CN105779022A - Cyclone separator and gas-liquid-solid separating system - Google Patents
Cyclone separator and gas-liquid-solid separating system Download PDFInfo
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- CN105779022A CN105779022A CN201610136938.5A CN201610136938A CN105779022A CN 105779022 A CN105779022 A CN 105779022A CN 201610136938 A CN201610136938 A CN 201610136938A CN 105779022 A CN105779022 A CN 105779022A
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- cyclone separator
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- riser
- liquid
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
Abstract
The invention provides a cyclone separator and a gas-liquid-solid separating system. The cyclone separator comprises a first shell (101), a feeding opening structure (104) and a gas-lifting pipe (106); a gas outlet (102) is formed in the upper part of the first shell (101); a solid-liquid mixture outlet (103) is formed in the lower part of the first shell (101); the feeding opening structure (104) is arranged at the upper part of the first shell (101); the gas-lifting pipe (106) is arranged in the first shell (101); the interior of the gas-lifting pipe (106) is communicated with the gas outlet (102); a separating cavity is formed between the gas-lifting pipe (106) and the first shell (101); an overflowing structure (107) is arranged on the circumferential side wall of the gas-lifting pipe (106). According to the technical scheme of the invention, the problem that a crude gas purifying effect is poor in the prior art can be effectively solved.
Description
Technical field
The present invention relates to gas-liquid-solid separation technology field, in particular to a kind of cyclone separator and gas-liquid-solid piece-rate system.
Background technology
At present, coal water slurry gasification is the important step of coal producing light olefins industry, Nitrogenous Fertilizer Industry and coal liquifaction industry etc..The raw gas that coal water slurry gasification produces is typically passed through chilling process primary wash, cooling and gas-liquid-solid and separates.Light component raw gas after separation is sent to follow-up workshop section.Owing to coal water slurry gasification generally carries out in gasification furnace combustor, raw gas can carry flying dust, slag is directly entered shock chamber, this water quality resulted in shock chamber is poor, the moisture that the impurity such as a large amount of flying dusts are carried secretly along with raw gas enters in scrubbing tower through venturi, and then have impact on the water quality in scrubbing tower and the cleannes of scrubbing tower top exit purge gas.Meanwhile, also there are some impurity unavoidably in the relatively clean liquid phase part of wash tower bottoms, this liquid phase part is sent to chilling ring of gasifying furnace through Quench water pump pressure-raising, filter after filtering, and the raw gas that gasification furnace combustor is come carries out primary wash, cooling.Therefore, in the water cycle process of gasification, owing to raw gas purifying is thorough, often occur that chilled water plugged filter, chilling ring fouling be serious, zooming phenomenon drops in SR, thus cause production can not stability contorting, even destroy the balance of grey water treatment system.
Additionally, the raw gas that coal water slurry gasification prepares generally goes through fed downstream operation after shock chamber, syngas outlet spray, Venturi scrubber, scrubbing tower water-bath and demister Pyatyi cleaning dust.Coal Gasification water consumption is relatively big, and gasified water system is usually maintained in higher circulating load.But, although raw gas have passed through multistage washing, purifying, but coal gas band water band ash is inevitable, and this results in the fresh water that needs to be continuously replenished to maintain the balance of water system the battery limit (BL) outside, and therefore, improvement system water quality is most important.
There is a kind of gas washing in the prior art and purify technique.It is as follows that this technique mainly implements step: a part of Heisui River come from scrubbing tower Heisui River storage tank pressurization is delivered to Venturi scrubber by washings circulating pump, mixing with from out-of-bounds raw gas, in venturi, Heisui River enters separator after being undertaken solid particles such as the lime-ash carried secretly in raw gas moistening, bond and increase and carries out one-level washing.In the separated device of raw gas, down-comer flows downward, and major part lime-ash enters in separator bottom liquid phase, and the Heisui River of generation enters black water treatment system.Raw gas ascends in scrubbing tower water-bath along down-comer and airway annular space.Raw gas is flowed up by water-bath, carries out reverse contact with another part Heisui River and the external technique moisturizing from washings circulating pump on the tower tray of scrubbing tower top.Coal gas after two grades of washings sends into subsequent conversion operation by the baffle plate demister on tower tray top, and the Heisui River that scrubbing tower produces enters black water treatment system.But, this technique in implementation process, come into operation the initial stage because of water quality good, solid content is few, and raw gas is possessed good spray atomizing and clean result by Venturi scrubber.Along with the long-play produced, the solid content in wash tower bottoms Heisui River will certainly increase, and passes it through pump pressurization and delivers to venturi and will result in blockage venturi spray apertures, causes that the pressure drop increase of gasification system and energy consumption increase.Additionally, solid content increase in wash tower bottoms Heisui River also results in scrubbing tower top contact cleaning dust effect reverse with coal gas and is remarkably decreased, being unfavorable for the purification of coal gas, longtime running raw gas is extremely difficult to intended clean-up effect.
