CN203240840U - Energy saving system integrated by conversion section waste heat recovery and rectisol process refrigeration station - Google Patents
Energy saving system integrated by conversion section waste heat recovery and rectisol process refrigeration station Download PDFInfo
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- CN203240840U CN203240840U CN2013202173487U CN201320217348U CN203240840U CN 203240840 U CN203240840 U CN 203240840U CN 2013202173487 U CN2013202173487 U CN 2013202173487U CN 201320217348 U CN201320217348 U CN 201320217348U CN 203240840 U CN203240840 U CN 203240840U
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Abstract
The utility model relates to an energy saving system integrated by a conversion section waste heat recovery and rectisol process refrigeration station. The energy saving system comprises a first level propylene compressor (C1), a second level propylene compressor (C2), a propylene water cooler (E1), a propylene subcooler (NEW1), a heat exchanger (NEW2) and a separator (S1) which are sequentially connected. The bottom of the separator (S1) is connected with the first level propylene compressor (C1) through an evaporator system (E2), and the top of the separator (S1) is connected with the second level propylene compressor (C2). The propylene subcooler (NEW1) is communicated with a bromine cooling machine system (B1) to achieve heat exchange. A heat source of the bromine cooling machine system is from surplus low-pressure steam in the former working section, namely a conversion section, of a rectisol process. Heat exchange is conducted on the propylene subcooler and the bromine cooling machine system, heat is provided for the bromine cooling machine system, cooling capacity is obtained at the same time, and the refrigerating efficiency of refrigeration circulation is effectively improved.
Description
Technical field
The utility model relates to refrigeration and waste heat utilization technology field, relates in particular to the integrated energy conserving system of a kind of conversion section Waste Heat Recovery and low-temp methanol washing process refrigeration station.
Background technology
Low-temp methanol washing process is a kind of gas purifying technique.This technique utilizes methyl alcohol at low temperatures to the great good characteristic of sour gas solubility take cold methanol as lyosoption, removes the sour gas in the unstripped gas.Because the irreversibility of absorption, desorb and heat transfer process, and pump certain temperature rise of meeting generation in course of conveying, therefore, low-temp methanol washing process needs outer for cold.
Fig. 1 is the process chart of existing low-temperature rectisol.Its technological process is as follows:
The 5.4MPa that the transformation into itself comes, 40 ℃ conversion gas 1 converge with the circulating air 2 that flashed vapour compressor C3001 sends here, for preventing that conversion gas is cooled to the icing phenomenon of appearance below freezing, spray into the poor methanol liquid 23 of 1303kg/h, then be cooled to-20.15 ℃ through unstripped gas heat exchanger E3001 and purified gas 4, carbon dioxide 5, tail gas 6 heat exchange, after separator V3001 isolated methanol aqueous solution, dry unstripped gas entered Methanol Wash Column T3001 again.
Methanol Wash Column T3001 divides up and down two parts, and lower tower section is mainly used in desulfurization, and upper tower section can be divided into again three sections: the top section is fine wash sections, with-54.99 ℃, the poor methanol stream gang 24 a small amount of CO that come to remain in the absorption of gases of 358906kg/h
2And H
2S is with CO in the purified gas 4 of guaranteeing the downstream
2≤ 3%, H
2S≤0.1ppm; Middle two sections is CO
2Absorber portion is used the fine wash sections cleaning solution 31 after recycle methanol cooler E3006 heat exchange, enters CO under-35.75 ℃
2CO in the absorber portion absorption of gases
2CO
2The efflux 30 of absorber portion is back to CO after 3# methyl alcohol chiller E3005, recycle methanol cooler E3006 cooling
2CO in the absorber portion absorption of gases
2About 52% methyl alcohol rich solution 25 takes out from upper tower bottom tower tray, in methyl alcohol cooler E3017 and purified gas 4 heat exchange, be cooled to-31.65 ℃ through 2# methyl alcohol chiller E3004 again, enter 2# circulating air flash tank V3003 through reducing to 1850kPa, make the most of H that is dissolved in the methanol solution
2Steam.
