CN101948698A - Novel energy-saving device for condensing and recovering oil shale in retorting oil gas and method - Google Patents
Novel energy-saving device for condensing and recovering oil shale in retorting oil gas and method Download PDFInfo
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Abstract
The invention relates to a novel energy-saving device for condensing and recovering oil shale in retorting oil gas and a method. Diesel is extracted from the lateral line of a fractionating tower and heavy oil is recovered from the bottom of the tower. Gaseous phase at the top of the fractionating tower accesses to a quench tower. Two streams of circulating water with different temperature are used for cooling. Oil water mixture at the bottom of the quench tower accesses to an oil-water separator. Gaseous phase at the top of the quench tower accesses to a phase-separating tank. Gasoline separated from the phase-separating tank accesses to a gasoline absorption tower from the top thereof. The gas separated from the phase-separating tank is mixed with the liquid phase at the bottom of the gasoline absorption tower and the gaseous phase at the top of a gasoline desorber to access to a balance tank. The liquid at the bottom of the balance tank accesses to the gasoline desorber from the top thereof. The gas at the top of the gasoline absorption tower accesses to a diesel absorption tower, thereby further absorbing heavy components in the gas. The method of the invention can not only recover the shale oil in the high-temperature retorting oil gas, but also divide the shale oil into the gasoline, the qualified diesel and the heavy oil. The qualified dry gas and gasoline can be obtained by the gasoline absorption tower, the gasoline desober and a diesel absorber.
Description
Technical field
The present invention relates to energy saver and method that a kind of novel oil shale distillation oil gas condensation is reclaimed.
Background technology
Resinous shale is a kind of solid fossil fuel.China's oil shale resources are abundant, have a very wide distribution, and mainly are distributed in east and middle part, are Qinghai-Tibet, western part and southern secondly.Resinous shale prediction resource in the whole nation is 7,200 hundred million t, convert for the shale oil resource be 47,600,000,000 t.Resinous shale finds out that resource is 50,000,000,000 t, and the resource of finding out of converting to shale oil is about 27.4 hundred million t, and the shale oil resource of finding out that wherein can develop is about 1,100,000,000 t.This shows that the oil shale resources of China are abundant, have excellent development to utilize prospect.
In recent years, along with the world energy sources crisis constantly aggravation and global demand of petroleum constantly rise, international oil price continues high, makes countries in the world all for seeking new energy effort, the development and utilization of resinous shale has obtained attention again.Utilizing resinous shale to produce the alternative petroleum resources of shale oil by retorting technique has become important alternatives, has been subjected to the great attention of national governments and business circles.
Condensate recovery system in the oil shale distillation technology directly has influence on the quality of product, and the energy consumption of technology and environmental issue are the important steps in the oil shale distillation technology.Domestic most oil shale distillation oil gas condensate recovery system all is the washing process of using for reference on the coking industry at present, has shortcomings such as energy recovery rate is low, quantity of circulating water is big.The condensation of oil shale distillation oil gas is reclaimed the washing technical process and is seen accompanying drawing 2.The washing process flow process is as follows: the high temperature carbonization oil gas from the destructive distillation workshop enters water wash column 40.The temperature of high temperature carbonization oil gas is reduced to 80-90 ℃ in water wash column 40, has the shale oil oil gas condensation of 50%-60% to get off simultaneously.Vapour-liquid slag mixture at the bottom of water wash column 40 towers enters vapour liquid separator 41 together.Isolated liquid-solid mixture enters mechanical settling tank 47.Mechanical settling tank 41 isolated water are delivered to burning except small part as surplus water, and rest part enters recirculated water medial launder 48 and circulating water channel 49 as recirculated water, deliver to water wash column 40 cooling oil shale retorting oil gas by water circulating pump 50.Behind the shale oil process shale oil medial launder 51 and shale oil groove 52 after the separation, deliver to the tank field by shale oil pump 53.The destructive distillation gas at vapour liquid separator 41 tops enters transverse pipe initial cooler 42, with water coolant and chilled water coal gas is cooled to 22～30 ℃ indirectly respectively, and epimere and hypomere phlegma are delivered to mechanical settling tank 47 by condensate pump 55 behind subcooling condensate circulation groove 54.After the destructive distillation gas of process transverse pipe initial cooler 42 is boosted by gas blower 43, enter electrical tar precipitator 44, reclaim shale oil once more.The electrically trapped tar oil phlegma is delivered to mechanical settling tank 47 by phlegma submerged pump 46 after entering electrically trapped tar oil condensation liquid bath 45.The washing process flow process is relatively backward, and required recirculated water consumption is big, and the energy consumption height is invested bigger.