Additionally, there is also in the prior art a kind of dust-laden raw gas occasion by main washing, water-bath, secondary washing, cyclonic separation combination unit vertical separator.Above-mentioned vertical separator work process is: raw gas enters from gas feed, mixed with the washings entered from main wash mill by the entrance inside extending tube being arranged in gas feed, by entering gas cylinder after water washing dedust in central tube, it is fully contacted with washings after being then passed through the bubble that bulb-breaking device elimination is big and carries out water-bath washing.Raw gas after water-bath carries out secondary washing, carries out gas-liquid separation by cyclone separator, and the raw gas after dedusting is got rid of raw gas separator by gas outlet, and dust-laden washings are discharged by device bottom outlet through collection cone balling-up.But this technique is in implementation process, more because arranging washings, the flow velocity that coal gas is higher in addition, raw gas can be caused to carry part dust particale and to go out coal gas outlet, and the pressure drop that can cause separator increases, energy consumption increases, and is unfavorable for maintaining the even running produced.
Summary of the invention
A kind of cyclone separator of offer and gas-liquid-solid piece-rate system, the problem bad to solve raw gas purifying effect of the prior art are provided.
To achieve these goals, according to an aspect of the invention, it is provided a kind of cyclone separator, including: the first housing, the top of the first housing has gas outlet, and the bottom of the first housing has solidliquid mixture outlet；Feeding inlet structure, is arranged on the top of the first housing；Riser, is arranged in the first housing, and the inside of riser connects with gas outlet, forms disengagement chamber, the circumferential side wall of riser had flow structure between riser and the first housing.
Further, cross flow structure and include the gap that multiple axial direction along riser extends.
Further, cyclone separator also includes cooling water pipe bundle, and cooling water pipe bundle is arranged in the circumferential side wall of the first housing.
Further, multiple gaps are arranged along the circumferential direction interval of riser.
Further, shift to install between two often adjacent gaps.
Further, flow structure is multiple excessively, and multiple flow structures excessively are arranged along the axial direction interval of riser.
Further, crossing in flow structure multiple, the density in the multiple gaps crossed in flow structure of close riser end is less than the density in the multiple gaps crossing flow structure being arranged in the middle part of riser.
Further, feeding inlet structure is two that are symmetricly set in the first housing circumferential side wall, and each feeding inlet structure includes arc feeding-passage.
Further, each feeding inlet structure also includes the first charging aperture being arranged on arc feeding-passage end, and the place plane of two the first charging apertures be arranged in parallel.
Further, feeding inlet structure is charging cover, and the inner wall of end of charging cover and the circumferential side wall of the first housing are tangent.
Further, cyclone separator also includes the steady whirlpool device being arranged in the first housing, steady whirlpool device is between riser and solidliquid mixture export, steady whirlpool device includes plate body and is arranged on plate body towards the conical structure on riser side, and conical structure includes first conical structure and multiple second conical structures arranged around the first conical structure.
Further, cyclone separator also includes the Gas-Rotation-Plate Dust Separator being arranged in the first housing, and Gas-Rotation-Plate Dust Separator is positioned at the close solidliquid mixture exit end of riser.
Further, cyclone separator also includes the one-level atomizing sprayer that is positioned at above Gas-Rotation-Plate Dust Separator.
According to a further aspect in the invention, provide a kind of gas-liquid-solid piece-rate system, including Venturi scrubber, scrubbing tower and primary cyclone, Venturi scrubber connects with scrubbing tower, primary cyclone is above-mentioned cyclone separator, and the gas outlet of primary cyclone is connected with Venturi scrubber by the first pipeline.
Further, gas-liquid-solid piece-rate system also includes secondary cyclone, secondary cyclone includes the second housing, the top of the second housing has the second charging aperture and liquid outlet, the bottom of the second housing has solid outlet, second charging aperture is by the second pipeline and solidliquid mixture outlet, and liquid outlet is connected with the tower tray of scrubbing tower by the 3rd pipeline.
Further, gas-liquid-solid piece-rate system also includes the static mixer that is arranged on the second pipeline.
Further, gas-liquid-solid piece-rate system also includes lock hopper collection slag system, and lock hopper collection slag system is connected with solid outlet by the 4th pipeline.
Application technical scheme, set up flow structure in the circumferential side wall of riser.When gas-liquid-solid mixture (such as raw gas) is purified, above-mentioned gas-liquid-solid mixture first passes through feeding inlet structure and enters in the first housing, and moves downward outside riser.In motor process, the part light-component gas in gas-liquid-solid mixture can be entered directly in riser by above-mentioned flow structure of crossing, and rises to gas outlet along riser, flows to follow-up equipment by gas outlet.Remaining gas-liquid-solid mixture continues on riser and moves downward, and carries out the separation of gas and solidliquid mixture in disengagement chamber.The light-component gas separated enters and rises to gas outlet from the lower port of riser, and heavy constituent solidliquid mixture sinks down into solidliquid mixture outlet, and flows to follow-up equipment by solidliquid mixture outlet.Above-mentioned flow structure of crossing can make the part light-component gas in gas-liquid-solid mixture enter directly in riser, reduces cyclone separator internal pressure drops, thus improve gas-liquid-solid separation efficiency, clean-up effect is better.
