CN105779022B - Cyclone separator and gas-liquid solid separation system - Google Patents
Cyclone separator and gas-liquid solid separation system Download PDFInfo
- Publication number
- CN105779022B CN105779022B CN201610136938.5A CN201610136938A CN105779022B CN 105779022 B CN105779022 B CN 105779022B CN 201610136938 A CN201610136938 A CN 201610136938A CN 105779022 B CN105779022 B CN 105779022B
- Authority
- CN
- China
- Prior art keywords
- gas
- shell
- riser
- cyclone separator
- cyclone
- 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
- 239000007787 solid Substances 0.000 title claims abstract description 63
- 239000007788 liquid Substances 0.000 title claims abstract description 62
- 238000000926 separation method Methods 0.000 title claims abstract description 59
- 239000000203 mixture Substances 0.000 claims abstract description 46
- 239000002893 slag Substances 0.000 claims description 39
- 238000005201 scrubbing Methods 0.000 claims description 25
- 230000003068 static effect Effects 0.000 claims description 21
- 239000000498 cooling water Substances 0.000 claims description 13
- 230000000694 effects Effects 0.000 abstract description 12
- 239000007789 gas Substances 0.000 description 87
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 41
- 238000005406 washing Methods 0.000 description 16
- 239000003795 chemical substances by application Substances 0.000 description 13
- 238000002309 gasification Methods 0.000 description 13
- 238000004458 analytical method Methods 0.000 description 12
- 239000003245 coal Substances 0.000 description 11
- 238000000034 method Methods 0.000 description 11
- 239000003034 coal gas Substances 0.000 description 10
- 238000002156 mixing Methods 0.000 description 10
- 239000006196 drop Substances 0.000 description 9
- 239000007921 spray Substances 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 239000002956 ash Substances 0.000 description 8
- 239000000428 dust Substances 0.000 description 8
- 238000010586 diagram Methods 0.000 description 7
- 239000007791 liquid phase Substances 0.000 description 7
- 238000005192 partition Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 238000005070 sampling Methods 0.000 description 6
- 230000009471 action Effects 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 238000000746 purification Methods 0.000 description 5
- 230000002000 scavenging effect Effects 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 230000003020 moisturizing effect Effects 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- 239000008247 solid mixture Substances 0.000 description 4
- 239000000470 constituent Substances 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 239000010797 grey water Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000010866 blackwater Substances 0.000 description 2
- 239000010882 bottom ash Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000035939 shock Effects 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003250 coal slurry Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 210000003205 muscle Anatomy 0.000 description 1
- 239000000618 nitrogen fertilizer Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000006798 recombination Effects 0.000 description 1
- 238000005215 recombination Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/026—Dust removal by centrifugal forces
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/02—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising gravity
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/40—Combinations of devices covered by groups B01D45/00 and B01D47/00
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Cyclones (AREA)
Abstract
The present invention provides a kind of cyclone separator and gas-liquid solid separation systems, wherein cyclone separator includes：There is gas vent (102), the lower part of first shell (101) there is solidliquid mixture to export (103) on the top of first shell (101), first shell (101)；Feeding inlet structure (104) is arranged on the top of first shell (101)；Riser (106), setting is in first shell (101), the inside of riser (106) is connected to gas vent (102), disengagement chamber is formed between riser (106) and first shell (101), and there is flow structure (107) in the circumferential side wall of riser (106).Technical scheme of the present invention can efficiently solve the bad problem of raw gas purifying effect in the prior art.
Description
Technical field
The present invention relates to gas-liquid-solid separation technology fields, are detached in particular to a kind of cyclone separator and gas-liquid-solid
System.
Background technology
Currently, coal water slurry gasification is the important link of coal producing light olefins industry, Nitrogenous Fertilizer Industry and coal liquifaction industry etc..Water
The raw gas that coal slurry gasification generates is typically passed through chilling process primary wash, cooling and gas-liquid-solid separation.It is light after separation
Component raw gas is sent to follow-up workshop section.Since coal water slurry gasification usually carries out in gasification furnace combustion chamber, raw gas can carry winged
Ash, slag are directly entered shock chamber, this results in the indoor water quality of Quench poor, and the impurity such as a large amount of flying dusts are carried secretly with raw gas
Moisture enter in scrubbing tower through venturi, and then affect the water quality in scrubbing tower and scrubbing tower top exit purified gas
Cleannes.Meanwhile inevitably can also there are some impurity, the liquid phase part in the relatively clean liquid phase part of wash tower bottoms
It is sent to chilling ring of gasifying furnace after Quench water pump pressure-raising, filter filtering, the raw gas that gasification furnace combustion chamber is come is carried out preliminary
Washing, cooling.Therefore, in the water cycle process of gasification, since raw gas purifying is not thorough, it often will appear chilled water filtering
The phenomenon that device blocks, chilling ring fouling is serious, system resistance drop rapid increase, is unable to stability contorting, even so as to cause production
Destroy the balance of grey water treatment system.
In addition, raw gas made from coal water slurry gasification generally goes through shock chamber, syngas outlet spray, Venturi scrubbing
Fed downstream process after device, scrubbing tower water-bath and demister Pyatyi cleaning dust.Coal Gasification water consumption is larger, and gasify water system
It is usually maintained in higher internal circulating load.However, although raw gas have passed through multistage washing, purifying, coal gas band water band ash can not be kept away
Exempt from, this results in needing to be continuously replenished outside battery limit (BL) fresh water to maintain the balance of water system, therefore, improves system water quality to closing weight
It wants.
