CN104629816A - Self-made cold type coke oven crude gas primary cooling device - Google Patents
Self-made cold type coke oven crude gas primary cooling device Download PDFInfo
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- CN104629816A CN104629816A CN201510050651.6A CN201510050651A CN104629816A CN 104629816 A CN104629816 A CN 104629816A CN 201510050651 A CN201510050651 A CN 201510050651A CN 104629816 A CN104629816 A CN 104629816A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
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- 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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
The invention discloses a self-made cold type coke oven crude gas primary cooling device which comprises a gas heat recovery cooler, a gas circulating water cooler and a gas refrigerating water cooler, wherein a gas inlet is formed on the top of the gas heat recovery cooler; a gas outlet is formed on the lower part of the gas refrigerating water cooler; the gas heat recovery cooler is connected with a generating evaporator; the generating evaporator and a generating condenser are combined as a whole; the generating condenser is connected with an absorbing evaporator; the generating evaporator is connected with a solution heat exchanger; the solution heat exchanger is connected with the absorbing evaporator; the solution heat exchanger is connected with a solution circulating pump; the solution heat exchanger is connected with the gas heat recovery cooler; the absorbing evaporator and the absorbing condenser are combined as a whole; the absorbing evaporator is connected with the gas refrigerating water cooler,; the absorbing condenser is connected with the solution circulating pump; the solution circulating pump is connected with a solution heat exchanger; the absorbing evaporator, the absorbing condenser, the generating evaporator and the generating condenser are connected with a vacuum pump. The device disclosed by the invention is high in heat exchange efficiency.
Description
Technical field
The invention belongs to coking chemistry equipment Technology field, particularly relate to a kind of from the preliminary refrigerating unit of refrigeration mode coal oven dithio-gas.
Background technology
The primary cooler of coal oven dithio-gas is the important technological equipment of coke oven gas purification, its operation runs quality not only to the running cost of gas purification and the stable operation important of environmental quality and postorder unit, and also has great effect to Chemicals processing and coking technique.
In process of coking, raw gas (also referred to as the raw gas) temperature of overflowing through upcast from coke furnace carbonization chamber is about about 850 DEG C, the cooling of coal gas is carried out in two steps, first enter in the process of effuser through bridge tube, the cyclic ammonia water be sprayed is cooled to 80-85 DEG C, then through primary cooler, gas temperature is down to 22-25 DEG C by gas line.At this, most of water vapor, tar, naphthalene and solid micronic dust (mainly coal dust) contained in raw gas are separated, the corrosive medium such as part H2S and HCN also dissolves in phlegma, thus blocking and the corrosion of gas purification equipment and pipeline can be alleviated, and coal gas is made to obtain rough purification.
The structure and function of traditional coke oven gas primary-cooling device: epimere adopts recirculated water (about 32 DEG C) that coal gas is cooled to about 45 DEG C, hypomere adopts low temperature (refrigeration) water that coal gas is further cooled to 22 ~ 23 DEG C, reaches except technic index requirements such as naphthalenes.Primary cooler is shell-and-tube rectangular structure, in primary cooler, coal gas is walked pipe outer (shell side) and is from top to bottom walked manage interior (tube side) adverse current with recirculated water or water at low temperature and cross-flow passes carries out heat exchange cooling, coal gas while cooled, condensation phlegma: water, tar and naphthalene etc.Be prevent naphthalene etc. from generally adopting steam-refrigerated and combustion gas Refrigeration Technique to prepare water at low temperature, strengthening condensing cooling effect to the blocking of subsequent handling and working (machining) efficiency in low-temperature zone.Due to the naphthalene of crystallization on the cooling surface of heat transfer tube, the tar that can be condensed constantly dissolves, thus makes coal gas obtain rough purification.For washing coal gas entrained solid particle further and improving molten naphthalene effect, spray tar or tar ammonia mixture each section of pipe external space, through coal gas primary cooler cooling, in coal gas, steam, tar and naphthalene major part are condensed, and form phlegma and are separated.After just cold, coal gas is generally 0.5-1g/m3, tar fog 2-5g/m3 containing naphthalene.
