CN103343740B - The energy-saving method of carbon-dioxide gas compressor and system thereof - Google Patents
The energy-saving method of carbon-dioxide gas compressor and system thereof Download PDFInfo
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- CN103343740B CN103343740B CN201310200523.6A CN201310200523A CN103343740B CN 103343740 B CN103343740 B CN 103343740B CN 201310200523 A CN201310200523 A CN 201310200523A CN 103343740 B CN103343740 B CN 103343740B
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Abstract
The invention discloses a kind of energy-saving and cost-reducing method of carbon-dioxide gas compressor and system thereof, solve energy in existing dry-powder air-current bed coal gasification apparatus gases used compressor compresses process and fail rational and efficient use, flow process is complicated, energy consumption is large, operating cost is high problem.The inventive method is that low-temp low-pressure carbon dioxide sends into gas compressor, send into after pre-heat exchanger and gas compressor latter end high-pressure carbon dioxide out carry out pre-heat exchange after one section, two sections of gas compressor compressions, again through the further heat exchange of second stage exit heat exchanger, the cooled carbon dioxide of heat exchange enters three sections of continuation compressions of gas compressor again, sends into coal gasification apparatus and use after the high-pressure carbon dioxide after pre-heat exchanger heat exchange heats up meets coal gasification apparatus gas temperature requirement.Present invention eliminates original steam preheating pipeline, optimize technological process, have that technological process is simple, energy-saving and cost-reducing, equipment investment and the low advantage of operating cost.
Description
Technical field
The present invention relates to a kind of dry-powder air-current bed coal gasification apparatus compressor and energy-saving method thereof.
Background technique
Dry-powder air-current bed coal gasification apparatus generally needs to consume a large amount of carbon dioxides and carries out coal dust conveying, pipeline purging, safety valve purging, filter blowback, inflammable gas displacement etc. in actual moving process, according to coal gasification apparatus Liquified gas tanker, carbon dioxide used generally needs high pressure conditions, and will meet certain temperature requirement (general temperature requirement is more than 100 DEG C).Therefore, the low-temp low-pressure carbon dioxide sent from subsequent purification device (low-temperature rectisol) needs through compressor boost and could supply coal gasification apparatus after preheating to use.
The general pressure requirements of the carbon dioxide that dry-powder air-current bed coal gasification apparatus uses higher (8.1MPaG and more than), tolerance is larger, and the out-of-bounds carbon dioxide gas pressure of air feed lower (close to normal pressure), use after therefore generally first selecting to adopt carbon-dioxide gas compressor to carry out compression supercharging to it.Carbon dioxide is compressed into the process of pressurized gas from low pressure, because compression ratio is comparatively large, and the multistage compression of general employing multistage.In real gas compression process, owing to there is heat exchange with the external world, generally belong to changeable compression process, namely only some is exported the heat that produces of compression work, major part is actually taken up by gas and causes gas temperature to raise, want to allow compressor in the ideally operation comparatively close to isothermal compression, reduce power consumpiton, improve operational efficiency, prevent gas temperature too high and cause lubricant oil carbonization and carbon deposit, ensure that compressor normal table runs, the heat produced when just gas must be compressed is removed as much as possible, meet the inlet temperature requirements into compressor next stage compressing section.Therefore, in compressor multi-stage compression process, each compressing section is intersegmental needs configuration interstage cooler (also known as heat exchanger), enters next stage compression after intersegmental exit gas being cooled in advance lower temperature (about 40 DEG C) again, to ensure that compressor is close to isothermal compression, safety and steady runs.
With reference to Fig. 1, for the dry-powder air-current bed coal gasification apparatus of certain as-fired coal 1100 ton per day, the high-pressure carbon dioxide gas nominal situation for this gasification installation needs 24000Nm
3/ h, declared working condition needs 27000Nm
3/ h.This strand of carbon dioxide is sent from the low-temperature rectisol operation of subsequent purification device, temperature 30 DEG C, pressure 0.16MPaA, the pressure requirements entering gasification installation is 8.2MPaA, temperature 120 DEG C, centrifugal carbon-dioxide gas compressor is adopted to compress, be divided into four sections of compressions, intersegmental employing recirculated cooling water enters next compressing section of compressor after being cooled to 40 DEG C to the follow-up each section of inlet gas of compressor, compressor latter end outlet carbon dioxide gas pressure 8.298MPaA, temperature 92.4 DEG C, now need to adopt low pressure steam gas delivery gasifying device after heat exchanger is preheating to 120 DEG C to use.As calculated, 340t/h is about for the circulating cooling water consumption of the intersegmental cooled carbon dioxide gas of carbon-dioxide gas compressor under nominal situation, compressor outlet is used for the low pressure steam consumption of preheating carbon dioxide and is about 1t/h, and energy consumption is comparatively large and improve cost of production.
Summary of the invention
The object of the invention is to solve the problems of the technologies described above, the energy-saving method of the carbon-dioxide gas compressor that a kind of technique is simple, energy-saving and cost-reducing, operating cost is low is provided.
The present invention also provides a kind of energy-saving and cost-reducing system of the carbon-dioxide gas compressor for said method.
