CN101780389B - Fluid bed reactor used for gasoline desulfuration - Google Patents
Fluid bed reactor used for gasoline desulfuration Download PDFInfo
- Publication number
- CN101780389B CN101780389B CN200910076756A CN200910076756A CN101780389B CN 101780389 B CN101780389 B CN 101780389B CN 200910076756 A CN200910076756 A CN 200910076756A CN 200910076756 A CN200910076756 A CN 200910076756A CN 101780389 B CN101780389 B CN 101780389B
- Authority
- CN
- China
- Prior art keywords
- conversion zone
- reactor
- gas
- distributor
- bed reactor
- 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.)
- Active
Links
- 239000012530 fluid Substances 0.000 title abstract description 4
- 238000006477 desulfuration reaction Methods 0.000 title abstract 2
- 239000003054 catalyst Substances 0.000 claims abstract description 32
- 239000000428 dust Substances 0.000 claims abstract description 29
- 238000009826 distribution Methods 0.000 claims abstract description 7
- 238000006243 chemical reaction Methods 0.000 claims description 43
- 239000003638 chemical reducing agent Substances 0.000 claims description 17
- 238000011001 backwashing Methods 0.000 claims description 15
- 238000005204 segregation Methods 0.000 claims description 15
- 239000008187 granular material Substances 0.000 claims description 12
- 230000001172 regenerating effect Effects 0.000 claims description 12
- 239000003795 chemical substances by application Substances 0.000 claims description 10
- 230000000903 blocking effect Effects 0.000 claims description 8
- 230000003628 erosive effect Effects 0.000 claims description 6
- 238000005520 cutting process Methods 0.000 claims description 5
- 239000007789 gas Substances 0.000 abstract description 48
- 239000002245 particle Substances 0.000 abstract description 7
- 238000012423 maintenance Methods 0.000 abstract description 4
- 238000001914 filtration Methods 0.000 abstract description 2
- 230000002265 prevention Effects 0.000 abstract 3
- 230000003116 impacting effect Effects 0.000 abstract 1
- 230000001737 promoting effect Effects 0.000 abstract 1
- 239000012495 reaction gas Substances 0.000 abstract 1
- 238000000034 method Methods 0.000 description 6
- 238000005243 fluidization Methods 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012065 filter cake Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000011295 pitch Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Images
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention provides a fluid bed reactor used for gasoline desulfuration, which belongs to the field of petrochemical industry and is characterized in that an automatic back wash filter, a dust reduction machine, a catalyst bed, a backflow prevention distributor and an impact prevention distributor are arranged in a reactor, and the reactor is externally connected with a reductor and an acceptor. By utilizing the reactor, the filtering performance of the filter can be automatically and efficiently restored in time, thereby reducing the labor strength; catalyst particles are prevented from flowing back below the reactor, thereby enabling gas to be evenly distributed on the section of the whole reactor; the dust content of the gas is effectively reduced, thereby greatly reducing the load of the automatic back wash filter, effectively prolonging the operating period of the automatic back wash filter and reducing equipment investments and maintenance charges; the influent gas is prevented from impacting the backflow prevention distributor, thereby promoting the even distribution of the gas and improving the benefit of the reactor; and moreover, reaction gas and a catalyst flow out of different paths after entering the reactor through different paths, thereby realizing high-treatment capacity continuous operation.
Description
Technical field
The invention belongs to petrochemical industry, be specifically related to a kind of fluidized-bed reactor that is used for gasoline desulfur.
Background technology
Gasoline desulfur mainly adopts fixed bed hydrogenation reactor at present, and catalyst is in closely knit filling state in reactor.The most typical fluidized-bed reactor is a FCC riser in the petrochemical equipment, and its top is provided with fast minute member, strengthens the gas-solid separating effect of gas and catalyst; Gas in the riser reactor and catalyst are bottom-up to flow, and flow velocity is a kind of high speed fluidized state generally at 12-20m/s.
In the prior art; Publication number is that the application of CN1824378A discloses and is used for the synthetic fluidized-bed reactor of Fischer-Tropsch; It is synthetic that this fluidized-bed reactor is used for Fischer-Tropsch, and the problem of its existence is: 1) filter on it is operation continuously, the problem if filter generation pressure drop exceeds standard etc.; Filter will be compelled out of service, and then whole reactor will quit work; 2) the filter integral installation is unfavorable for maintenance at inside reactor.