Traditional coal gas primary cooler is the simple object achieving coal gas cooling, and does not consider the recycling of waste heat of coke oven crude gas.In order to reach, a large amount of steam or coal gas be consumed to prepare water at low temperature to the low temperature purification of coal gas, not only consume the energy and also add running cost and environmental pressure.
Industry was caused to pay close attention in recent years for Btu utilization more than coal oven dithio-gas.But system high efficiency utilizes and rests on following several mode.Current primary cooler extensively adopts the syllogic coal gas primary cooler of band waste heat recovery section, and the high temperature section (83 ~ 77 DEG C) of coal gas adopts the mode of waste heat recovery to cool coal gas and reclaims heat simultaneously, and the heat of recovery has following purposes:
1. recirculated water primary cooler high temperature section being absorbed heat is used for solving heating problem, but can only use in the winter time, and service efficiency is low, range of application is comparatively narrow.
2, recirculated water primary cooler high temperature section being absorbed heat uses for the production of (16 ~ 23 DEG C) water at low temperature supply primary cooler low-temperature zone.But circulating water temperature (65 DEG C) can matter not high and again by interchanger indirect heating lithium-bromide solution, add heat exchange number of times, make total heat transfer efficiency lower, cause unit cooler and heat-exchange system equipment huge, investment all can not solve greatly the preparation of whole water at low temperature, also need steam, combustion gas refrigeration supplementary, comprehensive benefit is undesirable.
3. primary cooler high temperature section is absorbed heat recuperation to be used for heating doctor solution supply next procedure use, but vacuum potassium carbonate type sulfur removal technology can only be used for, and very little to consumption.Due to the deficiency of vacuum potassium carbonate desulfurization technique itself, domestic this sulfur removal technology of rare employing, thus this kind of thermal utilization mode is subject to about.
Above three kinds of primary cooler high temperature section heat recovery technologies, although achieve the waste heat recovery of primary cooler high temperature section to a certain extent, all also exist obvious deficiency, are in local, interruption, inefficient state.Still can not realize the high efficiente callback of waste heat of coke oven crude gas, coupling utilizes continuously.Primary cooler needs to use a large amount of recirculated water and water at low temperature on the one hand, and power consumption is large, running cost is high, and water at low temperature needs other refrigeration equipment, and facility investment is large, energy expenditure is large, working cost is high, and floor space is large.Another side waste heat of coke oven crude gas runs off in vain and also by the temperature that water cooling tower reduces recirculated water, heat is removed, and then causes the huge waste of the energy and water resources.
Summary of the invention
Object of the present invention is exactly the problems referred to above existed for solving prior art, provides a kind of from the preliminary refrigerating unit of refrigeration mode coal oven dithio-gas; Refrigeration of the present invention adopts water at low temperature part directly to evaporate reduction temperature and obtains chilled water, compared with evaporating indirect heat exchange with the water as refrigerant of prior art, compact equipment, heat exchange efficiency is high, and decrease indirect type water cooler, reduce equipment manufacturing cost, be widely used in coal gas cooling and the coal gas heat recovery of coking chemical enterprise and gasification enterprise.
