CN105176582A - Aromatics combination plant - Google Patents
Aromatics combination plant Download PDFInfo
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- CN105176582A CN105176582A CN201510671026.3A CN201510671026A CN105176582A CN 105176582 A CN105176582 A CN 105176582A CN 201510671026 A CN201510671026 A CN 201510671026A CN 105176582 A CN105176582 A CN 105176582A
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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
Abstract
The invention provides an aromatics combination plant. The aromatics combination plant comprises a first deoxygenated water branch pipe (11), a second deoxygenated water branch pipe (12), a third deoxygenated water branch pipe (13) and a fourth deoxygenated water branch pipe (14) which are connected to a deoxygenated water filling total pipe (10); the first deoxygenated water branch pipe (11) can subjected to heat exchange with methylbenzene overhead gas through a first steam heat exchanger (21); the second deoxygenated water branch pipe (12) can be subjected to heat exchange with heavy aromatics overhead gas through a second steam heat exchanger (22); the third deoxygenated water branch pipe (13) can be subjected to heat exchange with aromatics of an adsorption separation tower through a third steam heat exchanger (23); the fourth deoxygenated water branch pipe (14) can be subjected to heat exchange with a desorption agent of the adsorption separation tower through a fourth steam heat exchanger (24). According to the aromatics combination plant provided by the invention, low-temperature waste heat of the aromatics combination plant is recycled and utilized, the investment of air cooling equipment is reduced, the scale and the energy consumption of a power station and a refrigeration station in the aromatics combination plant are reduced, the electricity consumption of a whole factory is saved through waste heat power generation, the operation cost of the aromatics combination plant is reduced on the whole, and economic benefits are brought for the factory.
Description
Technical field
A kind of Aromatic Hydrocarbon United Plant of the present invention.
Background technology
Aromatic Hydrocarbon United Plant flow process is complicated, and recycle stock is many, and energy consumption remains high always.This is because aromatic hydrocarbon product purity requirement is high, component boiling point is close, and in product separation flow process, reflux ratio is large, needs larger hot and cold load.In order to reclaim this part heat, by the mode of heat integration, by tower top, materials at bottom of tower and other processing medium heat exchange are to reclaim this part heat.Not high for some thermal medium potential temperatures, can not find the heat exchange with it of suitable processing medium at device, in the design of routine, often adopt air cooler to be cooled, wasted a lot of energy like this.In the p-Xylene unit of a set of 600,000 tons/year, the low-temperature heat quantity of waste reaches 150.52MW, and being folded to product per ton is 7.24GJ, if can reclaim this part energy, then greatly can reduce the production energy consumption of device.On the other hand, sending hydrogen purity outside to improve reformation, improving the liquid yield of aromatic hydrocarbon product, needing to use a lot of refrigeration duty in aromatic device, in order to processing medium to be cooled to 4 DEG C ~ 12 DEG C, to realize the maximization that liquid is received.No matter adopt compression-type refrigeration or absorption refrigeration, all need extra energy consumption, the actual comprehensive energy consumption index also indirectly having raised device.
The also few of Low Temperature Thermal recovery technology is adopted in current domestic built Aromatic Hydrocarbon United Plant, major cause is that the low-temperature heat quantity of aromatic device mainly concentrates on 90 DEG C ~ 150 DEG C, low-pressure steam and the low-temperature water heating potential temperature of generation are not high, and its energy conversion efficiency is lower.Some design engineer are for security consideration on the other hand, do not wish to introduce steam in aromatic device.Due in aromatics production technique, a large amount of catalyzer using molecular sieve composition, sorbent material etc.Because molecular sieve is more responsive to water-content, if interchanger leaks in occurring, then can cause processing medium band water, and molecular sieve is polluted.
Summary of the invention
In order to solve the problem that in existing Aromatic Hydrocarbon United Plant, heat recovery technology level is lower, the invention provides a kind of Aromatic Hydrocarbon United Plant, the low temperature exhaust heat slatterned in aromatic device can fully reclaim by this Aromatic Hydrocarbon United Plant, reasonably mated by potential temperature, recovered energy achieves optimum use.