Only need go up tower during lower tower desulfurization and absorb CO
2The part methanol solution, its amount is about 48% of total amount, the methanol solution 26 that comprises whole sulphur after lower tower washing flows out from Methanol Wash Column T3001 tower bottom, respectively in heat exchange of methanol device E3007,1# methyl alcohol chiller E3003 heat exchange cooling, after being decompressed to 1850kPa, enter 1# circulating air flash tank V3002, make the most of H that is dissolved in the methanol solution
2Flash distillation out.1# circulating air flash tank V3002 and 2# circulating air flash tank V3003 flash distillation H out
2By recycle gas compressor C3001, pressure-raising is cooled to-40 ℃ to the compressed machine water cooler of 5560kPa E3002, sends back on the unstripped gas pipeline of entrance to recycle.
That draws from 2# circulating air flash tank V3003 bottom contains CO
2The methanol solution 32 of sulfur-bearing not, through throttling expansion, pressure drops to 0.29MPa, enters CO
2Analytic Tower T3002 top of tower flashes off most of CO
2Gas, a part is as CO
2The phegma 37 on Analytic Tower T3002 top, a part is as H
2The phegma 36 on S concentration tower T3003 top.
The sulfur-bearing and the CO that draw from 1# circulating air flash tank V3002 bottom
2Methanol solution 33, through throttling expansion, pressure drops to 0.35MPa, enters CO
2The 8th column plate place, Analytic Tower T3002 middle part, at this, part CO
2And H
2S parses from methanol solution, and methanol solution 38 is sent into H
2S concentration tower T3003 flashes off part CO
2And H
2S obtains rich methanol liquid 34 by pressure-raising, enter methyl alcohol flash tank V3007 and separate through 3# poor methanol cooler E3008, recycle methanol cooler E3006 successively, liquid part 35 is gone heat exchange of methanol device E3007 heat exchange through pressurization again, and then flashed vapour 13, liquid part 35 enter CO simultaneously
2Tower under the Analytic Tower T3002 tower is raised to-28.88 ℃ by-63.13 ℃ because advancing tower methanol solution temperature, along with the rising of temperature, CO
2Solubility in methyl alcohol reduces, at CO
2Tower parses a large amount of CO under the Analytic Tower T3002
2From CO
2The methanol solution 39 of Analytic Tower T3002 bottom enters H
2Behind the S concentration tower T3003 tower middle part, further gone out CO by low-pressure nitrogen 15 air lifts
2, this part CO
2In company with air lift nitrogen and CO
2The carbon dioxide 5 of Analytic Tower T3002 tower overhead gas reclaims cold through unstripped gas heat exchanger E3001 together.Crouse's hydrogenation tail gas 14 enters H
2At the bottom of the S concentration tower T3003 tower.H
2S concentration tower T3003 bottom methanol solution 41 temperature be-43.46 ℃, through pressurizeing, enter successively 2# poor methanol cooler E3009 and 1# poor methanol cooler E3010 temperature is elevated to 87.4 ℃, then enter on the 26th block of column plate of the hot regenerator T3004 of methyl alcohol.Be dissolved in the whole H in the methanol solution
2S, CO
2Be reproduced tower reboiler E3011 and add thermogenetic methanol steam air lift, methanol steam 22 air lifts that distilled out by methanol-water/knockout tower T3005 cat head simultaneously.Out sour gas of heating is carried the sour gas/methyl alcohol 16 of part methanol steam secretly and is drawn by cat head, after sour gas water cooler E3012 cooling, most of methanol vapor is condensed, isolate methanol condensed liquid 42 as phegma through backflow flow container V3006, send back to the hot regenerator T3004 of methyl alcohol top of tower, leave the rich sulphur steam 17 at backflow flow container V3006 top, at H
2By precooling, then in the sour gas chiller E3013 of the hot regenerator of methyl alcohol, further cool off among the S cut heat exchanger E3014.At this, nearly all methanol steam all is condensed, and separates through sour gas separator V3005 again, and condensate liquid 40 is delivered to H
2S concentration tower T3003 tower bottom is processed, and sour gas 18 parts are circulated to H
2On the 25th block of column plate of S concentration tower T3003, part is through H
2S cut heat exchanger E3014 delivers to out-of-bounds sulfur recovery after reclaiming cold.
Take out regenerated methanol 43 from the hot regenerator T3004 of methyl alcohol bottom, deliver to methyl alcohol collecting tank V3004 after in 1# poor methanol cooler E3010, being cooled, then be pressurized to 6.5MPa, after methanol-water cooler E3018 cooling, except a small amount of conduct spray methyl alcohol, all the other deliver to Methanol Wash Column T3001 top of tower as the fine wash sections cleaning solution after 2# poor methanol cooler E3009,3# poor methanol cooler E3008 are cooled to-54.99 ℃.