The technical scheme of technical solution problem of the present invention is:
A kind of from the preliminary refrigerating unit of refrigeration mode coal oven dithio-gas, comprise the coal gas heat recuperation water cooler connected successively from top to bottom, coal gas water recirculator, gas refrigeration watercooler, described coal gas heat recuperation water cooler top is provided with gas inlet, coal gas water recirculator is provided with circulating cooling water inlet, circulating cooling water out, gas refrigeration watercooler bottom is provided with gas exit, absorbent solution is passed in the heat transfer tube of coal gas heat recuperation water cooler, recirculated water is passed in coal gas water recirculator heat transfer tube, chilled water is passed in the heat transfer tube of gas refrigeration watercooler, the liquid outlet of described coal gas heat recuperation water cooler is connected with generation vaporizer by pipeline, there is vaporizer and become an entirety with generation condenser by gas phase baffling combination of channels, occur to be connected with absorption vaporizer by pipeline bottom condenser, the absorbent solution outlet that base of evaporator occurs is connected with the hot side medium entrance of solution heat exchanger by the fluid-tight of U-shaped pipe, the hot side medium outlet of solution heat exchanger is connected with the absorption agent strong solution import of absorptive condenser top, solution heat exchanger cold side medium entrance is connected by pipeline with solution circulated pump discharge, and solution heat exchanger cold side media outlet is connected with the tube side absorbent solution import in the heat transfer tube of coal gas heat recuperation water cooler, absorb vaporizer and become an entirety with absorptive condenser by gas phase baffling combination of channels, described absorptive condenser top is provided with circulating water heat transfer tube, recirculated water is passed in circulating water heat transfer tube, the top subcooling water inlet of described absorption vaporizer exports with gas refrigeration watercooler water at low temperature and is connected, outlet bottom absorptive condenser is connected with solution circulated pump inlet by pipeline, and the liquid outlet of solution circulation pump is connected with solution heat exchanger, described absorption vaporizer, absorptive condenser, generation vaporizer, generation condenser are connected with vacuum pump respectively by pipeline, the extraction pipe of its intermediate pump is connected with the interface that vacuumizes absorbing vaporizer top, the 16 DEG C of chilled water water outlets absorbing base of evaporator are connected with the water-in of chilled water recycle pump, and the water outlet of chilled water recycle pump is connected with the water-in of the heat transfer tube of gas refrigeration watercooler.
Gas-phase space in the middle part of described absorption vaporizer has intermediary interface, there is condenser overhead and be provided with exhaust port, intermediary interface is connected by intermediate conduit with exhaust port, and described intermediate conduit is provided with the pressure difference absorbed between vaporizer and absorptive condenser and pressure regulator valve, the control instruments that the pressure difference between condenser and generation vaporizer detects and regulate occurs.
The interface that vacuumizes at described absorptive condenser top is provided with W type vapour liquid separator.Coordinated by gas phase baffling passage, strengthening gas liquid separating function, prevents entrainment.
The bottom of described absorption vaporizer, absorptive condenser, generation condenser, generation vaporizer is provided with automatic liquid level regulating device.The liquid level of absorption vaporizer, absorptive condenser, generation condenser, generation base of evaporator is controlled by automatic liquid level regulating device.
Described coal gas heat recuperation water cooler, absorptive condenser adopt shaped telescopic tube efficient heat-exchanging pipe.Both being conducive to absorption outside heat transfer tube also can cooling heat transferring in enhanced tube.
The heat transfer tube of described generation condenser adopts the double helix heat exchange pipe that heat transfer efficiency is high.
Described solution heat exchanger can be shell-and-tube or the efficient heat exchanger structure such as board-like.
Beneficial effect of the present invention:
1. the cold that the heat of gas recovery is converted to water at low temperature by the present invention is cooled to 22 ~ 23 DEG C coal gas, the temperature of self is reduced with the energy of coal gas self, there is efficiency high, invest little, the advantage that working cost is low, realizes continuous, efficient, the coupling utilization of waste heat of coke oven crude gas warming, cooling in summer; Refrigeration of the present invention adopts water at low temperature part directly to evaporate reduction temperature and obtains chilled water, compared with evaporating indirect heat exchange with the water as refrigerant of prior art, compact equipment, heat exchange efficiency is high, is widely used in coal gas cooling and the coal gas heat recovery of coking chemical enterprise and gasification enterprise.
2. coal gas high-temperature section waste heat is directly used in heating and cooling absorbing medium, thermal efficiency ratio coal gas waste-heat hot water, and the indirect heat exchange mode thermo-efficiency that hot water reheats refrigerant charge medium improves more than 20%;
3. coal gas and absorbing medium heat exchange adopt efficient convergent-divergent heat transfer tube, and heat exchange efficiency improves more than 15% than common heat transfer tube;
4. the heat recovering process of coke-oven gas is also the process of cooling of coal gas simultaneously, and the conversion of heat and cold and the cooling of coal gas are all integrated in a device, compact construction, and thermo-efficiency is high;
5. refrigeration adopts water at low temperature part directly to evaporate the method for reduction temperature acquisition chilled water, and than the method for existing water as refrigerant evaporation indirect heat exchange, efficiency is higher and decrease an indirect type water cooler, reduces equipment manufacturing cost.