Accompanying drawing explanation
The Figure of description constituting the part of the application is used for providing a further understanding of the present invention, and the schematic description and description of the present invention is used for explaining the present invention, is not intended that inappropriate limitation of the present invention.In the accompanying drawings:
Fig. 1 illustrates the structural representation of the embodiment of the cyclone separator according to the present invention；
Fig. 2 illustrates the schematic top plan view of the feeding inlet structure of the cyclone separator of Fig. 1；
Fig. 3 illustrates that the A-A of Fig. 1 is to cross-sectional schematic；
Fig. 4 illustrates the interior flow field schematic diagram under the cyclone separator of Fig. 1 is in working order；
Fig. 5 illustrates the schematic top plan view of the Gas-Rotation-Plate Dust Separator of the cyclone separator of Fig. 1；
Fig. 6 illustrates the schematic top plan view of two grades of atomizing sprayers of the cyclone separator of Fig. 1；
Fig. 7 illustrates the interior flow field schematic diagram under two grades of atomizing sprayers of Fig. 6 are in working order；
Fig. 8 illustrates the structural representation of the cone nozzle of two grades of atomizing sprayers of Fig. 6；
Fig. 9 illustrates the structural representation of the embodiment of the gas-liquid-solid piece-rate system according to the present invention；
Figure 10 illustrates the structural representation of the static mixer of the gas-liquid-solid piece-rate system of Fig. 9；
Figure 11 illustrates the schematic side view of the static mixer of Figure 10；
Figure 12 illustrates the interior flow field schematic diagram under the static mixer of Figure 10 is in working order.
Wherein, above-mentioned accompanying drawing includes the following drawings labelling:
101, the first housing；102, gas outlet；103, solidliquid mixture outlet；104, feeding inlet structure；1041, arc feeding-passage；1042, the first charging aperture；105, cooling water pipe bundle；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, dividing plate；1092, circular solids plate；110, one-level atomizing sprayer；120, two grades of atomizing sprayers；1201, circular spray tube；1201a, condensate inlet；1202, cone nozzle；130, solidliquid mixture sample analysis point；200, Venturi scrubber；300, scrubbing tower；301, tower tray；100, primary cyclone；400, secondary cyclone；401, the second housing；402, the second charging aperture；403, liquid outlet；404, solid outlet；405, discharging tube；406, solid-liquor separation baffle plate；407, auxiliary receives slag pipeline；408, scavenging solution sample analysis point；500, static mixer；501, static mixing entrance；502, static mixing outlet；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, lock hopper collection slag ladle slag-drip opening；604, lock hopper collection slag rinses water pot；605, low pressure buck series house steward；606, auxiliary receives pulp pump；607, high pressure grey water inlet series house steward；700, flash system.
Detailed description of the invention
It should be noted that when not conflicting, the embodiment in the application and the feature in embodiment can be mutually combined.Describe the present invention below with reference to the accompanying drawings and in conjunction with the embodiments in detail.
As it is shown in figure 1, the raw gas that the cyclone separator of the present embodiment produces for scrubbing water coal slurry gasification.This cyclone separator includes the first housing 101, feeding inlet structure 104 and riser 106.Wherein, the top of the first housing 101 has gas outlet 102, and the bottom of the first housing 101 has solidliquid mixture outlet 103.Feeding inlet structure 104 is arranged on the top of the first housing 101.Riser 106 is arranged in the first housing 101 and coaxial with the first housing 101.The inside of riser 106 connects with gas outlet 102, forms disengagement chamber between riser 106 and the first housing 101.The circumferential side wall of riser 106 had flow structure 107.
The cyclone separator of application the present embodiment, set up flow structure 107 in the circumferential side wall of riser 106.When raw gas is purified, above-mentioned raw gas first passes through feeding inlet structure 104 and enters in the first housing 101, and moves downward along riser 106.In motor process, the part light-component gas in raw gas can pass through above-mentioned flow structure 107 of crossing and enter directly in riser 106, and rises to gas outlet 102 along riser 106, flows to follow-up equipment by gas outlet 102.Remaining raw gas continues on riser 106 and moves downward, and carries out the separation of gas and solidliquid mixture in disengagement chamber.The light-component gas separated enters and rises to gas outlet 102 from the lower port of riser 106, and heavy constituent solidliquid mixture sinks down into solidliquid mixture outlet 103, and flows to follow-up equipment by solidliquid mixture outlet 103.Above-mentioned flow structure 107 of crossing can make the part light-component gas in raw gas enter directly in riser 106, reduces cyclone separator internal pressure drops, thus improve gas-liquid-solid separation efficiency, clean-up effect is better.