Domestic research aspect oil shale distillation oil gas condensate recovery system at present also seldom, technology is also immature, therefore also needs a large amount of fundamental researchs.This patent has proposed energy saver and the method that a kind of novel oil shale distillation oil gas condensation is reclaimed, and remedies domestic breach in research aspect this.
Summary of the invention
Purpose of the present invention is to reclaim energy saver and method for oil shale distillation gas provides a kind of novel condensation.The present invention adopts five tower flow processs, obtains qualified dry gas after the separation, gasoline, diesel oil and heavy oil.
Technical scheme of the present invention is as follows:
The energy saver that a kind of novel oil shale distillation oil gas condensation is reclaimed comprises separation column 1, quench tower 2, naphtha scrubber 3, gasoline desorption tower 4, diesel oil absorption tower 5, side line diesel oil stripping tower 14 and gun barrel 15; It is characterized in that entering separation column 1 and be provided with destructive distillation gas inlet 18; Separation column 1 is provided with a plurality of pump circulations; Separation column 1 side line outlet 19 is connected with stripping tower 14; Stripping tower 14 cat head gaseous phase outlets 20 are connected with separation column 1; Separation column 1 cat head gas phase 21 is connected with at the bottom of quench tower 2 towers; Chilling Tata bottom outlet 22 is connected with water-and-oil separator 15; Water-and-oil separator top is provided with fuel dispensing outlet 23; The water of water-and-oil separator outlet 24 is connected with quenched water first-stage condenser 11, and the quenched water of first-stage condenser exports 25 and is connected with quench tower 2 middle parts and quenched water secondary condenser 12 respectively, and quenched water secondary condenser 26 exports and is connected with quench tower 2 tops; Quench tower 2 cat head gas phases 27 are connected with compressor 13, are connected with phase separation tank 16 through condenser 10 backs then; The fuel dispensing outlet 29 of phase separation tank 16 side lines is connected with the cat head of naphtha scrubber 3; The liquid phase 30 at the bottom of phase separation tank 16 top gas 28, naphtha scrubber 3 towers and the gas 32 of gasoline desorption tower 4 cats head are connected with surge tank 17; The gaseous phase outlet 33 of surge tank 17 is connected with at the bottom of the tower of naphtha scrubber 3, and the liquid phase of surge tank 17 outlet 34 is connected with gasoline desorption tower 4 cats head; Be provided with reboiler 9 at the bottom of gasoline desorption tower 4 towers; Q-grade gasoline outlet 39 is set at the bottom of the gasoline desorb Tata; The pneumatic outlet 31 of naphtha scrubber 3 cats head is connected with at the bottom of 5 towers of diesel oil absorption tower; Diesel oil absorption tower 5 cats head are provided with dry gas outlet 36, and liquid phase outlet 35 is set at the bottom of the tower.
Described separation column 1 epimere is provided with efficient structured packing 37, and the tower hypomere is provided with anti-clogging plug internals 38.Structured packing 37 has 20～40 theoretical stages; Anti-clogging plug internals 38 are herringbone baffle plate or grid packing.
The extraction position of separation column 1 side line extraction diesel oil 19 is the 6th theoretical stage～20th theoretical stage.Be provided with the circulation of 1～6 pump in the separation column.