The technical solution adopted for the present invention to solve the technical problems is: a kind of Aromatic Hydrocarbon United Plant, comprise supply mains on deaerated water, on deaerated water, supply mains is connected with the first deaerated water arm, the second deaerated water arm, the 3rd deaerated water arm and the 4th deaerated water arm; First deaerated water arm is provided with the first vapor heat exchanger; Second deaerated water arm is provided with the second vapor heat exchanger; 3rd deaerated water arm is provided with the 3rd vapor heat exchanger; 4th deaerated water arm is provided with the 4th vapor heat exchanger; First deaerated water arm can pass through the first vapor heat exchanger and the heat exchange of toluene tower top gas; Second deaerated water arm can pass through the second vapor heat exchanger and the heat exchange of heavy aromatics overhead gas; 3rd deaerated water arm can pass through the aromatic hydrocarbons heat exchange of the 3rd vapor heat exchanger and absorptive separation column; 4th deaerated water arm can pass through the strippant heat exchange of the 4th vapor heat exchanger and absorptive separation column.
On deaerated water, supply mains is also connected with the 5th deaerated water arm and the 6th deaerated water arm; 5th deaerated water arm is provided with the 5th vapor heat exchanger; 6th deaerated water arm is provided with the 6th vapor heat exchanger; 5th deaerated water arm can pass through the 5th vapor heat exchanger and the heat exchange of Extract overhead gas; 6th deaerated water arm can pass through the 6th vapor heat exchanger and the heat exchange of raffinate column top gas.
The invention has the beneficial effects as follows, the low temperature exhaust heat slatterned in aromatic device can fully reclaim by this Aromatic Hydrocarbon United Plant, and reasonably mated by potential temperature, recovered energy achieves optimum use.Present invention also offers a set of sfgd. simultaneously, effectively reduce and cause processing medium by the risk of steam contamination because leaking in interchanger.In addition, this Aromatic Hydrocarbon United Plant has recycled the low temperature exhaust heat of device, decreases the investment of air cooling apparatus, save device internally-powered station, the scale of refrigeration plant and energy consumption, save full factory power consumption by cogeneration, save the operation cost of device on the whole, bring economic answering to factory.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the present invention is described in further detail.
Fig. 1 is the schema that Aromatic Hydrocarbon United Plant low pressure steam utilizes.
Fig. 2 is the schema that in Aromatic Hydrocarbon United Plant, low-temperature water heating utilizes.
Wherein supply mains on 10. deaerated water, 11. first deaerated water arms, 12. second deaerated water arms, 13. the 3rd deaerated water arms, 14. the 4th deaerated water arms, 15. the 5th deaerated water arms, 16. the 6th deaerated water arms, 17. first steam manifolds, 18. second steam manifolds, 19. steam condensate house stewards;
21. first vapor heat exchangers, 22. second vapor heat exchangers, 23. the 3rd vapor heat exchangers, 24. the 4th vapor heat exchangers, 25. the 5th vapor heat exchangers, 26. the 6th vapor heat exchangers, 27. the 7th vapor heat exchangers;
Supply mains on 30. hot water, 31. first hot-water branches, 32. second hot-water branches, 33. the 3rd hot-water branches, 34. the 4th hot-water branches, 35. the 5th hot-water branches, 36. the 6th hot-water branches, 37. the 7th hot-water branches, 38. house stewards hot water backwater, 39. Recovery of the hot water house stewards, 310. refrigerated water upper hoses, 311. refrigerated water return water pipes;
41. first hot water heat exchangers, 42. second hot water heat exchangers, 43. the 3rd hot water heat exchangers, 44. the 4th hot water heat exchangers, 45. the 5th hot water heat exchangers, 46. the 6th hot water heat exchangers, 47. the 7th hot water heat exchangers.
Embodiment
It should be noted that, when not conflicting, the embodiment in the application and the feature in embodiment can combine mutually.Below with reference to the accompanying drawings and describe the present invention in detail in conjunction with the embodiments.
A kind of Aromatic Hydrocarbon United Plant, comprise supply mains 10 on deaerated water, on deaerated water, supply mains 10 is connected with the first deaerated water arm 11, second deaerated water arm 12, the 3rd deaerated water arm 13 and the 4th deaerated water arm 14; First deaerated water arm 11 is provided with the first vapor heat exchanger 21; Second deaerated water arm 12 is provided with the second vapor heat exchanger 22; 3rd deaerated water arm 13 is provided with the 3rd vapor heat exchanger 23; 4th deaerated water arm 14 is provided with the 4th vapor heat exchanger 24; First deaerated water arm 11 can carry out heat exchange by the first vapor heat exchanger 21 with toluene tower top gas; Second deaerated water arm 12 can carry out heat exchange by the second vapor heat exchanger 22 with heavy aromatics overhead gas; 3rd deaerated water arm 13 can carry out heat exchange by the 3rd vapor heat exchanger 23 with the aromatic hydrocarbons of absorptive separation column; 4th deaerated water arm 14 can carry out heat exchange by the 4th vapor heat exchanger 24 with the strippant of absorptive separation column, as shown in Figure 1.