As depicted in figs. 1 and 2, in the cyclone separator of the present embodiment, feeding inlet structure 104 is two of the middle and upper part being symmetricly set on the first housing 101 circumferential side wall, and each feeding inlet structure 104 includes arc feeding-passage 1041.In the present embodiment, feeding inlet structure 104 is charging cover, and the inner wall of end of charging cover and the circumferential side wall of the first housing 101 are tangent.Each feeding inlet structure 104 also includes the first charging aperture 1042 being arranged on arc feeding-passage 1041 end, and the first charging aperture 1042 is all rectangular.The place plane of two the first charging apertures 1042 be arranged in parallel, and namely the first charging aperture 1042 of two rectangles is symmetrically disposed in the first housing 101 circumferential side wall in 180 degree of angles.Said structure can improve the treating capacity of the raw gas of cyclone separator, and can improve the symmetry of charging aperture air-flow, thus improving the gas-liquid-solid separation efficiency of cyclone separator.
As depicted in figs. 1 and 2, in the cyclone separator of the present embodiment, riser 106 is cylindrical.Crossing flow structure 107 for multiple, multiple flow structures 107 excessively are arranged along the axial direction interval of riser 106.Each flow structure 107 of crossing includes the gap 1071 that multiple axial direction along riser 106 extends.Multiple gaps 1071 are arranged along the circumferential direction interval of riser 106.Above-mentioned multiple gap 1071 is that the narrow and long rectangular being vertically arranged carefully is stitched.Shift to install between two often adjacent gaps 1071.Crossing in flow structure 107 multiple, the density in the multiple gaps 1071 crossed in flow structure 107 of close riser 106 end is less than the density in the multiple gaps 1071 crossing flow structure 107 being arranged in the middle part of riser 106.Namely on riser 106, multiple cross the distribution density in gap 1071 in flow structure 107 and present the distribution trend of " upper dredge in close lower dredge ", and cross and be respectively provided with certain distance between flow structure 107 and gas outlet 102, solidliquid mixture outlet 103.Said structure while ensureing that flow structure 107 had suitable air inflow, without influence on the material stress of riser 106, can make riser 106 intensity reliable.As shown in Figure 4, raw gas passed through flow structure 107 and formed axisymmetric flow field action plane in riser 106, and conplane raw gas forms air-flow in axial direction after entering riser 106.Carefully stitch it should be noted that gap 1071 is not limited to narrow and long rectangular, in other embodiments unshowned in the drawings, it is possible to as required gap 1071 is set to other seam shape, such as ellipse etc..
As shown in Figure 1 and Figure 5, in the cyclone separator of the present embodiment, cyclone separator also includes being arranged on the Gas-Rotation-Plate Dust Separator 109 in the first housing 101 and one-level atomizing sprayer 110.Wherein, Gas-Rotation-Plate Dust Separator 109 is positioned at the close solidliquid mixture of riser 106 and exports 103 one end.One-level atomizing sprayer 110 is positioned at above Gas-Rotation-Plate Dust Separator 109, and retains and have certain distance between one-level atomizing sprayer 110 and Gas-Rotation-Plate Dust Separator 109.Being provided with several dividing plates 1091 in above-mentioned Gas-Rotation-Plate Dust Separator 109, each dividing plate 1091 is intersected on central circular solid slab 1092 in the shape of a spiral, and the angle between each dividing plate 1091 is 15 to 30 degree.Dividing plate 1091 can be arranged as required to into 6,8,12,16 etc., and each dividing plate 1091 place plane spends angles horizontal by 5 to 15.One-level atomizing sprayer 110 is positioned at 0.5 to 1.5 meter of directly over Gas-Rotation-Plate Dust Separator 109, the top of one-level atomizing sprayer 110 can be nozzle structure, single spraying head, double; two shower nozzle or annular many shower nozzles can be arranged to as required, it is also possible to be low-resistance descending liquid body structure of distributor.The light-component gas separated in disengagement chamber is carried out further dedusting by said structure.
As shown in figures 1 and 3, in the cyclone separator of the present embodiment, cyclone separator also includes the steady whirlpool device 108 being arranged in the first housing 101.Steady whirlpool device 108 exports between 103 at riser 106 and solidliquid mixture.Between steady whirlpool device 108 and solidliquid mixture outlet 103, there is certain distance.Steady whirlpool device 108 includes plate body 1081 and is arranged on plate body 1081 towards the conical structure on riser 106 side.Conical structure includes first conical structure 1082 and multiple second conical structures 1083 arranged around the first conical structure 1082.Said structure can reduce whirlpool, steady whirlpool better effects if further.When process technique tolerance is relatively big, air velocity is very fast, said structure can be avoided purified gas to carry the impurity such as solidliquid mixture and enter follow-up system.