There is a kind of gas washing purification technique in the prior art.The main implementation steps of the technique are as follows：Washings follow
Ring pump send a part of Heisui River pressurization come from scrubbing tower Heisui River storage tank to Venturi scrubber, is mixed with from out-of-bounds raw gas
It closes, enters after the solid particles such as the lime-ash carried secretly in raw gas are moistened, bonded and increased by Heisui River in venturi and detach
Device carries out level-one washing.Raw gas down-comer in separator flows downward, and most of lime-ash enters in separator bottom liquid phase,
The Heisui River of generation is discharged into black water treatment system.Raw gas is ascended into along down-comer and gas-guide tube annular space in scrubbing tower water-bath.Slightly
Coal gas is flowed up by water-bath, with from washing water-circulating pump another part Heisui River and external technique moisturizing in scrubbing tower
It is inversely contacted on the tower tray of top.Coal gas after two level washing is sent into subsequent conversion by the baffle plate demister on tower tray top
Process, the Heisui River that scrubbing tower generates are discharged into black water treatment system.However, the technique, in implementation process, initial stage of coming into operation is because of water quality
Good, solid content is few, and Venturi scrubber has preferable spray atomizing and washing effect to raw gas.With the long-time of production
It runs, the solid content in wash tower bottoms Heisui River certainly will will increase, and pass it through pump pressurization and send to venturi and will result in blockage
Venturi spray apertures cause the pressure drop increase of gasification system and energy consumption to increase.In addition, the increase of wash tower bottoms Heisui River solid content is also
It can cause inversely to contact the decline of cleaning dust significant effect at the top of scrubbing tower with coal gas, be unfavorable for the purification of coal gas, longtime running
Raw gas is extremely difficult to expected clean-up effect.
In addition, there is also one kind in the prior art passes through main washing, water-bath, secondary washing, rotation in dust-laden raw gas occasion
The vertical separator of flow separation combination unit.The above-mentioned vertical separator course of work is：Raw gas enters from gas feed, passes through
Entrance inside extending tube in gas feed is mixed with the washings entered from main wash mill, by being washed in central tube
Enter gas cylinder after dedusting, comes into full contact with carry out water-bath washing after then eliminating big bubble by bulb-breaking device with washings.Water
Raw gas after bath carries out secondary washing, carries out gas-liquid separation by cyclone separator, the raw gas after dedusting is by gas vent
Rough coal gas separating device is excluded, dust-laden washings are exported by device bottom through collection cone balling-up and are discharged.But the technique is in reality
During applying, because setting washings are more, the higher flow velocity of coal gas, can cause raw gas to carry part dust particale and produce coal in addition
Gas outlet, and the pressure drop of separator can be caused to increase, energy consumption increases, and is unfavorable for maintaining the even running of production.
Invention content
The main purpose of the present invention is to provide a kind of cyclone separator and gas-liquid solid separation systems, to solve the prior art
In the bad problem of raw gas purifying effect.
To achieve the goals above, according to an aspect of the invention, there is provided a kind of cyclone separator, including：First
There is gas vent, the lower part of first shell to be exported with solidliquid mixture on the top of shell, first shell；Feeding inlet structure,
It is arranged on the top of first shell；Riser is arranged in first shell, and the inside of riser is connected to gas vent, rises gas
Disengagement chamber is formed between pipe and first shell, there is flow structure in the circumferential side wall of riser.
Further, it includes the gap that multiple axial directions along riser extend to cross flow structure.
Further, cyclone separator further includes cooling water tube bank, and the peripheral side in first shell is arranged in cooling water tube bank
On wall.
Further, multiple gaps are arranged along the circumferential direction interval of riser.
Further, it is shifted to install between every two adjacent gaps.
Further, it is multiple to cross flow structure, and multiple flow structures of crossing are arranged along the axial direction interval of riser.
Further, it is crossed in flow structure multiple, the density for crossing multiple gaps in flow structure close to riser end
Less than the density for crossing multiple gaps in flow structure in the middle part of riser.
Further, feeding inlet structure is two be symmetricly set in first shell circumferential side wall, each feed inlet knot
Structure includes arc feeding-passage.
Further, each feeding inlet structure further includes the first charging aperture being arranged in arc feeding-passage end, two
The place plane of first charging aperture is arranged in parallel.
Further, feeding inlet structure is that charging is covered, and the circumferential side wall of the inner wall of end and first shell that feed cover is tangent.
Further, cyclone separator further includes the steady whirlpool device being arranged in first shell, steady whirlpool device be located at riser and
Between solidliquid mixture outlet, steady whirlpool device includes plate body and is arranged in plate body towards the conical structure on riser side, round
Wimble structure includes first conical structure and multiple second conical structures for being arranged around the first conical structure.
Further, cyclone separator further includes the Gas-Rotation-Plate Dust Separator being arranged in first shell, Gas-Rotation-Plate Dust Separator
Positioned at the close solidliquid mixture exit end of riser.
Further, cyclone separator further includes the level-one atomizing sprayer being located above Gas-Rotation-Plate Dust Separator.
According to another aspect of the present invention, a kind of gas-liquid solid separation system, including Venturi scrubber, scrubbing tower are provided
And primary cyclone, Venturi scrubber are connected to scrubbing tower, primary cyclone is above-mentioned cyclone separator,
The gas vent of primary cyclone is connected to by the first pipeline with Venturi scrubber.
Further, gas-liquid solid separation system further includes secondary cyclone, and secondary cyclone includes second shell
There is second charging aperture and liquid outlet, the lower part of second shell to have solid outlet, the second charging on the top of body, second shell
By the second pipeline and solidliquid mixture outlet, liquid outlet is connected to by third pipeline with the tower tray of scrubbing tower mouth.
Further, gas-liquid solid separation system further includes the static mixer being arranged on the second pipeline.
Further, gas-liquid solid separation system further includes lock hopper collection slag system, lock hopper collection slag system by the 4th pipeline with
Solid outlet is connected to.
It applies the technical scheme of the present invention, flow structure was added in the circumferential side wall of riser.It is mixed when to gas-liquid-solid
When object (such as raw gas) is purified, above-mentioned gas-liquid-solid mixture first passes through feeding inlet structure and enters in first shell, and
It is moved downward along riser outside.During the motion, the part light-component gas in gas-liquid-solid mixture can be by upper
It stated flow structure to enter directly into riser, and gas vent is risen to along riser, after being flowed to by gas vent
Continuous equipment.Remaining gas-liquid-solid mixture continues on riser and moves downward, and gas and solid-liquid are carried out in disengagement chamber
The separation of mixture.The light-component gas separated enters from the lower port of riser and rises to gas vent, heavy constituent
Solidliquid mixture sinks down into solidliquid mixture outlet, and by solidliquid mixture outlet stream to follow-up equipment.It is above-mentioned to cross flow structure
The part light-component gas in gas-liquid-solid mixture can be made to enter directly into riser, reduce pressure inside cyclone separator
Drop, to improve gas-liquid-solid separative efficiency, clean-up effect is more preferable.
