CN101093089A - Method for retrieving and using technical remaining heat in petroleum refining process - Google Patents
Method for retrieving and using technical remaining heat in petroleum refining process Download PDFInfo
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Abstract
This invention relates to a method for recovering and utilizing waste heat in oil refining including: 1, a high temperature hot water system recovers waste heat of all high temperature level and part of low temperature level and a low temperature hot water system recovers residual low temperature waste heat at a source part, 2, a heat trap part is divided into a stable part and an unstable part, the stable trap is taken as the main part of the high temperature hot water system and the unstable one is taken as the main part of the low temperature hot water system, 3, hot water is cooled to a stipulated temperature by a cooling system then sent to the source part to collect heat before returning to the source part.
Description
Technical field
The present invention relates to the waste heat recovery field in the petroleum refining industry, be specifically related to a kind of method of in petroleum refining, utilizing many hot-water heating systems to reclaim and utilize the technology waste heat.
Background technology
In China's process industrial, petroleum refining industry has occupied very important position, and the product of petroleum refining industry is to satisfy the requisite base stock of national economy every profession and trade, the modernization of national defense and people's lives.The characteristics of petroleum refining industry are exactly to drive by heat energy, different component in the oil is separated, therefore, produced a large amount of low temperature process waste heats in the oil refining apparatus production process, if can reasonably utilize these technology waste heats efficiently, the energy consumption of petroleum refining industry is further reduced.But the technology low temperature exhaust heat after the technology heat exchange, wide because of its source, the big characteristics of load difference have limited it and have utilized scope, thus adopt hot water as heating agent usually, with low temperature process residual heat collection unified utilization of getting up.Traditional process adopts a cover hot-water heating system to carry out low temperature process waste heat recovery-utilization, but thermal source part cold flow is on the low side in the hot water network, limited the reasonable coupling of cold and hot logistics in the network, in addition, in hot trap part, there is hot-fluid problem on the low side equally, not only limits hot trap user's low temperature process UTILIZATION OF VESIDUAL HEAT IN, cause hot water network heat recovery-utilization rate low; Because the complexity and the polytropy of hot trap user's heat situation constantly produce network and disturb, because a cover hot-water heating system makes network flexible not enough, traditional process has the big problem of operation fluctuation usually again simultaneously.
Summary of the invention
For overcoming existing recovery and utilizing the above-mentioned shortcoming of technology waste heat method, the invention provides the method for utilizing many hot-water heating systems in petroleum refining, to reclaim and utilize the technology waste heat, comprise thermal source part heat-obtaining, return the technological process of thermal source part heat-obtaining after the heat supply of hot trap part, the heat supply again, specifically may further comprise the steps:
(1) thermal source part heat-obtaining: in the thermal source part, the technology waste heat is divided into 200～120 ℃ high potential temperature and 120～70 ℃ low potential temperature two classes, accordingly hot-water heating system is divided into two kinds of high-temperature-hot-water system (the whole temperature of hot water heat exchange is 130～100 ℃) and low-temperature water heating systems (the whole temperature of hot water heat exchange is 100～85 ℃), wherein the high-temperature-hot-water system places the upstream of process-stream waste heat recovery flow process, to reclaim the technology waste heat of whole high potential temperatures and the low potential temperature of part, and as the regulating measure of high-temperature technology logistics (going out 200～120 ℃ of heat-exchange network temperature), the low-temperature water heating system then places the downstream of process-stream waste heat recovery flow process, reclaim residue low temperature process waste heat, and as the regulating measure of low temperature process logistics (going out 120～70 ℃ of heat-exchange network temperature);
(2) hot trap part heat supply: in hot trap part, will be divided into steady heat trap and unstable hot trap according to its variation with hot user with thermic load; The high-temperature-hot-water system is based on supply steady heat trap, and the low-temperature water heating system is then to supply unstable hot trap;
(3) last, respectively the hot water of high-temperature systems and cryogenic system is cooled to 70～50 ℃ by cooling system, and then delivers to thermal source part heat-obtaining.
Technology waste heat among the present invention is meant the technology waste heat in 200～70 ℃ of scopes.