Adopt device of the present invention to handle the technology of high temperature oil shale retorting oil gas, it is characterized by high temperature oil shale retorting oil gas and enter separation column.Side line is extracted diesel oil out, and diesel oil enters a steam stripped tower and meets the requirements with the initial boiling point that guarantees diesel oil.Heavy oil extraction at the bottom of the tower.In order to take the waste heat of separation column away, in separation column, be provided with 1～6 pump circulation.The gas phase of fractionator overhead enters quench tower.Adopt the recirculated water of two bursts of differing tempss to cool off in quench tower, the oil-water mixture at the bottom of the chilling Tata enters water-and-oil separator, and the quench tower middle part is returned in isolated water cooling rear section, and another part continues to be cooled to more and enters the quench tower top behind the low temperature.Quench tower cat head gas phase enters the laggard people's phase separation tank of condenser condenses through after the compressor pressurizes.The isolated gasoline of phase separation tank enters naphtha scrubber from cat head.The isolated gas of phase separation tank with enter surge tank after the gas phase of liquid phase at the bottom of the naphtha scrubber tower and gasoline desorption tower cat head is mixed.The gas at surge tank top enters the naphtha scrubber bottom, and the liquid phase of surge tank bottom enters gasoline desorption tower cat head.Gasoline desorb Tata still is provided with reboiler.The overhead gas of naphtha scrubber enters the diesel oil absorption tower, further the heavy constituent in the gas is absorbed.
Novel oil shale distillation oil gas condensation is reclaimed in the energy-saving technique, and high temperature carbonization oil gas temperature is 420～600 ℃.Separation column pressure is 0.05～0.3Mpa, and tower top temperature is controlled at 60～150 ℃, and column bottom temperature is controlled at 280～360 ℃, and theoretical stage is 20～60; Quench tower pressure is 0.06～0.16Mpa, and tower top temperature is controlled at 30～50 ℃, and column bottom temperature is controlled at 60～85 ℃, theoretical stage numerical digit 10～40; The pressure of naphtha scrubber is 0.5～2Mpa, and cat head is controlled at 20～60 ℃, and theoretical stage is 20～50; Gasoline desorption tower, pressure are 0.6～1.5Mpa, and cat head is controlled at 30～70 ℃, and theoretical stage is 20～60; The pressure on diesel oil absorption tower is 0.6～1.3Mpa, and cat head is controlled at 20～60 ℃, and theoretical stage is 20～60.
The present invention proposes a kind of novel oil shale distillation oil gas condensation and reclaim energy-saving technique, except with the shale oil recovery in the high temperature carbonization oil gas, also shale oil is cut into gasoline, qualified diesel oil and heavy oil.By naphtha scrubber, gasoline desorption tower and diesel oil absorption tower finally obtain qualified dry gas and gasoline.
Description of drawings
Fig. 1 is that the energy-saving technique schema is reclaimed in novel shale retorting oil gas condensation of the present invention;
Fig. 2 is that recovery washing process flow sheet is coagulated in the air cooling of shale oil empyreumatic oil;
Wherein: 1-separation column, 2-quench tower, 3-naphtha scrubber, 4-gasoline desorption tower, 5-diesel oil absorption tower, the circulation of 6-bottom pump; The pump circulation of 7-stage casing; The pump circulation of 8-top; 9-gasoline desorption tower reboiler; The 10-condenser; 11-quenched water-level condenser; 12-quenched water secondary condenser; The 13-compressor, 14-side line steam stripped tower; The 15-water-and-oil separator; The 16-phase separation tank; The 17-surge tank; 18-destructive distillation gas inlet; The 40-water wash column; The 41-vapour liquid separator; The 42-transverse pipe initial cooler; The 43-gas blower; The 44-electrical tar precipitator; 45-electrical tar precipitator condensation liquid bath; 46-phlegma submerged pump; The 47-mechanical settling tank; 48-shale oil medial launder; 49-shale oil groove; 50-shale oil pump; 51-recirculated water medial launder; The 52-circulating water channel, the 53-water circulating pump; 54-phlegma circulation groove; The 55-condensate pump.
