CN115232647A - Separation of yellow phosphorus from synthesis gas and CO 2 And H 2 S purification system - Google Patents
Separation of yellow phosphorus from synthesis gas and CO 2 And H 2 S purification system Download PDFInfo
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- CN115232647A CN115232647A CN202211033654.5A CN202211033654A CN115232647A CN 115232647 A CN115232647 A CN 115232647A CN 202211033654 A CN202211033654 A CN 202211033654A CN 115232647 A CN115232647 A CN 115232647A
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- OBSZRRSYVTXPNB-UHFFFAOYSA-N tetraphosphorus Chemical compound P12P3P1P32 OBSZRRSYVTXPNB-UHFFFAOYSA-N 0.000 title claims abstract description 48
- 238000000746 purification Methods 0.000 title claims abstract description 22
- 238000000926 separation method Methods 0.000 title claims description 13
- 230000015572 biosynthetic process Effects 0.000 title abstract description 9
- 238000003786 synthesis reaction Methods 0.000 title abstract description 9
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 129
- 238000005406 washing Methods 0.000 claims abstract description 66
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 61
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 35
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 35
- 239000011574 phosphorus Substances 0.000 claims abstract description 35
- 239000000428 dust Substances 0.000 claims abstract description 31
- 239000012528 membrane Substances 0.000 claims abstract description 30
- 239000003245 coal Substances 0.000 claims abstract description 24
- 238000010521 absorption reaction Methods 0.000 claims abstract description 23
- 238000000034 method Methods 0.000 claims abstract description 18
- 238000002309 gasification Methods 0.000 claims abstract description 16
- 230000008929 regeneration Effects 0.000 claims abstract description 13
- 238000011069 regeneration method Methods 0.000 claims abstract description 13
- 238000003795 desorption Methods 0.000 claims abstract description 12
- 238000001704 evaporation Methods 0.000 claims abstract description 6
- 230000008020 evaporation Effects 0.000 claims abstract description 6
- 125000004122 cyclic group Chemical group 0.000 claims abstract description 4
- 239000007791 liquid phase Substances 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 120
- 239000007788 liquid Substances 0.000 claims description 12
- 239000002245 particle Substances 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 4
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 239000002904 solvent Substances 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 2
- 238000006297 dehydration reaction Methods 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- 239000002994 raw material Substances 0.000 claims description 2
- 229910052757 nitrogen Inorganic materials 0.000 claims 1
- 239000000126 substance Substances 0.000 abstract description 5
- 238000011084 recovery Methods 0.000 abstract description 3
- 238000001914 filtration Methods 0.000 abstract 1
- 239000010802 sludge Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 4
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000003513 alkali Substances 0.000 description 2
- 238000004061 bleaching Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- LRDIEHDJWYRVPT-UHFFFAOYSA-N 4-amino-5-hydroxynaphthalene-1-sulfonic acid Chemical compound C1=CC(O)=C2C(N)=CC=C(S(O)(=O)=O)C2=C1 LRDIEHDJWYRVPT-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/04—Purification of phosphorus
- C01B25/047—Purification of phosphorus of yellow phosphorus
-
- 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
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
-
- 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
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/005—Carbon dioxide
-
- 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
- C10K1/024—Dust removal by filtration
-
- 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
- C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
-
- 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
- C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a method for separating yellow phosphorus from synthesis gas and realizing CO 2 And H 2 S purification system relates to phosphorus chemical industry technical field. The system comprises a phosphorus coal gasification furnace, furnace gas of the phosphorus coal gasification furnace enters a membrane filter for filtration, filtered dust is discharged into a spiral ash discharge machine, the filtered furnace gas enters a water washing tower for washing, yellow phosphorus steam and a small amount of dust in the furnace gas enter a liquid phase, and the washed furnace gas enters an absorption tower for removing CO 2 And H 2 S obtaining purified gas. Absorption of CO in an absorption column 2 And H 2 And (3) allowing the rich methanol of the S to enter a medium-pressure flash tower for flash evaporation, allowing the flash-evaporated rich methanol to enter a desorption tower for flash evaporation and gas stripping under normal pressure to realize partial regeneration, allowing the rich methanol to enter a thermal regeneration tower for thermal regeneration to obtain poor methanol, and allowing the poor methanol to enter an absorption tower again for cyclic utilization through pressurization. The system can realize the high-efficiency recovery of yellow phosphorus in the furnace gas of the phosphorus coal gasification furnace and purify CO 2 And H 2 And S, obtaining CO synthetic gas.