In addition, on deaerated water, supply mains 10 is also connected with the 5th deaerated water arm 15 and the 6th deaerated water arm 16; 5th deaerated water arm 15 is provided with the 5th vapor heat exchanger 25; 6th deaerated water arm 16 is provided with the 6th vapor heat exchanger 26; 5th deaerated water arm 15 can carry out heat exchange by the 5th vapor heat exchanger 25 with Extract overhead gas; 6th deaerated water arm 16 can carry out heat exchange by the 6th vapor heat exchanger 26 with raffinate column top gas, as shown in Figure 1.Described Aromatic Hydrocarbon United Plant also comprises the first steam manifold 17 and the second steam manifold 18, first steam manifold 17 and the second steam manifold 18 are arranged in parallel, the exit end of the first deaerated water arm 11, the exit end of the second deaerated water arm 12, the exit end of the 3rd deaerated water arm 13 is all connected with the first steam manifold 17 with the exit end of the 4th deaerated water arm 14, the exit end of the 5th deaerated water arm 15 is all connected with the second steam manifold 18 with the exit end of the 6th deaerated water arm 16, air pressure in first steam manifold 17 is greater than the air pressure in the second steam manifold 18, as shown in Figure 1.
Concrete, the first steam manifold 17 is the 0.4MPaG low-pressure steam pipe network of full factory, the 0.2MPaG low-pressure steam pipe network of the full factory of the second steam manifold 18.During use, the thermal medium of the thermal medium of the toluene tower top gas in this Aromatic Hydrocarbon United Plant, the thermal medium of heavy aromatics overhead gas, the thermal medium of the aromatic hydrocarbons of absorptive separation column and the strippant of absorptive separation column respectively with deaerated water heat exchange, the 0.4MPaG low-pressure steam that heat exchange generates is incorporated to full factory 0.4MPaG low-pressure steam pipe network.The thermal medium of Extract overhead gas and the thermal medium of raffinate column top gas also respectively with deaerated water heat exchange, the 0.2MPaG low-pressure steam that heat exchange generates is incorporated to full factory 0.2MPaG low-pressure steam pipe network, processing medium return mechanism after heat exchange, as toluene tower top gas is back to toluene tower after heat release.
Reclaim the vapor heat exchanger that Low Temperature Thermal is arranged, if there is tube bank or tube sheet leakage, processing medium band water can be caused, and molecular sieve catalyst or sorbent material are polluted.For reducing this risk, present invention also offers a kind of sfgd..Concrete mode is, first vapor heat exchanger 21, second vapor heat exchanger 22, 3rd vapor heat exchanger 23, 4th vapor heat exchanger 24, 5th vapor heat exchanger 25 and the 6th vapor heat exchanger 26 all adopt the mode of multiple stage interchanger parallel connection to arrange, as the first vapor heat exchanger 21 is made up of the interchanger of multiple stage parallel connection, number of units in parallel is not less than 2, remaining each vapor heat exchanger is also the interchanger composition of multiple stage parallel connection, the processing medium outlet of every this interchanger of platform is equipped with water analyzer, once detect water-content in certain interchanger processing medium to exceed set(ting)value, then cut out system, and leakage interchanger is placed under repair.For overhead gas thermal medium interchanger, also need arrange a point water bag on return tank of top of the tower, a small amount of water leaked out like this can separate in water bag, and can not bring large impact to subsequent operations.Namely toluene tower return tank, heavy aromatics tower return tank, Extract tower return tank and raffinate column return tank are equipped with Fen Shuibao.