Description of the drawings
The accompanying drawings which form a part of this application are used to provide further understanding of the present invention, and of the invention shows
Meaning property embodiment and its explanation are not constituted improper limitations of the present invention for explaining the present invention.In the accompanying drawings：
Fig. 1 shows the structural schematic diagram of the embodiment of cyclone separator according to the present invention；
Fig. 2 shows the schematic top plan views of the feeding inlet structure of the cyclone separator of Fig. 1；
Fig. 3 shows the A-A of Fig. 1 to schematic cross-sectional view；
Fig. 4 shows the interior flow field schematic diagram of the cyclone separator of Fig. 1 in the operating condition；
Fig. 5 shows the schematic top plan view of the Gas-Rotation-Plate Dust Separator of the cyclone separator of Fig. 1；
Fig. 6 shows the schematic top plan view of the two level atomizing sprayer of the cyclone separator of Fig. 1；
Fig. 7 shows the interior flow field schematic diagram of the two level atomizing sprayer of Fig. 6 in the operating condition；
Fig. 8 shows the structural schematic diagram of the cone nozzle of the two level atomizing sprayer of Fig. 6；
Fig. 9 shows the structural schematic diagram of the embodiment of gas-liquid solid separation system according to the present invention；
Figure 10 shows the structural schematic diagram of the static mixer of the gas-liquid solid separation system of Fig. 9；
Figure 11 shows the schematic side view of the static mixer of Figure 10；
Figure 12 shows the interior flow field schematic diagram of the static mixer of Figure 10 in the operating condition.
Wherein, above-mentioned attached drawing includes the following drawings label：
101, first shell；102, gas vent；103, solidliquid mixture exports；104, feeding inlet structure；1041, arc
Feeding-passage；1042, first charging aperture；105, cooling water is restrained；106, riser；107, flow structure is crossed；1071, gap；
108, steady whirlpool device；1081, plate body；1082, the first conical structure；1083, the second conical structure；109, Gas-Rotation-Plate Dust Separator；
1091, partition board；1092, circular solids plate；110, level-one atomizing sprayer；120, two level atomizing sprayer；1201, annular
Spray tube；1201a, condensate inlet；1202, cone nozzle；130, solidliquid mixture sampling analysis point；200, venturi is washed
Wash device；300, scrubbing tower；301, tower tray；100, primary cyclone；400, secondary cyclone；401, second shell；
402, second charging aperture；403, liquid outlet；404, solid outlet；405, drain pipe；406, solid-liquor separation baffle；407, it assists
Receive slag pipeline；408, scavenging solution sampling analysis point；500, static mixer；501, static mixing entrance；502, static mixing goes out
Mouthful；503, water treatment agent entrance；600, lock hopper collection slag system；601, lock hopper collection slag ladle；602, lock hopper collection slag ladle entrance；603, it locks
Bucket collection slag ladle slag-drip opening；604, lock hopper collection slag rinses water pot；605, low pressure buck series manifold；606, auxiliary receives pulp pump；607、
High pressure grey water inlet series manifold；700, flash system.
Specific implementation mode
It should be noted that in the absence of conflict, the features in the embodiments and the embodiments of the present application can phase
Mutually combination.The present invention will be described in detail below with reference to the accompanying drawings and embodiments.
As shown in Figure 1, the cyclone separator of the present embodiment is used to purify the raw gas of coal water slurry gasification generation.The whirlwind point
Include first shell 101, feeding inlet structure 104 and riser 106 from device.Wherein, the top of first shell 101 has gas
There is solidliquid mixture to export 103 for the bottom of outlet 102, first shell 101.Feeding inlet structure 104 is arranged in first shell 101
Top.The setting of riser 106 is in first shell 101 and coaxial with first shell 101.The inside of riser 106 and gas
102 connection of outlet, disengagement chamber is formed between riser 106 and first shell 101.Had in the circumferential side wall of riser 106
Flow structure 107.
Using the cyclone separator of the present embodiment, flow structure 107 was added in the circumferential side wall of riser 106.When right
When raw gas is purified, above-mentioned raw gas first passes through feeding inlet structure 104 and enters in first shell 101, and along a liter gas
Pipe 106 moves downward.During the motion, the part light-component gas in raw gas can cross flow structure 107 directly by above-mentioned
It connects and enters in riser 106, and gas vent 102 is risen to along riser 106, after being flowed to by gas vent 102
Continuous equipment.Remaining raw gas continues on riser 106 and moves downward, and gas and solid-liquid mixing are carried out in disengagement chamber
The separation of object.The light-component gas separated enters from the lower port of riser 106 and rises to gas vent 102, recombination
Divide solidliquid mixture to sink down into solidliquid mixture outlet 103, and follow-up equipment is flowed to by solidliquid mixture outlet 103.It is above-mentioned
Crossing flow structure 107 can be such that the part light-component gas in raw gas enters directly into riser 106, reduce cyclonic separation
Device internal pressure drops, to improve gas-liquid-solid separative efficiency, clean-up effect is more preferable.
As depicted in figs. 1 and 2, in the cyclone separator of the present embodiment, feeding inlet structure 104 is to be symmetricly set on first
Two of the middle and upper part of 101 circumferential side wall of shell, each feeding inlet structure 104 include arc feeding-passage 1041.In this implementation
In example, feeding inlet structure 104 is that charging is covered, and inner wall of end and the circumferential side wall of first shell 101 for feeding cover are tangent.Each into
Material mouth structure 104 further includes the first charging aperture 1042 being arranged in 1041 end of arc feeding-passage, and first charging aperture
1042 is rectangular.The place plane of two first charging apertures 1042 is arranged in parallel, i.e., the first charging aperture 1042 of two rectangles
It is symmetrically disposed in 101 circumferential side wall of first shell in 180 degree angle.Above structure can improve the rough coal of cyclone separator
The treating capacity of gas, and the symmetry of feed inlet air-flow can be improved, to improve the gas-liquid-solid separative efficiency of cyclone separator.