Embodiment
The present invention is described in further detail below in conjunction with accompanying drawing:
The washing technical process is reclaimed in oil shale distillation oil gas condensation in the Comparative Examples, as shown in Figure 2.
With certain refinery is example, and its high temperature carbonization oil and gas content is 22187kg/h, and feeding temperature is 490 ℃.High temperature carbonization oil gas enters water wash column.The temperature of destructive distillation oil gas is reduced to 90 ℃ by 490 ℃ in water wash column, has 60% shale oil oil gas condensation to get off simultaneously.Solid-liquid slag mixture at the bottom of the washing Tata enters vapour liquid separator.Isolated solidliquid mixture enters mechanical settling tank.The isolating water major part of mechanical settling tank is circulated to water wash column and is used for cooling down high-temperature destructive distillation oil gas, and small part is delivered to burning as surplus water.Be pumped to the tank field by shale oil behind the isolating shale oil process shale oil tank.Regularly act as a fuel after the shale dregs of fat are collected and sell.Gasoline trap top gas phase enters transverse pipe initial cooler, uses water coolant (32～40 ℃) and chilled water (16～32 ℃) that destructive distillation gas is cooled to 45 ℃ and 22 ℃ indirectly respectively.The phlegma of transverse pipe initial cooler is delivered to mechanical settling tank by condensate pump behind the subcooling condensate groove.After boosting by gas blower through the destructive distillation gas of transverse pipe initial cooler, enter electrical tar precipitator, reclaim tar once more after.
Embodiments of the invention:
Novel oil shale distillation oil gas condensation of the present invention is reclaimed energy-saving technique as shown in Figure 1, has described mode of connection in summary of the invention in detail, operational condition, and flow process etc. are exemplary illustration at this.
High temperature oil shale retorting oil gas enters separation column.Side line is extracted diesel oil out, and diesel oil enters a steam stripped tower and meets the requirements with the initial boiling point that guarantees diesel oil.Heavy oil extraction at the bottom of the tower.In order to take the waste heat of separation column away, in separation column, be provided with three pumps and follow.The gas phase of fractionator overhead enters quench tower.Adopt the recirculated water of two bursts of differing tempss to cool off in quench tower, the oil-water mixture at the bottom of the chilling Tata enters water-and-oil separator, and the quench tower middle part is returned in isolated water cooling rear section, and another part continues to be cooled to more to enter the quench tower top behind the low temperature.Quench tower cat head gas phase enters the laggard people's phase separation tank of condenser condenses through after the compressor pressurizes.The isolated gasoline of phase separation tank enters naphtha scrubber from cat head.With the gasoline in gas cooling, enter surge tank after mixing at the bottom of the gas phase tower of isolated gas and liquid phase at the bottom of the naphtha scrubber tower and gasoline desorption tower cat head for further.The gas at surge tank top is connected with the naphtha scrubber bottom, and liquid phase enters gasoline desorption tower cat head.Gasoline desorb Tata still is provided with reboiler.The overhead gas of naphtha scrubber enters the diesel oil absorption tower, further the heavy constituent in the gas is absorbed.
Under conditions such as same treatment capacity, feed conditions, above-mentioned two kinds of art breading effects are compared, comparative result is as follows:
1. energy recovery
The energy recovery table of table 1 embodiment
In the Comparative Examples, 490 ℃ high temperature carbonization oil gas enters water wash column, cools off with a large amount of 85 ℃ hot water, and the destructive distillation gas that cat head is 90 ℃ enters transverse pipe initial cooler and further cools off with water coolant.92 ℃ oil-water mixture at the bottom of the tower, through after the oily water separation, a large amount of recirculated waters are circulated to water wash column top cooling raw gas.From said process as can be known, the energy of 490 ℃ of destructive distillation oil gas is mainly used in less water evaporation and a large amount of recirculated water intensifications.The temperature of recirculated water is about 92 ℃ of degree, and this portion of energy utilization ratio is limited maybe can't be utilized.Therefore the energy of high temperature raw gas is not well reclaimed.
