CN113599850B - Method for recycling waste heat of rich oil heater - Google Patents
Method for recycling waste heat of rich oil heater Download PDFInfo
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- CN113599850B CN113599850B CN202110937962.XA CN202110937962A CN113599850B CN 113599850 B CN113599850 B CN 113599850B CN 202110937962 A CN202110937962 A CN 202110937962A CN 113599850 B CN113599850 B CN 113599850B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B3/00—Other methods of steam generation; Steam boilers not provided for in other groups of this subclass
- F22B3/04—Other methods of steam generation; Steam boilers not provided for in other groups of this subclass by drop in pressure of high-pressure hot water within pressure- reducing chambers, e.g. in accumulators
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
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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
- C10K1/002—Removal of contaminants
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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
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
- C10K1/18—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids hydrocarbon oils
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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- Combustion & Propulsion (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
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- Mechanical Engineering (AREA)
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Abstract
The invention discloses a method for recycling waste heat of a rich oil heater, which comprises the following steps: s1, providing medium-pressure superheated steam to a rich oil heater; s2, steam-water mixed liquid generated in the rich oil heater enters a flash tank, and the steam-water mixed liquid is formed by mixing steam and steam condensate water; and S3, conveying the steam condensate generated in the flash tank to an ammonium sulfate mother liquor heater for heating the ammonium sulfate mother liquor. According to the method for recycling the waste heat of the rich oil heater, the condensed water is sent to the mother liquor heater of the ammonium sulfate saturator for preheating the ammonium sulfate mother liquor through the self-pressure of the flash tank, the waste heat of the condensed water of the rich oil heater is fully utilized, and energy conservation and environmental protection are realized.
Description
Technical Field
The invention belongs to the technical field of waste heat and waste energy recycling, and particularly relates to a method for recycling waste heat of a rich oil heater.
Background
In the existing coke oven gas purification process, a crude benzene distillation unit originally adopts a mode of heating rich oil by a tubular furnace to remove and recover crude benzene in the rich oil, and due to the combustion mode of the coke oven gas by the tubular furnace, hot waste gas is generated and simultaneously nitrogen oxide is generated, so that certain influence is caused on the environment, and meanwhile, the energy consumption is higher, and certain safety problems of easy explosion and the like exist when the coke oven gas is combusted. At present, the temperature of rich oil is increased by heating the rich oil in a rich oil heater by medium-pressure steam, the heated rich oil enters a debenzolization tower for debenzolization, the medium-pressure steam heats the rich oil in the rich oil heater and simultaneously generates low-pressure steam and a certain amount of steam condensate water, the part of the steam condensate water is generally sent to a desalted water station to be used as raw water, before the steam condensate water enters a raw water tank, circulating cooling water is used for heating or heat exchange is carried out between desalted water and the steam condensate water, and the cooled steam condensate water can enter the raw water tank of desalted water to be used as the raw water.
At present, the methods for removing impurities in the gas include the following methods:
firstly, condensed water of a rich oil heater is recycled and sent to a raw water tank of a power plant, and needs to be cooled before entering the raw water tank, and generally, firstly, desalted water is considered for heat exchange, but because condensed water of a steam turbine of the power plant boiler can be reused for the power plant boiler, the required amount of the desalted water is not large, and the desalted water cannot reduce steam condensed water to normal temperature, so that the condensed water of the steam needs to be cooled by circulating cooling water and then enters the raw water tank, and if the condensed water of the steam turbine of the power plant boiler is not cooled, stable operation of desalted water station equipment is affected; the waste heat of the steam condensate of the rich oil heater cannot be effectively utilized;
and secondly, the condensed water of the rich oil heater is connected with the riser waste heat recovery device, the condensed water is directly sent to the riser to recover the waste heat of the riser, but if the rich oil heater leaks and is not found, the riser waste heat recovery device is easy to explode.
Disclosure of Invention
The present invention is directed to solving at least one of the problems of the prior art. Therefore, the invention provides a method for recycling waste heat of a rich oil heater, and aims to fully utilize the waste heat of steam condensate water of the rich oil heater and realize energy conservation and environmental protection.