As shown in figures 1 and 3, in the cyclone separator of the present embodiment, cyclone separator also includes cooling water pipe bundle 105.First housing 101 includes straight tube degree and conical section.This cooling water pipe bundle 105 is uniformly arranged in the circumferential side wall of straight tube degree.Flow of cooling water direction in cooling water pipe bundle 105 is adverse current with raw gas flow direction in the axial direction, and above-mentioned cooling water enters from the bottom of straight tube degree, flows out from the top of straight tube degree heteropleural.Above-mentioned cooling water and raw gas flow direction reverse heat-exchange, it is easy to solidliquid mixture refrigerated separation from gas, be conducive to isolated solidliquid mixture to act on preferably with water treatment agent in follow-up system, avoid solidliquid mixture slagging scorification, dross on the first housing 101 sidewall simultaneously.Above-mentioned conical section is positioned at the part below steady whirlpool device 108 and forms solidliquid mixture collecting bin.Solidliquid mixture outlet 103 is positioned at the bottom of this solidliquid mixture collecting bin.The sidewall of this solidliquid mixture collecting bin is provided with remote liquid level transmitter LT, and its control valve LV exporting 103 with solidliquid mixture hangs with interlocking.Preferably, exporting at solidliquid mixture and arrange high pressure nitrogen arm between the bivalve of 103, this high pressure nitrogen arm is as accident treatment active redundancy pipeline.When solidliquid mixture exports 103 appearance blocking, opening the two pass valve on the second pipeline manually or automatically, and upwards repeatedly instead push up blocking material under the effect of high pressure nitrogen arm, wherein high pressure nitrogen pressure ratio cyclone system pressure is high 20 to 30 kilograms.
Present invention also provides a kind of gas-liquid-solid piece-rate system.The gas-liquid-solid piece-rate system of the present embodiment may be used for the higher coal of content of ashes, petroleum coke or solid carbon hydrogen compound for gasified raw material, and the raw gas purifying with entrained flow gasification chilling process separates.Above-mentioned gas-liquid-solid piece-rate system includes Venturi scrubber 200, scrubbing tower 300 and primary cyclone 100.Venturi scrubber 200 connects with scrubbing tower 300.Primary cyclone 100 is above-mentioned cyclone separator.The gas outlet 102 of primary cyclone 100 is connected with Venturi scrubber 200 by the first pipeline.
As shown in Fig. 1, Fig. 6 to Fig. 9, in the gas-liquid-solid piece-rate system of the present embodiment, gas-liquid-solid piece-rate system also includes two grades of atomizing sprayers 120.Above-mentioned two grades of atomizing sprayers 120 are arranged on the first pipeline, and are positioned at the top of gas outlet 102.These two grades of atomizing sprayers 120 are annular spray equipment, it has circular spray tube 1201 and four cone nozzles 1202 in 90 degree of angles connected with circular spray tube 1201, angle between any two symmetrical buses of vertex of a cone part of cone nozzle 1202 is 90 degree, naturally it is also possible to be 45 degree, 60 degree angles not etc..Cone nozzle 1202 inserts a segment distance in the first pipeline, is not close to tube wall.Condensed fluid enters circular spray tube 1201 from condensate inlet 1201a, and wherein condensate inlet 1201a can be single, two or four etc..Condensed fluid forms flow field from four cone nozzle 1202 ejections.Said structure can fully be atomized moistening gas, it is simple to purge gas enters purifying and dedusting during follow-up system (such as Venturi scrubber).
As it is shown in figure 9, in the gas-liquid-solid piece-rate system of the present embodiment, gas-liquid-solid piece-rate system also includes secondary cyclone 400.Secondary cyclone 400 includes the second housing 401.The top of the second housing 401 has the second charging aperture 402 and liquid outlet 403.Being provided with discharging tube 405 in second housing 401, the top of discharging tube 405 connects with liquid outlet 403.The bottom of the second housing 401 has solid outlet 404.Second charging aperture 402 exports 103 by the second pipeline with solidliquid mixture and connects.Liquid outlet 403 is connected with the tower tray 301 of scrubbing tower 300 by the 3rd pipeline.Gas-liquid-solid piece-rate system also includes static mixer 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 connected with solid outlet 404 by the 4th pipeline.
Raw gas separates through the primary purifying of primary cyclone 100, and light-component gas enters scrubbing tower 300 from gas outlet 102 through Venturi scrubber 200.The heavy constituent solidliquid mixture that primary separation goes out exports 103 entrance and the static mixer 500 being arranged on the second pipeline through solidliquid mixture.Solidliquid mixture through in static mixer 500 with the chemical action of water treatment agent and the physical separation in secondary cyclone 400 after, most of solid component falls into the bottom ash bucket of the second housing 401, and enters in lock hopper collection slag system 600 through solid outlet 404；Liquid phase component after purification rises to liquid outlet 403 through discharging tube 405, delivers to and does tower tray moisturizing on the some layers of tower tray 301 being positioned at scrubbing tower 300 middle and upper part.
As shown in Fig. 9 to Figure 12, in the gas-liquid-solid piece-rate system of the present embodiment, static mixer 500 be solidliquid mixture with water treatment agent be sufficiently mixed place, it is forward-reverse spiral structure, it has static mixing entrance 501, static mixing outlet 502 and water treatment agent entrance 503, water treatment agent entrance 503 is positioned at the top of static mixing entrance 501, so contributes to the comprehensive immixture of flow at high speed liquid and water treatment agent.Static mixing outlet 502 is connected with the second charging aperture 402 of secondary cyclone 400.Water treatment agent enters in static mixer 500 from water treatment agent entrance 503 and is sufficiently mixed generation chemical reaction with solidliquid mixture.
