CN103553168B - Process for realizing cascade comprehensive utilization of heat energy of natural gas purifying plant - Google Patents
Process for realizing cascade comprehensive utilization of heat energy of natural gas purifying plant Download PDFInfo
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- CN103553168B CN103553168B CN201310536438.7A CN201310536438A CN103553168B CN 103553168 B CN103553168 B CN 103553168B CN 201310536438 A CN201310536438 A CN 201310536438A CN 103553168 B CN103553168 B CN 103553168B
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Abstract
The invention discloses a process for realizing cascade comprehensive utilization of heat energy of a natural gas purifying plant. Steam from a boiler is used as an I-effect heat source, I-effect evaporated secondary steam is used as an II-effect heat source, II-effect evaporated secondary steam is used as an III-effect heat source, and so on, the energy is utilized in a cascade manner; high-level steam generated by a boiler heat feeding unit enters a natural gas purifying unit; generated high-temperature condensed water is exhausted to a strong brine comprehensive treatment unit of an evaporation crystallization unit for preheating strong brine to be treated; and meanwhile, high-temperature poor-amine liquor generated by the natural gas purifying unit is exhausted to the strong brine comprehensive treatment unit of the evaporation crystallization unit for preheating the strong brine to be treated, and the poor-amine liquor is returned to the natural gas purifying unit after being cooled. The process disclosed by the invention has the positive effects that the evaporation crystallization unit can realize wastewater zero exhaustion of the natural gas purifying unit by only needing to consume a little high-level heat energy as waste heat of the boiler heat feeding unit and the natural gas purifying unit is utilized, and energy-saving effect is obvious.
Description
Technical field
The invention belongs to the energy-saving and emission-reduction field in green technology, be specifically related to a kind of technique that realizes the comprehensive utilization of Gas Purification Factory thermal energy step.
Background technology
Sweet natural gas is consumed meeting through natural gas conditioning process from exploiting to, natural gas conditioning is mainly to remove impurity, desulfurization and dehydration, in scavenging process, produced a large amount of waste heat such as steam condensate, and in the technique purifying, have a large amount of high temperature feed liquids to need cooling, consumed a large amount of water coolants or electric energy.In scavenging process, inevitably can produce a large amount of production wastes, factory effluent and maintenance sewage, need to process simultaneously.
Domestic Gas Purification Factory adopted the direct back boiler system of steam condensate in the past conventionally, and high temperature feed liquid is cooling by water cooler, has wasted heat energy and has consumed a large amount of refrigerants and electric energy simultaneously.A small amount of low-pressure steam that boiler systems produces cannot be utilized, and simple extensive outer row, wastes energy equally.The strong brine producing in production adopts " re-injection ", and Gas Purification Factory water consumption is larger, and fresh water mostly carried by pipe long-distance, and water cost is higher, in addition water resources is day by day deficient, and all kinds of sewage in factory are carried out carrying out after advanced treatment the reuse trend that is inevitable.
Summary of the invention
In order to overcome the above-mentioned shortcoming of prior art, the invention provides a kind of technique that realizes the comprehensive utilization of Gas Purification Factory thermal energy step.
The technical solution adopted for the present invention to solve the technical problems is: a kind of technique that realizes the comprehensive utilization of Gas Purification Factory thermal energy step, comprises the steps:
Step 1, the higher-grade steam that boiler produces to hot cell is through pressure and temperature reducing, reach after the required pressure and temperature in evaporative crystallization unit, enter the I single-effect evaporator of evaporative crystallization unit, thermal source as I effect, the secondary steam that I single-effect evaporator evaporates enters II single-effect evaporator, thermal source as II effect, the secondary steam that II single-effect evaporator evaporates enters III single-effect evaporator, thermal source as III effect, the secondary steam that III single-effect evaporator evaporates enters IV single-effect evaporator, thermal source as IV effect, the exhaust steam that IV single-effect evaporator is discharged enters vacuum system condensation and obtains product water, product water reuse is other water of productive use in recirculated cooling water make up water or factory,
The higher-grade steam that step 2, boiler produce to hot cell enters natural gas conditioning unit, as the thermal source of regenerator column reboiler; The strong brine comprehensive treating process unit that the high-temperature condensation water that natural gas conditioning unit produces is discharged to evaporative crystallization unit carries out preheating to the strong brine of need processing; The strong brine comprehensive treating process unit that the poor amine liquid of high temperature that natural gas conditioning unit produces is simultaneously discharged to evaporative crystallization unit carries out preheating to the strong brine of need processing, after poor amine liquid cooling, returns to natural gas conditioning unit.
Compared with prior art, positively effect of the present invention is: owing to having utilized the waste heat of boiler to hot cell and natural gas conditioning unit, evaporative crystallization unit only need to consume a small amount of high-grade heat energy, just can realize Gas Purification Factory sewage zero-discharge, energy-saving effect is very obvious, treatment effect is good and stable, easy and simple to handle, applied widely.