6. the interface that vacuumizes at absorptive condenser top is provided with W type vapour liquid separator, is coordinated by gas phase baffling passage, and strengthening gas-liquid separation effect, prevents entrainment.
7. coal gas heat recuperation water cooler, absorptive condenser adopt shaped telescopic tube efficient heat-exchanging pipe, and being both conducive to absorption outside heat transfer tube also can cooling heat transferring in enhanced tube; Double helix heat exchange pipe improves the heat transfer tube that condenser occurs and adopts heat transfer efficiency.
8. absorb vaporizer, absorptive condenser, generation condenser, the liquid level of vaporizer occurs controlled by automatic liquid level regulating device, regulation and control precisely, reliability and efficiency high.
Accompanying drawing explanation
Fig. 1 is the structural representation of invention.
Embodiment
In order to understand the present invention better, explain embodiments of the present invention in detail below in conjunction with accompanying drawing.
As shown in drawings, in figure: 1. gas inlet, 2. coal gas heat recuperation water cooler, 3. coal gas water recirculator, 4. gas refrigeration watercooler, 5. gas exit, 6. solution circulation pump, 7. chilled water recycle pump, 8. vacuum pump, 9. absorptive condenser, 10. absorb vaporizer, 11. solution heat exchangers, the fluid-tight of 12.U shape pipe, 13. automatic liquid level regulating devices, 14. there is vaporizer, 15. there is condenser, 16. pressure regulator valves, 17. control instrumentss, 18. coal gas water recirculator circulating water intakes, 19. coal gas water recirculator circulating water outlets, 20. there is condenser cooling water import, 21. there is condenser cooling water outlet, 22. absorb evaporator cools water inlet, 23. absorb evaporator cools water out, 24. water at low temperature supplement mouth, 25. intermediate conduit.
A kind of from the preliminary refrigerating unit of refrigeration mode coal oven dithio-gas, comprise the coal gas heat recuperation water cooler 2 connected successively from top to bottom, coal gas water recirculator 3, gas refrigeration watercooler 4, described coal gas heat recuperation water cooler 2 top is provided with gas inlet 1, coal gas water recirculator 3 is provided with circulating cooling water inlet 18, circulating cooling water out 19, gas refrigeration watercooler 4 bottom is provided with gas exit 5, absorbent solution is passed in the heat transfer tube of coal gas heat recuperation water cooler 2, recirculated water is passed in coal gas water recirculator 3 heat transfer tube, chilled water is passed in the heat transfer tube of gas refrigeration watercooler 4, raw gas enters successively through coal gas heat recuperation water cooler 2 from gas inlet 1, coal gas water recirculator 3, the cavity of the heat transfer tube outside of gas refrigeration watercooler 4 is flowed out from gas exit 5 by after the medium cooling in heat transfer tube.Heat recuperation water cooler 2 of the present invention, coal gas water recirculator 3, gas refrigeration watercooler 4 is tube shell type structure, walk coal gas outside pipe and be in turn connected into an entirety from top to bottom, raw gas temperature after ammoniacal liquor directly sprays of coke oven collecting main is reduced to 83 ~ 82 DEG C, and raw gas enters from gas inlet 1 and flowed out from gas exit 5 by after the medium cooling in heat transfer tube through the heat transfer tube of described three equipment successively.