Present invention also offers a kind of Low Temperature Thermal classified utilization technology, by the low-pressure steam that waste heat recovery before obtains, arranging in device according to its potential temperature characteristic different utilizes a little, its concrete mode adopted is: the first steam manifold 17 can be the first steam-electric power unit (as 0.4MPaG low-pressure steam generating set) air feed, first steam manifold 17 can also by the 7th vapor heat exchanger 27 for the reboiler at the bottom of the solvent regeneration tower of sulfur recovery facility provides heating steam, second steam manifold 18 can be processing medium and instrument companion heat stations steam supply, second steam manifold 18 can also be that air feed organized by the second steam driven generator (as 0.2MPaG low-pressure steam generating set).Described Aromatic Hydrocarbon United Plant comprises steam condensate house steward 19, condensed water after the second steam-electric power unit utilizes, the condensed water after processing medium and instrument accompany heat stations to utilize, the condensed water after this reboiler utilizes and the condensed water after the first steam-electric power unit utilization all import steam condensate house steward 19, and steam condensate house steward 19 can supply water to supply mains on deaerated water 10.
Concrete, the 0.4MPaG low-pressure steam in described first steam manifold 17 is a part of through pressure and temperature reducing process, for the solvent reclamation bottom reboiler in desulfurizer provides thermal source after Pressure Drop to 0.3MPaG.Lime set flash distillation in the container of 0.2MPaG pressure that reboiler produces, obtain gas phase and import 0.2MPaG low-pressure steam pipe network (i.e. the second steam manifold 18), the liquid phase obtained sends into coagulation hydroenergy backwater system (i.e. steam condensate house steward 19).A 0.2MPaG low-pressure steam part in described second steam manifold 18 introduces technique companion's heat stations and instrument companion heat stations, and after heat release, lime set sends into coagulation hydroenergy backwater system (i.e. steam condensate house steward 19).In first steam manifold 17, in remaining 0.4MPaG low-pressure steam and the second steam manifold 18,0.2MPaG low-pressure steam delivers to steam-electric power unit (0.4MPaG low-pressure steam generating set and 0.2MPaG low-pressure steam generating set), steam is done manual work step-down in turbine, condensation obtains lime set and delivers to coagulation hydroenergy backwater system (i.e. steam condensate house steward 19), and generating set electricity is incorporated to full factory electrical network.Preferably, the Steam Turbine of 0.4MPaG low-pressure steam generating set and 0.2MPaG low-pressure steam generating set adopts screw.In condensate system, condensed water needs through deoxygenation, and purifying treatment Posterior circle returns supply mains 10 on deaerated water, and the deaerated water as vapor heat exchanger supplies water.
The invention provides low temperature exhaust heat in a kind of retrieving arrangement there is the technology of low-temperature water heating, its technique means mainly adopted: the disproportionation reaction product thermal medium in this Aromatic Hydrocarbon United Plant, disproportionation stabilizer tower top gas thermal medium, para-xylene product thermal medium, finishing column top gas thermal medium, isomerization reaction product thermal medium, isomerization deheptanizer column top gas thermal medium and reformate overhead gas thermal medium and low-temperature water heating heat exchange, the processing medium return mechanism (reformate overhead gas returns reformate tower after heat release) after heat exchange.Concrete, described Aromatic Hydrocarbon United Plant also comprises supply mains 30 on hot water, and on hot water, supply mains 30 is connected with the first hot-water branch 31, second hot-water branch 32, the 3rd hot-water branch 33, the 4th hot-water branch 34, the 5th hot-water branch 35, the 6th hot-water branch 36 and the 7th hot-water branch 37; First hot-water branch 31 is provided with the first hot water heat exchanger 41; Second hot-water branch 32 is provided with the second hot water heat exchanger 42; 3rd hot-water branch 33 is provided with the 3rd hot water heat exchanger 43; 4th hot-water branch 34 is provided with the 4th hot water heat exchanger 44; 5th hot-water branch 35 is provided with the 5th hot water heat exchanger 45; 6th hot-water branch 36 is provided with the 6th hot water heat exchanger 46; 7th hot-water branch 37 is provided with the 7th hot water heat exchanger 47; First hot-water branch 31 can carry out heat exchange by the first hot water heat exchanger 41 with disproportionation reaction product; Second hot-water branch 32 can carry out heat exchange by the second hot water heat exchanger 42 with disproportionation stabilizer tower top gas; 3rd hot-water branch 33 can carry out heat exchange by the 3rd hot water heat exchanger 43 with para-xylene product; 4th hot-water branch 34 can carry out heat exchange by the 4th hot water heat exchanger 44 with finishing column top gas; 5th hot-water branch 35 can carry out heat exchange by the 5th hot water heat exchanger 45 with isomerization reaction product; 6th hot-water branch 36 can carry out heat exchange by the 6th hot water heat exchanger 46 with isomerization deheptanizer column top gas; 7th hot-water branch 37 can carry out heat exchange by the 7th hot water heat exchanger 47 with reformate overhead gas, as shown in Figure 2.