As depicted in figs. 1 and 2, in the cyclone separator of the present embodiment, riser 106 is cylinder.Cross flow structure 107
To be multiple, multiple flow structures 107 of crossing are arranged along the axial direction interval of riser 106.Each flow structure 107 of crossing includes multiple edges
The gap 1071 that the axial direction of riser 106 extends.Multiple gaps 1071 are arranged along the circumferential direction interval of riser 106.
The narrow and long rectangular fine crack that above-mentioned multiple gaps 1071 are vertically arranged.It is shifted to install between per two adjacent gaps 1071.
Multiple to cross in flow structure 107, the density close to the multiple gaps 1071 of 106 end of riser crossed in flow structure 107 is less than position
The density for crossing multiple gaps 1071 in flow structure 107 in 106 middle part of riser.I.e. on riser 106, multiple overcurrent knots
The distribution trend of " close lower thin in above dredging " is presented in the distribution density in gap 1071 in structure 107, and crosses flow structure 107 and go out with gas
Certain distance is all had between mouth 102, solidliquid mixture outlet 103.Above structure can ensure that it is suitable that flow structure 107 has
While suitable air inflow, the material stress of riser 106 is not interfered with, keeps 106 intensity of riser reliable.As shown in figure 4, thick
Coal gas forms axisymmetric flow field action plane by crossing flow structure 107 in riser 106, and conplane raw gas enters
Air-flow in axial direction is formed after riser 106.It should be noted that gap 1071 is not limited to narrow and long rectangular fine crack, scheming
In in unshowned other embodiment, gap 1071 can be set to other seam shapes, such as ellipse as needed.
As shown in Figure 1 and Figure 5, in the cyclone separator of the present embodiment, cyclone separator further includes being arranged in first shell
Gas-Rotation-Plate Dust Separator 109 in body 101 and level-one atomizing sprayer 110.Wherein, Gas-Rotation-Plate Dust Separator 109 is located at riser
106 close solidliquid mixture exports 103 one end.Level-one atomizing sprayer 110 is located at 109 top of Gas-Rotation-Plate Dust Separator, and
And retain between level-one atomizing sprayer 110 and Gas-Rotation-Plate Dust Separator 109 with certain distance.Above-mentioned Gas-Rotation-Plate Dust Separator
Several partition boards 1091 are disposed on 109, each partition board 1091 is intersected in the shape of a spiral on central circular solid slab 1092, each partition board
Angle between 1091 is in 15 to 30 degree.Partition board 1091 can be arranged as required into 6,8,12,16 etc., and every
1091 place plane of a partition board is horizontal by 5 to 15 degree angles.Level-one atomizing sprayer 110 is located at Gas-Rotation-Plate Dust Separator
Right over 109 at 0.5 to 1.5 meter, the top of level-one atomizing sprayer 110 can be nozzle structure, can set as needed
Single nozzle, double nozzles or the more nozzles of annular are set to, can also be low-resistance descending liquid body structure of distributor.Above structure is in disengagement chamber
The light-component gas of middle separation carries out further dedusting.
As shown in figures 1 and 3, in the cyclone separator of the present embodiment, cyclone separator further includes being arranged in first shell
Steady whirlpool device 108 in body 101.Steady whirlpool device 108 is located between riser 106 and solidliquid mixture outlet 103.Steady whirlpool device 108 with
There is certain distance between solidliquid mixture outlet 103.Steady whirlpool device 108 includes plate body 1081 and is arranged in 1081 direction of plate body
Conical structure on 106 side of riser.Conical structure is including first conical structure 1082 and surrounds the first circular cone knot
Multiple second conical structures 1083 that structure 1082 is arranged.Above structure can be further reduced whirlpool, and steady whirlpool effect is more preferable.Work as place
When science and engineering skill tolerance is larger, air velocity is very fast, it is miscellaneous that above structure can carry solidliquid mixture etc. to avoid purified gas
Matter enters follow-up system.
As shown in figures 1 and 3, in the cyclone separator of the present embodiment, cyclone separator further includes cooling water tube bank
105.First shell 101 includes straight tube degree and conical section.Cooling water tube bank 105 is uniformly arranged on the circumferential side wall of straight tube degree
On.Flow of cooling water direction in cooling water tube bank 105 is in the axial direction with raw gas flow direction in adverse current, above-mentioned cooling
Water enters from the bottom of straight tube degree, is flowed out from the top of straight tube degree heteropleural.Above-mentioned cooling water is inversely changed with raw gas flow direction
Heat, be convenient for solidliquid mixture refrigerated separation from gas, the solidliquid mixture for being conducive to isolate in follow-up system at water
Reason agent preferably acts on, while avoiding solidliquid mixture slagging, dross on 101 side wall of first shell.Above-mentioned taper section
Solidliquid mixture collecting bin is formed in the part of 108 lower section of steady whirlpool device.Solidliquid mixture outlet 103 is located at the solidliquid mixture and receives
The bottom of Ji Cang.The side wall of the solidliquid mixture collecting bin is equipped with remote liquid level transmitter LT, is exported with solidliquid mixture
103 control valve LV hangs with interlocking.Preferably, high pressure nitrogen branch pipe, the height are set between the bivalve of solidliquid mixture outlet 103
Press nitrogen branch pipe as accident treatment active redundancy pipeline.When solidliquid mixture outlet 103 blocks, the is manually or automatically opened
Two pass valve on two pipelines, and anti-top blocks substance, wherein high pressure nitrogen repeatedly upwards under the action of high pressure nitrogen branch pipe
Pressure ratio cyclone system pressure is 20 to 30 kilograms high.