The methanol/water 27 of coming from separator V3001 among methanol/water knockout tower feed heater E3016 with by methyl alcohol at the bottom of the hot regenerator T3004 tower through cooled poor methanol 45 heat exchange, temperature rises on 60.80 ℃ of the 21st block of column plates that enter methanol/water knockout tower T3005 tower through methanol/water knockout tower charging separator V3008, simultaneously, after washings 51 pressurizations behind the washing tail gas, heat up in water-to-water heat exchanger E3019 and deliver on the 13rd block of column plate of methanol-water/knockout tower T3005 tower, their common participations are distilled.Tower bottom steam is produced by methanol/water knockout tower reboiler E3015 heat exchange, methanol steam is directly sent into the hot regenerator T3004 of methyl alcohol after 51 column plate distillations, and delivers to methanol-water/knockout tower T3005 top as phegma by the cooled poor methanol 45 of methanol-water/knockout tower feed heater E3016.Waste water 49 at the bottom of the tower is disposed to Waste Water Treatment reclaim heat in water-to-water heat exchanger E3019 after, and its discharge capacity is 2277kg/h.
At present, the supporting refrigeration station refrigerating method of low-temp methanol washing process mainly contains propylene compression refrigeration, ammonia compression refrigeration, ammonia absorption refrigeration, ammonia compression absorption hybrid refrigeration etc.If for the production of synthetic ammonia, suggestion selects ammonia to make cold-producing medium, otherwise recommends to make cold-producing medium with propylene.The cryogenic temperature of propylene can reach-40 ℃, is that ammonia institute is inaccessiable under the normal pressure.In addition, the compressor inlet of propylene is malleation, and the design of compressor is also more convenient.
The load of the compressor of the supporting propylene of existing low-temp methanol washing process refrigeration station is high, and the load of propylene water cooler is also higher, and the propylene consumption is large.
Conversion section is because a lot of low-pressure steams of overheated generation, this part low-pressure steam can become high-quality steam continuation utilization by increasing waste heat boiler, even if like this, the low-pressure steam that conversion section produces in actual factory is along with the conversion fluctuation in season is larger, so be difficult to this part inferior thermal source is utilized.
The basic structure of bromine cooling machine (lithium bromide refrigerator) as shown in Figure 4.Lithium bromide refrigerator is take steam as thermal source, and lithium-bromide solution is absorbent, take water as cold-producing medium, has the refrigeration machine of second generation process and an absorption process.Its detailed operation principle can be published in reference to Yang Weirong " Guangdong chemical industry " the 5th phase of the 36th volume in 2009 " structure of lithium-bromide absorption-type refrigerating machine and principle ".On engineering, the used heat energy of bromine cooling machine is generally the inferior heat energy such as industrial waste heat, waste heat, solar energy, and can use the diversified energy forms such as natural gas, coal gas, is a kind of energy-saving equipment.
The utility model content
The purpose of this utility model is to provide a kind of new conversion section Waste Heat Recovery and low-temp methanol washing process refrigeration station integrated energy conserving system, endothermic effect is realized refrigeration when namely adopting the propylene liquid gasification, for low-temp methanol washing process provides enough colds, simultaneously can with the heat exchange of bromine cooling machine system, for it provides heat and obtains cold.
Propylene liquid gasifies in evaporator system provides cold, constantly carries out in order to make evaporation process, needs constantly to extract steam out from evaporator system, constantly liquid is replenished into again.Make at normal temperatures condensation of steam, then need steam pressure is brought up to saturation pressure under the normal temperature, this has just realized that refrigeration working medium evaporates under low-temp low-pressure, produce refrigeration effect and condensation under HTHP, outwards emits heat.Liquid gasification refrigeration by gasify, boost, condensation, step-down Four processes form, propylene compression refrigeration circulates and continuous provides cold to low-temp methanol washing process.
For reaching this purpose, the utility model by the following technical solutions:
The energy conserving system that a kind of conversion section Waste Heat Recovery and low-temp methanol washing process refrigeration station are integrated, described system comprises one-level propylene compressor, secondary propylene compressor, propylene water cooler, propylene subcooler, heat exchanger and the separator that connects successively, the bottom of described separator connects the one-level propylene compressor by evaporator system, and described separator top connects the secondary propylene compressor; Described propylene subcooler and bromine cooling machine system connectivity realize heat exchange.
