenwu Environment Energy Technology Group Co., Ltd. |
|
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160810 |
|
| RJ01 | Rejection of invention patent application after publication |