For better realization the present invention, can take following prioritization scheme:
The flow process of thermal source part heat-obtaining is in the described step (1): in the thermal source part, first from the high-temperature-hot-water system hot water of cooling system with the heat exchange of fractionation cat head oil gas, and then with a heat exchange of top circulating reflux, the hot water temperature of high-temperature-hot-water system reaches 100～130 ℃ after the heat exchange; First with fractionation top pumparound secondary heat exchange from the low-temperature water heating system hot water of cooling system, with diesel oil and stable gasoline logistics heat exchange, the hot water temperature reaches 85～90 ℃ after the heat exchange again;
The flow process of hot trap part heat supply is in the described step (2): in hot trap part, the heat exchange process of steady heat trap is, deliver to gas fractionation unit earlier from the high-temperature-hot-water system hot water (100～130 ℃) that thermal source partly comes, and then, deliver to the cooling system cooling at last as the thermal source of heating crude oil; The heat exchange process of astable hot trap is that the low-temperature water heating system hot water (85～100 ℃) from thermal source partly comes is used as the heating thermal source earlier, then is used as oil product and accompanies thermal source, and then as unboiled water heating thermal source, deliver to the cooling system cooling at last.
Method of the present invention is the optimization improvement to the oil refining apparatus of petrochemical industry and technology UTILIZATION OF VESIDUAL HEAT IN in the chemical plant installations and recovery method.This method has partly carried out optimizing improvement at the technology waste heat recovery with utilizing thermal source and hot trap in the system respectively:
At first, the present invention adopts hot water as heating agent the technology waste heat to be reclaimed, by high low temperature two cover hot-water heating systems, the technology waste heat is carried out step to be reclaimed, realize the maximization of energy recovery efficiency, two cover hot-water heating systems are respectively the regulating measure of high potential temperature heat-exchange network and low potential temperature heat-exchange network simultaneously, have improved the flexibility ratio and the operability of device heat-exchange network.
Secondly, the present invention in hot trap part, will be divided into two classes according to its variation with thermic load by analyzing hot trap characteristics with hot user, and first kind user's heat load does not change substantially in time, keeps stable always, is called the steady heat trap; Second class user's heat load is with seasonal variations, and perhaps it is referred to as unstable hot trap with the bigger variation of the irregular generation of thermic load.In the technology residual neat recovering system, the high-temperature-hot-water system is based on the steady heat trap, and low potential temperature hot-water heating system is then based on the hot trap of instability, and the potential temperature height according to hot trap mates with hot water then, forms the technology residual neat recovering system.By to classification heat supply, not only improved the energy utilization efficiency of system, and strengthened the stability of system simultaneously with hot user.
The present invention compared with prior art also has following advantage and beneficial effect:
1, existing hot water heat-exchange network flow process that the present invention is perfect has been optimized the recovery of system capacity, has reduced the cooling and the heating load of relevant apparatus.
2, the present invention is that the useful of process-stream heat-exchange network replenished, and has increased its flexibility and stability.
3, the present invention has improved existing hot water energy and has utilized flow process, has optimized the utilization of hot water energy, has strengthened the stability of hot-water heating system simultaneously.
Description of drawings
Fig. 1 is existing 1 catalytic cracking unit hot water heat-exchange network block diagram;
Fig. 2 has 2 catalytic cracking unit hot water heat-exchange network block diagrams now;
Fig. 3 is existing 1,2 catalytic cracking unit hot water heat-exchange network principle process schematic diagrames;
The hot water heat-exchange network principle process schematic diagram of Fig. 4 embodiment 1;
The high-temperature-hot-water heat-exchange network of Fig. 5 embodiment 1 and low-temperature water heating heat-exchange network block diagram.
The specific embodiment
Below in conjunction with drawings and Examples, the present invention is done detailed description further, but protection scope of the present invention of the present invention is not limited in this.