System described in the utility model comprises one-level propylene compressor, secondary propylene compressor, propylene water cooler, propylene subcooler, heat exchanger, separator and evaporator system; Described one-level propylene compressor connects the secondary propylene compressor, the secondary propylene compressor connects the propylene water cooler, the propylene water cooler connects the propylene subcooler, the propylene subcooler connects heat exchanger, described heat exchanger connects separator, the bottom of described separator is by evaporator system access one-level propylene compressor, and the secondary propylene compressor is accessed at described separator top; Described propylene subcooler and bromine cooling machine system connectivity realize heat exchange.
In the utility model, the bottom of described separator is by evaporator system access one-level propylene compressor, and the top of described separator and one-level propylene compressor together enter the secondary propylene compressor.
After entering the pressurization of one-level propylene compressor from the propylene steam of evaporator system, together enter the pressurization of secondary propylene compressor with the gas phase from separator, enter propylene water cooler, propylene subcooler after the compression, enter and enter separator after heat exchanger reduces the gas phase fraction, isolated liquid phase enters evaporator system evaporation gasification.In said process, propylene subcooler and bromine cooling machine system realize heat exchange, and system provides heat for bromine cooling machine, and the propylene liquid in the propylene subcooler obtains corresponding cold.
Evaporator system described in the utility model is for low-temp methanol washing process provides cold, is respectively: ammonia cooler, middle part, absorption tower ammonia cooler, middle part, absorption tower phegma ammonia cooler, hot regenerator cat head chiller at the bottom of the absorbing tower.
Heat exchanger described in the utility model is the heat exchanger of connecting with hot regenerator cat head chiller, and hot regenerator cat head chiller load is 423KW in the former technique, and the heat exchanger afterload of the present utility model of connecting becomes 177KW, and residue 246kW cold is provided by heat exchanger.It is the variation of hot regenerator cat head chiller load that the front and back of evaporator system described in the utility model change.
The utility model is to have increased propylene subcooler and heat exchanger with respect to the difference of prior art maximum, and propylene subcooler and bromine cooling machine system connectivity realization heat exchange, and bromine cooling machine utilizes the waste hot steam of conversion section.The design of propylene subcooler and heat exchanger can reduce the load of propylene compressor and propylene water cooler cooling water, and the consumption of propylene is reduced, and the more important thing is so that compressor load reduces.In addition, the propylene subcooler by with the heat exchange of bromine cooling machine system, system provides heat for bromine cooling machine, obtains simultaneously cold, Effective Raise the refrigerating efficiency of kind of refrigeration cycle.What the thermal source of bromine cooling machine used is the low-pressure steam more than needed of the previous workshop section-conversion section of low-temp methanol washing process, has realized the recycling of low-quality thermal source.
The shell side entrance of propylene subcooler described in the utility model is communicated with the outlet of the shell side of propylene water cooler, and the shell side outlet of described propylene subcooler is communicated with the shell side entrance of heat exchanger; Passing into the water of bromine cooling machine system in the tube side of described propylene subcooler, is propylene liquid in the shell side.The tube side entrance of described propylene subcooler is communicated with the choke valve of bromine cooling machine system, and outlet is communicated with the absorber of bromine cooling machine system.
The shell side outlet of heat exchanger described in the utility model is communicated with separator; Pass in the tube side of described heat exchanger in the low-temp methanol washing process from the isolated rich sulphur steam of backflow flow container.In heat exchanger, the isolated rich sulphur steam of the backflow flow container at the hot regenerator of methyl alcohol top carries out heat exchange in propylene liquid and the low-temp methanol washing process.
The shell side entrance of evaporator system described in the utility model is communicated with the bottom of separator, and the shell side outlet of described evaporator system is communicated with one-level propylene compressor entrance.Pass into the CO of Methanol Wash Column in the low-temp methanol washing process in the shell side of described evaporator system
2The absorber portion efflux.In evaporator system, from the liquid phase (propylene liquid) of separator bottom and the CO of Methanol Wash Column
2Absorber portion efflux (methanol solution) carries out heat exchange, and in heat transfer process, propylene liquid obtains gasification, and the endothermic effect during owing to gasification is CO
2Absorber portion efflux (methanol solution) provides cold, realizes refrigeration.