The liquid outlet of described coal gas heat recuperation water cooler 2 is connected with generation vaporizer 14 by pipeline, coal gas heat recuperation water cooler 2 absorbent solution enters generation vaporizer 14 by pipeline after by heated by gas (also cooling coal gas) simultaneously, there is vaporizer 14 and become an entirety with generation condenser 15 by gas phase baffling combination of channels, occur to be connected with absorption vaporizer 10 by pipeline bottom condenser 15.The part water vapor that absorbent solution evaporates at generation vaporizer 14 enters generation condenser 15 by gas phase baffling passage, there is condenser 15 top and be provided with high efficiency cooling heat transfer tube, recirculated cooling water enters in cooling tube by there is condenser cooling water import 20, flow out from generation condenser cooling water outlet 21 after the water vapour of vaporizer 14 generation occurs in cooling, water vapor condensation Cheng Shuihou enters and occurs bottom condenser 15, by the bottom of pipeline self to absorption vaporizer 10.Occur to enter through the absorption agent strong solution of part evaporation in vaporizer 14 to occur bottom vaporizer 14.Gas phase baffling passage, as the connecting passage absorbing vaporizer and absorptive condenser, plays gas liquid separating function simultaneously.The hot side medium entrance of solution heat exchanger 11 to be exported with the absorbent solution occurred bottom vaporizer 14 by U-shaped pipe fluid-tight 12 and is connected, and the hot side medium outlet of solution heat exchanger 11 is connected with the absorption agent strong solution import of absorptive condenser 9 top; Solution heat exchanger 11 cold side medium entrance is exported with solution circulation pump 6 and is connected by pipeline, and solution heat exchanger 11 cold side media outlet is connected with the tube side absorbent solution import in the heat transfer tube of coal gas heat recuperation water cooler 2.Solution heat exchanger 11 can be shell-and-tube or the efficient heat-exchanger type formula such as board-like.
Absorb vaporizer 10 and become an entirety with absorptive condenser 9 by gas phase baffling combination of channels, described absorptive condenser 9 top is provided with circulating water heat transfer tube, circulating water heat transfer tube comprises circulating cooling water inlet 22, circulating cooling water out 23, recirculated water is passed in circulating water heat transfer tube, the top subcooling water inlet of described absorption vaporizer 10 exports with gas refrigeration watercooler 4 water at low temperature and is connected, outlet bottom absorptive condenser 9 is connected with solution circulation pump 6 import by pipeline, and the liquid outlet of solution circulation pump is connected with solution heat exchanger 11.After the water at low temperature of gas refrigeration watercooler 4 evaporates part water vapour after entering into and absorbing vaporizer 10 top, temperature reduction enters and absorbs bottom vaporizer 10, the water vapour evaporated is entered in the middle part of absorptive condenser 9 by gas phase baffling passage, upwards absorbed by the absorption agent strong solution that top is sprayed, absorb liberated heat and taken away by the recirculated water in the heat transfer tube of absorptive condenser 9 top.The absorption agent dilute solution absorbing water vapour enters into bottom absorptive condenser 9, is connected, from outlet removes solution heat exchanger 11 after being pressurizeed by solution circulation pump through outlet at bottom by pipeline with solution circulation pump 6 import.
Described absorption vaporizer 10, absorptive condenser 9, generation vaporizer 14 are connected with vacuum pump 8 respectively by pipeline with generation condenser 15, the extraction pipe of vacuum pump 8 is connected with the interface that vacuumizes absorbing vaporizer 10 top, the water-in of chilled water recycle pump 7 is connected with the 16 DEG C of chilled water water outlets absorbed bottom vaporizer 10, and water outlet is connected with the water-in of the heat transfer tube of gas refrigeration watercooler 4.Absorbing vaporizer 10, absorptive condenser 9, vaporizer 14 occurring and condenser 15 occurs is high-vacuum apparatus, vacuum is realized by vacuum pump 8, the extraction pipe of vacuum pump 8 is connected with the interface that vacuumizes absorbing vaporizer 10 top, gas leakage in draw-out device operational process, and the non-condensable gas produced, the condition of high vacuum degree of assurance device vacuum area.Absorption vaporizer 10 supplements mouth 24 with water at low temperature and is connected with supplementary chilled water.