Description
Technical Field
The invention relates to the technical field of phosphorus and coal chemical industry, in particular to a method for separating yellow phosphorus and synthesis gas in furnace gas of a phosphorus coal gasification furnace and realizing CO 2 And H 2 S purification system.
Background
Yellow phosphorus and CO are important chemical raw materials, and various chemical products are produced through further processing. At present, the industrial production method of yellow phosphorus is an electric furnace method, but the method has the defects of high power consumption and small tail gas amount (2800-3300 Nm) 3 Ton P 4 ) And CO in the tail gas is difficult to realize large-scale utilization. In view of this, the combined production system of yellow phosphorus and synthesis gas (application number 202110735639.4) and the phosphorus coal gasification reaction device for the combined production of yellow phosphorus and synthesis gas (application number 202110736690.7) disclose a device for simultaneously producing yellow phosphorus and CO synthesis gas by using a phosphorus coal gasification furnace, the gas amount at the outlet of the phosphorus coal gasification furnace can reach as high as 20 ten thousand Nm 3 The catalyst is used for reaction, and the catalyst contains 80-90% of CO. However, the existing yellow phosphorus collection technology mainly adopts multi-stage water washing, so that a large amount of sludge phosphorus dangerous solid waste is generated, and the energy consumption for recovering yellow phosphorus from sludge phosphorus is high. CO in furnace gas 2 And H 2 The S purification method mainly comprises a water washing-alkali washing purification process, a catalytic oxidation process, a temperature and pressure swing adsorption separation process and the like. The water washing-alkali washing purification process has low desulfurization and decarburization efficiency, the decarburization rate is about 50%, and the desulfurization rate is about 80%. After the catalytic oxidation process is used for desulfurization, the content of hydrogen sulfide is less than 0.1mg/Nm 3 (ii) a Purifying gas, CO, by temperature and pressure swing adsorption separation process 2 The content is less than 10mg/Nm 3 Total sulfur content less than 1mg/Nm 3 But the investment is large, the purification cost is high, the capacity of the treated gas is small, and the popularization is limited. Mature low temperature methanol washing technique for CO 2 And H 2 The S acid gas has good absorption effect, is suitable for treating large-flow gas and can be widely appliedIn coal chemical industry enterprises, but not used for yellow phosphorus tail gas CO 2 And H 2 And (5) purifying S.
Disclosure of Invention
The invention aims to solve the technical problem of how to provide a high-efficiency energy-saving method which can improve the yellow phosphorus collection efficiency and efficiently remove CO in furnace gas of a phosphorus furnace 2 And H 2 And S.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows: separating yellow phosphorus from synthesis gas and realizing CO 2 And H 2 S purification' S system, its characterized in that: including phosphorus coal gasifier, phosphorus coal gasifier's top burner gas export and membrane filter's entry linkage, the export of membrane filter bottom and the entry linkage of spiral ash exhauster, the filterable dust of membrane filter get into spiral ash exhauster, the export at membrane filter top and the entry linkage of one-level scrubber, the burner gas that gets rid of most dust through membrane filter gets into one-level scrubber, retrieves yellow phosphorus and further removes the dust in the burner gas, the entry linkage of one-level scrubber top burner gas export and second grade scrubber, second grade scrubber reduces the temperature of burner gas and further retrieves yellow phosphorus through normal atmospheric temperature technology water washing, and the washing water of second grade scrubber is carried to one-level scrubber burner gas washing tower burner gas washing, second grade scrubber top burner gas export and the entry linkage of gas separator, get into the prewashing section, utilizes the NH among the cold methanol desorption burner gas to retrieve yellow phosphorus, and the washing water of burner gas carries to one-level scrubber gas separator burner gas washing, and the entry linkage of second grade scrubber top burner gas export and gas 3 And HCN and other trace components, the liquid in the gas-liquid separation section is a methanol-water mixture and is sent to a rectifying tower to recover a methanol solvent, the separated gas enters an absorption tower, and CO is removed by methanol absorption liquid 2 And H 2 S, enabling the rich methanol from the absorption tower to enter a flash tower to flash and separate H 2 And CO is recovered, the flashed rich methanol enters a desorption tower, and CO is desorbed in a flash evaporation section of the desorption tower 2 Introducing low-pressure nitrogen gas into the gas stripping section to further desorb CO 2 The rich methanol from the desorption tower enters a thermal regeneration tower, and H is desorbed from the upper section of the thermal regeneration tower 2 S, primarily concentrating water in the methanol at the lower section, and then sending the methanol with higher water content into a rectifying tower for rectifying and dehydrating, wherein the rectifying tower mainly separates feed gas and carries the feed gasWater and a small amount of solid particles in the system are separated, the separated water is conveyed to a first-stage water washing tower to wash furnace gas, lean methanol reflows to enter a thermal regeneration tower, and the regenerated methanol is pressurized and cooled and then is sent back to an absorption tower for cyclic utilization.
The further technical scheme is as follows: after the furnace gas from the phosphorus coal gasification furnace is filtered by a membrane filter, dust with the particle size of more than 10 mu m in the furnace gas is removed and enters a spiral ash discharger, and the temperature of the furnace gas in the membrane filter is maintained at 220-450 ℃.
The further technical scheme is as follows: over 90% of yellow phosphorus and dust in the furnace gas are washed in the primary water washing tower (4), the yellow phosphorus is further recovered, and the temperature of the furnace gas is reduced to below 70 ℃.
The further technical scheme is as follows: and (3) introducing more than or equal to 99% of yellow phosphorus and dust in the furnace gas washed by the secondary water washing tower into a liquid phase, reducing the temperature of the furnace gas to be below 40 ℃, and introducing washing water into the washing furnace gas of the primary water washing tower.
The further technical scheme is as follows: CO in furnace gas after methanol washing in the absorption tower 2 And H 2 The mass content of S is less than 0.1mg/Nm 3 。
Adopt the produced beneficial effect of above-mentioned technical scheme to lie in: the system provided by the invention can realize effective separation of phosphorus steam and dust in the furnace gas of the phosphorus coal gasifier, improve the primary yield of yellow phosphorus and greatly reduce the yield of sludge phosphorus. By applying the technology of the invention, more than 90% of dust is separated before entering the condensation process, the energy consumption and pollution of phosphorus bleaching and phosphorus sludge recovery are effectively reduced, and the production cost of yellow phosphorus is reduced. CO purification by low-temperature methanol washing 2 And H 2 S, the complete purification of the pollutant gas is realized, and the problems of low gas purification efficiency, high cost and incomplete purification are solved.
Drawings
The invention is described in further detail below with reference to the drawings and the detailed description.
FIG. 1 is a functional block diagram of a system according to an embodiment of the present invention;
wherein: 1-a phosphorus coal gasifier; 2-a membrane filter; 3-a spiral ash discharger; 4-first-stage water washing tower; 5-a second-stage water washing tower; 6-a gas-liquid separator; 7-an absorption column; 8-a flash column; 9-a stripper column; 10-a thermal regeneration column; 11-rectifying tower.
Detailed Description
The technical solutions in the embodiments of the present invention are clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, however, the present invention may be practiced otherwise than as specifically described herein, and it will be appreciated by those skilled in the art that the present invention may be practiced without departing from the spirit and scope of the present invention and that the present invention is not limited by the specific embodiments disclosed below.
As shown in general in FIG. 1, the embodiment of the invention discloses a method for separating yellow phosphorus from synthesis gas and realizing CO 2 And H 2 The S purification system comprises a phosphorus coal gasification furnace 1, wherein a furnace gas outlet at the top of the phosphorus coal gasification furnace 1 is connected with an inlet of a membrane filter 2, and an outlet at the bottom of the membrane filter 2 is connected with an inlet of a spiral ash discharger 3; the dust filtered by the membrane filter 2 enters a spiral dust discharging machine 3, an outlet at the top of the membrane filter 2 is connected with an inlet of a primary water washing tower 4, the furnace gas from which most of the dust is removed by the membrane filter 2 enters the primary water washing tower 4 and is washed by normal-temperature process water, yellow phosphorus is recovered, and the dust in the furnace gas is further removed; the furnace gas outlet at the top of the primary water scrubber 4 is connected with the inlet of the secondary water scrubber 5, the secondary water scrubber 5 reduces the temperature of the furnace gas and further recovers yellow phosphorus through normal-temperature process water scrubbing, and the washing water of the secondary water scrubber 5 is conveyed to the washing furnace gas of the primary water scrubber 4.
The furnace gas outlet at the top of the secondary water washing tower 5 is connected with the inlet of the gas-liquid separator 6, the furnace gas enters a prewashing section, and the cold methanol is used for removing NH in the furnace gas 3 And HCN and other trace components, and the liquid in the gas-liquid separation section is a methanol-water mixtureSending to a rectifying tower 11 for recovering methanol solvent, introducing the separated gas into an absorption tower 7, and removing CO by methanol absorption liquid 2 And H 2 S, the rich methanol from the absorption tower 7 enters a flash tower 8; flash evaporation of H 2 And CO are recovered, the flashed rich methanol enters a desorption tower 9, and CO is desorbed in a flash evaporation section of the desorption tower 9 2 Introducing low-pressure nitrogen gas into the gas stripping section to further desorb CO 2 The rich methanol from the desorption tower 9 enters a thermal regeneration tower 10, and H is desorbed from the upper section of the thermal regeneration tower 10 2 And S, primarily concentrating water in the methanol at the lower section, then sending the methanol with higher water content into a rectifying tower 11 for rectification and dehydration, wherein the rectifying tower 11 mainly separates water and a small amount of solid particles brought into a system in a feed gas, the separated water is conveyed to a washing furnace gas of a primary water washing tower 4, poor methanol reflows to enter a thermal regeneration tower 10, and the regenerated methanol is pressurized and cooled and then is sent back to an absorption tower 7 for cyclic utilization.
The above system is described in detail with reference to the following embodiments
Example one
After the furnace gas of the phosphorus coal gasification furnace in the system is filtered by the membrane filter, dust with the particle size larger than 10 mu m in the furnace gas is removed and enters the spiral ash discharger. The temperature of the furnace gas in the membrane filter was maintained at 220 ℃. And further, the furnace gas filtered by the membrane filter enters a primary water washing tower, 90% of yellow phosphorus and dust in the furnace gas are washed and enter water, the yellow phosphorus is further recovered, and the temperature of the furnace gas is reduced to 70 ℃. And further, the furnace gas washed by the primary washing tower enters a secondary washing tower, 99% of yellow phosphorus and dust remaining in the furnace gas are further washed and enter water, the temperature of the furnace gas is reduced to 30 ℃, and the washing water enters the primary washing tower to wash the furnace gas. Further, CO in furnace gas after methanol washing in the absorption tower 2 And H 2 The mass content of S is less than 0.1mg/Nm 3 。
Example two
After the furnace gas of the phosphorus coal gasification furnace in the system is filtered by the membrane filter, dust with the particle size larger than 10 mu m in the furnace gas is removed and enters the spiral ash discharger. The temperature of the furnace gas in the membrane filter was maintained at 330 ℃. Further, throughThe furnace gas filtered by the membrane filter enters a primary water washing tower, 93 percent of yellow phosphorus and dust in the furnace gas are washed and enter water, the yellow phosphorus is further recovered, and the temperature of the furnace gas is reduced to 60 ℃. And further, the furnace gas washed by the primary water washing tower enters a secondary water washing tower, 99.2 percent of yellow phosphorus and dust remaining in the furnace gas are further washed and enter water, the temperature of the furnace gas is reduced to below 40 ℃, and the washing water enters the primary water washing tower to wash the furnace gas. Further, CO in furnace gas after methanol washing in the absorption tower 2 And H 2 The mass content of S is less than 0.1mg/Nm 3 。
EXAMPLE III
After furnace gas of the phosphorus coal gasification furnace in the system is filtered by the membrane filter, dust with the particle size of more than 10 mu m in the furnace gas is removed and enters the spiral ash discharger. The temperature of the furnace gas in the membrane filter was maintained at 450 ℃. And further, the furnace gas filtered by the membrane filter enters a primary water washing tower, more than 95% of yellow phosphorus and dust in the furnace gas are washed and enter water, the yellow phosphorus is further recovered, and the temperature of the furnace gas is reduced to be below 55 ℃. And further, the furnace gas washed by the primary water washing tower enters a secondary water washing tower, 99.6% of yellow phosphorus and dust remaining in the furnace gas are further washed and enter water, the temperature of the furnace gas is reduced to below 35 ℃, and the washing water enters the primary water washing tower to wash the furnace gas. Further, CO in furnace gas after methanol washing in the absorption tower 2 And H 2 The mass content of S is less than 0.1mg/Nm 3 。
In conclusion, the system provided by the invention realizes effective separation of phosphorus steam and dust in the furnace gas of the phosphorus coal gasification furnace, improves the primary yield of yellow phosphorus and greatly reduces the yield of phosphorus sludge. By applying the technology of the invention, more than 90% of dust is separated before entering the condensation process, the energy consumption and pollution of phosphorus bleaching and phosphorus sludge recovery are effectively reduced, and the production cost of yellow phosphorus is reduced. CO purification by low-temperature methanol washing method 2 And H 2 S, the complete purification of the pollutant gas is realized, and the problems of low gas purification efficiency, high cost and incomplete purification are solved.
Claims (5)
1. Yellow phosphorus separation and synthesisGas and CO production 2 And H 2 S purification' S system, its characterized in that: including phosphorus coal gasifier (1), the top furnace gas export of phosphorus coal gasifier (1) and the entry linkage of membrane filter (2), the export of membrane filter (2) bottom and the entry linkage of spiral ash exhauster (3), and the filterable dust of membrane filter (2) gets into spiral ash exhauster (3), the export at membrane filter (2) top and the entry linkage of one-level washing tower (4), the burner gas that gets rid of most dust through membrane filter (2) gets into one-level washing tower (4), retrieves yellow phosphorus and further gets rid of the dust in the burner gas, one-level washing tower (4) top furnace gas export and the entry linkage of second grade washing tower (5), second grade washing tower (5) are through the temperature that normal atmospheric temperature process washing reduced the burner gas and further retrieve yellow phosphorus, and the washing water of second grade washing tower (5) is carried to one-level washing tower (4) washing burner gas, second grade washing tower (5) top furnace gas export and the entry linkage of vapour and liquid separator (6), and the burner gas gets into prewashing section, utilizes the NH in the cold methanol desorption burner gas 3 And HCN and other trace components, the liquid in the gas-liquid separation section is a methanol-water mixture and is sent to a rectifying tower (11) to recover the methanol solvent, the separated gas enters an absorption tower (7), and CO is removed through methanol absorption liquid 2 And H 2 S, the rich methanol from the absorption tower (7) enters a flash tower (8) to flash and separate H 2 And CO are recovered, the flashed rich methanol enters a desorption tower (9), and CO is desorbed in a flash evaporation section of the desorption tower (9) 2 Introducing low-pressure nitrogen into the gas stripping section to further desorb CO 2 The rich methanol from the desorption tower (9) enters a thermal regeneration tower (10), and the upper section of the thermal regeneration tower (10) further removes CO which is not completely desorbed 2 And all of H 2 S, primarily concentrating water in the methanol at the lower section, then sending the methanol with higher water content into a rectifying tower (11) for rectification and dehydration, wherein the rectifying tower (11) mainly separates water and a small amount of solid particles brought into a system in raw material gas, the separated water is conveyed to a washing furnace gas of a first-stage water washing tower (4), lean methanol flows back to a thermal regeneration tower (10), and the regenerated methanol is pressurized and cooled and then is sent back to an absorption tower (7) for cyclic utilization.
2. The separation of yellow phosphorus from syngas and CO achievement as claimed in claim 1 2 And H 2 S purification' S system, its characterized in that: after the furnace gas from the phosphorus coal gasification furnace (1) is filtered by the membrane filter (2), dust with the particle size larger than 10 mu m in the furnace gas is removed and enters the spiral ash discharger (3), and the temperature of the furnace gas in the membrane filter (2) is maintained at 220-450 ℃.
3. The separation of yellow phosphorus from syngas and CO achievement as claimed in claim 1 2 And H 2 S system of purifying, its characterized in that: over 90 percent of yellow phosphorus and dust in the furnace gas of the phosphorus coal gasification furnace are washed in the primary water washing tower (4), the yellow phosphorus is further recovered, and the temperature of the furnace gas is reduced to below 70 ℃.
4. The method of claim 1 for separating yellow phosphorus from syngas and achieving CO 2 And H 2 S purification' S system, its characterized in that: and (3) introducing more than or equal to 99% of yellow phosphorus and dust in the furnace gas washed by the secondary water washing tower (5) into a liquid phase, reducing the temperature of the furnace gas to be below 40 ℃, and introducing washing water into the primary water washing tower (4) to wash the furnace gas.
5. The separation of yellow phosphorus from syngas and CO achievement as claimed in claim 1 2 And H 2 S purification' S system, its characterized in that: CO in furnace gas after methanol washing in the absorption tower (7) 2 And H 2 The mass content of S is less than 0.1mg/Nm 3 。
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| CN202211033654.5A CN115232647A (en) | 2022-08-26 | 2022-08-26 | Separation of yellow phosphorus from synthesis gas and CO 2 And H 2 S purification system |
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Citations (7)
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| CN113322101A (en) * | 2021-06-30 | 2021-08-31 | 昆明理工大学 | Phosphorus coal gasification reaction device for combined production of yellow phosphorus and synthesis gas |
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