Present system comprises carbon-dioxide gas compressor, the second stage exit of described carbon-dioxide gas compressor is connected with three sections of imports through second stage exit heat exchanger, also include pre-heat exchanger, described second stage exit is connected with three sections of imports through pre-heat exchanger, second stage exit heat exchanger, and the latter end outlet of described carbon-dioxide gas compressor is connected with coal gasification apparatus through described pre-heat exchanger.
Present invention process comprises sends low-temp low-pressure carbon dioxide into carbon-dioxide gas compressor, send into after pre-heat exchanger and carbon-dioxide gas compressor latter end high-pressure carbon dioxide out carry out pre-heat exchange after one section, two sections of carbon-dioxide gas compressor compressions, again through the further heat exchange of second stage exit heat exchanger, the cooled carbon dioxide of heat exchange enters three sections of continuation compressions of carbon-dioxide gas compressor again, and the high-pressure carbon dioxide after pre-heat exchanger heat temperature raising sends into coal gasification apparatus.
Through described carbon-dioxide gas compressor latter end high-pressure carbon dioxide gas out behind pre-heat exchanger heat exchange to 100 ~ 200 DEG C, then send into coal gasification apparatus; Described carbon dioxide after two sections of compressions carries out heat exchange through pre-heat exchanger and carbon-dioxide gas compressor latter end high-pressure carbon dioxide out, then after second stage exit heat exchanger and the further heat exchange of recirculated cooling water to carbon-dioxide gas compressor entrance allowable temperature, send into carbon-dioxide gas compressor three sections are continued to compress.
Study discovery by analysis, the carbon dioxide temperature that carbon-dioxide gas compressor second stage exit temperature exports far above latter end, as carbon-dioxide gas compressor second stage exit temperatures as high 192.4 DEG C in background technique example, the recirculated cooling water needing to consume about 150t/h is cooled to 40 DEG C to it and enters three sections again and compress, and compressor latter end outlet temperature only has 92.4 DEG C, but need additionally to consume 1t/h low pressure steam and be preheated to 120 DEG C and can send into coal gasification apparatus and use.Consider to cancel the heat exchanger of carbon-dioxide gas compressor latter end outlet port for heating up to this claimant, the carbon dioxide that carbon-dioxide gas compressor latter end exports is returned cause two sections with three sections of intersegmental pre-heat exchangers in carry out pre-heat exchange with the carbon dioxide of second stage exit, make the carbon dioxide of second stage exit by while precooling, also the gas heating making carbon-dioxide gas compressor latter end export is directly used in coal gasification apparatus to the temperature expected, and through the carbon dioxide of precooling can be cooled to further with recirculated cooling water in second stage exit heat exchanger as required enter temperature requirement that suction port of compressor allows after enter three sections and proceed compression.
The concrete beneficial effect of the present invention is summarized as follows:
1, method of the present invention decreases the consumption of the intersegmental recirculated cooling water of carbon-dioxide gas compressor, makes the corresponding reduction of recirculated cooling water size of heat exchanger, decreases heat exchange equipment investment;
2, method of the present invention eliminates the low pressure steam consumption of preheating carbon-dioxide gas compressor latter end outlet carbon dioxide, eliminate Preheated steam pipeline, save steam pipe line investment, optimize technological process configuration, make whole carbon dioxide compressive flow journey more simply compact.
3. present system structure is simple, operating cost is low, energy-saving and cost-reducing, safe and reliable.
4. the engineering energy conservation and consumption reduction effects of the carbon dioxide temperature requirement of the present invention to carbon-dioxide gas compressor final outlet higher (the highest gas temperature lower than the outlet of compressor compresses section) is more obvious, better to the energy conservation and consumption reduction effects of the larger carbon-dioxide gas compressor engineering of scale larger carbon dioxide demand.
Accompanying drawing explanation
Fig. 1 is existing carbon dioxide compression process flow diagram;
Fig. 2 is present invention process flow chart and system diagram.
Wherein, 1-carbon-dioxide gas compressor, 1.1-one section, 1.2-two sections, 1.3-three sections, 1.4-four sections, 2-one section outlet heat exchanger, 3-second stage exit heat exchanger, 4-three sections of outlet heat exchangers, 5-pre-heat exchanger, 6-temperature rise heat exchangers.
Embodiment
Below in conjunction with accompanying drawing, explanation is further explained to the present invention:
With reference to Fig. 2, in the present embodiment, carbon-dioxide gas compressor 1 is that (quantity of concrete compressing section can need to arrange according to actual pressure in four compressing sections, as three compressing sections or five compressing sections) be respectively one section 1.1, two section 1.2, three section 1.3 and four section 1.4, one section of 1.1 outlet of described carbon-dioxide gas compressor is through one section outlet heat exchanger 2 and two section of 1.2 import, described two section of 1.2 outlet is through pre-heat exchanger 5, second stage exit heat exchanger 3 is connected with three section of 1.3 import, three section of 1.3 outlet is connected with four section of 1.4 import through three sections of outlet heat exchangers 4, four section of 1.4 outlet is connected with coal gasification apparatus through pre-heat exchanger 5.