Be provided with the first throttle valve between propylene subcooler described in the utility model and the heat exchanger.Be provided with the second choke valve between the bottom of separator described in the utility model and the evaporator system.The effect of first throttle valve and the second choke valve all is to make the further step-down of flow of propylene thigh.
Described bromine cooling machine system comprises absorber, evaporimeter, choke valve, the condenser that connects successively, wherein, replace described evaporimeter with described propylene subcooler, make the tube side of described propylene subcooler (NEW1) as the part in bromine cooling machine system (B1) circulation line.
The tube side entrance of described propylene subcooler is communicated with the outlet of the choke valve of bromine cooling machine system, and the tube side outlet of described propylene subcooler is communicated with the absorber entrance of bromine cooling machine system.
One-level propylene compressor described in the utility model and secondary propylene compressor adopt 2.5Mpa(G), 380 ℃ superheated steam driving steam turbine.
Compare with the prior art scheme, the utlity model has following beneficial effect:
The utility model is to utilize the waste hot steam of conversion section as the thermal source of bromine cooling machine, for the low-temp methanol washing process refrigerating plant provides above zero cold, improves the refrigerating efficiency of kind of refrigeration cycle.
The utility model has increased propylene subcooler and heat exchanger, and propylene subcooler and bromine cooling machine system connectivity are realized heat exchange.The design of propylene subcooler and heat exchanger can reduce the load of propylene compressor and propylene water cooler cooling water, and the consumption of propylene is reduced.In addition, the propylene subcooler by with the heat exchange of bromine cooling machine system, system provides heat for bromine cooling machine, obtains simultaneously cold, has realized the refrigeration with propylene liquid of taking full advantage of of heat, thereby provides enough colds for low-temp methanol washing process.The installation of heat exchanger is for different refrigeration ranks is provided, so that kind of refrigeration cycle energy-saving more.
Because compressor adopts 2.5Mpa(G), 380 ℃ superheated steam driving steam turbine, can significantly reduce the enterprise operation expense so reduce the load of compressor.
Take 600,000 ton/years of coal gasification methanol projects processed as support, has 5t/h at least in that actual device is in service, 0.3Mpa (g), 143 ℃ waste of steam.With the thermal source of this part steam as bromine cooling machine, reduced waste on the one hand in the utility model, bromine cooling machine can be again refrigerating plant 7 ℃ of chilled waters is provided on the other hand.The utility model can realize that by increasing propylene subcooler and bromine cooling machine equipment and heat exchanger newly compressor load reduces by 16.96%.Propylene refrigeration compression cycle cooling-water consumption reduces 1930KW, but the newly-increased 983KW of bromine cooling machine apparatus cools water consumption, final cooling-water consumption reduces 947KW, and propylene consumption reduces 4.8%.
Description of drawings
Fig. 1 is the process chart of original low-temperature rectisol;
Fig. 2 is former propylene compression refrigeration process chart;
Fig. 3 is the utility model propylene compression refrigeration process chart;
Fig. 4 is the structural representation of existing bromine cooling machine (lithium bromide refrigerator).
Among Fig. 2-4: C1-one-level propylene compressor; C2-secondary propylene compressor; E1-propylene water cooler; The E2-evaporator system; NEW1-propylene subcooler; The NEW2-heat exchanger; The S1-separator; V1-first throttle valve; V2-the second choke valve; B1-bromine cooling machine system; The 1-condenser; The 2-generator; The 3-solution pump; 4-solution choke valve; The 5-absorber; The 6-evaporimeter; The 7-choke valve.
The below further describes the utility model.But following example only is simple and easy example of the present utility model, does not represent or limit rights protection scope of the present utility model, and protection domain of the present utility model is as the criterion with claims.
The specific embodiment
For the utility model is described better, be convenient to understand the technical solution of the utility model, typical but non-limiting embodiment of the present utility model is as follows:
The energy conserving system that a kind of conversion section Waste Heat Recovery and low-temp methanol washing process refrigeration station are integrated, described system comprises one-level propylene compressor C1, secondary propylene compressor C2, propylene water cooler E1, propylene subcooler NEW1, heat exchanger NEW2, the separator S1 that connects successively, the bottom of described separator S1 connects one-level propylene compressor C1 by evaporator system E2, and described separator S1 top connects secondary propylene compressor C2; Described propylene subcooler NEW1 is communicated with the realization heat exchange with the B1 of bromine cooling machine system.