In addition; Publication number is that the prior art of CN2216860 discloses a kind of fluidized reaction device; The problem of its existence is: 1) distributor of its bottom adopts spheroid with magnetic and the magnet that can produce alternating magnetic field to form, and the gas of generation can only distribute near spheroid and awl section binding site, and gas is evenly distributed at the whole reactor cross section; Cause its space reactor utilization rate low thus, the treating capacity of reactor is difficult to enlarge; 2) the manual cleaning efficiency of its filter is low and manpower labour intensity is big, and depends on people's subjective judgement, is difficult to guarantee efficiently to clean timely; 3) owing to there is not the depositing dust facility, the dustiness of gas is high, and filter cleans frequent, has further increased operative employee's labour intensity; 4) can only realize intermittent operation, the powder that receives when the discharging receiver reaches in limited time must the replacing receiver, can only shut-down operation between the stage of replacement; 5) can only realize fluidisation less than 40 micron particles, this is because its distributor adopts the mode at magnetic spheres and taper connection place, if particle diameter is bigger, will be difficult to drop to receiver even block magnetic spheres.
Summary of the invention
The objective of the invention is to solve a difficult problem that exists in the above-mentioned prior art; A kind of fluidized-bed reactor that is used for gasoline desulfur is provided; Realize the automatic cleaning of filter; Guarantee filter long-period stable operation and convenient maintenance, promotion gas evenly distributes and then improves the space availability ratio of reactor and realize the high throughput continued operation.
The present invention realizes through following technical scheme:
A kind of fluidized-bed reactor that is used for gasoline desulfur, it comprises segregation section 4, expansion segment 3, conversion zone 1 from top to bottom successively, in said conversion zone 1, beds 2 is housed.In said expansion segment 3 segregation sections 4, be provided with dust settler 9, be used to reduce the gas dustiness.
In practical implementation, the fixed position of said dust settler 9 can specifically confirm according to the gas flow rate of beds, and when the gas flow rate design load of beds during greater than 0.35m/s, the lower edge of dust settler can be higher than the upper edge of expansion segment; Said dust settler 9 can adopt blocking type dust settler 20 or spiral-flow type dust settler 21; Said blocking type dust settler 20 can adopt conical structure; The hypotenuse of its conical structure and horizontal angle must be greater than the angles of repose of catalyst; So-called catalyst angle of repose is meant in gravitational field, the angle the when Free Surface of catalyst buildup body is in the limiting condition of balance between Free Surface and the horizontal plane.Said spiral-flow type dust settler 21 can adopt the twisted blade structure, and lobe numbers can be 3 to 8.From effect, blocking type dust settler 20 can reduce catalyst content that gas carries under the low speed circulating fluidized bed situation about 30%, and spiral-flow type dust settler 21 can reduce dustiness about 22% under the situation of higher speed fluid bed.
In practical implementation, can be provided with automatic backwashing filter 5 at the top of said segregation section 4, said automatic backwashing filter 5 is provided with reactor outlet flange 22 pairings at said segregation section 4 tops; Said automatic backwashing filter 5 tops are provided with gas vent 10, and the bottom is provided with filter core 23, and said filter core 23 stretches into the inside of said segregation section 4.In the course of the work; Catalyst dust causes pressure drop to raise at the filter cake that filter core 23 surface formation thickness increase gradually; When pressure drop is elevated to setting value or the time interval when reaching setting value, automatic backwashing filter will start backwashing procedures automatically, adopt gases at high pressure that filter core is carried out pulse backblowing; The filter cake fragmentation on filter core 23 surfaces is come off, and then recover strainability.