In the present embodiment, described Aromatic Hydrocarbon United Plant also comprises house steward hot water backwater 38, the exit end of the first hot-water branch 31, the exit end of the second hot-water branch 32, the exit end of the 3rd hot-water branch 33, the exit end of the 4th hot-water branch 34, the exit end of the 5th hot-water branch 35, the exit end of the 6th hot-water branch 36 is all connected with house steward hot water backwater 38 with the exit end of the 7th hot-water branch 37, house steward hot water backwater 38 can be that the heating of this Aromatic Hydrocarbon United Plant is supplied water, house steward hot water backwater 38 can be hot water generating set supplying hot water, house steward hot water backwater 38 can be lithium bromide refrigerator supplying hot water.Preferably, on hot water, in supply mains 30, upper water temp is not higher than 70 DEG C, and the return water temperature after heat exchange is not less than 95 DEG C, is incorporated to house steward hot water backwater 38.
Concrete, as shown in Figure 2, a described backwater part supplies water as building and heating, and a part delivers to lithium bromide refrigerator, and for vaporizer provides thermal load, remaining hot water backwater delivers to low-temperature water heating generating set, for organic vaporizer provides thermal load.Low Temperature Thermal backwater after release of heat, circulation heat recovery supply mains 30 waterborne, delivers to each low-temperature water heating interchanger.Namely described Aromatic Hydrocarbon United Plant also comprises Recovery of the hot water house steward 39, water after this heating utilizes, the water after this hot water generating set utilizes and the water after this lithium bromide refrigerator utilizes all import Recovery of the hot water house steward 39, and Recovery of the hot water house steward 39 can thermotropism supply mains 30 waterborne supply water.Described lithium bromide refrigerator produces the cryogenic freezing water of producing 75 deg. C ~ 7 DEG C, is sent to Separate System of Water-jet, for it provides refrigeration duty, then returns this lithium bromide refrigerator by refrigerated water return water pipe 311 circulation by refrigerated water upper hose 310.Generating set electricity is incorporated to full factory electrical network.
In the present embodiment, the refrigerated water that this lithium bromide refrigerator produces can be sent to Separate System of Water-jet, and this Separate System of Water-jet comprises contact tank of reforming again, disproportionation stablizes return tank of top of the tower, reformate return tank of top of the tower, raffinate return tank of top of the tower and deheptanizer top return tank.Contact tank, the disproportionation of reforming again is stablized return tank of top of the tower and reformate return tank of top of the tower and is unified into first module, and raffinate return tank of top of the tower and deheptanizer top return tank are also unified into second unit, this first module and second unit in parallel.Refrigerated water utilizes concrete mode to be: the gas phase media of separating tank is through cryogenic heat exchanger, and the liquid phase that condensation obtains returns separating tank, and the gas phase of not condensing enters downstream process pipeline.The refrigeration duty of cryogenic heat exchanger is by water extraction confession on refrigerated water, and water on the refrigerated water being re-cooled into 5 DEG C ~ 7 DEG C after interchanger backwater returns lithium bromide refrigerator, each cryogenic heat exchanger is returned in recirculation.Preferably, the cooling temperature of separating tank gas phase after cryogenic heat exchanger is determined according to technological operation demand.
Compared with prior art, aromatic device integrated energy-saving optimisation technique provided by the invention, the low temperature exhaust heat slatterned in aromatic device fully can be reclaimed, reasonably mated by potential temperature, recovered energy achieves optimum use.Present invention also offers a set of sfgd. simultaneously, effectively reduce and cause processing medium by the risk of steam contamination because leaking in interchanger.
The present invention can be used in Aromatic Hydrocarbon United Plant that is newly-built or that transform, is described below, supposes the Aromatic Hydrocarbon United Plant of certain refinery for certain refinery's device for modifying, annual benzene and the 730000 tons of para-xylene product producing 360,000 tons/year.Wherein disproportionation scale is 1,540,000 tons/year, and fractionation by adsorption scale is 3,170,000 tons/year, and isomery turns to 2,460,000 tons/year, and it is 4,080,000 tons/year that dimethylbenzene is separated scale.