Present invention also provides a kind of gas-liquid solid separation systems.The gas-liquid solid separation system of the present embodiment can be used for ash
It is gasified raw material, the rough coal with entrained flow gasification chilling process to divide the higher coal of content, petroleum coke or solid hydrocarbon
Gas purification separation.Above-mentioned gas-liquid solid separation system includes Venturi scrubber 200, scrubbing tower 300 and primary cyclone
100.Venturi scrubber 200 is connected to scrubbing tower 300.Primary cyclone 100 is above-mentioned cyclone separator.Primary rotation
The gas vent 102 of wind separator 100 is connected to by the first pipeline with Venturi scrubber 200.
As shown in Fig. 1, Fig. 6 to Fig. 9, in the gas-liquid solid separation system of the present embodiment, gas-liquid solid separation system further includes
Two level atomizing sprayer 120.Above-mentioned two level atomizing sprayer 120 is arranged on the first pipeline, and is located at gas vent 102
Top.The two level atomizing sprayer 120 is annular spray equipment, is sprayed with circular spray tube 1201 and with annular
Four cone nozzles 1202 in 90 degree of angles that pipe 1201 is connected to, arbitrary two of the vertex of a cone part of cone nozzle 1202 are right
Busbar between angle be referred to as 90 degree, naturally it is also possible to for 45 degree, 60 degree of angles differ.Cone nozzle 1202 is inserted into the first pipe
A distance in road, is not close to tube wall.Condensate liquid enters circular spray tube 1201 from condensate inlet 1201a, wherein condensing
Liquid entrance 1201a can be single, two or four etc..Condensate liquid forms flow field from four ejections of cone nozzle 1202.On
Moistening gas can be fully atomized by stating structure, purified and removed when entering follow-up system (such as Venturi scrubber) convenient for purified gas
Dirt.
As shown in figure 9, in the gas-liquid solid separation system of the present embodiment, gas-liquid solid separation system further includes secondary cyclone point
From device 400.Secondary cyclone 400 includes second shell 401.The top of second shell 401 has 402 He of second charging aperture
Liquid outlet 403.Drain pipe 405 is provided in second shell 401, the top of drain pipe 405 is connected to liquid outlet 403.The
The lower part of two shells 401 has solid outlet 404.Second charging aperture 402 is connected by the second pipeline and solidliquid mixture outlet 103
It is logical.Liquid outlet 403 is connected to by third pipeline with the tower tray 301 of scrubbing tower 300.Gas-liquid solid separation system further includes static mixed
Clutch 500 and lock hopper collection slag system 600.Wherein, static mixer 500 is arranged on the second pipeline.Lock hopper collection slag system 600 is logical
The 4th pipeline is crossed to be connected to solid outlet 404.
Raw gas is detached by the primary purifying of primary cyclone 100, and light-component gas is from 102 scripture of gas vent
Washer 200 enters scrubbing tower 300 in mound.The heavy constituent solidliquid mixture that primary is isolated through solidliquid mixture outlet 103 into
The static mixer 500 for entering and being arranged on the second pipeline.Solidliquid mixture pass through in static mixer 500 with water treatment agent
Chemical action and physical separation in secondary cyclone 400 after, most of solid phase components fall into second shell 401
Bottom ash bucket, and be discharged into lock hopper collection slag system 600 through solid outlet 404；Purified liquid phase component is through drain pipe 405
Liquid outlet 403 is risen to, if sending to making tower tray moisturizing on the dried layer tower tray 301 positioned at 300 middle and upper part of scrubbing tower.
As shown in Fig. 9 to Figure 12, in the gas-liquid solid separation system of the present embodiment, static mixer 500 is solid-liquid mixing
Object and water treatment agent are sufficiently mixed place, are forward-reverse spiral structure, with static mixing entrance 501, static mixing goes out
Mouth 502 and water treatment agent entrance 503, water treatment agent entrance 503 are located at the top of static mixing entrance 501, contribute in this way
The comprehensive immixture of flow at high speed liquid and water treatment agent.Static mixing outlet 502 and the of secondary cyclone 400
Two feed inlets 402 are connected.Water treatment agent enters in static mixer 500 from water treatment agent entrance 503 and is filled with solidliquid mixture
Mixing is divided to chemically react.
As shown in figure 9, in the gas-liquid solid separation system of the present embodiment, the second charging aperture of secondary cyclone 400
402 are arranged on the middle and upper part side wall of second shell 401.Preferably, second charging aperture 402 is arranged in second shell 401
In upper portion side wall and inlet tube slopes slightly downward 3 to 10 degree.Drain pipe 405 is cylinder, the drain pipe 405 and second shell
401 coaxial arrangements.Solid-liquor separation baffle 406 is provided at a distance of the underface of the lower port of drain pipe 405.Bottom
Ash bucket is located at the underface of above-mentioned solid-liquor separation baffle 406.The bottommost in second shell 401 is arranged in solid outlet 404.Liquid
Outlet 403 is located at the surface of drain pipe 405.Cooling water tube bank, the cooling water are again provided on secondary cyclone 400
Tube bank is arranged on the surrounding side wall of second shell 401, and such purpose is to keep the temperature of liquid phase component after purification more suitable
It is suitable for the tower tray moisturizing of tower tray 301, while avoids increasing pressure drop and energy consumption because of slagging inside secondary cyclone 400.
In addition, secondary cyclone 400, which further includes the auxiliary being arranged on the ash bucket side wall of bottom, receives slag pipeline 407.In secondary cyclone
For separator 400 under 601 connected state of lock hopper collection slag ladle, receiving slag pipeline 407 by auxiliary receipts pulp pump 606 and auxiliary can be from lock
Bucket is sent after collecting 601 top sucking buck pressurization of slag ladle to the ash bucket of bottom, loosens hopper bottom solid matter, promotion to play
Circular fluidic flow, auxiliary receive the effect of slag.