In practical implementation, can be provided with anti-backflow distributor 8 in the bottom of said conversion zone 1, be used to prevent that catalyst granules from flowing backwards to the below of said anti-backflow distributor 8; Said anti-backflow distributor 8 comprises distribution grid 19, one group of bubble cap 15 and group switching centre pipe 16; Evenly have one group of hole on the said distribution grid 19, a said central tube 16 is installed in each perforate; Each said central tube 16 upper end communicates with a bubble cap 15, and each said central tube 16 lower end has opening 18; Tooth-shape structure 17 is adopted in the lower surface of said bubble cap 15.Size through control opening, central tube, bubble cap; Particularly the internal diameter of central tube 16 guarantees that the gas flow rate in the various operating mode lower center tubes surpasses 5m/s; Thereby avoid catalyst granules to flow backwards, obtain at the equally distributed gas of whole reactor cross section to the distributor below.In addition, adopt anti-backflow distributor 8 can realize the fluidisation of larger particles, particle diameter reaches 110 microns in the practical application.
In practical implementation, be provided with gas access 6 in the bottom of said conversion zone 1, in said conversion zone 1 gas access 6 above be provided with erosion control distributor 7; Said erosion control distributor 7 adopts circular shield structure, and the diameter of circular shield is 1.3-1.9 a times of said gas access 6 diameters.
In practical implementation, on said conversion zone 1 top to being circumscribed with receiver 14; Said receiver 14 is connected with said conversion zone 1 through regenerative agent transverse tube 12, and the inlet of said regenerative agent transverse tube 12 is arranged on the position that is lower than beds 2 upper surfaces.
In practical implementation, in said conversion zone 1 bottom to being circumscribed with reductor 13; Said reductor 13 is connected with said conversion zone 1 through reducing agent inclined tube 11, and said reducing agent inclined tube 11 oblique cuttings are gone in the said conversion zone 1, and the outlet of reducing agent inclined tube 11 is positioned at anti-backflow distributor 8 tops.
The active catalyst that reduces gets into receiver 14 from regenerative agent transverse tube 12, finally removes regenerative system from receiver 14 bottoms.Said reductor 13 is connected with said conversion zone 1 through reducing agent inclined tube 11, and the outlet oblique cutting of said reducing agent inclined tube 11 is gone in the said conversion zone 1.Catalyst gets into reactor lower part from reductor 13 through reducing agent inclined tube 11.Therefore, the continued operation of fluid bed can be realized, the high throughput continued operation can be realized.
In practical implementation, in order to satisfy the requirement of low speed fluidisation, the gas flow rate in the said conversion zone 1 is controlled in the scope of 0.2-0.6m/s.
Compared with prior art, the invention has the beneficial effects as follows: 1. judge automatically and the startup backwash process, recovered the strainability of filter in time, automatically, efficiently, reduced labour intensity; Realized that easily filter integral body being hung out the realization response device overhauls outward; 2. effectively reduce the dustiness of gas, thereby significantly reduce the load of automatic backwashing filter, prolonged the automatic backwashing filter operation cycle effectively, reduced equipment investment and maintenance cost; 3. avoided catalyst granules to flow backwards to the distributor below; Gas is evenly distributed at the whole reactor cross section; And the gas of having avoided flowing into from the gas access impacts the anti-backflow distributor, has promoted that further gas evenly distributes, and has improved the space availability ratio and the efficient of reactor; 4. realized the fluidisation of larger particles, particle diameter reaches 110 microns in the practical application; 5. flow out from different paths again after the reacting gas path different with the catalyst process gets into conversion zone, realized the high throughput continued operation.
Description of drawings
Below in conjunction with accompanying drawing the present invention is described in further detail:
Fig. 1 is the structure chart of fluidized-bed reactor of the present invention
Fig. 2 is two kinds of structure charts of dust settler among the present invention
Fig. 3 is the structure chart of anti-backflow distributor among the present invention
The specific embodiment
As shown in Figure 1; A kind of fluidized-bed reactor that is used for gasoline desulfur; It comprises segregation section 4, expansion segment 3, conversion zone 1 from top to bottom successively; In said conversion zone 1, beds 2 is housed, on said conversion zone 1 top to being circumscribed with receiver 14, in said conversion zone 1 bottom to being circumscribed with reductor 13.Wherein, beds 2 relies on uprising gas to hold, and it highly is that catalyst inventory by gas flow rate and bed determines jointly.Under the stable situation of gas flow rate, can increase or reduce reserve through adding or drawing off catalyst, thus the height of adjusting beds 2.