In order to achieve the purpose, the invention adopts the technical scheme that: the method for recycling the waste heat of the rich oil heater comprises the following steps:
s1, providing medium-pressure superheated steam to a rich oil heater;
s2, steam-water mixed liquid generated by heat exchange and cooling of the medium-pressure superheated steam in the rich oil heater enters a flash tank, and the steam-water mixed liquid is formed by mixing steam and steam condensate;
and S3, self-pressure conveying the steam condensate generated in the flash tank to an ammonium sulfate mother liquor heater for heating ammonium sulfate mother liquor.
In the step S1, the pressure of the steam entering the rich oil heater is 1.5-3.2MPa, and the steam temperature is 380-450 ℃.
In the step S2, the pressure of the steam generated in the rich oil heater is 0.5-0.9MPa.
In step S3, the temperature of the steam condensate generated in the flash tank is 151-176 ℃.
And a control valve is arranged at the liquid outlet of the ammonium sulfate mother liquid heater and is used for controlling the opening and closing of the liquid outlet of the ammonium sulfate mother liquid heater.
And a liquid outlet of the ammonium sulfate mother liquor heater is provided with a detection device for detecting the content of the ammonium sulfate mother liquor components which may leak into the steam condensate.
The detection device is a conductivity meter or a PH meter.
In the step S3, the steam condensate generated in the flash tank is mixed with a small amount of low-pressure steam in the ammonium sulfate section, and then the ammonium sulfate mother liquor is heated.
In the step S3, under the condition of winter or other insufficient heat, a small amount of low-pressure steam is mixed with the steam condensate for heating the ammonium sulfate mother liquor.
The method for recycling the waste heat of the rich oil heater further comprises the following steps:
s4, conveying the steam condensate flowing out of the ammonium sulfate mother liquor heater to a desalted water heat exchanger;
s5, conveying the steam condensate flowing out of the demineralized water heat exchanger to a circulating cooler, and cooling the steam condensate to 30-45 ℃;
and S6, conveying the steam condensate flowing out of the circulating cooler to a desalted water raw water tank.
According to the method for recycling the waste heat of the rich oil heater, the condensed water is sent to the mother liquor heater of the ammonium sulfate saturator for preheating the ammonium sulfate mother liquor through the self-pressure of the flash tank, the waste heat of the condensed water of the rich oil heater is fully utilized, and energy conservation and environmental protection are realized.
Drawings
The description includes the following figures, the contents shown are respectively:
fig. 1 is a schematic flow chart of the method for recycling waste heat of the rich oil heater.
Detailed Description
The following detailed description of the embodiments of the present invention will be given with reference to the accompanying drawings for a purpose of helping those skilled in the art to more fully, accurately and deeply understand the concept and technical solution of the present invention and to facilitate its implementation.
As shown in fig. 1, the invention provides a method for recycling waste heat of a rich oil heater, comprising the following steps:
s1, supplying medium-pressure superheated steam to a rich oil heater;
s2, steam-water mixed liquid generated by heat exchange and cooling of the medium-pressure superheated steam in the rich oil heater enters a flash tank, and the steam-water mixed liquid is formed by mixing steam and steam condensate;
and S3, self-pressure conveying the steam condensate generated in the flash tank to an ammonium sulfate mother liquor heater for heating the ammonium sulfate mother liquor.
Specifically, in step S1, the depressurized medium-pressure superheated steam is sent to a rich oil heater and heated, and the pressure of the medium-pressure superheated steam entering the rich oil heater is 1.5 to 3.2MPa, and the temperature of the medium-pressure superheated steam is 380 to 450 ℃. The medium-pressure superheated steam is provided for a rich oil heater to serve as a heat source, and is also provided for a crude benzene regenerator of the same section after being decompressed by a branch pipe, and the crude benzene regenerator can be subjected to washing oil regeneration only by superheated steam at the temperature of about 380-450 ℃; the temperature of the medium-pressure superheated steam is set to be higher, so that the heat transfer efficiency of the rich oil heater can be improved, meanwhile, the rich oil heater is not fed in a saturated temperature state, so that the water hammer phenomenon of the rich oil heater can be reduced, and the stable operation of the rich oil heater is ensured.