As shown in figure 9, in the gas-liquid solid separation system of the present embodiment, gas-liquid solid separation system further includes being arranged second
On pipeline and close to the solidliquid mixture sampling analysis point 130 of solidliquid mixture outlet 103, adjusted according to its Analysis Results of Water Quality
Rectification control valve FV1 process operation parameters, wherein being provided with flowmeter before flow control valve FV1.It is taken in solidliquid mixture
130 top of sample analysis site is provided with backwash pipeline, is used for the emergent management of outlet line stopping state.Gas-liquid solid separation system
Further include being arranged on third pipeline and close to the scavenging solution sampling analysis point 408 of liquid outlet 403.It is sampled according in scavenging solution
The scavenging solution analysis result of analysis site 408 adjusts the technological parameter of flow control valve FV2 and FV3, wherein in flow control valve
Flowmeter is both provided with before FV2, FV3.
As shown in figure 9, in the gas-liquid solid separation system of the present embodiment, lock hopper collection slag system 600 includes lock hopper collection slag ladle
601, it is arranged in the underface of secondary cyclone 400.Lock hopper collection slag ladle entrance 602 be arranged solid outlet 404 just under
Square, lock hopper collection slag ladle 601 surface.Lock hopper collection slag ladle slag-drip opening 603 be arranged the underface of lock hopper collection slag ladle 601 and with lock
Bucket collection slag ladle entrance 602 is coaxial.Lock hopper collection slag rinses the level that water pot 604 is positioned above 601 certain distance of lock hopper collection slag ladle
On position, which rinses on water pot 604 and is mainly provided with lock hopper collection slag ladle blowdown line and clean-up line, these pipelines
It can be shared with the respective lines of gasification furnace bottom lock hopper slag collection system.Low pressure buck series manifold 605 is arranged in lock hopper Ji Zhachong
In the upper portion side wall of wash water tank 604.Auxiliary is received pulp pump 606 and is arranged on level ground, and high pressure grey water inlet series manifold 607 is set
It sets at lock hopper collection slag ladle inlet valve KV1, KV2, high pressure buck branch pipe is coupled between KV1, KV2 and assists to receive pulp pump 606
At suction line.Slag collecting pit and pulp water storehouse are arranged in parallel in 601 lower section of lock hopper collection slag ladle, and wherein slag collecting pit is located at lock hopper collection
The underface of slag ladle slag-drip opening 603.Preferably, be provided on lock hopper collection slag ladle 601 with the second of secondary cyclone 400 into
The pressure difference transmitter PDT of comparing calculation between material mouth 402, value range are 100 to 200kPa.
As shown in figure 9, the operation principle of the gas-liquid solid separation system of the present embodiment is as follows：
Carry the raw gas of certain water content and amount of dust by the centrifugation of primary cyclone 100 and again
Power settlement action realizes the initial gross separation of drop, dust and coal gas in raw gas.Light component purified gas after separation is from a liter gas
106 top of pipe enters follow-up dust pelletizing system after 120 spray atomizing of two level atomizing sprayer.The solidliquid mixture isolated from
(can partly send to flash system 700 as needed) is discharged in 100 bottom of primary cyclone, and through being added at doses water
It is acted on into secondary cyclone 400 with water treatment agent after managing the static mixer 500 of agent, by two-stage centrifugal separation and again
After power sedimentation, from the tower tray 301 of the feeding scrubbing tower 300 of drain pipe 405, (part can be sent to sudden strain of a muscle the liquid separated as needed
Steaming system 700), the higher ingredient of solid content is discharged into slag collecting pit through lock hopper collection slag system 600.
Specifically, raw gas enters first shell 101 from two first charging apertures 1042, through primary cyclone 100
Purification separation, most of light component purified gas through multiple gaps 1071 on 106 surrounding side wall of riser enter riser
106, light-component gas in remaining raw gas is from the bottom inlet of riser 106 through steady whirlpool device 108, Gas-Rotation-Plate Dust Separator
109 and the level-one atomizing sprayer 110 above it after enter riser 106 in, the purified gas after converging is together from gas
Outlet 102 enters scrubbing tower 300 through Venturi scrubber 200.The heavy constituent solidliquid mixture that primary is isolated is mixed from solid-liquid
Object outlet 103 enters the static mixer 500 being arranged on the second pipeline through Liquid level adjusting valve LV, wherein according to solidliquid mixture
The analysis result and technological requirement of sampling analysis point 130 can partly be sent to flash system 700 through flow control valve FV1 and be dodged
Processing static mixing outlet 502 is steamed through pipeline to be connected with the second charging aperture 402 of secondary cyclone 400.Solidliquid mixture
Most of solid phase components fall into bottom ash bucket after water treatment agent chemical action and the physical separation of secondary cyclone 400,
It is discharged into lock hopper collection slag system 600 through solid outlet 404.Purified liquid phase component rises to liquid outlet 403 through drain pipe 405
If being sent through flow control valve FV3 and making tower tray moisturizing on the dried layer tower tray 301 of scrubbing tower 300, according to scavenging solution sampling analysis point 408
Analysis result and technological requirement, Partial Liquid Phase component can be sent through flow control valve FV2 to 700 flash distillation process of flash system.
It can be seen from the above description that the above embodiments of the present invention realize following technique effect：
The gas-liquid solid separation system of the present embodiment focus on solve raw gas band water band ash is serious, system pressure drop is big, high energy consumption,
The problem of water quality inferiority.In above-mentioned gas-liquid solid separation system, primary cyclone makes the droop loss for handling identical tolerance
25% to 50% is reduced, grain size of the arresting efficiency at 99% reduces nearly 3 times.After the setting of double atomization spray equipment combines
The collective effect of continuous water treatment agent and secondary cyclone, make in the liquid separated dust-laden size tunable system 5um with
Interior, dustiness can be down to 0.5mg/m in purified gas3Below.