As shown in Table 1, in the technical process of the present invention, high temperature carbonization oil gas enters separation column, and by the cat head circulation, three parts that circulate at the bottom of stage casing circulation and the tower reclaim the waste heat of high-temperature oil gas.Cat head oil gas enters quencher, cools off with quenched water.Condensation is chilled to 60 ℃ to recirculated water after the oily water separation of tower bottoms body (76 ℃) through one-level, and this portion of energy can be used as energy output, and the energy of recovery is 3.3465Mkcal/h.Therefore high temperature carbonization oil gas is through technical process of the present invention, and pump circulation recoverable energy is 7.8291Mkcal/h.Except pump followed heat-obtaining, the temperature that goes out separation column stream capital stock body was very high, and this portion of energy also can fully be utilized.Side line diesel oil extraction temperature is 182.79 ℃, can be used to add thermal material or steam takes place.The temperature of tower still heavy oil is 315.74 ℃, and potential temperature is higher, can be used for taking place high pressure steam.
2. recirculated water consumption
Recirculated water scale in table 2 Comparative Examples
Recirculated water scale among table 3 embodiment
In the Comparative Examples technical process, come high temperature carbonization oil gas is cooled off with recirculated water, the consumption of recirculated water is very big, nearly 330t/h.Vapour liquid separator top gas phase enters transverse pipe initial cooler simultaneously, cools off with water coolant and chilled water respectively, and the consumption of water coolant and chilled water is respectively 720t/h and 16.11t/h.This shows that recirculated water and cooling water amount among the embodiment are big, the pump energy consumption that is used for the water conveying simultaneously is big.
In the embodiment technical process, high-temperature oil gas is introduced into main fractionating tower, diesel oil and heavy oil in the recovery high-temperature oil gas in most of energy and the condensed oil-gas.Cat head oil gas enters quench tower and cools off, and required quantity of circulating water is 155000t/h, and the consumption of recirculated water obviously reduces.
3. equipment contrast
The major equipment of Comparative Examples technical process has and mainly comprises water wash column, transverse pipe initial cooler, electrical tar precipitator etc.The washing process flow process mainly is the washing process of using for reference on the coking industry, this technology derives from the technical process of eighties of last century sixties USSR (Union of Soviet Socialist Republics), and in the development of decades, flow process changes less, most flow scheme design all is to design according to experience, so flow process and equipment are all relatively backward.
The equipment of embodiment technical process mainly contains separation column, quench tower, naphtha scrubber, gasoline desorption tower etc., this flow process combines a plurality of different process flow processs according to the characteristics of shale oil, designs the condensation that is fit to shale oil and reclaims technical process, the employed equipment of flow process all is through constantly development improvement, so equipment is more advanced.
In sum, reclaim energy-saving technique and device by novel oil shale distillation oil gas condensation of the present invention, can effectively reclaim the energy of high temperature carbonization oil gas, quantity of circulating water reduces significantly, reduces required pump energy consumption simultaneously.
Novel oil shale distillation air cooling condensation reclaiming system energy saver disclosed by the invention and method, those skilled in the art can be by using for reference this paper content, and links such as appropriate change processing parameter, structure design realize.System of the present invention is described by examples of implementation, and person skilled obviously can be changed or suitably change and combination system as herein described in not breaking away from content of the present invention, spirit and scope, realizes the technology of the present invention.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they are regarded as being included in spirit of the present invention, scope and the content.