Technological method:
From the low-temp low-pressure carbon dioxide (pressure 0 ~ 0.2MPaA of low-temperature rectisol, temperature is 0 ~ 40 DEG C) send into carbon-dioxide gas compressor 1, after one section of 1.1 compression of carbon-dioxide gas compressor 1, send into two section 1.2 through one section outlet heat exchanger 2 and recirculated cooling water indirect heat exchange to 15 ~ 50 DEG C compress, after two section of 1.2 compression, send into pre-heat exchanger 5 carry out pre-heat exchange to 100 ~ 160 DEG C indirectly with carbon-dioxide gas compressor 1 latter end 140 ~ 220 DEG C of high-pressure carbon dioxides out, again through second stage exit heat exchanger 3 and further indirect heat exchange to 15 ~ 50 DEG C of recirculated cooling water, carbon dioxide after heat exchange enters three section of 1.3 continuation compression of carbon-dioxide gas compressor 1 again, and then through three sections of outlet heat exchangers 4 and recirculated cooling water indirect heat exchange to 15 ~ 50 DEG C, finally by discharging high-pressure carbon dioxide after four section of 1.4 compression, (pressure is 8.0 ~ 9.0MPaA, temperature is 60 ~ 110 DEG C), high-pressure carbon dioxide is sent into coal gasification apparatus after sending into pre-heat exchanger 5 and two section of 1.2 carbon dioxide indirect heat exchange to 100 ~ 200 exported DEG C and is used.
As calculated, after being transformed by the technical program, can reduce by two section of 1.2 circulating cooling water consumption 10 ~ 300t/h, slip is 10 ~ 100%, steam consumption needed for the high-pressure carbon dioxide gas that can save preheating compressor outlet completely.Meanwhile, because circulating cooling water consumption reduces, recirculated cooling water size of heat exchanger is corresponding to diminish, and saves equipment component investment; Eliminate Preheated steam pipeline, decrease steam consumption, while saving steam pipe line investment, optimize technological process.
Claims (3)
1. the energy-saving and cost-reducing system of a carbon-dioxide gas compressor, comprise carbon-dioxide gas compressor, the second stage exit of described carbon-dioxide gas compressor is connected with three sections of imports through second stage exit heat exchanger, it is characterized in that, also include pre-heat exchanger, described second stage exit is connected with three sections of imports through pre-heat exchanger and second stage exit heat exchanger, and the latter end outlet of described carbon-dioxide gas compressor is connected with coal gasification apparatus through described pre-heat exchanger.
2. the energy-saving method of a carbon-dioxide gas compressor, it is characterized in that, comprise and low-temp low-pressure carbon dioxide is sent into carbon-dioxide gas compressor, carbon dioxide after one section of carbon-dioxide gas compressor and two sections of compressions is sent into after pre-heat exchanger and carbon-dioxide gas compressor latter end high-pressure carbon dioxide out carry out pre-heat exchange, again through the further heat exchange of second stage exit heat exchanger, the cooled carbon dioxide of heat exchange enters three sections of continuation compressions of carbon-dioxide gas compressor again, send into coal gasification apparatus after high-pressure carbon dioxide after pre-heat exchanger heat exchange heats up meets coal gasification apparatus gas temperature requirement to use.
3. the energy-saving method of carbon-dioxide gas compressor as claimed in claim 2, is characterized in that, through described carbon-dioxide gas compressor latter end high-pressure carbon dioxide out behind pre-heat exchanger heat exchange to 100 ~ 200 DEG C, then sends into coal gasification apparatus; Described carbon dioxide after two sections of compressions is after pre-heat exchanger and carbon-dioxide gas compressor latter end high-pressure carbon dioxide out carry out pre-heat exchange, then after second stage exit heat exchanger and the further heat exchange of recirculated cooling water to carbon-dioxide gas compressor entrance allowable temperature, send into carbon-dioxide gas compressor three sections are continued to compress.
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| GB0400986D0 (en) * | 2004-01-16 | 2004-02-18 | Cryostar France Sa | Compressor |
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| US3947146A (en) * | 1973-10-19 | 1976-03-30 | Linde Aktiengesellschaft | Removal of heat of compression |
| US4461154A (en) * | 1981-06-18 | 1984-07-24 | Air Products And Chemicals, Inc. | Method and apparatus for compressing gas |
| PL275978A1 (en) * | 1988-11-23 | 1990-05-28 | Kopalnia Wegla Kamiennego Mani | Apparatus for recovering waste heat from compressed gas precooling process in particular for use on impeller-type compressors |
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| CN102116529A (en) * | 2011-03-10 | 2011-07-06 | 中山市麦科尔热能技术有限公司 | Heat pump hot water system for carbon dioxide compressor |
| CN202326099U (en) * | 2011-11-15 | 2012-07-11 | 郑州计量节能检测中心 | Heat recovery system of water-cooling air compressor |
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| CN203335356U (en) * | 2013-05-27 | 2013-12-11 | 中国五环工程有限公司 | Energy saving and consumption reduction system of carbon dioxide gas compressor |
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