CN110563228A - Styrene process condensate and heat energy recovery system and control method - Google Patents
Styrene process condensate and heat energy recovery system and control method Download PDFInfo
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- CN110563228A CN110563228A CN201810567681.8A CN201810567681A CN110563228A CN 110563228 A CN110563228 A CN 110563228A CN 201810567681 A CN201810567681 A CN 201810567681A CN 110563228 A CN110563228 A CN 110563228A
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- 238000011084 recovery Methods 0.000 title claims abstract description 192
- 238000000034 method Methods 0.000 title claims abstract description 173
- 230000008569 process Effects 0.000 title claims abstract description 161
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 title claims abstract description 158
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 134
- 238000010438 heat treatment Methods 0.000 claims abstract description 14
- 230000001502 supplementing effect Effects 0.000 claims abstract description 12
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 126
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 44
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 44
- 239000004571 lime Substances 0.000 claims description 44
- 238000003860 storage Methods 0.000 claims description 37
- 238000005516 engineering process Methods 0.000 claims description 28
- 238000001914 filtration Methods 0.000 claims description 17
- 238000006392 deoxygenation reaction Methods 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 15
- 238000006356 dehydrogenation reaction Methods 0.000 description 7
- 239000002699 waste material Substances 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 125000003011 styrenyl group Chemical group [H]\C(*)=C(/[H])C1=C([H])C([H])=C([H])C([H])=C1[H] 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 239000008399 tap water Substances 0.000 description 2
- 235000020679 tap water Nutrition 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005536 corrosion prevention Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 239000011490 mineral wool Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- -1 polyethylbenzene Substances 0.000 description 1
- 229920002635 polyurethane Polymers 0.000 description 1
- 239000004814 polyurethane Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000009420 retrofitting Methods 0.000 description 1
- 239000007785 strong electrolyte Substances 0.000 description 1
- 150000003440 styrenes Chemical class 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229920003051 synthetic elastomer Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000005061 synthetic rubber Substances 0.000 description 1
- 238000010555 transalkylation reaction Methods 0.000 description 1
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 description 1
- 229920002554 vinyl polymer Polymers 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
Abstract
The invention discloses a styrene process condensate and heat energy recovery system and a control method, wherein the heat energy recovery system comprises a styrene process condensate stripping device, a first heat recovery device, a second heat recovery device and a condensate recovery device, the styrene process condensate stripping device is connected with the first heat recovery device and/or the second heat recovery device and/or the condensate recovery device, process condensate is subjected to heat recovery through the first heat recovery device and/or the second heat recovery device, and process condensate is subjected to condensate recovery through the condensate recovery device. The invention not only recycles the heat energy of the styrene process condensate, improves the heat energy utilization rate, but also reduces the amount of steam required for heating desalted water and reduces the production cost, and in addition, recycles the process condensate to be used as circulating water for supplementing water, thereby saving the circulating water supplementing cost.
Description
Technical Field
The invention belongs to the field of styrene, and particularly relates to a styrene process condensate and heat energy recovery system and a control method.
Background
Styrene is an organic compound formed by replacing one hydrogen atom of ethylene with benzene, the electron of vinyl is conjugated with a benzene ring, is insoluble in water, is dissolved in ethanol and ether, is gradually polymerized and oxidized when exposed to air, and is an important aromatic hydrocarbon. Industrially, they are important monomers for synthetic resins, ion exchange resins, synthetic rubbers and the like.
Styrene products in the market are produced by an ethylbenzene dehydrogenation process, the dehydrogenation reaction must be carried out in the presence of steam, and a large amount of process condensate is generated after condensation. The traditional treatment mode of the process condensate is that after organic matters are extracted by a process condensate stripping tower, a small part of the process condensate is used for supplying water to a boiler of a styrene device, and the rest part of the process condensate is discharged. The heat energy recovery is not fully carried out, a large amount of heat energy is wasted, and the process condensate is discharged outside, so that a large amount of water resource waste is caused.
The present invention has been made in view of this situation.
disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a styrene process condensate, a heat energy recovery system and a control method.
In order to solve the technical problems, the invention adopts the technical scheme that:
the first purpose of the invention is to provide a styrene process condensate and heat energy recovery system, the heat energy recovery system comprises a styrene process condensate stripping device, a first heat recovery device, a second heat recovery device and a condensate recovery device, the styrene process condensate stripping device is connected with the first heat recovery device and/or the second heat recovery device and/or the condensate recovery device, process condensate is subjected to heat recovery through the first heat recovery device and/or the second heat recovery device, and process condensate is subjected to condensate recovery through the condensate recovery device.
according to the technical scheme, the styrene process condensate stripping device is respectively connected with the first heat recovery device and the second heat recovery device, the first heat recovery device and the second heat recovery device are connected through pipelines, the first heat recovery device and the second heat recovery device are respectively connected with the condensate recovery device through pipelines, process condensate is subjected to heat recovery through the first heat recovery device and/or the second heat recovery device, and the process condensate is subjected to condensate recovery through the condensate recovery device.