Be provided with automatic backwashing filter 5 at the top of said segregation section 4, said automatic backwashing filter 5 is provided with reactor outlet flange 22 pairings at said segregation section 4 tops; Said automatic backwashing filter 5 tops are provided with gas vent 10, and the bottom is provided with filter core 23, and said filter core 23 stretches into the inside of said segregation section 4.In the course of the work, whenever can carry out automatic backwash one time usually, the filterability of filter core is restored at a distance from 10 to 100 minutes automatic backwashing filters 5.
In said expansion segment 3 and segregation section 4, be provided with dust settler 9, be used to reduce the upwards dustiness of flowing gas, reduce the filtration load of automatic backwashing filter 5.Specifically, the structure of dust settler 9 is as shown in Figure 2, and said dust settler 9 adopts blocking type dust settler 20 or spiral-flow type dust settler 21; Said blocking type dust settler 20 adopts conical structure, and the hypotenuse of its conical structure and horizontal angle must be greater than the angles of repose of catalyst.The catalyst granules that blocking type dust settler 20 carries when upwards flowing with gas bumps, and reduces the catalyst granules flow velocity even changes its direction of motion, stops catalyst granules to continue upwards to flow to reach the purpose that reduces the gas dustiness.Said spiral-flow type dust settler 21 adopts the twisted blade structure; Lobe numbers is 3 to 8; The twisted blade structure can guide the gas and the catalyst granules that upwards flow to produce the momentum that rotates in a circumferential direction; And then generation centrifugal force, utilize catalyst granules catalyst granules to be thrown to the purpose that reactor limit wall realizes reducing the gas dustiness much larger than the centrifugal force of gas.
Be provided with anti-backflow distributor 8 in the bottom of said conversion zone 1, be used to prevent that catalyst granules from flowing backwards to the below of said anti-backflow distributor 8.Specifically, its structure is as shown in Figure 3, and said anti-backflow distributor 8 comprises distribution grid 19, one group of bubble cap 15 and group switching centre pipe 16; Evenly have one group of hole on the said distribution grid 19, a said central tube 16 is installed in each perforate; Each said central tube 16 upper end communicates with a bubble cap 15, and each said central tube 16 lower end has opening 18; Tooth-shape structure 17 is adopted in the lower surface of said bubble cap 15.In the course of work, gas gets into central tube 16 through opening 18, and the tooth type structures 17 from bubble cap 15 lower surfaces gets in the conversion zone 1 then.Arrangement pitches through control bubble cap 15 guarantees that gas flows out the flow velocity of tooth-shape structure 17, thereby guarantees that gas is evenly distributed on the whole reactor cross section.Size through control opening, central tube, bubble cap; Particularly the internal diameter of central tube 16 guarantees that the gas flow rate in central tube surpasses 5m/s under the various operating modes; Thereby avoid catalyst granules to flow backwards, and guarantee that gas is evenly distributed on the whole reactor cross section to the distributor below.Like this, go out the size of central tube 16 through the big or small inverse of gas flow rate.
Said receiver 14 is connected with said conversion zone 1 through regenerative agent transverse tube 12, and the inlet of said regenerative agent transverse tube 12 is arranged on the position that is lower than beds 2 upper surfaces.The active catalyst that reduces gets into receiver 14 from regenerative agent transverse tube 12, finally removes regenerative system from receiver 14 bottoms.
Said reductor 13 is connected with said conversion zone 1 through reducing agent inclined tube 11, and said reducing agent inclined tube 11 oblique cuttings are gone in the said conversion zone 1, and said reducing agent inclined tube 11 outlets are positioned at the top of said anti-backflow distributor 8.Catalyst gets into reactor lower part from reducing agent 13 through reducing agent inclined tube 11.
Be provided with gas access 6 in the bottom of said conversion zone 1; In said conversion zone 1, the below of the top of gas access 6, anti-backflow distributor 8 is provided with erosion control distributor 7.Said erosion control distributor 7 adopts circular shield structure, and the diameter of circular shield is 1.3-1.9 a times of gas access 6 diameters.
In order to satisfy the requirement of low speed fluidisation, the gas flow rate in the said conversion zone 1 is controlled in the scope of 0.2-0.6m/s.