As shown in Figure 2, disproportionation reaction product thermal medium, disproportionation stablizes tower top thermal medium, para-xylene product thermal medium, finished product tower top thermal medium, isomerization reaction product, isomerization deheptanizer column top thermal medium and reformate tower top thermal medium and low-temperature water heating heat exchange, on low-temperature water heating, temperature is respectively 70 DEG C, return water temperature should be tried one's best height, and is not less than 95 DEG C.In this transformation, after the Low Temperature Thermal reclaiming each processing medium, in house steward, low-temperature water heating return water temperature is 104 DEG C.
As shown in Figure 1, the aromatic hydrocarbons thermal medium of toluene tower top gas thermal medium, heavy aromatics overhead gas thermal medium, absorptive separation column, the strippant thermal medium of absorptive separation column respectively in vapor heat exchanger with deaerated water heat exchange, heat exchange generate 0.4MPaG low-pressure steam be incorporated to full factory 0.4MPaG low-pressure steam pipe network.Extract overhead gas thermal medium and raffinate column top gas thermal medium respectively with deaerated water heat exchange, heat exchange generate 0.2MPaG low-pressure steam.
After transformation, the amount of this device recovery low temperature exhaust heat is shown in Table 1.
Table 1 low temperature retrieving arrangement reclaims heat summary table
As depicted in figs. 1 and 2, thermogenetic low-temperature water heating is changed respectively as heating water, lithium bromide refrigerator water, low-temperature water heating generating set.Change thermogenetic low-pressure steam respectively as sulfur recovery facility solvent regeneration tower reboiler, technique and instrument companion heat stations, low-pressure steam generating set vapour.
It is device gas that lithium bromide refrigerator produces refrigerated water, and liquid separation system provides low temperature load.Separate System of Water-jet comprises: contact tank of reforming again, disproportionation stablize return tank of top of the tower, reformate return tank of top of the tower, raffinate return tank of top of the tower and deheptanizer top return tank.Return tank gaseous component and refrigerated water heat exchange, the liquid phase component condensed out after cooling returns return tank, and non-condensable gas is to downstream process pipeline.
Processing medium and the vapor heat exchanger of deaerated water heat exchange be set as 2 in parallel.At every platform interchanger processing medium outlet line, water analyzer is set.Once detect that in certain interchanger processing medium, water-content exceedes set(ting)value, then cut out system by this interchanger, and in time leakage interchanger is placed under repair.Return tank of top of the tower after heat exchanger arranges water bag, comprises toluene tower return tank, heavy aromatics tower return tank, Extract tower return tank, raffinate column return tank, monitors in real time water bag liquid level.Even if like this interchanger because of interior leakage conductance cause processing medium band water time, water can separate in water bag, thus reduces the possibility that sorbent material and catalyzer be polluted by water.
After transformation, this device low temperature heat situation is shown in Table 2.Wherein operation cost is by generating set, and the general facilities consumption that lithium bromide refrigerator is used by oneself is converted to money.
Table 2 low temperature heat summary sheet
The technology of the present invention is adopted to transform Aromatic Hydrocarbon United Plant, full factory improvement expenses is about 400,000,000 yuan, and full factory reclaims low temperature exhaust heat 207.2MW altogether, and the heat of recovery is mainly device reboiler, processing medium and instrument companion heat, building and heating, lithium bromide refrigerator, low-temperature heat power generation unit etc. provides thermal load, calculated with 1 year 8400 hours, annual is that full factory saves technique 0.4MPaG steam 29.2 ten thousand tons, by-product refrigerated water 4,570,000 tons, saves generated energy 200273MW.With steam per ton 60 yuan, refrigerated water per ton 6 yuan, often spend electricity 0.82 yuan calculating, annual operation cost is 0.98 hundred million, 1 year saving fund about 1.107 hundred million yuan, and investment for trnasforming urban land cost 4 years is namely recoverable.
The above, be only specific embodiments of the invention, can not limit the scope that invention implements with it, so the displacement of its equivalent assemblies, or the equivalent variations done according to scope of patent protection of the present invention and modification, all still should belong to the category that this patent is contained.In addition, the technical characteristic in the present invention and all can using by independent assortment between technical characteristic, between technical characteristic and technical scheme, between technical scheme and technical scheme.