In the step S1, after the medium-pressure superheated steam entering the rich oil heater exchanges heat with the rich oil, steam and steam condensate are generated in the rich oil heater, the steam is low-pressure steam, and the pressure of the low-pressure steam generated in the rich oil heater is 0.5-0.9MPa, so that the total amount of the low-pressure steam required by a chemical production workshop can be reduced, and the steam can be saved; if the steam is set to other pressure, the pressure of the steam may not be consistent with the pressure of a low-pressure pipe network required by a chemical production workshop of the coke-oven plant, namely, the steam cannot enter a unified low-pressure pipe network to be supplemented by the steam, and only can be decompressed for use or wasted.
In the above step S2, the pressure of the steam entering the flash tank is 0.5 to 0.9MPa.
In the step S3, the temperature of the steam condensate separated and generated in the flash tank is 151-176 ℃, the pressure of the flash steam separated and generated in the flash tank is 0.5-0.9MPa, and the flash steam with the pressure enters a low-pressure steam pipe network of the plant area and can be utilized, so that the consumption of raw steam is reduced. The steam condensate is conveyed to an ammonium sulfate mother liquor heater positioned in an ammonium sulfate working section through a conveying pipeline under the pressure of flash steam in a flash evaporation tank, and is used for heating ammonium sulfate mother liquor in the ammonium sulfate mother liquor heater.
In the step S3, the conveying pipeline includes a conveying pipeline, the conveying pipeline is connected to the flash tank and the ammonium sulfate mother liquor heater, the conveying pipeline is a 304 or 316L stainless steel pipeline, and the conveying pipeline is subjected to heat preservation treatment to avoid heat loss.
In the step S3, a liquid outlet is disposed at the lower portion of the ammonium sulfate mother liquor heater, after the ammonium sulfate mother liquor heater heats the mother liquor, the steam condensate flows out from the liquid outlet of the ammonium sulfate mother liquor heater, a control valve is disposed at the liquid outlet of the ammonium sulfate mother liquor heater, the control valve is used for controlling opening and closing of the liquid outlet of the ammonium sulfate mother liquor heater, and the flow and pressure of the steam condensate flowing out from the liquid outlet of the ammonium sulfate mother liquor heater can be controlled by the control valve.
The ammonium sulfate mother liquor heater is heated by the steam condensate after the rich oil heater, so that the phenomenon that the ammonium sulfate mother liquor heater leaks due to the fact that the temperature of the pipe wall of the ammonium sulfate mother liquor heater is too high due to the fact that the steam directly heats the ammonium sulfate mother liquor heater is avoided, corrosivity of the ammonium sulfate mother liquor is enhanced.
The liquid outlet of the ammonium sulfate mother liquor heater is provided with a detection device for detecting the content of ammonium sulfate mother liquor in the steam condensate, and the detection device is a conductivity meter or a PH meter. The detection device is used for detecting the content of the ammonium sulfate mother liquor in the steam condensate and can be used for judging whether the ammonium sulfate mother liquor has blowby to the steam condensate.
Through utilizing rich oil heater back flash tank residual pressure, the supporting thiamine mother liquor heater of thiamine saturator is because be in the negative pressure section before thiamine mother liquor pump, is difficult for leaking during the thiamine mother liquor enters into the steam condensate, even leak into in the steam condensate still detection instrument such as conductivity meter, PH meter can in time detect out accidents such as letting through leak, in time cut out mother liquor heater system with the steam condensate, have dual guarantee to guaranteeing power plant demineralized water safety.
The conveying pipeline for connecting the flash tank and the ammonium sulfate mother liquor heater further comprises a stop valve and a bypass pipeline, a bypass valve is arranged in the bypass pipeline, and the detection device is interlocked with the stop valve, the bypass valve and the emptying valve. The emptying valve is used for sending unqualified steam condensate flowing out of the ammonium sulfate mother liquor heater to an ammonium sulfate underground tank for replenishing the saturator mother liquor.
The trip valve is connected with pipeline, and the trip valve is used for controlling pipeline's break-make. When the stop valve is opened, steam condensate in the flash tank enters an ammonium sulfate mother liquor heater through a conveying pipeline; when the stop valve is closed, the steam condensate in the flash tank can not enter the ammonium sulfate mother liquor heater through the conveying pipeline.