The gas-liquid solid separation system of the present embodiment dust separation gas, reduction system pressure drop from source, after making
Continuous process no longer in by coal gas dustiness limited, high dust collection efficiency.In addition, above-mentioned gas-liquid solid separation system can also avoid swashing
The quantity that comes into operation of the filtering separation devices such as cold water filter, follow-up water-gas separator, water-gas filter, reduce equipment at
This, meanwhile, the water internal circulating load in gasification system is drastically reduced, energy conservation and consumption reduction effects are notable.
The foregoing is only a preferred embodiment of the present invention, is not intended to restrict the invention, for the skill of this field
For art personnel, the invention may be variously modified and varied.All within the spirits and principles of the present invention, any made by repair
Change, equivalent replacement, improvement etc., should all be included in the protection scope of the present invention.
Claims (16)
1. a kind of cyclone separator, which is characterized in that including：
The top of first shell (101), the first shell (101) has gas vent (102), the first shell (101)
Lower part have solidliquid mixture export (103)；
Feeding inlet structure (104) is arranged on the top of the first shell (101)；
Riser (106), setting is in the first shell (101), inside and the gas vent of the riser (106)
(102) it is connected to, disengagement chamber is formed between the riser (106) and the first shell (101),
Wherein, there is flow structure (107) in the circumferential side wall of the riser (106)；The cyclone separator further includes setting
Set the steady whirlpool device (108) in the first shell (101), the steady whirlpool device (108) is located at the riser (106) and described
Between solidliquid mixture exports (103), the steady whirlpool device (108) includes plate body (1081) and is arranged in the plate body (1081)
Conical structure towards on the riser (106) side, the conical structure include first conical structure (1082) with
And multiple second conical structures (1083) around first conical structure (1082) setting.
2. cyclone separator according to claim 1, which is characterized in that the flow structure (107) excessively includes multiple along institute
State the gap (1071) that the axial direction of riser (106) extends.
3. cyclone separator according to claim 1, which is characterized in that the cyclone separator further includes cooling water tube bank
(105), the cooling water tube bank (105) is arranged in the circumferential side wall of the first shell (101).
4. cyclone separator according to claim 2, which is characterized in that multiple gaps (1071) are along the riser
(106) circumferential direction interval setting.
5. cyclone separator according to claim 4, which is characterized in that between per two adjacent gaps (1071)
It shifts to install.
6. cyclone separator according to claim 4 or 5, which is characterized in that it is described cross flow structure (107) be it is multiple, it is more
A flow structure (107) of crossing is arranged along the axial direction interval of the riser (106).
7. cyclone separator according to claim 6, which is characterized in that it is crossed in flow structure (107) the multiple, it is close
The density for crossing multiple gaps (1071) in flow structure (107) of riser (106) end, which is less than, is located at institute
State the density for crossing multiple gaps (1071) in flow structure (107) in the middle part of riser (106).
8. cyclone separator according to claim 1, which is characterized in that the feeding inlet structure (104) is arranged symmetrically
Two in the first shell (101) circumferential side wall, each feeding inlet structure (104) includes arc feeding-passage
(1041)。
9. cyclone separator according to claim 8, which is characterized in that each the feeding inlet structure (104) further includes
First charging aperture (1042) in arc feeding-passage (1041) end is set, two first charging apertures (1042)
Place plane is arranged in parallel.
10. cyclone separator according to claim 8, which is characterized in that the feeding inlet structure (104) is that charging is covered,
The inner wall of end and the circumferential side wall of the first shell (101) of the charging cover are tangent.
11. cyclone separator according to claim 1, which is characterized in that the cyclone separator further includes being arranged in institute
The Gas-Rotation-Plate Dust Separator (109) in first shell (101) is stated, the Gas-Rotation-Plate Dust Separator (109) is located at the riser (106)
Close to the solidliquid mixture export (103) one end.
12. cyclone separator according to claim 11, which is characterized in that the cyclone separator further includes positioned at described
Level-one atomizing sprayer (110) above Gas-Rotation-Plate Dust Separator (109).
13. a kind of gas-liquid solid separation system, which is characterized in that including Venturi scrubber (200), scrubbing tower (300) and just
Grade cyclone separator (100), the Venturi scrubber (200) are connected to the scrubbing tower (300), the primary cyclone separation
Device (100) is the cyclone separator described in any one of claim 1 to 12, the primary cyclone (100) it is described
Gas vent (102) is connected to by the first pipeline with the Venturi scrubber (200).
14. gas-liquid solid separation system according to claim 13, which is characterized in that the gas-liquid solid separation system further includes
Secondary cyclone (400), the secondary cyclone (400) include second shell (401), the second shell
(401) there is second charging aperture (402) and liquid outlet (403), the lower part of the second shell (401) to have solid on top
It exports (404), the second charging aperture (402) exports (103) with the solidliquid mixture by the second pipeline and is connected to, the liquid
Body outlet (403) is connected to by third pipeline with the tower tray (301) of the scrubbing tower (300).
15. gas-liquid solid separation system according to claim 14, which is characterized in that the gas-liquid solid separation system further includes
The static mixer (500) being arranged on second pipeline.