Claims (10)
1. an Aromatic Hydrocarbon United Plant, it is characterized in that, described Aromatic Hydrocarbon United Plant comprises supply mains on deaerated water (10), and on deaerated water, supply mains (10) is connected with the first deaerated water arm (11), the second deaerated water arm (12), the 3rd deaerated water arm (13) and the 4th deaerated water arm (14);
First deaerated water arm (11) is provided with the first vapor heat exchanger (21);
Second deaerated water arm (12) is provided with the second vapor heat exchanger (22);
3rd deaerated water arm (13) is provided with the 3rd vapor heat exchanger (23);
4th deaerated water arm (14) is provided with the 4th vapor heat exchanger (24);
First deaerated water arm (11) can by the first vapor heat exchanger (21) and the heat exchange of toluene tower top gas;
Second deaerated water arm (12) can by the second vapor heat exchanger (22) and the heat exchange of heavy aromatics overhead gas;
3rd deaerated water arm (13) can by the aromatic hydrocarbons heat exchange of the 3rd vapor heat exchanger (23) with absorptive separation column;
4th deaerated water arm (14) can by the strippant heat exchange of the 4th vapor heat exchanger (24) with absorptive separation column.
2. Aromatic Hydrocarbon United Plant according to claim 1, is characterized in that, on deaerated water, supply mains (10) is also connected with the 5th deaerated water arm (15) and the 6th deaerated water arm (16);
5th deaerated water arm (15) is provided with the 5th vapor heat exchanger (25);
6th deaerated water arm (16) is provided with the 6th vapor heat exchanger (26);
5th deaerated water arm (15) can by the 5th vapor heat exchanger (25) and the heat exchange of Extract overhead gas;
6th deaerated water arm (16) can by the 6th vapor heat exchanger (26) and the heat exchange of raffinate column top gas.
3. Aromatic Hydrocarbon United Plant according to claim 2, it is characterized in that, described Aromatic Hydrocarbon United Plant also comprises the first steam manifold (17) and the second steam manifold (18), first steam manifold (17) and the second steam manifold (18) parallel connection, the exit end of the first deaerated water arm (11), the exit end of the second deaerated water arm (12), the exit end of the 3rd deaerated water arm (13) is all connected with the first steam manifold (17) with the exit end of the 4th deaerated water arm (14), the exit end of the 5th deaerated water arm (15) is all connected with the second steam manifold (18) with the exit end of the 6th deaerated water arm (16), air pressure in first steam manifold (17) is greater than the air pressure in the second steam manifold (18).
4. Aromatic Hydrocarbon United Plant according to claim 2, it is characterized in that, first vapor heat exchanger (21), the second vapor heat exchanger (22), the 3rd vapor heat exchanger (23), the 4th vapor heat exchanger (24), the 5th vapor heat exchanger (25) and the 6th vapor heat exchanger (26) all adopt the mode of multiple stage interchanger parallel connection to arrange, the processing medium outlet of every this interchanger of platform is equipped with water analyzer, and toluene tower return tank, heavy aromatics tower return tank, Extract tower return tank and raffinate column return tank are equipped with Fen Shuibao.
5. Aromatic Hydrocarbon United Plant according to claim 2, it is characterized in that, first steam manifold (17) can be the first steam-electric power unit air feed, first steam manifold (17) can also by the 7th vapor heat exchanger (27) for the reboiler at the bottom of the solvent regeneration tower of sulfur recovery facility provides heating steam, second steam manifold (18) can be processing medium and instrument companion heat stations steam supply, and the second steam manifold (18) can also be the second steam-electric power unit air feed.
6. Aromatic Hydrocarbon United Plant according to claim 5, it is characterized in that, described Aromatic Hydrocarbon United Plant comprises steam condensate house steward (19), condensed water after the second steam-electric power unit utilizes, the condensed water after processing medium and instrument accompany heat stations to utilize, the condensed water after this reboiler utilizes and the condensed water after the first steam-electric power unit utilization all import steam condensate house steward (19), and steam condensate house steward (19) can supply water to supply mains on deaerated water (10).