Embodiment
A technique that realizes the comprehensive utilization of Gas Purification Factory thermal energy step, comprises the steps:
Step 1, the higher-grade steam that boiler produces to hot cell is through pressure and temperature reducing, reach the required pressure (0.5MPa in evaporative crystallization unit, refer to absolute pressure) and temperature (150 ℃) after, enter the I single-effect evaporator of evaporative crystallization unit, thermal source as I effect, the secondary steam that I single-effect evaporator evaporates is as the thermal source of II effect, the secondary steam that II single-effect evaporator evaporates is as the thermal source of III effect, the secondary steam that III single-effect evaporator evaporates is as the thermal source of IV effect, the exhaust steam that IV single-effect evaporator is discharged enters vacuum system condensation and obtains product water, product water reuse is other water of productive use in recirculated cooling water make up water or factory.
The higher-grade steam that step 2, boiler produce to hot cell enters natural gas conditioning unit, as the thermal source of regenerator column reboiler; The strong brine comprehensive treating process unit that the water of condensation (high temperature) that natural gas conditioning unit produces is discharged to evaporative crystallization unit carries out preheating to the strong brine of need processing; The strong brine comprehensive treating process unit that the poor amine liquid that natural gas conditioning unit produces simultaneously (have certain heat energy and need cooling) is discharged to evaporative crystallization unit carries out preheating to the strong brine of need processing, after poor amine liquid cooling, returns to natural gas conditioning unit.So both utilize the waste heat of poor amine liquid, simultaneously reduced again the required refrigerant of the poor amine liquid of natural gas conditioning unit cooling down high-temperature and the consumption of electric energy.
Described strong brine comprehensive treating process unit takes full advantage of the waste heat of high-temperature condensation water and the poor amine liquid of high temperature, comprise the steps: that strong brine enters one-level preheater, in one-level preheater: strong brine (30 ℃) carries out heat exchange with the poor amine liquid of high temperature (90 ℃) from natural gas conditioning unit, poor amine liquid after heat exchange cooling returns to natural gas conditioning unit, strong brine (50 ℃) part after heat exchange heats up enters IV single-effect evaporator (temperature is controlled at 57 ℃), and another part enters secondary preheater, secondary preheater comprises preheater and secondary preheating device, in a preheater: strong brine (50 ℃) carries out heat exchange with the water of condensation from secondary preheating device, water of condensation after heat exchange cooling returns to boiler to hot cell, strong brine (75 ℃) part after heat exchange heats up enters III single-effect evaporator (temperature is controlled at 83 ℃), another part enters secondary preheating device, in secondary preheating device: strong brine (75 ℃) with from the high-temperature condensation water (120 ℃) of natural gas conditioning unit with from the steam condensate of three grades of preheaters, carry out heat exchange, water of condensation after heat exchange cooling enters preheater No. one time, strong brine (100 ℃) part after heat exchange heats up enters II single-effect evaporator (temperature be controlled at 110 ℃), another part enters three grades of preheaters, in three grades of preheaters, strong brine (110 ℃) with from boiler, to the low-grade low-pressure steam (130 ℃) of hot cell, carry out heat exchange, the steam condensate producing after heat exchange enters secondary preheating device, strong brine (124 ℃) after heat exchange heats up enters I single-effect evaporator (temperature is controlled at 135 ℃).Described one, two, three preheater is plate-type heat exchanger.
Principle of work of the present invention is: in multiple-effect evaporation crystalline element, strong brine is through fresh feed pump, enter the mixing condensation water heat exchange out of plate-type heat exchanger and evaporative crystallization, the poor amine liquid of the high temperature heat exchange that strong brine after intensification and natural gas conditioning unit come, the high-temperature condensation water heat exchange that strong brine after intensification and natural gas conditioning unit come, again improve the temperature of dense water, finally by the low-pressure steam that boiler comes to hot cell, again improve the temperature of dense water, the water of condensation of low-pressure steam imports the high-temperature condensation water of natural gas conditioning unit as the thermal source of secondary preheating.
The steam that boiler comes is simultaneously as the thermal source of I effect, and the secondary steam that I effect evaporates is as the thermal source of II effect, and the secondary steam that II effect evaporates is as the thermal source of III effect, and the rest may be inferred, cascaded utilization of energy.The principle of this technology utilization multiple-effect evaporation realizes the cascade utilization of this unit energy, utilize simultaneously other unit need not or be difficult to utilize, the relatively low heat energy preheating strong brine of taste, realized the cascade utilization of the energy of whole system.Improved the heat economy of evaporation, conserve energy.