The bypass valve is used for controlling the on-off of the bypass pipeline, the bypass pipeline is connected with the conveying pipeline, after the bypass valve is opened, the bypass pipeline can guide the steam condensate from the conveying pipeline to the demineralized water heat exchanger and does not enter the ammonium sulfate mother liquor heater any more, and the bypass pipeline is connected with the demineralized water heat exchanger. When the shut-off valve is closed, the bypass valve is synchronously opened, the steam condensate entering the conveying pipeline flows into the bypass pipeline, and the steam condensate flowing into the bypass pipeline finally flows into the demineralized water heat exchanger, so that the steam condensate does not pass through the mother liquor heater any more.
As shown in fig. 1, in step S3, the vapor condensate generated in the flash tank may also be mixed with a small amount of low-pressure vapor in the ammonium sulfate section, and then the ammonium sulfate mother liquor is heated, where the amount of low-pressure vapor to be mixed is about 5% to 30% of the amount of low-pressure vapor required by the ammonium sulfate mother liquor heater before the heating by the vapor condensate.
As shown in fig. 1, in step S3, the steam condensate is blended with a small amount of low-pressure steam for heating the ammonium sulfate mother liquor in winter or other heat-deficient situations, wherein the amount of low-pressure steam blended is about 5% to 30% of the amount of low-pressure steam required by the ammonium sulfate mother liquor heater before heating with the steam condensate.
The ammonium sulfate mother liquor heater is provided with one steam supplementing port, the steam supplementing port can convey steam into the conveying pipeline, and the steam is mixed with steam condensate in the conveying pipeline. In order to ensure sufficient heat input required by a winter mother liquor heater, when the system works in a winter environment, a small amount of steam is mixed into a conveying pipeline before steam condensate flowing out of a flash tank enters an ammonium sulfate mother liquor heater, the amount of low-pressure steam mixed into the conveying pipeline is about 5% -30% of the amount of low-pressure steam required by the ammonium sulfate mother liquor heater before the steam condensate is not heated, the steam is mixed with the steam condensate in the conveying pipeline and then enters the ammonium sulfate mother liquor heater to heat mother liquor, meanwhile, the mixing amount of the steam in the conveying pipeline can be set and automatically adjusted according to required temperature, namely, when the temperature of the mother liquor passing through the ammonium sulfate mother liquor heater exceeds 60 ℃, a valve is automatically closed to stop the mixing of the steam, and if the temperature of the mother liquor is lower than 50 ℃, the valve is automatically opened to mix the steam. The arrangement mainly considers that the heat of the steam condensate generated by the rich oil heater of a certain scale coking plant just meets the steam quantity required by an ammonium sulfate saturator in summer, and if the heat of the steam condensate is slightly insufficient in winter, the steam is required to be additionally added to supplement the heat. However, a check valve is added before the low-pressure steam condensate flows to a condensate pipeline mixing device of the rich oil heater so as to prevent the condensate from returning to the steam pipeline.
The liquid outlet of the ammonium sulfate mother liquor heater can also be connected with a hot water pipeline, and the hot water pipeline is used for guiding the steam condensate flowing out of the ammonium sulfate mother liquor heater to an ammonium sulfate saturator or an ammonium sulfate centrifugal machine and flushing the ammonium sulfate saturator or the ammonium sulfate centrifugal machine, so that the steam and hot water consumption can be saved.
Compare with adopting steam direct heating ammonium sulfate mother liquor heater, because steam condensate malleation business turn over mother liquor heater, so adopt steam condensate still to have the advantage that can judge the ammonium sulfate mother liquor heater and lead to the hourglass through mother liquor temperature anomaly rises behind the mother liquor heater fast to ammonium sulfate mother liquor heater heating, be favorable to early discovery early maintenance.
As shown in fig. 1, the method for recycling waste heat of the rich oil heater further comprises the following steps:
s4, conveying the steam condensate flowing out of the ammonium sulfate mother liquor heater to a demineralized water heat exchanger, and further reducing the temperature of the steam condensate while heating the demineralized water;
s5, conveying the steam condensate flowing out of the demineralized water heat exchanger to a circulating cooler, and cooling the steam condensate to 30-45 ℃;
and S6, conveying the steam condensate flowing out of the circulating cooler to a desalted water raw water tank.