The shell side entrance of described propylene subcooler NEW1 is communicated with the shell side outlet of propylene water cooler E1, and the shell side outlet of described propylene subcooler NEW1 is communicated with the shell side entrance of heat exchanger NEW2; Pass into the lithium bromide water solution of the B1 of bromine cooling machine system in the tube side of described propylene subcooler NEW1.
The shell side outlet of described heat exchanger NEW2 is communicated with separator S1; Pass in the tube side of described heat exchanger NEW2 in the low-temp methanol washing process from the isolated rich sulphur steam of backflow flow container.
The shell side entrance of described evaporator system E2 is communicated with the bottom of separator S1, and the shell side outlet of described evaporator system E2 is communicated with one-level propylene compressor C1 entrance.
Be provided with first throttle valve V1 between described propylene subcooler NEW1 and the heat exchanger NEW2.Be provided with the second choke valve V2 between the bottom of described separator S1 and the evaporator system E2.
The described bromine cooling machine B1 of system comprises absorber, evaporimeter, choke valve, the condenser that connects successively, wherein, replace described evaporimeter with described propylene subcooler NEW1, make the tube side of described propylene subcooler (NEW1) as the part in bromine cooling machine system (B1) circulation line.
The tube side entrance of described propylene subcooler NEW1 is communicated with the choke valve outlet of the B1 of bromine cooling machine system, and the tube side outlet of described propylene subcooler NEW1 is communicated with the absorber entrance of the B1 of bromine cooling machine system.
Described one-level propylene compressor C1 and secondary propylene compressor C2 adopt 2.5Mpa(G), 380 ℃ superheated steam driving steam turbine.
As shown in Figure 2, former propylene compression refrigeration technological process is as follows:
Propylene steam from evaporator system E2 flows (40 ℃ on thigh, 1.41bar, 49850kg/h) enter the refrigeration station battery limit (BL), be forced into 4.86bar, 26.55 ℃ through one-level propylene compressor C1, enter secondary propylene compressor C2 after mixing with separator S1 gas phase (5.68 ℃, 4.86bar, 22320kg/h) again, be compressed to 16.49bar, 88.02 ℃, enter propylene water cooler E1.The stream thigh temperature that goes out propylene water cooler E1 is 40 ℃, enters afterwards first throttle valve V1, and pressure decreased is to 4.86bar.The liquid phase stream thigh of separator V1, temperature are-5.68 ℃, through sending to evaporator system E2 evaporation gasification after the second choke valve V2 decompression.
As shown in Figure 3, the utility model propylene compression refrigeration technological process is as follows:
Propylene steam from evaporator system E2 flows (40 ℃ on thigh, 1.41bar, 47360kg/h) enter the refrigeration station battery limit (BL), be forced into 4.86bar, 26.55 ℃ through one-level propylene compressor C1, enter secondary propylene compressor C2 after mixing with separator S1 gas phase (5.68 ℃, 4.86bar, 17000kg/h) again, be compressed to 16.49bar, 89.48 ℃, enter propylene water cooler E1.The stream thigh temperature that goes out propylene water cooler E1 is 40 ℃, enters afterwards propylene subcooler NEW1.
Propylene subcooler NEW1 is supplied and the propylene liquid heat exchange by the B1 of bromine cooling machine system.The stream thigh temperature that goes out propylene subcooler NEW1 is 18 ℃, then enters first throttle valve V1, and pressure decreased passes through heat exchanger NEW2 again to 4.86bar, and the gas phase fraction of stream thigh is reduced to 0.1078 by 0.1504.The liquid phase stream thigh of separator S1, temperature are-5.68 ℃, through sending to evaporator system E2 evaporation after the second choke valve V2 decompression.
Table 1 former propylene compression refrigeration technique and the contrast of the utility model technique
Take 600,000 ton/years of coal gasification methanol projects processed as example, by technical solutions of the utility model preferred embodiment, namely can realize that by increasing propylene subcooler and bromine cooling machine equipment and heat exchanger newly compressor load reduces by 16.96%.Propylene refrigeration compression cycle cooling-water consumption reduces 1930KW, though the newly-increased 983KW of bromine cooling machine apparatus cools water consumption, final cooling-water consumption reduces 947KW, and propylene consumption reduces 4.8%.