Gas-phase space in the middle part of described absorption vaporizer 10 has intermediary interface, there is condenser 15 top and be provided with exhaust port, intermediary interface is connected by intermediate conduit 25 with exhaust port, described intermediate conduit 25 is provided with the pressure difference absorbed between vaporizer 10 and absorptive condenser 9 and pressure regulator valve 16, the control instruments 17 that the pressure difference between condenser 14 and generation vaporizer 15 detects and regulate occurs, so that to absorption vaporizer 10 and absorptive condenser 9, and the pressure difference occurred between condenser 14 and generation vaporizer 15 detects in real time and regulates.The interface that vacuumizes at described absorptive condenser 9 top is provided with W type vapour liquid separator, is coordinated by gas phase baffling passage, and strengthening gas liquid separating function, prevents entrainment.
The bottom of described absorption vaporizer 10, absorptive condenser 9, generation condenser 15, generation vaporizer 14 is provided with automatic liquid level regulating device 13, and the liquid level absorbed bottom vaporizer 10, absorptive condenser 9, generation condenser 15, generation vaporizer 14 is controlled by automatic liquid level regulating device 13.
Described coal gas heat recuperation water cooler 2, absorptive condenser 9 adopt shaped telescopic tube efficient heat-exchanging pipe.Both being conducive to absorption outside heat transfer tube also can cooling heat transferring in enhanced tube.The heat transfer tube of described generation condenser 15 adopts double helix heat exchange pipe, the heat transfer efficiency outside enhanced tube and in pipe.
Principle of work of the present invention and working process:
After being reduced to 83 ~ 82 DEG C from the raw gas temperature directly sprayed through ammoniacal liquor of coke oven collecting main, coal gas heat recuperation water cooler 2 is entered from the gas inlet 1 at self-control cold-pressed briquette air cooling device top, flow from top to bottom in space outside heat transfer tube, with the heat exchange of heat transfer tube inner absorbent dilute solution, the temperature of absorption agent dilute solution is elevated to 75 DEG C from 60 DEG C, gas temperature is reduced to about 76 DEG C from 83 DEG C, the pressure of coal gas side is-0.005MPa, absorption agent dilute solution pressure 0.2MPa, heat transfer tube adopts the stainless efficient convergent-divergent heat transfer tube of material S30408, by rounded projections arranged.
Raw gas enters coal gas water recirculator 3 after the heat exchange of coal gas heat recuperation water cooler 2, temperature from 76 DEG C be reduced to ~ 45 DEG C, finally enter gas refrigeration watercooler 4, continue to be cooled to the chilled water heat exchange in heat transfer tube ~ 22 DEG C, go to follow-up workshop section to carry out gas purification and chemical products recovery from gas exit 5.
Chilled water recycle pump 7 extracts and absorbs 16 DEG C of chilled water bottom vaporizer 10, is pressed and delivered in the heat transfer tube of gas refrigeration watercooler 4, after coal gas heat exchange outside chilled water and heat transfer tube, temperature is elevated to 23 DEG C and enters and absorb vaporizer 10, the high vacuum lower part evaporation releases heat being-0.098MPa at pressure makes temperature be reduced to 16 DEG C, flow back to absorption base of evaporator, cooled water-circulating pump extracts and pressurizes and sends to cooling coal gas again, circulates and so forth.
Absorbing after the water vapour evaporated in vaporizer 10 goes out by gas phase baffling channel separation the water droplet carried secretly in water vapour enters in the middle part of absorptive condenser 9, by the dense absorbent solution from top spray in the outer membranaceous absorption of condensing heat-exchange, absorb the heat produced and absorbed by the recirculated water in heat transfer tube.
The pressure of absorptive condenser is-0.098MPa, dense absorbent solution inlet temperature is 45 DEG C, dilute solution is become after the water vapour of dense absorbent solution absorption refrigeration water section evaporation, dilute solution is pressed and delivered in solution heat exchanger by solution pump 6 carries out heat exchange with the dense absorbent solution that vaporizer 14 occurs, the temperature of strong solution turnover solution heat exchanger is 67 DEG C-46 DEG C, the temperature of dilute solution turnover solution heat exchanger is 38 DEG C-60 DEG C, dilute solution enters in the heat transfer tube of coal gas heat recuperation water cooler 2 after heat exchange, heated by the coal gas of high temperature outside heat transfer tube, coal gas of high temperature obtains cooling simultaneously.