Comparative example: the technology waste heat recovery in the existing catalytic cracking unit and utilize method
The recovery of technology waste heat and utilizing in the method in the existing catalytic cracking unit, hot water network heat recovery section heat exchange process is as described below.Oil plant has the identical catalytic cracking unit of two covers and is respectively 1 catalytic cracking unit and 2 catalytic cracking units, and this two covers catalytic cracking unit all has separately independently hot-water heating system, in order to reclaim the low temperature process waste heat in this device.As shown in Figure 1, at 1 catalytic cracking unit, hot water once (650t/h) in parallel three tunnel is followed cat head oil gas, stable gasoline three times, three heat exchange of diesel oil respectively by heat exchanger 1-6, heat exchanger 19-22 and heat exchanger 7-10 respectively, merges after the heat exchange, and temperature is increased to 80 ℃ from 65 ℃; And be divided into three the tunnel once more, one tunnel not heat exchange, in addition two-way respectively by heat exchanger 11-14 (two and two strings) and heat exchanger 15-18 (two and two strings) with top circulating reflux and diesel oil secondary heat exchange, three tunnel merging then, the hot water temperature is increased to 95 ℃ from 80 ℃, enters the thermal water utilization system then.As shown in Figure 2, at 2 catalytic cracking units, hot water backwater (465t/h) is 75 ℃ with cat head oil gas heat exchange temperature from 60 ℃ of risings by heat exchanger 23-28 earlier, two-way in parallel then, lead up to heat exchanger 31-34, heat exchanger 29 respectively with top circulating reflux and stable gasoline secondary heat exchange, another road by heat exchanger 35-38 and heat exchanger 30 respectively with three heat exchange among diesel oil three times and, two-way merging then, the hot water temperature reaches 95 ℃, sends the thermal water utilization system to.
As shown in Figure 3, the heat exchange process of existing thermal water utilization part is, 90 ℃ of hot water from 1 catalytic cracking unit are distributed to gas separation unit, crude oil tank farm heating and living area heating use by sending out the power transformation workshop, owing to be subjected to seasonal effect serious with thermic load, return water temperature fluctuates between 80 ℃～70 ℃, backwater is delivered to cooler and is chilled to 65 ℃, returns 1 catalytic cracking unit main fractionating tower and recycles; 99 ℃ of hot water from 2 catalytic cracking units are distributed to product purification heating, process-stream companion's heat and living area heating use by sending out the power transformation workshop, because company's product purification scheme changes and mainly adopts steam to do process-stream and accompany thermal source, the utilization rate of its hot water is very low, return water temperature fluctuates about 80 ℃, it is but cold by the back substantially to reclaim heat, after backwater is delivered to cooler and is chilled to 60 ℃, send 2 catalytic cracking unit main fractionating towers back to and recycle.
The recovery of embodiment 1 technology waste heat of the present invention and utilize method
Annotate: 1 alleged in 1 catalytic unit described in this example and 2 catalytic units and above-mentioned comparing embodiment catalytic unit is identical with 2 catalytic units.1 catalytic cracking unit main fractionating tower top circulating reflux is called for short 1 catalysis top and follows, one mid-pumparound of 1 catalytic cracking unit main fractionating tower is called for short in 1 catalysis one, 2 catalytic cracking unit main fractionating tower top circulating refluxs are called for short 2 catalysis top to be followed, and one mid-pumparound of 2 catalytic cracking unit main fractionating towers is called for short in 2 catalysis one.
Be illustrated in figure 4 as of the present invention pair of hot water network system, thermal water utilization part flow process.The two cover hot-water heating systems that adopt present embodiment realize two cover catalytic cracking unit technology afterheat utilization in the precedent, and wherein Fig. 4 left side represents that the high-temperature-hot-water system supply stablizes the hot trap of class, and the right is the astable hot trap of low-temperature water heating system supply.
120 ℃ of high-temperature-hot-water system hot water and 90 ℃ of low-temperature water heating system hot water are delivered to high-temperature-hot-water surge tank and low-temperature water heating surge tank respectively by online oily detector.Hot water stopped in surge tank 10～20 minutes, was delivered to by heat-exchanger pump and used hot user, realized recycling of hot water.