Technique scheme is one embodiment of the present invention; For those skilled in the art; On the basis that the invention discloses application process and principle, be easy to make various types of improvement or distortion, and be not limited only to the described method of the above-mentioned specific embodiment of the present invention; Therefore the mode of front description is preferably, and does not have restrictive meaning.
Claims (6)
1. fluidized-bed reactor that is used for gasoline desulfur, it comprises segregation section (4), expansion segment (3), conversion zone (1) from top to bottom successively, and beds (2) is housed in said conversion zone (1), it is characterized in that:
In said expansion segment (3) and segregation section (4), be provided with dust settler (9), be used to reduce the gas dustiness;
Said dust settler (9) adopts blocking type dust settler (20) or spiral-flow type dust settler (21); Said blocking type dust settler (20) adopts conical structure, and the hypotenuse of its conical structure and horizontal angle must be greater than the angles of repose of catalyst; Said spiral-flow type dust settler (21) adopts the twisted blade structure, and lobe numbers is 3 to 8;
Gas flow rate in the said conversion zone (1) is 0.2-0.6m/s;
Be provided with automatic backwashing filter (5) at the top of said segregation section (4), said automatic backwashing filter (5) is provided with reactor outlet flange (22) pairing at said segregation section (4) top; Said automatic backwashing filter (5) top is provided with gas vent (10), and the bottom is provided with filter core (23), and said filter core (23) stretches into the inside of said segregation section (4).
2. the fluidized-bed reactor that is used for gasoline desulfur as claimed in claim 1 is characterized in that:
Be provided with anti-backflow distributor (8) in the bottom of said conversion zone (1), be used to prevent that catalyst granules from flowing backwards to the below of said anti-backflow distributor (8); Said anti-backflow distributor (8) comprises distribution grid (19), one group of bubble cap (15) and a group switching centre pipe (16); Evenly have one group of hole on the said distribution grid (19), a said central tube (16) is installed in each perforate; Each said central tube (16) upper end communicates with a bubble cap (15), and each said central tube (16) lower end has opening (18); Tooth-shape structure (17) is adopted in the lower surface of said bubble cap (15).
3. the fluidized-bed reactor that is used for gasoline desulfur according to claim 1 and 2 is characterized in that:
Be provided with gas access (6) in the bottom of said conversion zone (1), the top of gas access (6) is provided with erosion control distributor (7) in said conversion zone (1); Said erosion control distributor (7) adopts circular shield structure, and the diameter of circular shield is 1.3-1.9 a times of said gas access (6) diameter.
4. the fluidized-bed reactor that is used for gasoline desulfur according to claim 1 and 2 is characterized in that:
On said conversion zone (1) top to being circumscribed with receiver (14); Said receiver (14) is connected with said conversion zone (1) through regenerative agent transverse tube (12), and the inlet of said regenerative agent transverse tube (12) is arranged on the position that is lower than beds (2) upper surface.
5. the fluidized-bed reactor that is used for gasoline desulfur according to claim 1 and 2 is characterized in that:
In said conversion zone (1) bottom to being circumscribed with reductor (13); Said reductor (13) is connected with said conversion zone (1) through reducing agent inclined tube (11), and said reducing agent inclined tube (11) oblique cutting is gone in the said conversion zone (1), and the outlet of reducing agent inclined tube (11) is positioned at anti-backflow distributor (8) top.