In the step S4, the temperature of the steam condensate flowing out of the ammonium sulfate mother liquor heater is about 60-80 ℃, the steam condensate does not contain residual steam any more, and the steam condensate at the temperature is sent to a desalted water heat exchanger for a power plant to exchange heat with the desalted water heat exchanger. The steam condensate behind the rich oil heater contains partial residual steam, if the residual steam is directly sent to a power plant for utilization without being cooled, the pipeline has a small amount of water hammer and vibration conditions, if the residual steam is not contained after heat exchange with the ammonium sulfate mother liquor at the temperature of 45-55 ℃, the temperature is reduced, the residual steam is not contained any more, the pipeline and equipment vibration phenomenon can not be generated, and the stable recovery as demineralized water is facilitated.
In the step S5, the steam condensate flowing out of the demineralized water heat exchanger is conveyed to the circulation cooler, the steam condensate entering the circulation cooler exchanges heat with the cooling water in the circulation cooler, so as to reduce the temperature of the steam condensate, and the cooling water in the circulation cooler flows in a circulating manner.
In the above step S6, the steam condensate flowing out of the circulation cooler is transferred to the demineralized water raw water tank, and the temperature of the steam condensate entering the demineralized water raw water tank is in the range of 30 to 45 ℃.
The invention is described above by way of example with reference to the accompanying drawings. It is to be understood that the specific implementations of the invention are not limited in this respect. Any insubstantial improvements over the methods and technical solutions of the present invention; the above-mentioned conception and technical solutions of the present invention may be directly applied to other fields without any improvement, and all of them are within the scope of the present invention.
Claims (5)
1. The method for recycling the waste heat of the rich oil heater is characterized by comprising the following steps:
s1, providing medium-pressure superheated steam to a rich oil heater;
s2, steam-water mixed liquid generated by heat exchange and cooling of the medium-pressure superheated steam in the rich oil heater enters a flash tank, and the steam-water mixed liquid is formed by mixing steam and steam condensate water;
s3, conveying the steam condensate generated in the flash tank to an ammonium sulfate mother liquor heater under self-pressure for heating the ammonium sulfate mother liquor;
s4, conveying the steam condensate flowing out of the ammonium sulfate mother liquor heater to a demineralized water heat exchanger;
s5, conveying the steam condensate flowing out of the demineralized water heat exchanger to a circulating cooler, and cooling the steam condensate to 30-45 ℃;
s6, conveying the steam condensate flowing out of the circulating cooler to a desalted water raw water tank;
in the step S1, the pressure of steam entering the rich oil heater is 1.5-3.2MPa, and the steam temperature is 380-450 ℃;
in the step S2, the pressure of the steam generated in the rich oil heater is 0.5-0.9MPa;
in the step S3, the vapor condensate is conveyed to an ammonium sulfate mother liquor heater located in an ammonium sulfate working section through a conveying pipeline under the pressure of flash steam in the flash tank for heating ammonium sulfate mother liquor in the ammonium sulfate mother liquor heater, the conveying pipeline comprises a conveying pipeline, the conveying pipeline is connected with the flash tank and the ammonium sulfate mother liquor heater, and the conveying pipeline is subjected to heat preservation treatment;
in the step S3, the steam condensate generated in the flash tank is mixed with low-pressure steam in an ammonium sulfate section, and then ammonium sulfate mother liquor is heated;
a liquid outlet of the ammonium sulfate mother liquor heater is provided with a detection device for detecting the content of ammonium sulfate mother liquor components possibly leaked into the steam condensate;
the conveying pipeline for connecting the flash tank and the ammonium sulfate mother liquor heater also comprises a stop valve and a bypass pipeline, a bypass valve is arranged in the bypass pipeline, and the detection device is interlocked with the stop valve, the bypass valve and the emptying valve;
the emptying valve is used for sending unqualified steam condensate flowing out of the ammonium sulfate mother liquor heater to an ammonium sulfate underground tank for supplementing saturator mother liquor;
the stop valve is connected with the conveying pipeline and used for controlling the on-off of the conveying pipeline; when the stop valve is opened, steam condensate in the flash tank enters an ammonium sulfate mother liquor heater through a conveying pipeline; when the stop valve is closed, the steam condensate in the flash tank cannot enter the ammonium sulfate mother liquor heater through the conveying pipeline;
the bypass valve is used for controlling the on-off of a bypass pipeline, the bypass pipeline is connected with the conveying pipeline, after the bypass valve is opened, the bypass pipeline guides steam condensate from the conveying pipeline to the demineralized water heat exchanger, the steam condensate does not enter the ammonium sulfate mother liquor heater any more, and the bypass pipeline is connected with the demineralized water heat exchanger; when the shut-off valve is closed, the bypass valve is synchronously opened, steam condensate entering the conveying pipeline flows into the bypass pipeline, and the steam condensate flowing into the bypass pipeline finally flows into the demineralized water heat exchanger, so that the steam condensate does not pass through the mother liquor heater any more;
a control valve is arranged at the liquid outlet of the ammonium sulfate mother liquid heater and used for controlling the opening and closing of the liquid outlet of the ammonium sulfate mother liquid heater, and the flow and the pressure of the steam condensate flowing out of the liquid outlet of the ammonium sulfate mother liquid heater are controlled by the control valve;
in the step S4, the temperature of the steam condensate flowing out of the ammonium sulfate mother liquor heater is 60-80 ℃, and the steam condensate at the temperature is sent to a desalted water heat exchanger for a power plant to exchange heat with the desalted water heat exchanger.