In the high-temperature-hot-water system, from 120 ℃ of surge tank, 500t/h hot water through the heat-exchanger pump pressurized delivered to the moisturizing valve, hot water enters the silent steam afterburner after moisturizing, after injecting the low-pressure steam concurrent heating, hot water is delivered to gas fractionation unit, thermo-power station and crude oil tank farm, do gas separation unit thermal source, preheating unboiled water thermal source and heating in crude oil thermal source respectively.From the next high-temperature-hot-water system hot water of high-temperature-hot-water surge tank, elder generation's supply gas fractionating device, 120 ℃ of high-temperature-hot-waters, 500t/h two-way at first in parallel are respectively as deisobutanizer and depropanizing tower tower bottom reboiler, temperature is reduced to 105 ℃ after the heat exchange, continuation is as propylene tower reboiler thermal source, and temperature is reduced to 78 ℃ after the heat exchange.78 ℃ of hot water are respectively as dethanizer, deisobutanizer feed preheater, dethanizer feed preheater thermal source, remerging after the heat exchange is one road hot water, temperature is reduced to 71 ℃, two-way in parallel is then delivered to tank field preheating crude oil and thermo-power station preheating unboiled water respectively, after hot water goes out tank field and thermo-power station, mix the back temperature and reduce to 55 ℃.
In the low-temperature water heating system, from 90 ℃ of next low-temperature water heating 1300t/h of low-temperature water heating surge tank, hot water enters the silent steam afterburner after moisturizing, after injecting the low-pressure steam concurrent heating, respectively as living area heating thermal source, crude oil is accompanied thermal source and power station demineralized water heating thermal source with hot water in parallel three tunnel.Hot water mixes after leaving living area, thermo-power station and crude oil pipeline, and temperature is reduced to 73 ℃.55 ℃ of hot water 500t/h of high-temperature-hot-water system and 65 ℃ of hot water 1300t/h of low-temperature water heating system from hot trap partly returns deliver to cooler respectively and are cooled to 55 ℃ and 65 ℃, deliver to 1 catalytic cracking unit and 2 catalytic cracking unit heat-obtainings then.
As shown in Figure 5, the heat exchange process of of the present invention pair of hot water network system heat recovery part.
At first, at first enter 1 catalytic cracking unit heat-obtaining from 55 ℃ of high-temperature-hot-water 500t/h of cooler, at 1 catalytic cracking unit, hot water is earlier by the cat head oil gas heat exchange of heat exchanger 1-6 with 114 ℃.After the heat exchange, oil gas cools to 79 ℃, and hot water then is warmed up to 82 ℃, goes heat exchanger 11-14 to follow a heat exchange with 150 ℃ 1 catalysis top again and is warming up to 107 ℃.Wherein the top is followed and is cooled to 102 ℃, and 107 ℃ hot water goes heat exchanger 7-8 with after three heat exchange to 111 of diesel oil ℃ again, and diesel oil then cools to 110 ℃.Hot water is then delivered to 2 catalytic cracking units and is continued heat-obtaining after 1 catalytic cracking unit is heated to 110 ℃.At 2 catalytic cracking units, hot water follows a heat exchange by heat exchanger 31-32 with 133 ℃ 2 catalysis top earlier and is warming up to 117 ℃.After the heat exchange, the top is followed and is cooled to 120 ℃, 117 ℃ of hot water go heat exchanger 37-38 to follow three heat exchange of 2 catalytic cracking unit diesel oil of 145 ℃ again, wherein diesel oil cools to 126 ℃, hot water then is warmed up to 119 ℃, parallel connection goes that secondary (63t/h) heat exchange is warming up to 125 ℃ in heat exchanger 41 and 2 catalysis one of heat exchanger 30 heel part then, secondary in one after the heat exchange (63t/h, 136 ℃) then with have neither part nor lot in 219 ℃ of the hot water heat exchange, the by-pass stream of 75t/h and mix, 181 ℃ are returned tower then.
Secondly, deliver to 1 catalytic cracking unit main fractionating tower, 2 catalytic cracking unit main fractionating tower heat-obtainings and solvent deasphalting unit heat-obtaining respectively from 65 ℃ of parallel connections three tunnel of low-temperature water heating of cooler.