As it is shown in figure 9, in the gas-liquid-solid piece-rate system of the present embodiment, the second charging aperture 402 of secondary cyclone 400 is arranged on the middle and upper part sidewall of the second housing 401.Preferably, the second charging aperture 402 be arranged on the middle and upper part sidewall of the second housing 401 and inlet tube slope slightly downward 3 to 10 degree.Discharging tube 405 is cylindrical, and this discharging tube 405 and the second housing 401 are coaxially disposed.A segment distance place of the underface of the lower port of discharging tube 405 is provided with solid-liquor separation baffle plate 406.Bottom ash bucket is positioned at the underface of above-mentioned solid-liquor separation baffle plate 406.Solid outlet 404 is arranged on the bottommost of the second housing 401.Liquid outlet 403 is positioned at the surface of discharging tube 405.Secondary cyclone 400 is again provided with cooling water pipe bundle, this cooling water pipe bundle is arranged on the surrounding sidewall of the second housing 401, such in order that after making purification the temperature of liquid phase component be more suitable for the tower tray moisturizing of tower tray 301, avoid in internal pressure drop and the energy consumption of increasing because of slagging scorification of secondary cyclone 400 simultaneously.Additionally, the auxiliary that secondary cyclone 400 also includes being arranged on the ash bucket sidewall of bottom receives slag pipeline 407.Under secondary cyclone 400 with lock hopper collection slag ladle 601 connected state, receive pulp pump 606 by assisting and assist receipts slag pipeline 407 can deliver to bottom ash bucket after sucking buck pressurization from lock hopper collection slag ladle 601 top, thus playing loosening hopper bottom solid matter, promotion circular fluidic flow, assisting the effect receiving slag.
As shown in Figure 9, in the gas-liquid-solid piece-rate system of the present embodiment, gas-liquid-solid piece-rate system also includes being arranged on the second pipeline and exports the solidliquid mixture sample analysis point 130 of 103 near solidliquid mixture, adjust flow control valve FV1 process operation parameter according to its Analysis Results of Water Quality, wherein before flow control valve FV1, be provided with effusion meter.It is provided above backwash pipeline, for the emergent management of outlet line stopping state at solidliquid mixture sample analysis point 130.Gas-liquid-solid piece-rate system also includes being arranged on the 3rd pipeline also near the scavenging solution sample analysis point 408 of liquid outlet 403.Analyze result according to the scavenging solution at scavenging solution sample analysis point 408 and adjust the technological parameter of flow control valve FV2 and FV3, wherein before flow control valve FV2, FV3, be both provided with effusion meter.
As it is shown in figure 9, in the gas-liquid-solid piece-rate system of the present embodiment, lock hopper collection slag system 600 includes lock hopper collection slag ladle 601, is arranged on the underface of secondary cyclone 400.Lock hopper collection slag ladle entrance 602 is arranged on the surface of the underface of solid outlet 404, lock hopper collection slag ladle 601.Lock hopper collection slag ladle slag-drip opening 603 is arranged on the underface of lock hopper collection slag ladle 601 and coaxial with lock hopper collection slag ladle entrance 602.Lock hopper collection slag rinses water pot 604 and is positioned above on the horizontal level of lock hopper collection slag ladle 601 certain distance, this lock hopper collection slag rinses and is mainly provided with lock hopper collection slag ladle blowdown line and clean-up line on water pot 604, and these pipelines can share with the respective lines of lock hopper slag collection system bottom gasification furnace.Low pressure buck series house steward 605 is arranged on lock hopper collection slag and rinses in the upper portion side wall of water pot 604.Auxiliary is received pulp pump 606 and is arranged on level ground, and high pressure grey water inlet series house steward 607 is arranged on lock hopper collection slag ladle inlet valve KV1, KV2 place, and high pressure buck arm is coupled with between KV1, KV2 and auxiliary receives pulp pump 606 suction line place.Slag collecting pit and pulp water storehouse are arranged in parallel in below lock hopper collection slag ladle 601, and wherein slag collecting pit is positioned at the underface of lock hopper collection slag ladle slag-drip opening 603.Preferably, lock hopper collection slag ladle 601 being provided with the pressure difference transmitter PDT of comparing calculation between the second charging aperture 402 of secondary cyclone 400, its span is 100 to 200kPa.
As it is shown in figure 9, the operation principle of the gas-liquid-solid piece-rate system of the present embodiment is as follows:
Carry the raw gas of certain water content and the amount of dust centrifugation by primary cyclone 100 and gravitational settling effect realizes the initial gross separation of drop in raw gas, dust and coal gas.Light component purge gas after separation enters follow-up dust pelletizing system from riser 106 top after two grades of atomizing sprayer 120 spray atomizings.Isolated solidliquid mixture discharges (can partly deliver to flash system 700 as required) bottom primary cyclone 100, and enter secondary cyclone 400 with water treatment agent effect after adding the static mixer 500 of doses water treatment agent, separate and after gravitational settling through two-stage centrifugal, the liquid separated sends into the tower tray 301 (part can deliver to flash system 700 as required) of scrubbing tower 300 from discharging tube 405, and the composition that solid content is higher enters slag collecting pit through lock hopper collection slag system 600.