Applicant's statement, the utility model illustrates detailed connected mode and the architectural feature of the utility model technical equipment by above-described embodiment, but the utility model is not limited to above-mentioned connected mode and architectural feature, does not mean that namely the utility model must rely on above-mentioned detailed construction feature and process could be implemented.The person of ordinary skill in the field should understand; to any improvement of the present utility model; to the increase of the equivalence replacement of the selected parts of the utility model and accessory, the selection of concrete mode etc., all drop within protection domain of the present utility model and the open scope.
Claims (8)
1. the integrated energy conserving system of a conversion section Waste Heat Recovery and low-temp methanol washing process refrigeration station, it is characterized in that, described system comprises one-level propylene compressor (C1), secondary propylene compressor (C2), propylene water cooler (E1), propylene subcooler (NEW1), heat exchanger (NEW2) and the separator (S1) that connects successively, the bottom of described separator (S1) connects one-level propylene compressor (C1) by evaporator system (E2), and described separator (S1) top connects secondary propylene compressor (C2); Described propylene subcooler (NEW1) is communicated with bromine cooling machine system (B1) realizes heat exchange.
2. the system as claimed in claim 1, it is characterized in that, the shell side entrance of described propylene subcooler (NEW1) is communicated with the shell side outlet of propylene water cooler (E1), and the shell side outlet of described propylene subcooler (NEW1) is communicated with the shell side entrance of heat exchanger (NEW2).
3. system as claimed in claim 1 or 2 is characterized in that, the shell side outlet of described heat exchanger (NEW2) is communicated with separator (S1).
4. system as claimed in claim 1 or 2 is characterized in that, the shell side entrance of described evaporator system (E2) is communicated with the bottom of separator (S1), and the shell side outlet of described evaporator system (E2) is communicated with one-level propylene compressor (C1) entrance.
5. the system as claimed in claim 1 is characterized in that, is provided with first throttle valve (V1) between described propylene subcooler (NEW1) and the heat exchanger (NEW2).
6. the system as claimed in claim 1 is characterized in that, is provided with the second choke valve (V2) between the bottom of described separator (S1) and the evaporator system (E2).
7. the system as claimed in claim 1, it is characterized in that, described bromine cooling machine system (B1) comprises absorber, evaporimeter, choke valve, the condenser that connects successively, wherein, replace described evaporimeter with described propylene subcooler (NEW1), make the tube side of described propylene subcooler (NEW1) as the part in bromine cooling machine system (B1) circulation line.
8. system as claimed in claim 7, it is characterized in that, the tube side entrance of described propylene subcooler (NEW1) is communicated with the choke valve outlet of bromine cooling machine system (B1), and the tube side outlet of described propylene subcooler (NEW1) is communicated with the absorber entrance of bromine cooling machine system (B1).
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104987279A (en) * | 2015-07-09 | 2015-10-21 | 华南理工大学 | Methanol-making system and method through coal gasification integrating waste heat cooling and carbon trapping |
| CN105536440A (en) * | 2015-12-15 | 2016-05-04 | 七台河宝泰隆煤化工股份有限公司 | Low temperature methanol washing device |
| CN114688756A (en) * | 2022-03-31 | 2022-07-01 | 华南理工大学 | Efficient refrigerating device and process for coal-based natural gas by using low-temperature waste heat |
-
2013
- 2013-04-25 CN CN2013202173487U patent/CN203240840U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104987279A (en) * | 2015-07-09 | 2015-10-21 | 华南理工大学 | Methanol-making system and method through coal gasification integrating waste heat cooling and carbon trapping |
| CN104987279B (en) * | 2015-07-09 | 2017-02-01 | 华南理工大学 | Methanol-making system and method through coal gasification integrating waste heat cooling and carbon trapping |
| CN105536440A (en) * | 2015-12-15 | 2016-05-04 | 七台河宝泰隆煤化工股份有限公司 | Low temperature methanol washing device |
| CN114688756A (en) * | 2022-03-31 | 2022-07-01 | 华南理工大学 | Efficient refrigerating device and process for coal-based natural gas by using low-temperature waste heat |
| CN114688756B (en) * | 2022-03-31 | 2023-01-06 | 华南理工大学 | Efficient refrigerating device and process for coal-based natural gas by using low-temperature waste heat |
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