At 1 catalytic cracking unit main fractionating tower, 300t/h, 65 ℃ backwater in parallel by heat exchanger 19-20 and heat exchanger 9-10 respectively with 90 ℃ 1 catalytic cracking unit stable gasoline (166t/h) and four (85t/h) heat exchange of 1 catalytic cracking unit diesel oil of 110 ℃.Stable gasoline to change the back temperature be 71 ℃, diesel oil to change the back temperature be 70 ℃, hot water then is heated to 76 ℃, and then follows secondary (435t/h) heat exchange to 89 ℃ with 102 ℃ 1 catalysis top, goes to send out a power transformation workshop, the top is followed and is then cooled to 85 ℃.
At 2 catalytic cracking unit main fractionating towers, 750t/h, 65 ℃ backwater and be unified into three the tunnel.One road 400t/h is warming up to 86 ℃ by heat exchanger 23-28 (parallel connection) with cat head oil gas (104 ℃, 172t/h) heat exchange, and after the heat exchange, oil gas cools to 86 ℃; Another road 300t/h follows secondary (120 ℃, 484t/h) heat exchange by heat exchanger 33-34 and heat exchanger 39-40 (two and two strings) with 2 catalysis top, and after the heat exchange, the top is followed and cooled to 82 ℃ and return tower, and hot water then is warmed up to 97 ℃.Last road 50t/h, series connection follows 2 catalytic cracking unit diesel oil four times (126 ℃, 84t/h) and 2 catalytic cracking unit stable gasolines (125 ℃, 127t/h) heat exchange to be warming up to 108 ℃ respectively by heat exchanger 35-36 and heat exchanger 29, after the heat exchange, diesel oil cools to 89 ℃, stable gasoline cools to 111 ℃, and it is 92 ℃ that three strands of hot water mix the back temperature.
The hot water of aforementioned two-way low-temperature water heating system and mixes from 96 ℃ of hot water 250t/h of solvent deasphalting unit.After the mixing, the hot water of low-temperature water heating system reaches 90 ℃.
Present embodiment has proposed a kind of new method and a kind of new method of utilizing the technology waste heat based on hot-water heating system in gas fractionation unit, power houses, oil product workshop, heating that reclaims the catalytic cracking process waste heat based on hot-water heating system.Energy-saving effect is as follows:
1, reduces the equivalent recirculated cooling water and consume 2750t/h.Wherein 1 catalytic cracking unit 800t/h, the 1000t/h of high-temperature-hot-water system, the 950t/h of low-temperature water heating system.The recirculated cooling water energy consumption is pressed 0.1KgEO/t and is calculated, and adds up to save ideal fuels oil consumption 275KgEO/h.
2, reduce low-pressure steam and consume 33t/h.Wherein gas separation unit 24t/h, power station 9t/h.Push steam energy consumption 76KgEO/t and calculate, save ideal fuels oil 2508KgEO/h.
3, the needs of adjusting owing to 2 catalytic cracking unit hot-water heating system heat exchange processes, middle pressure steam 4t/h takes place in 2 catalytic cracking unit slurry oils less, presses middle pressure steam energy consumption quota 88KgEO/t and calculates, and energy loss is 352KgEO/h.
Add up to above-mentioned three, this low temperature technology waste heat recovery with utilize the total amount of energy saving 2431KgEO/h of scheme.Press crude runs 649.55t/h and calculate the decline 3.7KgEO/t of refining energy consumption crude oil.
As mentioned above, can realize the present invention preferably.
Claims (3)
1, reclaim and utilize the method for technology waste heat in a kind of petroleum refining, comprise thermal source part heat-obtaining, return the technological process of thermal source part heat-obtaining after the heat supply of hot trap part, the heat supply again, it is characterized in that, may further comprise the steps:
(1) thermal source part heat-obtaining: in the thermal source part, the technology waste heat is divided into 200～120 ℃ high potential temperature and 120～70 ℃ low potential temperature two classes, accordingly hot-water heating system is divided into two kinds of high-temperature-hot-water system and low-temperature water heating systems, wherein the high-temperature-hot-water system places the upstream of process-stream waste heat recovery flow process, to reclaim the technology waste heat of whole high potential temperatures and the low potential temperature of part, and as the regulating measure of high-temperature technology logistics, the low-temperature water heating system then places the downstream of process-stream waste heat recovery flow process, reclaim residue low temperature process waste heat, and as the regulating measure of low temperature process logistics;
(2) hot trap part heat supply: in hot trap part, will be divided into steady heat trap and unstable hot trap according to its variation with hot user with thermic load; The high-temperature-hot-water system is based on supply steady heat trap, and the low-temperature water heating system is then to supply unstable hot trap;
(3) last, respectively high-temperature systems hot water and cryogenic system hot water are cooled to 70～50 ℃ by cooling system, and then deliver to thermal source part heat-obtaining.