The dilute solution being heated to 75 DEG C by coal gas of high temperature enters generation vaporizer 14, be evaporate under the high vacuum of-0.093MPa at pressure, strong solution is become after moisture in dilute solution is evaporated, strong solution to be sprayed on condensing heat-exchanging pipe outer wall to absorptive condenser through solution heat exchanger and to form liquid film, absorbing flows in absorptive condenser liquid capsule by becoming dilute solution after the water vapour outside heat transfer tube, then again extracted out by solution circulation pump 6, circulate and so forth, the heat of coal gas of high temperature is constantly recovered and is converted into the cold needed for refrigeration, coal gas is cooled simultaneously.
Dilute solution enters into the middle part that condenser 15 occurs after the water droplet that gas phase baffling channel separation is carried secretly at the water vapor occurring to evaporate in vaporizer, flow automatically to absorption base of evaporator after being recycled water condensation.
The evaporation of chilled water and absorbent solution and absorption complete under high vacuum state, high vacuum relies on vacuum pump 8 to realize, the gas-phase space absorbing vaporizer 10 and absorptive condenser 9 communicates, two equipment are arranged on a housing inner-use clapboard separately, pressure is-0.098MPa, condenser 15 occurs and vaporizer 14 gas-phase space occurs to communicate, two equipment are arranged on a housing inner-use clapboard separately, and pressure is-0.093MPa.
The setting of generation condenser 15 top is vacuumized interface and is connected with gas-phase space in the middle part of absorptive condenser 10 by pipeline, and vacuum pump vacuumizes the condition of high vacuum degree of the non-condensable gas assurance device vacuum area of gas leakage and generation interface draw-out device operational process from absorptive condenser 10 top.
By reference to the accompanying drawings the embodiment of invention is described although above-mentioned; but not limiting the scope of the invention; on the basis of technical scheme of the present invention, those skilled in the art do not need to pay various amendment or distortion that creative work can make still within protection scope of the present invention.
Claims (7)
1. one kind from the preliminary refrigerating unit of refrigeration mode coal oven dithio-gas, it is characterized in that, comprise the coal gas heat recuperation water cooler connected successively from top to bottom, coal gas water recirculator, gas refrigeration watercooler, described coal gas heat recuperation water cooler top is provided with gas inlet, coal gas water recirculator is provided with circulating cooling water inlet, circulating cooling water out, gas refrigeration watercooler bottom is provided with gas exit, absorbent solution is passed in the heat transfer tube of coal gas heat recuperation water cooler, recirculated water is passed in coal gas water recirculator heat transfer tube, chilled water is passed in the heat transfer tube of gas refrigeration watercooler, the liquid outlet of described coal gas heat recuperation water cooler is connected with generation vaporizer by pipeline, there is vaporizer and become an entirety with generation condenser by gas phase baffling combination of channels, occur to be connected with absorption vaporizer by pipeline bottom condenser, the absorbent solution outlet that base of evaporator occurs is connected with the hot side medium entrance of solution heat exchanger by the fluid-tight of U-shaped pipe, the hot side medium outlet of solution heat exchanger is connected with the absorption agent strong solution import of absorptive condenser top, solution heat exchanger cold side medium entrance is connected by pipeline with solution circulated pump discharge, and solution heat exchanger cold side media outlet is connected with the tube side absorbent solution import in the heat transfer tube of coal gas heat recuperation water cooler, absorb vaporizer and become an entirety with absorptive condenser by gas phase baffling combination of channels, described absorptive condenser top is provided with circulating water heat transfer tube, recirculated water is passed in circulating water heat transfer tube, the top subcooling water inlet of described absorption vaporizer exports with gas refrigeration watercooler water at low temperature and is connected, outlet bottom absorptive condenser is connected with solution circulated pump inlet by pipeline, and the liquid outlet of solution circulation pump is connected with solution heat exchanger, described absorption vaporizer, absorptive condenser, generation vaporizer, generation condenser are connected with vacuum pump respectively by pipeline, the extraction pipe of its intermediate pump is connected with the interface that vacuumizes absorbing vaporizer top, the 16 DEG C of chilled water water outlets absorbing base of evaporator are connected with the water-in of chilled water recycle pump, and the water outlet of chilled water recycle pump is connected with the water-in of the heat transfer tube of gas refrigeration watercooler.