6. the fluidized-bed reactor that is used for gasoline desulfur according to claim 3 is characterized in that:
On said conversion zone (1) top to being circumscribed with receiver (14); Said receiver (14) is connected with said conversion zone (1) through regenerative agent transverse tube (12), and the inlet of said regenerative agent transverse tube (12) is arranged on the position that is lower than beds (2) upper surface;
In said conversion zone (1) bottom to being circumscribed with reductor (13); Said reductor (13) is connected with said conversion zone (1) through reducing agent inclined tube (11), and said reducing agent inclined tube (11) oblique cutting is gone in the said conversion zone (1), and the outlet of reducing agent inclined tube (11) is positioned at anti-backflow distributor (8) top.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910076756A CN101780389B (en) | 2009-01-19 | 2009-01-19 | Fluid bed reactor used for gasoline desulfuration |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910076756A CN101780389B (en) | 2009-01-19 | 2009-01-19 | Fluid bed reactor used for gasoline desulfuration |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101780389A CN101780389A (en) | 2010-07-21 |
| CN101780389B true CN101780389B (en) | 2012-08-29 |
Family
ID=42520604
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200910076756A Active CN101780389B (en) | 2009-01-19 | 2009-01-19 | Fluid bed reactor used for gasoline desulfuration |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101780389B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105861053B (en) * | 2015-01-22 | 2018-05-11 | 中国石化工程建设有限公司 | A kind of method for suppressing gasoline desulfurization reactor filter coking |
| KR102404282B1 (en) * | 2019-09-24 | 2022-05-30 | 주식회사 엘지화학 | Fluidized bed reactor |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2116209U (en) * | 1992-04-04 | 1992-09-16 | 曹洁秀 | Blockage proof blowing pressure sampler |
| CN2216860Y (en) * | 1994-12-19 | 1996-01-10 | 中国科学院成都有机化学所 | Fluidised reaction equipment |
| CN2402386Y (en) * | 1999-12-10 | 2000-10-25 | 金成洙 | Smoke-discharging dust-eliminating device |
| CN1621741A (en) * | 2003-05-29 | 2005-06-01 | 巴布考克及威尔考克斯公司 | Bubble cap assembly |
-
2009
- 2009-01-19 CN CN200910076756A patent/CN101780389B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2116209U (en) * | 1992-04-04 | 1992-09-16 | 曹洁秀 | Blockage proof blowing pressure sampler |
| CN2216860Y (en) * | 1994-12-19 | 1996-01-10 | 中国科学院成都有机化学所 | Fluidised reaction equipment |
| CN2402386Y (en) * | 1999-12-10 | 2000-10-25 | 金成洙 | Smoke-discharging dust-eliminating device |
| CN1621741A (en) * | 2003-05-29 | 2005-06-01 | 巴布考克及威尔考克斯公司 | Bubble cap assembly |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101780389A (en) | 2010-07-21 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10758921B2 (en) | Separation device | |
| CN100464830C (en) | Combined catalyst stripper | |
| CN201454508U (en) | Fluidized bed reactor with dust-settling device | |
| CN204564077U (en) | Gas feed distributor and three phase slurry bed bioreactor | |
| CN204058374U (en) | Fluid prearranged assignment device and fluid prearranged assignment dish | |
| CN105349187A (en) | Pressurized pulverized coal gasified synthetic gas dedusting apparatus and dedusting method thereof | |
| CA2951572A1 (en) | Media bed filters for filtering fine particles from a raw liquid flow and method of using the same | |
| CN201632251U (en) | Fluid bed reactor with automatic back flush filter | |
| CN101780389B (en) | Fluid bed reactor used for gasoline desulfuration | |
| CN204051631U (en) | A kind of fluid distributor and fluid predistribution dish | |
| JP4599335B2 (en) | Upflow type manganese contact tower | |
| CN208244386U (en) | Separator | |
| CN201664606U (en) | Fluidized bed reactor with anti-backflow distributor | |
| CN100364652C (en) | A fouling dispenser | |
| CN111874973A (en) | Spray foam desulfurization dust remover | |
| CN204746286U (en) | Thick liquid attitude bed reactor's ft synthesis result piece -rate system | |
| CN100371061C (en) | A delay accumulator | |
| CN211111879U (en) | Cyclone jet type scale deposit device | |
| CN215427479U (en) | Timing solid-liquid separator | |
| CN213037569U (en) | Cyclone air-float clarification tank | |
| CN212998852U (en) | Device for pre-removing coarse particle ash in front of SCR (Selective catalytic reduction) denitration device | |
| CN210544005U (en) | Tail gas washing tower integrating three-level washing of anhydrous calcium chloride | |
| CN108114510B (en) | Gas-liquid-solid three-phase separator and fluidized bed reactor comprising same | |
| CN201505526U (en) | Gas-liquid-solid three-phase separator | |
| CN113181689A (en) | Timing solid-liquid separator |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C53 | Correction of patent for invention or patent application | ||
| CB02 | Change of applicant information |
Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant after: Sinopec Corp. Co-applicant after: Sinopec Engineering Incorporation Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant before: Sinopec Corp. Co-applicant before: Engrg Construction Co., SINOPEC |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |