CN117126687A - Novel coal chemical gas purification combined process - Google Patents
Novel coal chemical gas purification combined process Download PDFInfo
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- CN117126687A CN117126687A CN202311398530.1A CN202311398530A CN117126687A CN 117126687 A CN117126687 A CN 117126687A CN 202311398530 A CN202311398530 A CN 202311398530A CN 117126687 A CN117126687 A CN 117126687A
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- 238000000034 method Methods 0.000 title claims abstract description 37
- 230000008569 process Effects 0.000 title claims abstract description 37
- 239000003245 coal Substances 0.000 title claims abstract description 23
- 239000000126 substance Substances 0.000 title claims abstract description 23
- 238000000746 purification Methods 0.000 title claims abstract description 21
- 238000005406 washing Methods 0.000 claims abstract description 95
- 238000011084 recovery Methods 0.000 claims abstract description 73
- 238000006243 chemical reaction Methods 0.000 claims abstract description 70
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 60
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 58
- 239000011593 sulfur Substances 0.000 claims abstract description 56
- 230000007246 mechanism Effects 0.000 claims abstract description 44
- 230000006835 compression Effects 0.000 claims abstract description 17
- 238000007906 compression Methods 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims description 179
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 177
- 239000007788 liquid Substances 0.000 claims description 37
- 230000001360 synchronised effect Effects 0.000 claims description 28
- 238000005273 aeration Methods 0.000 claims description 27
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 22
- 239000007921 spray Substances 0.000 claims description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 19
- 238000005507 spraying Methods 0.000 claims description 15
- 238000004891 communication Methods 0.000 claims description 14
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 13
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 13
- 229910021529 ammonia Inorganic materials 0.000 claims description 11
- 230000008929 regeneration Effects 0.000 claims description 10
- 238000011069 regeneration method Methods 0.000 claims description 10
- 238000007789 sealing Methods 0.000 claims description 6
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 5
- 238000004140 cleaning Methods 0.000 claims 4
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 238000001816 cooling Methods 0.000 description 19
- 239000003507 refrigerant Substances 0.000 description 19
- 239000006185 dispersion Substances 0.000 description 17
- 238000005984 hydrogenation reaction Methods 0.000 description 11
- 239000002918 waste heat Substances 0.000 description 11
- 230000000903 blocking effect Effects 0.000 description 8
- 238000002485 combustion reaction Methods 0.000 description 8
- 239000000243 solution Substances 0.000 description 8
- 239000006227 byproduct Substances 0.000 description 7
- 238000010438 heat treatment Methods 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 239000002253 acid Substances 0.000 description 6
- 238000006555 catalytic reaction Methods 0.000 description 6
- 239000000314 lubricant Substances 0.000 description 6
- 239000010687 lubricating oil Substances 0.000 description 6
- 239000003921 oil Substances 0.000 description 6
- 238000004064 recycling Methods 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 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 4
- 238000010586 diagram Methods 0.000 description 4
- 238000010926 purge Methods 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- 230000005540 biological transmission Effects 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 208000012839 conversion disease Diseases 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 210000001503 joint Anatomy 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 125000001741 organic sulfur group Chemical group 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000009615 deamination Effects 0.000 description 1
- 238000006481 deamination reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000003541 multi-stage reaction Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
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- 238000011946 reduction process Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000002912 waste gas Substances 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
- C10K1/08—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
- C10K1/165—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids at temperatures below zero degrees Celsius
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
- B01D53/185—Liquid distributors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
- B01D53/8609—Sulfur oxides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
- C01B17/0408—Pretreatment of the hydrogen sulfide containing gases
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—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
- C10K1/002—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
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
- C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Treating Waste Gases (AREA)
Abstract
The application relates to the technical field of sulfur recovery equipment, in particular to a novel coal chemical gas purification combined process. The conversion device, the conversion gas washing and purifying device and the Claus sulfur recovery device are connected in sequence; a plurality of compression cavities are arranged in the compressor main body, each compression cavity is internally connected with a crank piston mechanism, the power device is connected with any crank piston mechanism, and a synchronizing device is arranged between every two adjacent crank piston mechanisms, so that the two adjacent crank piston mechanisms synchronously rotate or can relatively rotate between the two adjacent crank piston mechanisms. The novel coal chemical gas purification combined process improves the yield of sulfur, the total sulfur yield is close to 100%wt, when the equipment does not need to run at full load, the load of the power device can be reduced, compared with the full load running of the gas compressor, the energy consumption of the power device can be reduced, and the running cost of the equipment is further reduced.
Description
Technical Field
The application relates to the technical field of sulfur recovery equipment, in particular to a novel coal chemical gas purification combined process.
Background
The total sulfur yield of the conventional Claus sulfur recovery process is only about 95%, and a series of new processes are developed for improving the total sulfur yield. For example, the most widely used tail gas hydrogenation reduction absorption process at present can improve the total sulfur yield to more than 99.9 percent, and incinerate SO in the tail gas 2 The content is about 200-400 mg/Nm 3 The process flow is complex, the construction investment is 2 times of that of the conventional Claus, the operation cost and the energy consumption are high, and the tail gas emission index (sulfur content) can not meet the environmental protection requirement of the environment-sensitive area.
Raw materials of the sulfur recovery device in coal chemical industry mainly come from H-containing devices of conversion and low-temperature methanol washing devices 2 S acid gases, such as H 2 S concentration is low, CO 2 The content is high, higher requirements are put on the adaptability of the sulfur recovery device, a long-flow tail gas hydrogenation reduction absorption process is adopted, the process flow is complex, the construction investment is high, the operation cost and the energy consumption are also high, the tail gas emission does not reach the standard, and a tail gas deep purification facility needs to be added; the short-flow super/super-optimal Claus process is adopted, so that the investment, the operation cost and the energy consumption are reduced, but the sulfur yield is correspondingly reduced, and the tail gas deep purification facilities are also added to ensure thatAnd the tail gas is discharged after reaching the standard.
The tail gas produced in the current sulfur recovery process contains H 2 S gas, and finally, trace H in the tail gas is burnt 2 Oxidation of S to SO 2 And after treatment, the tail gas is discharged, and the dry discharge tail gas contains a small amount of sulfur, so that the sulfophobic yield can not reach 100%.
Disclosure of Invention
The application aims to solve the technical problems that: overcomes the defects of the prior art, and provides a novel coal chemical gas purification combined process which can absorb tail gas in a recycling way so as to improve the yield of sulfur recovery.
The technical scheme adopted for solving the technical problems is as follows: the novel coal chemical gas purification combined process comprises a conversion device, a conversion gas washing and purifying device, a Claus sulfur recovery device and a heat pump unit, wherein the conversion device, the conversion gas washing and purifying device and the Claus sulfur recovery device are sequentially connected, an evaporator and a condenser of the heat pump unit are simultaneously connected with the conversion device, the conversion gas washing and purifying device and the Claus sulfur recovery device, the temperatures of the conversion device, the conversion gas washing and purifying device and the Claus sulfur recovery device are respectively regulated, a gas compressor is arranged between the Claus sulfur recovery device and the conversion gas washing and purifying device, an input port of the gas compressor is communicated with the Claus sulfur recovery device, and an output port of the gas compressor is communicated with the conversion gas washing and purifying device;
the gas compressor comprises a compressor main body, crankshaft piston mechanisms, a power device and a synchronizing device, wherein a plurality of compression cavities are arranged in the compressor main body, the crankshaft piston mechanisms are connected in the compression cavities, the power device is connected with any one of the crankshaft piston mechanisms, the synchronizing device is arranged between every two adjacent crankshaft piston mechanisms, and the synchronizing device enables the two adjacent crankshaft piston mechanisms to synchronously rotate or enables the two adjacent crankshaft piston mechanisms to relatively rotate.
Preferably, the synchronizing device comprises a synchronizing sleeve, a synchronizing shaft and a driving device, wherein the synchronizing sleeve is rotatably arranged on the compressor main body, the synchronizing sleeve and a crankshaft of the crankshaft piston mechanism are coaxially arranged, one end, close to the synchronizing sleeve, of the crankshaft is provided with a synchronizing hole, the inner wall of the synchronizing hole is provided with an internal spline, the inner wall of the synchronizing sleeve is also provided with an internal spline, the synchronizing shaft is a spline shaft, the synchronizing shafts are slidably arranged at two ends of the synchronizing sleeve, the driving device is connected with the two synchronizing shafts simultaneously and drives the two synchronizing shafts to synchronously move, so that the two synchronizing shafts respectively extend into the synchronizing holes at corresponding sides or are moved out from the synchronizing holes.
Preferably, the driving device comprises a compressed gas channel arranged on the main body of the compressor and a communication hole arranged on the synchronizing sleeve, an annular groove is arranged on the outer wall of the surrounding synchronizing sleeve, the communication hole is arranged at the bottom of the annular groove, a plurality of communication holes are arranged at intervals around the synchronizing sleeve, the compressed gas channel is communicated with the annular groove, the diameters of two ends of the synchronizing sleeve are larger than those of the middle part, the communication hole is communicated with the middle part of the synchronizing sleeve, and all the synchronizing shafts and the synchronizing sleeve are arranged in a sealing manner.
Preferably, the driving device further comprises a tension spring, the tension spring is arranged in the synchronous sleeve, two ends of the tension spring are respectively connected with the synchronous shafts on the corresponding sides, and the two synchronous shafts are moved out of the corresponding synchronous holes.
Preferably, the crankshaft piston mechanism comprises a piston, a crankshaft and a connecting rod, wherein two ends of the crankshaft are respectively and rotatably arranged on the compressor main body, the piston is slidably arranged in the corresponding compression cavity, one end of the connecting rod is rotatably connected with the crankshaft, and the other end of the connecting rod is rotatably connected with the piston.
Preferably, the shift gas washing and purifying device comprises an ammonia washing tower, a methanol washing tower, a nitrogen gas stripping tower, a hydrogen sulfide concentration tower, a cold energy recovery device and a methanol regeneration tower, wherein an input port of the hydrogen sulfide concentration tower is communicated with the methanol washing tower and the nitrogen gas stripping tower, an output port of the hydrogen sulfide concentration tower is communicated with the cold energy recovery device and the methanol regeneration tower, an input port of the ammonia washing tower is connected with an output end of the shift device, and an output port of the ammonia washing tower is connected with an input end of the Claus sulfur recovery device.
Preferably, the methanol washing tower comprises a washing tower body, a spraying disc, a dispersing disc and an aeration disc, wherein the spraying disc, the dispersing disc and the aeration disc are sequentially arranged in the washing tower body from top to bottom, an air inlet of the washing tower body is communicated with the aeration disc, a liquid inlet of the washing tower body is communicated with the spraying disc, a plurality of dispersing discs are arranged at intervals, and the top of the washing tower body is an air outlet.
Preferably, the methanol washing tower further comprises a circulating pump, an input port of the circulating pump is communicated with the bottom of the washing tower main body, and an output port of the circulating pump is communicated with the spraying disc.
Preferably, the methanol washing tower further comprises a return pipe and a fan, one end of the return pipe is communicated with the top of the washing tower body, the other end of the return pipe is communicated with an input port of the fan, and an output port of the fan is communicated with the aeration disc.
Preferably, the spraying tray in be provided with and spray the chamber, be provided with a plurality of breather pipes on the spraying tray, the breather pipe runs through the setting of spraying tray to with the both sides intercommunication of spraying tray, and seal between each breather pipe and the spraying tray and set up, the lower part of each breather pipe all is provided with out the liquid hole, go out the liquid hole with spray the bottom in chamber and the breather pipe inner chamber intercommunication that corresponds.
Compared with the prior art, the application has the following beneficial effects:
the acid gas of the conversion device and the conversion gas washing and purifying device of the novel coal chemical gas purification combined process is sent to the Claus sulfur recovery device for treatment and recovery of sulfur, the tail gas treatment of the Claus sulfur recovery device is put into the conversion gas washing and purifying device for completion, the tail gas is sent back to the conversion gas washing and purifying device again after being compressed and recovered by a gas compressor, the recycling of the middle sulfur of the tail gas is realized, the tail gas reaches the standard and even zero emission, the investment and the operation cost of the conversion gas washing and purifying device are not increased, the yield of sulfur is improved, and the total sulfur yield is close to 100%wt; the synchronous device is arranged between every two adjacent crank shaft piston mechanisms of the gas compressor, the working quantity of the crank shaft piston mechanisms can be adjusted according to requirements, when the exhaust emission is large, all the crank shaft piston mechanisms work, namely the gas compressor works at full load, when the exhaust emission is small, only part of the crank shaft piston mechanisms work, when the equipment does not need to operate at full load, the load of the power device can be reduced, compared with the full load operation of the gas compressor, the energy consumption of the power device can be reduced, and the operation cost of the equipment is further reduced.
Drawings
FIG. 1 is a schematic diagram of a novel coal chemical gas purification combination process;
FIG. 2 is a schematic diagram in front elevation cross-section of a methanol scrubber;
FIG. 3 is an enlarged view of a portion of FIG. 2 at A;
FIG. 4 is a schematic front cross-sectional view of a shower tray;
FIG. 5 is a partial enlarged view at B in FIG. 4;
FIG. 6 is a schematic front cross-sectional view of a dispersion disk;
FIG. 7 is a schematic view in front cross-section of an aeration disc;
FIG. 8 is an enlarged view of a portion of FIG. 7 at C;
FIG. 9 is a schematic diagram of a heat pump unit;
FIG. 10 is a schematic view in front cross-section of a gas compressor;
fig. 11 is a partial enlarged view of D in fig. 10.
In the figure: 1. a shift reaction furnace; 2. a shift gas heat recovery device; 3. a gas-liquid switching device; 4. unconverted heat recovery means; 5. unconverted liquid separating device; 6. a condenser stripping means; 7. an ammonia scrubber; 8. a methanol washing tower; 801. a washing tower main body; 802. a dispersion plate; 8021. an introduction unit; 8022. a liquid separation part; 8023. a washing part; 8024. an air inlet part; 803. a spray tray; 8031. a vent pipe; 8032. a liquid outlet hole; 804. a return pipe; 805. washing a reversing valve; 806. a blower; 807. an aeration disc; 8071. a liquid blocking cover; 8072. an exhaust pipe; 8073. an annular plate; 8074. an exhaust hole; 808. a circulation pump; 809. a mounting rod; 9. a cold energy recovery device; 10. a hydrogen sulfide concentration column; 11. a methanol regeneration tower; 12. a nitrogen stripping tower; 13. a sulfur-making combustion furnace; 14. a claus reactor; 15. a tail gas hydrogenation device; 16. a tail gas cooling device; 17. a gas compressor; 1701. a compressor main body; 1702. an annular groove; 1703. an intake valve; 1704. an exhaust valve; 1705. a piston; 1706. a connecting rod; 1707. a crankshaft; 1708. a compressed gas passage; 1709. a synchronizing sleeve; 1710. a synchronizing hole; 1711. a synchronizing shaft; 1712. a communication hole; 1714. a tension spring; 1715. a connection part; 1716. a limiting table; 18. a cooler; 19. a cooling coil; 20. a refrigerant compressor; 21. an oil separator; 22. a heat pump reversing valve; 23. a lubricating oil tank; 24. a constant temperature coil; 25. a lubricant delivery pump; 26. a refrigerant storage tank; 27. a refrigerant delivery pump; 28. an expansion valve; 29. a heating coil; 30. a check valve; 31. a heat exchanger.
Detailed Description
The present application will be further described with reference to specific embodiments, however, it will be appreciated by those skilled in the art that the detailed description herein with reference to the accompanying drawings is for better illustration, and that the application is not necessarily limited to such embodiments, but rather is intended to cover various equivalent alternatives or modifications, as may be readily apparent to those skilled in the art.
Fig. 1 to 11 are diagrams illustrating preferred embodiments of the present application, and the present application is further described below with reference to fig. 1 to 11.
The novel coal chemical gas purification combined process comprises a conversion device, a conversion gas washing and purifying device, a Claus sulfur recovery device and a heat pump unit, wherein the conversion device, the conversion gas washing and purifying device and the Claus sulfur recovery device are sequentially connected, an evaporator and a condenser of the heat pump unit are simultaneously connected with the conversion device, the conversion gas washing and purifying device and the Claus sulfur recovery device, the temperatures of the conversion device, the conversion gas washing and purifying device and the Claus sulfur recovery device are respectively regulated, a gas compressor 17 is arranged between the Claus sulfur recovery device and the conversion gas washing and purifying device, an input port of the gas compressor 17 is communicated with the Claus sulfur recovery device, and an output port of the gas compressor 17 is communicated with the conversion gas washing and purifying device; the gas compressor 17 comprises a compressor main body 1701, a crank piston mechanism, a power device and a synchronization device, wherein a plurality of compression cavities are arranged in the compressor main body 1701, each compression cavity is internally connected with the crank piston mechanism, the power device is connected with any crank piston mechanism, the synchronization device is arranged between every two adjacent crank piston mechanisms, and the synchronization device enables the two adjacent crank piston mechanisms to synchronously rotate or enables the two adjacent crank piston mechanisms to relatively rotate. The acid gas of the conversion device and the conversion gas washing and purifying device of the novel coal chemical gas purification combined process is sent to the Claus sulfur recovery device for treatment and recovery of sulfur, the tail gas treatment of the Claus sulfur recovery device is put into the conversion gas washing and purifying device for completion, the tail gas is sent back to the conversion gas washing and purifying device again after being compressed and recovered by a gas compressor, the recycling of the sulfur in the tail gas is realized, the tail gas reaches the standard and even zero emission, the investment and the running cost of the conversion gas washing and purifying device are not increased, and the total sulfur yield is close to 100%wt; the synchronous device is arranged between every two adjacent crank piston mechanisms of the gas compressor 17, the working quantity of the crank piston mechanisms can be adjusted according to requirements, when the exhaust emission is large, all the crank piston mechanisms work, namely the gas compressor 17 works under full load, when the exhaust emission is small, only part of the crank piston mechanisms work at the moment, when the equipment does not need to operate under full load, the load of the power device can be reduced, compared with the full load operation of the gas compressor 17, the energy consumption of the power device can be reduced, and the operation cost of the equipment is further reduced.
Specific: as shown in fig. 1: the conversion device comprises a conversion part, an unconverted part and a condensate gas part, the raw gas from gasification enters the conversion device, and the main component H 2 、CO、CO 2 、H 2 O、H 2 S、COS、NH 3 According to different requirements of downstream products, the waste gas enters a conversion part in a certain proportion, the rest enters an unconverted part, the conversion part comprises a conversion reaction furnace 1, a conversion gas energy recovery device 2 and a conversion gas liquid separation device 3, a conversion catalyst is filled in the conversion reaction furnace 1, and CO+H is generated 2 Conversion of O to CO 2 +H 2 According to the raw materials, the shift reaction can be single-stage reaction or multi-stage reaction, in the embodiment, the shift reaction furnace 1 is three-stage reaction, wherein the temperature of the first-stage reaction is 400-450 ℃, the temperature of the second-stage reaction is 280-310 ℃, the temperature of the third-stage reaction is 260-300 ℃, the shift gas after the reaction enters a shift gas heat recovery device 2 for heat recovery, and the shift gas heat recovery device 2 comprises a gas-gas heat exchanger, a steam generator,The preheater is used for preheating gas at the inlet of each stage of conversion reaction, the by-product superheated medium/low-pressure steam is used for preheating boiler water, desalted water and the like, condensate is fractionated in the heat recovery conversion gas cooling process, and finally the conversion gas is cooled to 40 ℃.
The unconverted part comprises an unconverted heat recovery device 4 and an unconverted liquid separating device 5, the unconverted heat recovery device 4 comprises a steam generator and a preheater, so as to preheat boiler water, desalted water and the like by utilizing byproduct superheated medium/low-pressure steam, the heat recovery and the temperature reduction process are used for classifying and separating condensate, the unconverted part is finally cooled to 40 ℃, and an organic sulfur hydrolysis tank can be arranged according to the content of organic sulfur in the raw gas to hydrolyze the organic sulfur (COS) in the raw gas; the low-temperature condensate with converted air and non-converted separation enters a condenser stripping device 6, and low-pressure steam is used for providing a heat source to dissolve H 2 S、NH 3 All the acid gases are stripped to obtain qualified condensate and sent out, and the stripped acid gases are sent to a Claus sulfur recovery device.
The gas-liquid separator 3 and the non-gas-liquid separator 5 may be conventional gas-liquid separators.
The shift gas washing and purifying device comprises an ammonia washing tower 7, a methanol washing tower 8, a nitrogen stripping tower 12, a hydrogen sulfide concentration tower 10, a cold energy recovery device 9 and a methanol regeneration tower 11.
The input port of the hydrogen sulfide concentration tower 10 is simultaneously communicated with the methanol washing tower 8 and the nitrogen stripping tower 12, and the output port of the hydrogen sulfide concentration tower 10 is simultaneously communicated with the cold energy recovery device 9 and the methanol regeneration tower 11. The ammonia scrubber 7 receives the shifted and non-shifted gas from the upstream, and mainly comprises H 2 、CO、CO 2 、H 2 O、H 2 S、NH 3 Two towers may be provided for removing residual ammonia in the shifted and non-shifted gas by using high pressure boiler water and methanol, and the shifted and non-shifted gas may be washed separately. The cold recovery device 9 is one of the evaporators.
The converted gas after deamination enters a methanol washing tower 8, and H in the converted gas is removed by low-temperature methanol 2 S and CO 2 Operating temperature-60 to-50 ℃ and converting H in the air 2 S、CO 2 And othersDissolving impurities in low-temperature methanol to form rich methanol, and removing H 2 S and CO 2 The methanol-rich solution enters a hydrogen sulfide concentration tower 10, nitrogen in a nitrogen stripping tower 12 is introduced into the hydrogen sulfide concentration tower 10, and the methanol-rich solution is stripped by the nitrogen to dissolve CO in the methanol-rich solution 2 Stripping and desorbing to H 2 S is concentrated to remove H 2 CO of S 2 The purified gas is directly exhausted after passing through a cold recovery device 9 or enters a subsequent process flow to recover CO 2 。
Concentrate H 2 The rich methanol of S enters a methanol regeneration tower 11 and is regenerated under the condition of an external heat supply, the regeneration temperature is controlled between 90 ℃ and 100 ℃, and the dissolved H in the methanol is contained 2 The S acid gas is totally resolved, the regenerated lean methanol is recycled to the methanol washing tower 8, and the resolved acid gas is cooled and separated and then is sent to the sulfur-making combustion furnace 13 of the Claus sulfur recovery device.
The Claus sulfur recovery device comprises a sulfur-making combustion furnace 13, a Claus reactor 14, a tail gas hydrogenation device 15, a waste heat recovery system and a tail gas cooling device 16, wherein the Claus reactor 14 is communicated with the sulfur-making combustion furnace 13 through the front end of the waste heat recovery device, the rear end of the Claus reactor is communicated with the tail gas hydrogenation device 15, and the sulfur-making combustion furnace 13, the Claus reactor 14 and the tail gas hydrogenation device 15 are all communicated with the waste heat recovery system. The waste heat recovery system is a condenser.
The sulfur-producing combustion furnace 13 receives the H-containing gas from the upstream shift device and the shift gas washing and purifying device 2 S acid gas, through strictly controlling the air or oxygen adding amount, generates high temperature Claus reaction in the sulfur-making combustion furnace, the reaction temperature is 950-1400 ℃, so that the impurities such as hydrocarbon, organic matters and the like in the acid gas are decomposed at high temperature in the furnace, and part of H 2 S is converted into elemental sulfur and SO 2 The high-temperature Claus reaction process generates a large amount of heat, the heat recovery and utilization can be realized through byproduct medium/low-pressure steam of the waste heat recovery system, and the elemental sulfur is recovered through the waste heat recovery system.
The sulfur-making process gas after waste heat recovery enters a Claus reactor 14, and a plurality of stages of Claus reactors 14 are arranged in the reactorUnder the action of internal catalyst, H in process gas 2 S and SO 2 The reaction is converted into elemental sulfur, wherein the temperature of the primary catalytic reaction is controlled between 300 ℃ and 340 ℃, the temperature of the secondary catalytic reaction is controlled between 210 ℃ and 250 ℃, heat is generated in the catalytic reaction process, low-pressure steam as a byproduct can be recycled through a waste heat recovery system, medium-pressure steam as a byproduct can be used for heating process gas, so that the process gas reaches the initial reaction temperature of entering a Claus reactor, and then enters the reactor for catalytic reaction, and redundant medium-pressure steam is merged into a system pipe network; the byproduct low-pressure steam can be used for heat tracing of equipment and pipelines, and the excess part is integrated into a system pipe network or sent out from the device. The temperature of the process gas after waste heat recovery is reduced to 150-160 ℃, and elemental sulfur can be separated from the process gas and recovered by a recovery system.
The sulfur-making tail gas after the catalytic reaction enters a tail gas hydrogenation device 15, the tail gas hydrogenation device 15 is a hydrogenation reactor, and an external hydrogen supply source is used in the hydrogenation reactor under the action of a tail gas hydrogenation catalyst to produce SO in the tail gas 2 Is reduced and hydrolyzed to H 2 S, the reaction temperature is controlled at 260-330 ℃, heat is also generated in the catalytic reaction process, low-pressure steam can be produced as a byproduct through a waste heat recovery system for recycling, and the process gas after waste heat recovery is cooled to 150-170 ℃ and enters the tail gas cooling device 16. In the tail gas cooling device 16, the sulfur-making tail gas is cooled to 40 ℃ by a quenching agent, then is boosted to 2-3 bar by a gas compressor 17, and the temperature of the boosted gas is increased, then is cooled to 40 ℃ by a cooler 18, and is conveyed to a conversion gas washing and purifying device.
Wherein the tail gas of the Claus sulfur recovery device is sent to a shift gas washing and purifying device after being boosted and cooled, is subjected to heat exchange with the low-temperature methanol aqueous solution of the ammonia washing tower 7, is further cooled to-5 ℃, is sent to a nitrogen gas stripping tower 12, is used for stripping the methanol rich in the hydrogen sulfide concentration tower 10 together with nitrogen, and simultaneously is H in the tail gas 2 S is dissolved in rich methanol to achieve the aim of purifying tail gas, and the tail gas and CO are purified 2 The purified gas is directly exhausted after cold energy recovery, and H in the purified gas 2 S content is extremely low, less than 1.0ppmv, even zeroThe aim of up-to-standard emission and even zero emission of sulfur recovery tail gas is fulfilled; dissolve H 2 The rich methanol of S enters a methanol regeneration tower 11 and is regenerated under the condition of an external heat supply source, and the dissolved H-contained 2 S acid gas is completely resolved and sent to a Claus sulfur recovery device to continuously recover sulfur, thereby achieving the aim of improving the yield of sulfur.
As shown in fig. 2: the methanol washing column 8 includes a washing column main body 801, a shower tray 803, a dispersion tray 802, and an aeration tray 807 provided in the washing column main body 801. Spray trays 803, dispersion trays 802, and aeration trays 807 are spaced from top to bottom, wherein spray trays 803 are used to feed methanol and spray the methanol down onto dispersion trays 802. Aeration disk 807 is used to disperse the gas into scrubber body 801, and dispersion disk 802 is used to bring the methanol into sufficient contact with the gas, thereby achieving scrubbing of the methanol.
Methanol scrubber 8 also includes return line 804, fan 806, wash reversing valve 805, and circulation pump 808.
One end of the return pipe 804 is communicated with the top of the washing tower main body 801, the other end is communicated with one input port of the washing reversing valve 805, the other input port of the washing reversing valve 805 is used for inputting gas, the input port of the fan 806 is communicated with the output port of the washing reversing valve 805, and the output port of the fan 806 is communicated with the aeration disc 807. The bottom of the washing tower main body 801 is provided with an air outlet, the air outlet is provided with an air outlet valve, the on-off of air outlet can be controlled through the air outlet valve, and then the air outlet valve is matched with a fan 806, so that the circulating washing of the air entering the washing tower main body 801 can be realized. The two input ports of the purge reversing valve 805 are alternately communicated with the output ports, thereby realizing switching of modes of continuously purging the gas or circularly purging the gas in the purge column main body 801.
The input port of the circulating pump 808 is communicated with the bottom of the washing tower main body 801, and the output port of the circulating pump 808 is communicated with the spray tray 803, thereby realizing the recycling of methanol. A methanol input pipe is also arranged at the bottom of the washing tower main body 801, and a methanol input valve is arranged on the methanol input pipe.
A cooling coil 19 is arranged around the outer wall of the washing tower main body 801, the cooling coil 19 is an evaporator of the heat pump unit, and the cooling coil 19 is used for cooling the washing tower main body 801. An insulating layer may be provided outside the cooling coil 19 to avoid loss of cooling capacity.
As shown in fig. 3: the side of the aeration disc 807 is disposed at an interval from the inner wall of the main body 801, and the side of the aeration disc 807 is fixedly connected to the main body 801 by a mounting rod 809 so that the methanol solution can smoothly flow to the bottom of the main body 801.
Any one of the mounting rods 809 is circular, and an output port of the fan 806 is communicated with the aeration disc 807 through the circular mounting rod 809.
As shown in fig. 4-5: be provided with the spray chamber in the spray tray 803, set up a plurality of vertical breather pipes 8031 on the spray tray 803, breather pipe 8031 runs through the spray tray 803 and sets up, breather pipe 8031 will spray the upper and lower both sides intercommunication of tray 803 to make the gas of downside flow to the upside of spray tray 803. The vent tube 8031 is sealed with the shower tray 803.
The lower part at each breather pipe 8031 is provided with a liquid outlet hole 8032, the liquid outlet hole 8032 is arranged along the radial direction of the breather pipe 8031, the liquid outlet hole 8032 is communicated with the inner cavity of the breather pipe 8031 by a spray cavity, each breather pipe 8031 is provided with a plurality of liquid outlet holes 8032, and each liquid outlet hole 8032 is arranged around the breather pipe 8031 at intervals.
Methanol is fed into the spray chamber of the spray tray 803 via the circulation pump 808, and flows into each of the breather pipes 8031 via the liquid outlet holes 8032, thereby being in full contact with the gas flowing through the breather pipe 8031.
As shown in fig. 6: the dispersion plate 802 is provided with a plurality of dispersion holes, the dispersion holes penetrate through the dispersion plate 802 and communicate the upper side and the lower side of the dispersion plate 802, methanol flows to the lower side of the dispersion plate 802 through the dispersion holes, and gas flows to the upper side of the dispersion plate 802 through the dispersion holes.
The dispersion hole includes an introduction portion 8021, a liquid separation portion 8022, a washing portion 8023, and an air intake portion 8024, which are sequentially provided from top to bottom. The diameters of the introducing part 8021 and the liquid separating part 8022 are gradually reduced from top to bottom, the bottom of the introducing part 8021 is in butt joint with the top of the liquid separating part 8022, the included angle between a bus of the introducing part 8021 and the vertical direction is larger than the included angle between the liquid separating part 8022 and the vertical direction, the methanol solution can be prevented from being stored on the upper side of the dispersion disc 802 by the introducing part 8021, and the liquid separating part 8022 can enable methanol to flow along the inner wall of the liquid separating part 8022. The washing portion 8023 is cylindrical, and the top of the washing portion 8023 is in butt joint with the bottom of the liquid separation portion 8022, so that methanol can flow along the inner wall of the washing portion 8023 at a constant speed. The top of the air inlet portion 8024 is in butt joint with the bottom of the washing portion 8023, the diameter of the air inlet portion 8024 is gradually increased from bottom to top, gas enters the washing portion 8023 through the air inlet portion 8024, and the diameter of the air inlet portion 8024 is gradually increased along the air flow direction, so that the flow speed of the gas is gradually slowed down, the contact time of the gas and methanol is further ensured to be long, and the washing effect of the gas is ensured to be good.
As shown in fig. 7-8: the upper portion of aeration disk 807 has a convex arc shape in the middle, and can allow methanol solution falling to the top of aeration disk 807 to flow downward and to the bottom of scrubber body 801. The top of aeration disk 807 is provided with a plurality of aeration nozzles.
The aeration nozzle comprises an exhaust pipe 8072, a liquid blocking cover 8071 and an annular plate 8073, wherein the lower end of the exhaust pipe 8072 extends into the aeration disk 807 and is communicated with the inner cavity of the aeration disk 807, the exhaust pipe 8072 is in middle sealing connection with the aeration disk 807, the annular plate 8073 is sleeved outside the exhaust pipe 8072, the annular plate 8073 is arranged at the top of the exhaust pipe 8072, the liquid blocking cover 8071 is a hemispherical with the raised middle part, the liquid blocking cover 8071 is arranged on the upper side of the annular plate 8073, the inner wall of the liquid blocking cover 8071 is in sealing connection with the outer edge of the annular plate 8073, the lower end of the liquid blocking cover 8071 is lower than the annular plate 8073, and a plurality of exhaust holes 8074 are formed in the annular plate 8073.
The gas entering the aeration disk 807 enters the cavity between the liquid blocking cover 8071 and the annular plate 8073 through the exhaust pipe 8072, and is sprayed onto the top surface of the aeration disk 807 through the exhaust hole 8074, and then contacts with the downward flowing methanol solution on the top surface, so that the gas is further washed. Since the bottom of the liquid blocking cover 8071 is lower than the annular plate 8073, liquid can be prevented from entering the exhaust pipe 8072.
As shown in fig. 9: the heat pump unit includes a refrigerant compressor 20, an oil separator 21, a lubricant tank 23, a condenser, an evaporator, and a refrigerant storage tank 26. Wherein the condenser is a cooling coil 19, and the cooling coil 19 is provided with a plurality of cooling coils; the evaporator is a heating coil 29, and the heating coil 29 is also provided with a plurality of heating coils.
The refrigerant outlet of the refrigerant compressor 20 is communicated with the input port of the oil separator 21, the refrigerant outlet of the oil separator 21 is connected with a heat pump reversing valve 22, each output port of the heat pump reversing valve 22 is respectively communicated with the input port of each cooling coil 19, and each output port of each cooling coil 19 is communicated with the top of the refrigerant storage tank 26.
The heat pump reversing valve 22 may also be implemented by a plurality of solenoid valves, wherein the input port of each cooling coil 19 is communicated with the output port of the oil separator 21, and solenoid valves are provided between the input port of each cooling coil 19 and the output port of the oil separator 21.
The output port of the refrigerant storage tank 26 is connected with a refrigerant conveying pump 27, the output port of the refrigerant conveying pump 27 is simultaneously communicated with the input ports of the heating coils 29, and the output ports of the heating coils 29 are connected in series with a check valve 30 and then are communicated with the refrigerant inlet of the refrigerant compressor 20.
The output port of the lubricant tank 23 is connected with a lubricant pump 25, and the output port of the lubricant pump 25 is communicated with the lubricant input port of the refrigerant compressor 20. The constant temperature coil pipe 24 is arranged around the outer wall of the lubricating oil tank 23, the input port of the constant temperature coil pipe 24 is communicated with the output port of the refrigerant conveying pump 27, and the output port of the constant temperature coil pipe 24 is communicated with the refrigerant inlet of the refrigerant compressor 20, so that the lubricating oil is kept at a constant temperature by utilizing the refrigerant, and the fluidity of the lubricating oil is further ensured. A temperature control valve can be arranged on the constant temperature coil 24 so as to ensure that the lubricating oil maintains constant temperature.
As shown in fig. 10-11: the gas compressor 17 includes a compressor body 1701, a crank piston mechanism, a power unit, and a synchronization unit.
The left side of compressor main part 1701 is provided with a plurality of compression chamber, and each compression intracavity all installs crank shaft piston mechanism, and power device is connected with arbitrary crank shaft piston mechanism to drive this crank shaft piston mechanism motion, and then realized compressing tail gas. And a synchronizing device is arranged between every two adjacent crankshaft piston mechanisms, so that the synchronizing device can synchronously work the two adjacent crankshaft piston mechanisms, and can disconnect transmission between the two adjacent crankshaft piston mechanisms, thereby adjusting the number of the working crankshaft piston mechanisms, further reducing the load of the power device and further reducing energy consumption. The power device is an electric motor or an internal combustion engine. The compressor body 1701 is provided separately to facilitate disassembly and maintenance of the crankshaft piston mechanism and the synchronizing device, wherein lubricating oil is directly fed into the compression chambers. In this embodiment, two compression chambers are provided side by side.
An intake valve 1703 and an exhaust valve 1704 are provided at the left end of each compression chamber, and the intake valve 1703 and the exhaust valve 1704 are check valves.
The crankshaft piston device comprises a crankshaft 1707, a piston 1705 and a connecting rod 1706, wherein the crankshaft 1707 is rotatably arranged in the compressor main body 1701, the piston 1705 is slidably arranged in the compression cavity, the piston 1705 and the inner wall of the compression cavity are arranged in a sealing mode, one end of the connecting rod 1706 is hinged to the crankshaft 1707, and the other end of the connecting rod 1706 is rotatably connected with the piston 1705. The lower end of the lower crankshaft 1707 extends out of the compressor main body 1701 and is further connected with a power device, the power device drives the crankshaft 1707 to rotate, and then the crankshaft 1707 drives the piston 1705 to reciprocate, and further the lower end of the lower crankshaft 1707 is matched with the air inlet valve 1703 and the air outlet valve 1704 to compress air.
A synchronizing device is provided between the two crankshafts 1707, the synchronizing device comprising a synchronizing sleeve 1709, a synchronizing shaft 1711 and a driving device, wherein the driving device comprises a compressed gas passage 1708 provided on the compressor body 1701 and a communication hole 1712 provided on the synchronizing sleeve 1709.
The compressor main body 1701 is provided with a mounting hole for mounting the synchronizing sleeve 1709, annular limiting tables 1716 are arranged at two ends surrounding the mounting hole, the synchronizing sleeve 1709 is arranged between the two limiting tables 1716, and further the axial positioning of the synchronizing sleeve 1709 is realized, and the synchronizing sleeve 1709 and the compressor main body 1701 can rotate relatively. The inner diameter of both ends of the synchronizing sleeve 1709 is larger than the inner diameter of the middle part, and connecting parts 1715 are formed at both ends of the synchronizing sleeve 1709, the inner wall of each connecting part 1715 is provided with an internal spline, and a limiting part is formed between the two connecting parts 1715 of the synchronizing sleeve 1709.
An annular groove 1702 is formed in the middle of the outer wall of the surrounding synchronous sleeve 1709, a communication hole 1712 is formed in the bottom of the annular groove 1702, the communication hole 1712 is used for communicating the annular groove 1702 with the inner wall of the synchronous sleeve 1709, the communication hole 1712 is formed in the middle of the synchronous sleeve 1709, a plurality of communication holes 1712 are formed in the surrounding synchronous sleeve 1709 at intervals, a compressed gas channel 1708 is communicated with the annular groove 1702, and compressed gas is conveniently introduced into the synchronous sleeve 1709 or discharged.
A synchronizing hole 1710 is provided at an end of each crankshaft 1707, the synchronizing hole 1710 is coaxial with the connecting portion 1715 and spaced apart, and an internal spline is provided around an inner wall of the synchronizing hole 1710.
Each connecting portion 1715 is connected with a synchronizing shaft 1711, the synchronizing shaft 1711 is a spline shaft, and the synchronizing shaft 1711 and the connecting portions 1715 are arranged in a sealing way. When compressed air is introduced into the synchronizing sleeve 1709 through the compressed air passage 1708, the compressed air pushes the synchronizing shafts 1711 on both sides to move outwards and enter the synchronizing holes 1710 on the crankshafts 1707 on the corresponding sides, and at this time, both crankshafts 1707 on both sides keep rotating synchronously with the synchronizing sleeve 1709. When negative pressure is applied to the compressed air passage 1708, the two synchronizing shafts 1711 can be moved into the synchronizing sleeve 1709 and retained on the retaining portion, and the synchronizing shafts 1711 are separated from the synchronizing holes 1710 of the crankshafts 1707, and power transmission between the two crankshafts 1707 is disconnected.
Further, a tension spring 1714 is disposed between the two synchronizing shafts 1711, two ends of the tension spring 1714 are respectively connected with the synchronizing shafts 1711 on the corresponding sides, the tension spring 1714 is in a stretched state, and further after the compressed air channel 1708 is disconnected, the tension spring 1714 can pull the synchronizing shafts 1711 on the two sides to synchronously move inwards, and disconnect transmission with the crankshafts 1707 on the corresponding sides respectively.
The utility model discloses coal industry gas purification combination technology can adjust the work load of gas compressor 17 as required when the during operation, and then reduced power device's load to power device's consumption is reduced.
The above description is only a preferred embodiment of the present application, and is not intended to limit the application in any way, and any person skilled in the art may make modifications or alterations to the disclosed technical content to the equivalent embodiments. However, any simple modification, equivalent variation and variation of the above embodiments according to the technical substance of the present application still fall within the protection scope of the technical solution of the present application.
Claims (10)
1. A novel coal chemical gas purification combination process is characterized in that: the device comprises a conversion device, a conversion gas washing and purifying device, a Claus sulfur recovery device and a heat pump unit, wherein the conversion device, the conversion gas washing and purifying device and the Claus sulfur recovery device are sequentially connected, an evaporator and a condenser of the heat pump unit are simultaneously connected with the conversion device, the conversion gas washing and purifying device and the Claus sulfur recovery device, the temperatures of the conversion device, the conversion gas washing and purifying device and the Claus sulfur recovery device are respectively adjusted, a gas compressor (17) is arranged between the Claus sulfur recovery device and the conversion gas washing and purifying device, an input port of the gas compressor (17) is communicated with the Claus sulfur recovery device, and an output port of the gas compressor (17) is communicated with the conversion gas washing and purifying device;
the gas compressor (17) comprises a compressor main body (1701), a crankshaft piston mechanism, a power device and a synchronizing device, wherein a plurality of compression cavities are formed in the compressor main body (1701), the crankshaft piston mechanisms are connected in the compression cavities, the power device is connected with any one crankshaft piston mechanism, the synchronizing device is arranged between every two adjacent crankshaft piston mechanisms, and the synchronizing device enables the two adjacent crankshaft piston mechanisms to synchronously rotate or enables the two adjacent crankshaft piston mechanisms to relatively rotate.
2. The novel coal chemical gas cleaning combination process according to claim 1, wherein: the synchronous device comprises a synchronous sleeve (1709), a synchronous shaft (1711) and a driving device, wherein the synchronous sleeve (1709) is rotatably arranged on a compressor main body (1701), the synchronous sleeve (1709) and a crankshaft (1707) of a crankshaft piston mechanism are coaxially arranged, one end, close to the synchronous sleeve (1709), of the crankshaft (1707) is provided with a synchronous hole (1710), the inner wall of the synchronous hole (1710) is provided with an internal spline, the inner wall of the synchronous sleeve (1709) is also provided with an internal spline, the synchronous shaft (1711) is a spline shaft, the synchronous shafts (1701) are slidably arranged at two ends of the synchronous sleeve (1709), and the driving device is simultaneously connected with the two synchronous shafts (1711) and drives the two synchronous shafts (1711) to synchronously move, so that the two synchronous shafts (1711) respectively extend into the synchronous holes (1710) at corresponding sides or are removed from the synchronous holes (1710).
3. The novel coal chemical gas purification combination process according to claim 2, wherein: the driving device comprises a compressed air channel (1708) arranged on a compressor main body (1701) and a communication hole (1712) arranged on a synchronizing sleeve (1709), an annular groove (1702) is formed in the outer wall of the surrounding synchronizing sleeve (1709), the communication hole (1712) is arranged at the bottom of the annular groove (1702), a plurality of communication holes (1712) are arranged at intervals around the synchronizing sleeve (1709), the compressed air channel (1708) is communicated with the annular groove (1702), the diameter of two ends of the synchronizing sleeve (1709) is larger than that of the middle part, the communication holes (1712) are communicated with the middle part of the synchronizing sleeve (1709), and all the synchronizing shafts (1711) and the synchronizing sleeve (1709) are in sealing arrangement.
4. The novel coal chemical gas purification combined process according to claim 3, wherein: the driving device further comprises a tension spring (1714), the tension spring (1714) is arranged in the synchronizing sleeve (1709), two ends of the tension spring (1714) are respectively connected with the synchronizing shafts (1711) at the corresponding sides, and the two synchronizing shafts (1711) are moved out of the corresponding synchronizing holes (1710).
5. The novel coal chemical gas purification combination process according to claim 1 or 2, characterized in that: the crankshaft piston mechanism comprises a piston (1705), a crankshaft (1707) and a connecting rod (1706), wherein two ends of the crankshaft (1707) are respectively and rotatably arranged on the compressor main body (1701), the piston (1705) is slidably arranged in a corresponding compression cavity, one end of the connecting rod (1706) is rotatably connected with the crankshaft (1707), and the other end of the connecting rod is rotatably connected with the piston (1705).
6. The novel coal chemical gas cleaning combination process according to claim 1, wherein: the shift gas washing purification device comprises an ammonia washing tower (7), a methanol washing tower (8), a nitrogen gas stripping tower (12), a hydrogen sulfide concentration tower (10), a cold energy recovery device (9) and a methanol regeneration tower (11), wherein an input port of the hydrogen sulfide concentration tower (10) is communicated with the methanol washing tower (8) and the nitrogen gas stripping tower (12), an output port of the hydrogen sulfide concentration tower (10) is communicated with the cold energy recovery device (9) and the methanol regeneration tower (11), an input port of the ammonia washing tower (7) is connected with an output end of the shift device, and an output port of the ammonia washing tower (7) is connected with an input end of the Claus sulfur recovery device.
7. The novel coal chemical gas cleaning combination process according to claim 6, wherein: the methanol washing tower (8) comprises a washing tower main body (801), a spraying disc (803), a dispersing disc (802) and an aeration disc (807), wherein the spraying disc (803), the dispersing disc (802) and the aeration disc (807) are sequentially arranged in the washing tower main body (801) from top to bottom, an air inlet of the washing tower main body (801) is communicated with the aeration disc (803), a liquid inlet of the washing tower main body (801) is communicated with the spraying disc (803), a plurality of dispersing discs (802) are arranged at intervals, and the top of the washing tower main body (801) is an air outlet.
8. The novel coal chemical industry gas purification combination process according to claim 7, wherein: the methanol washing tower (8) further comprises a circulating pump (808), an input port of the circulating pump (808) is communicated with the bottom of the washing tower main body (801), and an output port of the circulating pump (808) is communicated with the spraying disc (803).
9. The novel coal chemical gas cleaning combination process according to claim 6, wherein: the methanol washing tower (8) also comprises a return pipe (804) and a fan (806), one end of the return pipe (804) is communicated with the top of the washing tower main body (801), the other end of the return pipe is communicated with an input port of the fan (806), and an output port of the fan (806) is communicated with the aeration disc (807).
10. The novel coal chemical industry gas purification combination process according to claim 7, wherein: spray set (803) in be provided with and spray the chamber, be provided with a plurality of breather pipes (8031) on spraying set (803), breather pipe (8031) run through and spray set (803) setting to with the both sides intercommunication that sprays set (803), and seal between each breather pipe (8031) and spraying set (803), the lower part of each breather pipe (8031) all is provided with out liquid hole (8032), goes out liquid hole (8032) and will spray the bottom of chamber and breather pipe (8031) inner chamber intercommunication that corresponds.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311398530.1A CN117126687B (en) | 2023-10-26 | 2023-10-26 | Novel coal chemical gas purification combined process |
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| CN1823233A (en) * | 2003-06-11 | 2006-08-23 | 阿瑟·诺尔斯 | Drive engagement apparatus |
| CN104454427A (en) * | 2013-09-19 | 2015-03-25 | 叶启康 | Air compressor device |
| CN106115632A (en) * | 2016-06-28 | 2016-11-16 | 山东三维石化工程股份有限公司 | Improve device and the recovery method thereof of sulfur recovery rate |
| CN210715640U (en) * | 2019-09-17 | 2020-06-09 | 新乡市创达公路设备有限公司 | Double-shaft power takeoff |
| CN112955638A (en) * | 2018-10-31 | 2021-06-11 | 品纳科动力有限公司 | Hybrid power opposed piston type internal combustion engine |
| CN116641866A (en) * | 2023-05-31 | 2023-08-25 | 吕梁学院 | Single-double-cylinder self-adaptive pumping device based on steady flow conveying and pumping method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1823233A (en) * | 2003-06-11 | 2006-08-23 | 阿瑟·诺尔斯 | Drive engagement apparatus |
| CN104454427A (en) * | 2013-09-19 | 2015-03-25 | 叶启康 | Air compressor device |
| CN106115632A (en) * | 2016-06-28 | 2016-11-16 | 山东三维石化工程股份有限公司 | Improve device and the recovery method thereof of sulfur recovery rate |
| CN112955638A (en) * | 2018-10-31 | 2021-06-11 | 品纳科动力有限公司 | Hybrid power opposed piston type internal combustion engine |
| CN210715640U (en) * | 2019-09-17 | 2020-06-09 | 新乡市创达公路设备有限公司 | Double-shaft power takeoff |
| CN116641866A (en) * | 2023-05-31 | 2023-08-25 | 吕梁学院 | Single-double-cylinder self-adaptive pumping device based on steady flow conveying and pumping method thereof |
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