2. as claimed in claim 1 from the preliminary refrigerating unit of refrigeration mode coal oven dithio-gas, it is characterized in that, gas-phase space in the middle part of described absorption vaporizer has intermediary interface, there is condenser overhead and be provided with exhaust port, intermediary interface is connected by intermediate conduit with exhaust port, and described intermediate conduit is provided with the pressure difference absorbed between vaporizer and absorptive condenser and pressure regulator valve, the control instruments that the pressure difference between condenser and generation vaporizer detects and regulate occurs.
3. as claimed in claim 1 from the preliminary refrigerating unit of refrigeration mode coal oven dithio-gas, it is characterized in that, the interface that vacuumizes at described absorptive condenser top is provided with W type vapour liquid separator.
4. as claimed in claim 1 from the preliminary refrigerating unit of refrigeration mode coal oven dithio-gas, it is characterized in that, the bottom of described absorption vaporizer, absorptive condenser, generation condenser, generation vaporizer is provided with automatic liquid level regulating device.
5. as claimed in claim 1 from the preliminary refrigerating unit of refrigeration mode coal oven dithio-gas, it is characterized in that, described coal gas heat recuperation water cooler, absorptive condenser adopt shaped telescopic tube efficient heat-exchanging pipe.
6. as claimed in claim 1 from the preliminary refrigerating unit of refrigeration mode coal oven dithio-gas, it is characterized in that, the heat transfer tube of described generation condenser adopts the double helix heat exchange pipe that heat transfer efficiency is high.
7. as claimed in claim 1 from the preliminary refrigerating unit of refrigeration mode coal oven dithio-gas, it is characterized in that, described solution heat exchanger adopts shell-and-tube or plate-type heat exchanger structure.
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| JPS6420293A (en) * | 1987-07-14 | 1989-01-24 | Maekawa Seisakusho Kk | Dehydration method for city gas or the like |
| CN1209450A (en) * | 1997-08-21 | 1999-03-03 | 鞍山钢铁集团公司 | Gas-recovering technical apparatus of using after heat refrigerating to supply low-temp. water to gas primary cooler |
| CN101619243A (en) * | 2009-07-29 | 2010-01-06 | 马鞍山钢铁股份有限公司 | Gas naphthalene washing process in primary-cooling working procedure of coke oven gas purification unit |
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| CN101870882A (en) * | 2010-04-28 | 2010-10-27 | 大庆油田有限责任公司 | Shale oil condensation recycling water-washing process system and operation method |
| CN103484169A (en) * | 2013-10-30 | 2014-01-01 | 北京中亿孚佑科技有限公司 | New method for performing preliminary condensation refrigeration on coking raw gas |
| CN104031692A (en) * | 2014-06-05 | 2014-09-10 | 大连理工大学 | Device and method for preparing process heat medium water by directly quenching coking raw coke oven gas at high temperature |
| CN104214990A (en) * | 2014-08-20 | 2014-12-17 | 河南中鸿集团煤化有限公司 | Raw coke oven gas sensible heat recovery cold water preparing system and raw coke oven gas sensible heat recovery cold water preparing method |
| CN204417445U (en) * | 2015-01-30 | 2015-06-24 | 济南冶金化工设备有限公司 | From the preliminary refrigerating unit of refrigeration mode coal oven dithio-gas |
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| CN104629816B (en) | 2016-09-28 |
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Denomination of invention: Self-made preliminary cooling device for raw gas of cold type coke oven Effective date of registration: 20230317 Granted publication date: 20160928 Pledgee: Postal Savings Bank of China Limited Jinan Changqing District sub branch Pledgor: JINAN METALLURGY CHEMICAL EQUIPMENT CO.,LTD. Registration number: Y2023980035136 |
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