Claims (6)
1. the energy saver that novel oil shale distillation oil gas condensation is reclaimed comprises separation column (1), quench tower (2), naphtha scrubber (3), gasoline desorption tower (4), diesel oil absorption tower (5), side line diesel oil stripping tower (14) and gun barrel (15); It is characterized in that entering separation column (1) and be provided with destructive distillation gas inlet (18); Separation column (1) is provided with a plurality of pump circulations; Separation column (1) side line outlet (19) is connected with stripping tower (14); Stripping tower (14) cat head gaseous phase outlet (20) is connected with separation column (1); Separation column (1) cat head gas phase (21) is connected with at the bottom of quench tower (2) tower; Chilling Tata bottom outlet (22) is connected with water-and-oil separator (15); Water-and-oil separator top is provided with fuel dispensing outlet (23); The water outlet (24) of water-and-oil separator is connected with quenched water first-stage condenser (11), the quenched water outlet (25) of first-stage condenser is connected with quench tower (2) middle part and quenched water secondary condenser (12) respectively, and quenched water secondary condenser (26) outlet is connected with quench tower (2) top; Quench tower (2) cat head gas phase (27) is connected with compressor (13), passes through condenser (10) back then and is connected with phase separation tank (16); The fuel dispensing outlet (29) of phase separation tank (16) side line is connected with the cat head of naphtha scrubber (3); The liquid phase (30) at the bottom of phase separation tank (16) top gas (28), naphtha scrubber (3) tower and the gas (32) of gasoline desorption tower (4) cat head are connected with surge tank (17); The gaseous phase outlet (33) of surge tank (17) is connected with at the bottom of the tower of naphtha scrubber (3), and the liquid phase outlet (34) of surge tank (17) is connected with gasoline desorption tower (4) cat head; Be provided with reboiler (9) at the bottom of gasoline desorption tower (4) tower; Q-grade gasoline outlet (39) is set at the bottom of the gasoline desorb Tata; The pneumatic outlet (31) of naphtha scrubber (3) cat head is connected with at the bottom of the tower of diesel oil absorption tower (5); Diesel oil absorption tower (5) cat head is provided with dry gas outlet (36), and liquid phase outlet (35) is set at the bottom of the tower.
2. the energy saver that novel oil shale distillation oil gas condensation as claimed in claim 1 is reclaimed is characterized in that separation column (1) epimere is provided with efficient structured packing (37), and the tower hypomere is provided with anti-clogging plug internals (38).
3. the energy saver that novel oil shale distillation oil gas condensation as claimed in claim 2 is reclaimed is characterized in that described structured packing (37) has 20～40 theoretical stages; Anti-clogging plug internals (38) are herringbone baffle plate or grid packing.
4. the energy saver that novel oil shale distillation oil gas condensation as claimed in claim 1 is reclaimed is characterized in that diesel oil (19) side line extraction position is the 6th theoretical stage～20th theoretical stage.
5. the energy saver that novel oil shale distillation oil gas condensation as claimed in claim 2 is reclaimed is characterized in that described 1～6 pump circulation that is provided with in separation column.
6. a kind of novel oil shale distillation oil gas condensation recycling method of claim 1 is characterized in that high temperature carbonization oil gas temperature is 420～600 ℃; Separation column pressure is 0.05～0.3Mpa, and tower top temperature is controlled at 60～150 ℃, and column bottom temperature is controlled at 280～360 ℃, and theoretical stage is 20～60; Quench tower pressure is 0.06～0.16Mpa, and tower top temperature is controlled at 30～50 ℃, and column bottom temperature is controlled at 60～85 ℃, theoretical stage numerical digit 10～40; The pressure of naphtha scrubber is 0.5～2Mpa, and cat head is controlled at 20～60 ℃, and theoretical stage is 20～50; Gasoline desorption tower, pressure are 0.6～1.5Mpa, and cat head is controlled at 30～70 ℃, and theoretical stage is 20～60; The pressure on diesel oil absorption tower is 0.6～1.3Mpa, and cat head is controlled at 20～60 ℃, and theoretical stage is 20～60.
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| CN109486505A (en) * | 2017-09-13 | 2019-03-19 | 中国石油化工股份有限公司 | The device and method of separating heavy from ethane cracking product |
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Inventor after: Sui Hong Inventor after: Li Xingang Inventor after: Li Hong Inventor after: Chen Juanjuan Inventor before: Chen Juanjuan Inventor before: Sui Hong Inventor before: Li Xingang Inventor before: Li Hong |
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