2, reclaim and utilize the method for technology waste heat in a kind of petroleum refining according to claim 1, it is characterized in that, the flow process of thermal source part heat-obtaining is in the described step (1): in the thermal source part, first from the high-temperature-hot-water system hot water of cooling system with the heat exchange of fractionation cat head oil gas, and then with a heat exchange of top circulating reflux, the hot water temperature of high-temperature-hot-water system reaches 100～130 ℃ after the heat exchange; First with fractionation top pumparound secondary heat exchange from the low-temperature water heating system hot water of cooling system, respectively with diesel oil and stable gasoline logistics heat exchange, the hot water temperature is 85～90 ℃ after the heat exchange again.
3, reclaim and utilize the method for technology waste heat in a kind of petroleum refining according to claim 1, it is characterized in that, the flow process of hot trap part heat supply is in the described step (2): in hot trap part, the heat exchange process of steady heat trap is, deliver to gas fractionation unit earlier from 100～130 ℃ the high-temperature-hot-water system hot water that thermal source partly comes, and then, deliver to the cooling system cooling at last as the thermal source of heating crude oil; The heat exchange process of astable hot trap is that 85～100 ℃ low-temperature water heating system hot water from thermal source partly comes is used as the heating thermal source earlier, then is used as oil product and accompanies thermal source, and then as unboiled water heating thermal source, deliver to the cooling system cooling at last.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105651067A (en) * | 2014-12-02 | 2016-06-08 | 上海优华系统集成技术有限公司 | High-temperature flue gas heat integration system |
| CN110287509A (en) * | 2019-04-25 | 2019-09-27 | 浙江大学 | Flexibility analysis and the fault of construction diagnosis of municipal heating systems and localization method and system |
| CN111219905A (en) * | 2020-02-21 | 2020-06-02 | 中国电力工程顾问集团西南电力设计院有限公司 | Cold and heat source combined configuration structure and operation method of centralized refrigeration and heating system of power plant |
| CN113110356A (en) * | 2021-05-06 | 2021-07-13 | 上海优华系统集成技术股份有限公司 | Intelligent optimization control equipment of low-temperature thermal system |
-
2007
- 2007-06-19 CN CNB2007100286719A patent/CN100480587C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105651067A (en) * | 2014-12-02 | 2016-06-08 | 上海优华系统集成技术有限公司 | High-temperature flue gas heat integration system |
| CN105651067B (en) * | 2014-12-02 | 2018-04-06 | 上海优华系统集成技术有限公司 | A kind of high-temperature flue gas heat integrated system |
| CN110287509A (en) * | 2019-04-25 | 2019-09-27 | 浙江大学 | Flexibility analysis and the fault of construction diagnosis of municipal heating systems and localization method and system |
| CN110287509B (en) * | 2019-04-25 | 2021-05-04 | 浙江大学 | Flexible analysis and structural defect diagnosis and positioning method and system for urban heat supply network |
| CN111219905A (en) * | 2020-02-21 | 2020-06-02 | 中国电力工程顾问集团西南电力设计院有限公司 | Cold and heat source combined configuration structure and operation method of centralized refrigeration and heating system of power plant |
| CN111219905B (en) * | 2020-02-21 | 2024-04-16 | 中国电力工程顾问集团西南电力设计院有限公司 | Cold and heat source combined configuration structure and operation method of concentrated refrigeration and heating system of power plant |
| CN113110356A (en) * | 2021-05-06 | 2021-07-13 | 上海优华系统集成技术股份有限公司 | Intelligent optimization control equipment of low-temperature thermal system |
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