16. gas-liquid solid separation system according to claim 14, which is characterized in that the gas-liquid solid separation system further includes
Lock hopper collection slag system (600), the lock hopper collection slag system (600) are connected to by the 4th pipeline with the solid outlet (404).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610136938.5A CN105779022B (en) | 2016-03-10 | 2016-03-10 | Cyclone separator and gas-liquid solid separation system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610136938.5A CN105779022B (en) | 2016-03-10 | 2016-03-10 | Cyclone separator and gas-liquid solid separation system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105779022A CN105779022A (en) | 2016-07-20 |
| CN105779022B true CN105779022B (en) | 2018-09-18 |
Family
ID=56388446
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610136938.5A Active CN105779022B (en) | 2016-03-10 | 2016-03-10 | Cyclone separator and gas-liquid solid separation system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105779022B (en) |
Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106398779A (en) * | 2016-10-26 | 2017-02-15 | 航天长征化学工程股份有限公司 | Synthetic gas washing, dedusting and dewatering system |
| BE1025405B1 (en) * | 2017-07-18 | 2019-02-18 | Atlas Copco Airpower Naamloze Vennootschap | FILTER ELEMENT AND LIQUID SEPARATOR WITH SUCH FILTER ELEMENT |
| CN107502692A (en) * | 2017-09-26 | 2017-12-22 | 中冶南方工程技术有限公司 | The tangential multi-pipeline cyclone dust collectors of blast furnace gas one-time dedusting |
| CN107875796B (en) * | 2017-12-15 | 2023-05-23 | 中冶焦耐(大连)工程技术有限公司 | Device and method for removing impurities of coke oven gas on coke oven gas pipeline |
| CN108168642A (en) * | 2018-01-31 | 2018-06-15 | 锦州中科制管有限公司 | A kind of aperture measurement of gas flow device and its measuring method |
| CN108706764B (en) * | 2018-05-28 | 2021-10-01 | 中国神华能源股份有限公司 | Desulfurization wastewater treatment equipment and treatment method |
| CN109628161B (en) * | 2019-02-18 | 2023-11-03 | 中国华能集团清洁能源技术研究院有限公司 | Washing tower with built-in cyclone and air guide plate group |
| CN109806673A (en) * | 2019-03-06 | 2019-05-28 | 中国石油大学(北京) | A kind of gas-liquid separation device for gas defoaming |
| CN110215765B (en) * | 2019-04-18 | 2024-07-16 | 中国石油大学(北京) | Cyclone separator and separation system for inhibiting coking of outer wall of riser |
| CN114185366B (en) * | 2021-05-20 | 2024-08-23 | 江苏华海测控技术有限公司 | Intelligent constant-speed flow controller |
| CN114806648A (en) * | 2022-06-27 | 2022-07-29 | 山西阳煤化工机械（集团）有限公司 | Crude gas separator and crude gas separation method |
| CN117427443B (en) * | 2023-10-31 | 2024-08-02 | 中国神华煤制油化工有限公司 | Multiphase flow material separator |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2186107Y (en) * | 1994-03-22 | 1994-12-28 | 陈启松 | Tornado microporous dust remover |
| CN103816724A (en) * | 2014-03-07 | 2014-05-28 | 中石化上海工程有限公司 | Efficient gas-liquid cyclone separator |
| CN104263415A (en) * | 2014-09-28 | 2015-01-07 | 中国东方电气集团有限公司 | Dry pulverized coal gasification device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5538696A (en) * | 1994-05-02 | 1996-07-23 | Mobil Oil Corporation | FCC process and apparatus with contained vortex third stage separator |
-
2016
- 2016-03-10 CN CN201610136938.5A patent/CN105779022B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2186107Y (en) * | 1994-03-22 | 1994-12-28 | 陈启松 | Tornado microporous dust remover |
| CN103816724A (en) * | 2014-03-07 | 2014-05-28 | 中石化上海工程有限公司 | Efficient gas-liquid cyclone separator |
| CN104263415A (en) * | 2014-09-28 | 2015-01-07 | 中国东方电气集团有限公司 | Dry pulverized coal gasification device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105779022A (en) | 2016-07-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105779022B (en) | Cyclone separator and gas-liquid solid separation system | |
| CN103301958B (en) | Gas-liquid separation apparatus | |
| CN108043145B (en) | Turbulent jet coupling integrated flue gas purification process for complex and difficult-to-treat flue gas | |
| CN105689154B (en) | A kind of black water flotation unit and technique | |
| CN103060018B (en) | Gas distributor for coal gas high-efficiency washing and cleaning technique, secondary coal gas washing tower, coal gas cleaning device and application thereof | |
| CN103056045B (en) | For the primary cyclone of gas purification, gas cleaning system, gas purifying method and application thereof | |
| CN202322761U (en) | Gas distributor, secondary coal gas scrubber and coal gas purifying device for efficient washing and purifying process of coal gas | |
| CN103252183B (en) | Classifying dropping-type coal slurry pretreating device | |
| CN111097249B (en) | Rotational flow-based high-efficiency turbulent flow atomization mixing desulfurization dust removal process | |
| CN208472004U (en) | A kind of cleaning dust device of synthesis gas | |
| RU104082U1 (en) | CENTRIFUGAL OIL AND GAS SEPARATOR | |
| CN107189824B (en) | A kind of efficient ash handling equipment of polynary gasification furnace exit gas and technique | |
| CN206751747U (en) | A kind of polynary efficient ash handling equipment of gasification furnace exit gas | |
| CA1129333A (en) | Cyclonic scrubber with perforated plate distributor | |
| CN213965801U (en) | Raw coal gas-liquid separator | |
| CN111632439B (en) | Enhanced separation type raw gas coalescence separator | |
| CN103060017A (en) | Combined spiral tower tray for gas washing tower, gas cleaning device and application thereof | |
| CN2330404Y (en) | Melamine-urea washing and gas-liquid separation combined equipment | |
| CN202398439U (en) | Primary cyclone separator for gas purification and gas purification system | |
| CN206121331U (en) | Centrifugal gas -liquid defroster | |
| CN105728201A (en) | Coal slime water flotation reagent vaporizing device and vaporizing method thereof | |
| CN117427443B (en) | Multiphase flow material separator | |
| CN206385102U (en) | A kind of dedusting dehydrating tower | |
| RU2299757C2 (en) | Screen-separator | |
| CN205995205U (en) | Venturi high-efficiency wet-type dust collector |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 100011 Shenhua building, 22 West Binhe Road, Dongcheng District, Beijing Patentee after: China Shenhua Energy Co.,Ltd. Patentee after: Guoneng Baotou Coal Chemical Co.,Ltd. Patentee after: CHINA SHENHUA COAL TO LIQUID AND CHEMICAL Co.,Ltd. Address before: 100011 Shenhua building, 22 West Binhe Road, Dongcheng District, Beijing Patentee before: China Shenhua Energy Co.,Ltd. Patentee before: SHENHUA BAOTOU COAL CHEMICAL Co.,Ltd. Patentee before: CHINA SHENHUA COAL TO LIQUID AND CHEMICAL Co.,Ltd. |