Specifically, raw gas enters the first housing 101 from two the first charging apertures 1042, purification separation through primary cyclone 100, the light component purge gas multiple gaps 1071 on riser 106 surrounding sidewall of major part enter riser 106, light-component gas in remaining raw gas enters in riser 106 after steady whirlpool device 108, Gas-Rotation-Plate Dust Separator 109 and the one-level atomizing sprayer 110 above it from the bottom inlet of riser 106, and the purge gas after converging enters scrubbing tower 300 from gas outlet 102 through Venturi scrubber 200 together.The heavy constituent solidliquid mixture that primary separation goes out exports 103 from solidliquid mixture and enters, through Liquid level adjusting valve LV, the static mixer 500 being arranged on the second pipeline, wherein according to the analysis result of solidliquid mixture sample analysis point 130 and technological requirement, part can be delivered to flash system 700 through flow control valve FV1 and carry out flash distillation and process static mixing outlet and 502 be connected with the second charging aperture 402 of secondary cyclone 400 through pipeline.Solidliquid mixture most of solid component after the physical separation of water treatment agent chemical action and secondary cyclone 400 falls into bottom ash bucket, enters lock hopper collection slag system 600 through solid outlet 404.Liquid phase component after purification rises to liquid outlet 403 through discharging tube 405 and send through flow control valve FV3 and do tower tray moisturizing on the some layers of tower tray 301 of scrubbing tower 300, analyzing result and technological requirement according to scavenging solution sample analysis point 408, Partial Liquid Phase component can be delivered to flash system 700 flash distillation through flow control valve FV2 and process.
As can be seen from the above description, the above embodiments of the present invention achieve following technique effect:
The gas-liquid-solid piece-rate system of the present embodiment focuses on that solution rough coal band of gas water is serious with ash, system pressure drop is big, energy consumption is high, the problem of water quality inferiority.In above-mentioned gas-liquid-solid piece-rate system, primary cyclone makes the droop loss processing identical tolerance reduce by 25% to 50%, and the arresting efficiency particle diameter when 99% decreases nearly 3 times.The combined effect arranged in conjunction with follow-up water treatment agent and secondary cyclone of double atomization spray equipment, makes in the liquid separated that dust-laden size tunable system is within 5um, and in purge gas, dustiness can be down to 0.5mg/m3Below.
The gas-liquid-solid piece-rate system of the present embodiment is from udst separation gas, reduction system pressure drop source, so that subsequent handling is no longer by dust-laden quantitative limitation in coal gas, efficiency of dust collection is high.In addition, above-mentioned gas-liquid-solid piece-rate system can also avoid the quantity that comes into operation of the filtering separation devices such as chilled water filter, follow-up water gas separator, water gas filter, reduces equipment cost, simultaneously, drastically reduce the area the water circulating load in gasification system, energy conservation and consumption reduction effects is notable.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.All within the spirit and principles in the present invention, any amendment of making, equivalent replacement, improvement etc., should be included within protection scope of the present invention.
Claims (17)
1. a cyclone separator, it is characterised in that including:
First housing (101), the top of described first housing (101) has gas outlet (102), and the bottom of described first housing (101) has solidliquid mixture outlet (103)；
Feeding inlet structure (104), is arranged on the top of described first housing (101)；
Riser (106), it is arranged in described first housing (101), the inside of described riser (106) connects with described gas outlet (102), disengagement chamber is formed between described riser (106) and described first housing (101)
Wherein, the circumferential side wall of described riser (106) had flow structure (107).
2. cyclone separator according to claim 1, it is characterised in that described flow structure (107) of crossing includes the gap (1071) that multiple axial direction along described riser (106) extends.
3. cyclone separator according to claim 1, it is characterized in that, described cyclone separator also includes cooling water pipe bundle (105), and described cooling water pipe bundle (105) is arranged in the circumferential side wall of described first housing (101).
4. cyclone separator according to claim 2, it is characterised in that multiple described gaps (1071) are arranged along the circumferential direction interval of described riser (106).
5. cyclone separator according to claim 4, it is characterised in that shift to install between two often adjacent described gaps (1071).
6. the cyclone separator according to claim 4 or 5, it is characterised in that described flow structure (107) excessively is for multiple, and multiple described flow structures (107) excessively are arranged along the axial direction interval of described riser (106).
7. cyclone separator according to claim 6, it is characterized in that, crossing in flow structure (107) the plurality of, the density in the described multiple described gap (1071) crossed in flow structure (107) of close described riser (106) end is less than the density in the described multiple described gap (1071) crossing flow structure (107) being arranged in described riser (106) middle part.
8. cyclone separator according to claim 1, it is characterized in that, described feeding inlet structure (104) is two that are symmetricly set in described first housing (101) circumferential side wall, and each described feeding inlet structure (104) includes arc feeding-passage (1041).