7. Aromatic Hydrocarbon United Plant according to claim 1, it is characterized in that, described Aromatic Hydrocarbon United Plant also comprises supply mains on hot water (30), and on hot water, supply mains (30) is connected with the first hot-water branch (31), the second hot-water branch (32), the 3rd hot-water branch (33), the 4th hot-water branch (34), the 5th hot-water branch (35), the 6th hot-water branch (36) and the 7th hot-water branch (37);
First hot-water branch (31) is provided with the first hot water heat exchanger (41);
Second hot-water branch (32) is provided with the second hot water heat exchanger (42);
3rd hot-water branch (33) is provided with the 3rd hot water heat exchanger (43);
4th hot-water branch (34) is provided with the 4th hot water heat exchanger (44);
5th hot-water branch (35) is provided with the 5th hot water heat exchanger (45);
6th hot-water branch (36) is provided with the 6th hot water heat exchanger (46);
7th hot-water branch (37) is provided with the 7th hot water heat exchanger (47);
First hot-water branch (31) can by the first hot water heat exchanger (41) and the heat exchange of disproportionation reaction product;
Second hot-water branch (32) can by the second hot water heat exchanger (42) and the heat exchange of disproportionation stabilizer tower top gas;
3rd hot-water branch (33) can by the 3rd hot water heat exchanger (43) and para-xylene product heat exchange;
4th hot-water branch (34) can by the 4th hot water heat exchanger (44) and the heat exchange of finishing column top gas;
5th hot-water branch (35) can by the 5th hot water heat exchanger (45) and isomerization reaction product heat exchange;
6th hot-water branch (36) can by the 6th hot water heat exchanger (46) and the heat exchange of isomerization deheptanizer column top gas;
7th hot-water branch (37) can by the 7th hot water heat exchanger (47) and the heat exchange of reformate overhead gas.
8. Aromatic Hydrocarbon United Plant according to claim 7, it is characterized in that, described Aromatic Hydrocarbon United Plant also comprises house steward hot water backwater (38), the exit end of the first hot-water branch (31), the exit end of the second hot-water branch (32), the exit end of the 3rd hot-water branch (33), the exit end of the 4th hot-water branch (34), the exit end of the 5th hot-water branch (35), the exit end of the 6th hot-water branch (36) is all connected with house steward hot water backwater (38) with the exit end of the 7th hot-water branch (37), house steward hot water backwater (38) can be that the heating of this Aromatic Hydrocarbon United Plant is supplied water, house steward hot water backwater (38) can be hot water generating set supplying hot water, house steward hot water backwater (38) can be lithium bromide refrigerator supplying hot water.
9. Aromatic Hydrocarbon United Plant according to claim 8, it is characterized in that, described Aromatic Hydrocarbon United Plant also comprises Recovery of the hot water house steward (39), water after this heating utilizes, the water after this hot water generating set utilizes and the water after this lithium bromide refrigerator utilizes all import Recovery of the hot water house steward (39), and Recovery of the hot water house steward (39) can thermotropism supply mains waterborne (30) supply water.
10. Aromatic Hydrocarbon United Plant according to claim 8, it is characterized in that, the refrigerated water that this lithium bromide refrigerator produces can be sent to Separate System of Water-jet, and this Separate System of Water-jet comprises contact tank of reforming again, disproportionation stablizes return tank of top of the tower, reformate return tank of top of the tower, raffinate return tank of top of the tower and deheptanizer top return tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201510671026.3A CN105176582B (en) | 2015-10-15 | 2015-10-15 | A kind of Aromatic Hydrocarbon United Plant |
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| CN201510671026.3A CN105176582B (en) | 2015-10-15 | 2015-10-15 | A kind of Aromatic Hydrocarbon United Plant |
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| CN105176582A true CN105176582A (en) | 2015-12-23 |
| CN105176582B CN105176582B (en) | 2016-08-24 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105507972A (en) * | 2016-01-11 | 2016-04-20 | 宁波中金石化有限公司 | Power generator based on waste heat of aromatic factory technique |
| CN108019247A (en) * | 2016-11-01 | 2018-05-11 | 中石化广州工程有限公司 | A kind of aromatics absorption separation waste heat reclaiming process and device |
-
2015
- 2015-10-15 CN CN201510671026.3A patent/CN105176582B/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105507972A (en) * | 2016-01-11 | 2016-04-20 | 宁波中金石化有限公司 | Power generator based on waste heat of aromatic factory technique |
| CN108019247A (en) * | 2016-11-01 | 2018-05-11 | 中石化广州工程有限公司 | A kind of aromatics absorption separation waste heat reclaiming process and device |
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| Publication number | Publication date |
|---|---|
| CN105176582B (en) | 2016-08-24 |
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