Claims (3)
1. a technique that realizes the comprehensive utilization of Gas Purification Factory thermal energy step, is characterized in that: comprise the steps:
Step 1, the higher-grade steam that boiler produces to hot cell is through pressure and temperature reducing, reach after the required pressure and temperature in evaporative crystallization unit, enter the I single-effect evaporator of evaporative crystallization unit, thermal source as I effect, the secondary steam that I single-effect evaporator evaporates enters II single-effect evaporator, thermal source as II effect, the secondary steam that II single-effect evaporator evaporates enters III single-effect evaporator, thermal source as III effect, the secondary steam that III single-effect evaporator evaporates enters IV single-effect evaporator, thermal source as IV effect, the exhaust steam that IV single-effect evaporator is discharged enters vacuum system condensation and obtains product water, product water reuse is other water of productive use in recirculated cooling water make up water or factory,
The higher-grade steam that step 2, boiler produce to hot cell enters natural gas conditioning unit, as the thermal source of regenerator column reboiler, the strong brine comprehensive treating process unit that the high-temperature condensation water that natural gas conditioning unit produces is discharged to evaporative crystallization unit carries out preheating to the strong brine of need processing, the strong brine comprehensive treating process unit that the poor amine liquid of high temperature that natural gas conditioning unit produces is simultaneously discharged to evaporative crystallization unit carries out preheating to the strong brine of need processing, after poor amine liquid cooling, returns to natural gas conditioning unit, the strong brine that described strong brine comprehensive treating process unit by using high-temperature condensation water and the heat of the poor amine liquid of high temperature are processed need carries out preheating, comprise the steps: that strong brine enters one-level preheater, in one-level preheater: strong brine carries out heat exchange with the poor amine liquid of high temperature from natural gas conditioning unit, poor amine liquid after heat exchange cooling returns to natural gas conditioning unit, a strong brine part after heat exchange heats up enters IV single-effect evaporator, and another part enters secondary preheater, secondary preheater comprises preheater and secondary preheating device, in a preheater: strong brine carries out heat exchange with the water of condensation from secondary preheating device, water of condensation after heat exchange cooling returns to boiler to hot cell, a strong brine part after heat exchange heats up enters III single-effect evaporator, another part enters secondary preheating device, in secondary preheating device: strong brine with from the high-temperature condensation water of natural gas conditioning unit with from the steam condensate of three grades of preheaters, carry out heat exchange, water of condensation after heat exchange cooling enters preheater No. one time, a strong brine part after heat exchange heats up enters II single-effect evaporator, another part enters three grades of preheaters, in three grades of preheaters, strong brine with from boiler, to the low-grade low-pressure steam of hot cell, carry out heat exchange, the steam condensate producing after heat exchange enters secondary preheating device, strong brine after heat exchange heats up enters I single-effect evaporator.
2. a kind of technique that realizes the comprehensive utilization of Gas Purification Factory thermal energy step according to claim 1, is characterized in that: described one, two, three preheater is plate-type heat exchanger.
3. a kind of technique that realizes the comprehensive utilization of Gas Purification Factory thermal energy step according to claim 1, is characterized in that: the strong brine after the heat exchange of one-level preheater heats up is 50 ℃, and the temperature of described IV single-effect evaporator is controlled at 57 ℃; Strong brine after the preheater heat exchange intensification of secondary preheater is 75 ℃, and the temperature of described III single-effect evaporator is controlled at 83 ℃; Strong brine after the secondary preheating device heat exchange intensification of secondary preheater is 100 ℃, and the temperature of described II single-effect evaporator is controlled at 110 ℃; Strong brine after three grades of preheater heat exchange heat up is 124 ℃, and the temperature of described I single-effect evaporator is controlled at 135 ℃.
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| CN103304104A (en) * | 2013-07-02 | 2013-09-18 | 中国石油集团工程设计有限责任公司 | Zero-sewage discharge novel process for development of natural gas fields |
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| CN103304104A (en) * | 2013-07-02 | 2013-09-18 | 中国石油集团工程设计有限责任公司 | Zero-sewage discharge novel process for development of natural gas fields |
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Effective date of registration: 20180110 Address after: 610041 Chengdu high tech Zone, Sichuan province sublimation Road No. 6 Patentee after: China Petroleum Engineering Construction Co Ltd Address before: 610041 Chengdu high tech Zone, Sichuan province sublimation Road No. 6 Patentee before: Engineering Design Co., Ltd., China Petroleum Group |
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Effective date of registration: 20210219 Address after: 100007 No. 9 North Main Street, Dongcheng District, Beijing, Dongzhimen Patentee after: CHINA NATIONAL PETROLEUM Corp. Patentee after: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. Address before: No. 6, Sichuan hi tech Zone, sublime Road, Chengdu, Sichuan Patentee before: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. |