9. cyclone separator according to claim 8, it is characterized in that, each described feeding inlet structure (104) also includes the first charging aperture (1042) being arranged on described arc feeding-passage (1041) end, and the place plane of two described first charging apertures (1042) be arranged in parallel.
10. cyclone separator according to claim 8, it is characterised in that described feeding inlet structure (104) is charging cover, the inner wall of end of described charging cover is tangent with the circumferential side wall of described first housing (101).
11. cyclone separator according to claim 1, it is characterized in that, described cyclone separator also includes steady whirlpool device (108) being arranged in described first housing (101), described steady whirlpool device (108) is positioned between described riser (106) and described solidliquid mixture outlet (103), described steady whirlpool device (108) includes plate body (1081) and is arranged on described plate body (1081) towards the conical structure on described riser (106) side, described conical structure includes first conical structure (1082) and multiple second conical structures (1083) arranged around described first conical structure (1082).
12. cyclone separator according to claim 1, it is characterized in that, described cyclone separator also includes the Gas-Rotation-Plate Dust Separator (109) being arranged in described first housing (101), and described Gas-Rotation-Plate Dust Separator (109) is positioned at close described solidliquid mixture outlet (103) one end of described riser (106).
13. cyclone separator according to claim 12, it is characterised in that described cyclone separator also includes the one-level atomizing sprayer (110) being positioned at described Gas-Rotation-Plate Dust Separator (109) top.
14. a gas-liquid-solid piece-rate system, it is characterized in that, including Venturi scrubber (200), scrubbing tower (300) and primary cyclone (100), described Venturi scrubber (200) connects with described scrubbing tower (300), the described primary cyclone (100) cyclone separator according to any one of claim 1 to 13, the described gas outlet (102) of described primary cyclone (100) is connected with described Venturi scrubber (200) by the first pipeline.
15. gas-liquid-solid piece-rate system according to claim 14, it is characterized in that, described gas-liquid-solid piece-rate system also includes secondary cyclone (400), described secondary cyclone (400) includes the second housing (401), the top of described second housing (401) has the second charging aperture (402) and liquid outlet (403), the bottom of described second housing (401) has solid outlet (404), described second charging aperture (402) exports (103) by the second pipeline with described solidliquid mixture and connects, described liquid outlet (403) is connected with the tower tray (301) of described scrubbing tower (300) by the 3rd pipeline.
16. gas-liquid-solid piece-rate system according to claim 15, it is characterised in that described gas-liquid-solid piece-rate system also includes the static mixer (500) being arranged on described second pipeline.
17. gas-liquid-solid piece-rate system according to claim 15, it is characterized in that, described gas-liquid-solid piece-rate system also includes lock hopper collection slag system (600), and described lock hopper collection slag system (600) is connected with described solid outlet (404) by the 4th pipeline.
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| CN201610136938.5A CN105779022B (en) | 2016-03-10 | 2016-03-10 | Cyclone separator and gas-liquid solid separation system |
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| CN201610136938.5A CN105779022B (en) | 2016-03-10 | 2016-03-10 | Cyclone separator and gas-liquid solid separation system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| 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 |
| 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 |
| CN107875796A (en) * | 2017-12-15 | 2018-04-06 | 中冶焦耐(大连)工程技术有限公司 | It is used for the device and method for removing coke-stove gas impurity on coke oven gas pipe |
| 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 |
| CN108706764A (en) * | 2018-05-28 | 2018-10-26 | 中国神华能源股份有限公司 | A kind of processing equipment and processing method of desulfurization wastewater |
| CN109260872A (en) * | 2017-07-18 | 2019-01-25 | 阿特拉斯·科普柯空气动力股份有限公司 | Liquid separator |
| CN109628161A (en) * | 2019-02-18 | 2019-04-16 | 中国华能集团清洁能源技术研究院有限公司 | Cyclone and the scrubbing tower of stator blade group built in a kind of band |
| 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 |
| CN110215765A (en) * | 2019-04-18 | 2019-09-10 | 中国石油大学(北京) | A kind of cyclone separator and separation system inhibiting the coking of riser outer wall |
| CN114185366A (en) * | 2021-05-20 | 2022-03-15 | 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 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| 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 |
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| 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 |
| CN107875796A (en) * | 2017-12-15 | 2018-04-06 | 中冶焦耐(大连)工程技术有限公司 | It is used for the device and method for removing coke-stove gas impurity on coke oven gas pipe |
| 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 |
| CN108706764A (en) * | 2018-05-28 | 2018-10-26 | 中国神华能源股份有限公司 | A kind of processing equipment and processing method of desulfurization wastewater |
| CN109628161A (en) * | 2019-02-18 | 2019-04-16 | 中国华能集团清洁能源技术研究院有限公司 | Cyclone and the scrubbing tower of stator blade group built in a kind of band |
| 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 |
| CN110215765A (en) * | 2019-04-18 | 2019-09-10 | 中国石油大学(北京) | A kind of cyclone separator and separation system inhibiting the coking of riser outer wall |
| CN114185366A (en) * | 2021-05-20 | 2022-03-15 | 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 |
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| CN105779022B (en) | 2018-09-18 |
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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. |
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