2. The method as claimed in claim 1, wherein the temperature of the steam condensate generated in the flash tank in step S3 is 151-176 ℃.
3. The method as claimed in claim 1, wherein the detecting device is a conductivity meter or a pH meter.
4. The method as claimed in claim 1, wherein the delivery conduit is 304 or 316L stainless steel conduit.
5. The rich heater waste heat recovery method as claimed in any one of claims 1 to 4, wherein in step S3, in case of winter or other heat shortage, the steam condensate is mixed with a small amount of low-pressure steam for heating the ammonium sulfate mother liquor.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202730077U (en) * | 2012-07-06 | 2013-02-13 | 唐山中润煤化工有限公司 | Coking debenzolization heat source supply device |
| CN109437239A (en) * | 2018-12-27 | 2019-03-08 | 中冶焦耐(大连)工程技术有限公司 | The low temperature position exhaust heat recovering method and device of process are absorbed in a kind of acid-making process |
| CN109929596A (en) * | 2019-04-12 | 2019-06-25 | 济南冶金化工设备有限公司 | A kind of raw coke oven gas washing, purifying and low temperature exhaust heat recyclable device and technique |
| CN212298944U (en) * | 2020-06-08 | 2021-01-05 | 唐山市宝凯科技有限公司 | Rich oil debenzolization condensate water circulation system of recycling |
| CN112610941A (en) * | 2020-12-30 | 2021-04-06 | 中冶焦耐(大连)工程技术有限公司 | Low-grade waste heat recovery system and process of coking production system |
| CN112978761A (en) * | 2019-12-12 | 2021-06-18 | 上海梅山钢铁股份有限公司 | Ammonia still ammonia steam waste heat utilization device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101760251B (en) * | 2009-12-29 | 2013-05-29 | 中冶焦耐(大连)工程技术有限公司 | New water-saving, energy-saving and less-equipment corrosion process and device for purifying coke oven gas |
-
2021
- 2021-08-16 CN CN202110937962.XA patent/CN113599850B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202730077U (en) * | 2012-07-06 | 2013-02-13 | 唐山中润煤化工有限公司 | Coking debenzolization heat source supply device |
| CN109437239A (en) * | 2018-12-27 | 2019-03-08 | 中冶焦耐(大连)工程技术有限公司 | The low temperature position exhaust heat recovering method and device of process are absorbed in a kind of acid-making process |
| CN109929596A (en) * | 2019-04-12 | 2019-06-25 | 济南冶金化工设备有限公司 | A kind of raw coke oven gas washing, purifying and low temperature exhaust heat recyclable device and technique |
| CN112978761A (en) * | 2019-12-12 | 2021-06-18 | 上海梅山钢铁股份有限公司 | Ammonia still ammonia steam waste heat utilization device |
| CN212298944U (en) * | 2020-06-08 | 2021-01-05 | 唐山市宝凯科技有限公司 | Rich oil debenzolization condensate water circulation system of recycling |
| CN112610941A (en) * | 2020-12-30 | 2021-04-06 | 中冶焦耐(大连)工程技术有限公司 | Low-grade waste heat recovery system and process of coking production system |
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