According to the further scheme, the styrene process condensate stripping device, the first heat recovery device, the second heat recovery device and the condensate recovery device are sequentially connected, process condensate sequentially passes through the first heat recovery device and the second heat recovery device to be subjected to heat recovery, and process condensate passes through the condensate recovery device to be subjected to condensate recovery.
In a further scheme, the first heat recovery device comprises a benzene storage device and a first heating pipeline for heating the benzene storage device, process condensate discharged by the styrene process condensate stripping device enters the first heating pipeline, and at least part of heat energy of the process condensate is transferred to a medium in the benzene storage device.
In a further aspect, the second heat recovery device includes a heat exchange device, the heat exchange device includes a desalted water pipeline for desalted water to circulate and a heat exchange medium pipeline for heat exchange medium to circulate, and when the process condensate flows through the heat exchange medium pipeline, at least part of heat energy of the process condensate is transferred to the desalted water.
In a further scheme, a water inlet of the heat exchange medium pipeline is connected with a water outlet of the first heating pipeline, and a water outlet of the heat exchange medium pipeline is connected with circulating water through a pipeline;
Preferably, the system further comprises a desalted water storage device of the thermal power plant, and the water outlet of the desalted water pipeline is connected with the desalted water storage device.
in a further scheme, a filtering device is arranged between the styrene process condensate stripping device and the first heat recovery device, and at least one part of process condensate discharged by the styrene process condensate stripping device enters the first heat recovery device after passing through the filtering device;
Preferably, the system also comprises a boiler water deoxygenation device connected with the filtering device, wherein after the process condensate discharged by the styrene process condensate stripping device passes through the filtering device, one part of the process condensate enters the first heat recovery device, and the other part of the process condensate enters the boiler water deoxygenation device.
According to a further scheme, the condensate recovery device comprises a circulating water station, the first heat recovery device and/or the second heat recovery device are/is connected to a water path of the circulating water station through a pipeline, and recovered process condensate is used for supplementing water to circulating water.
a second object of the present invention is to provide a method for controlling the above-mentioned condensation and heat energy recovery system of styrene process, which comprises: the heat energy of the process condensate discharged by the styrene process condensate stripping device is subjected to twice heat recovery by the first heat recovery device and the second heat recovery device in sequence, and the process condensate is recovered by the condensate recovery device.
In a further scheme, the process condensate is subjected to heat exchange with a medium in a benzene storage device through a first heat recovery device, cooled to 80 ℃, then enters a second heat recovery device, is subjected to heat exchange with desalted water, cooled to 41 ℃, and then enters a circulating water station to be used as circulating water for supplementing water and recovering the process condensate.
After adopting the technical scheme, compared with the prior art, the invention has the following beneficial effects:
1. The invention recycles the heat energy of the styrene process condensate twice, reduces the waste of the heat energy and improves the utilization rate of the heat energy of the process condensate.
2. The heat energy of the process condensate is recycled, and the temperature of the desalted water in the thermal power plant is heated in advance, so that the steam consumption for heating the desalted water in the thermal power plant can be reduced, and a large amount of cost is saved.
3. After the styrene process condensate is recycled by heat energy, the process condensate enters a condensate recycling device for condensate recycling, the condensate is further utilized, a large amount of water resources are saved, and the cost is saved.
4. After the heat energy of the styrene process condensate is recycled, the temperature of the styrene process condensate entering the circulating water station is reduced from 80 ℃ to 41 ℃, so that the evaporation capacity can be greatly reduced, the water supplementing amount for supplementing water due to large-scale evaporation is reduced, and the cost is saved.
The following describes embodiments of the present invention in further detail with reference to the accompanying drawings.
Drawings
the accompanying drawings, which are included to provide a further understanding of the invention, are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention without limiting the invention to its proper form. It is obvious that the drawings in the following description are only some embodiments, and that for a person skilled in the art, other drawings can be derived from them without inventive effort. In the drawings:
FIG. 1 is a schematic illustration of a styrene process condensate heat recovery system prior to retrofitting of the present invention;
Fig. 2 is a schematic diagram of a modified styrene process condensate heat recovery system of the present invention.
In the figure, 1 a styrene process condensate stripping device, 2 a first heat recovery device, 21 a benzene storage device, 3 a second heat recovery device, 31 a heat exchange device, 4 a condensate recovery device, 41 a circulating water station, 5 a first heating pipeline, 6 a desalting water pipeline, 7 a heat exchange medium pipeline, 8 a filtering device, 9 a boiler water deoxidizing device and 10 a stripping tower kettle liquid pump.
It should be noted that the drawings and the description are not intended to limit the scope of the inventive concept in any way, but to illustrate it by a person skilled in the art with reference to specific embodiments.
Detailed Description
in order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and the following embodiments are used for illustrating the present invention and are not intended to limit the scope of the present invention.
In the description of the present invention, it should be noted that the terms "upper", "lower", "front", "rear", "left", "right", "vertical", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; may be directly connected or indirectly connected through an intermediate. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Example one
This embodiment provides a styrene technology lime set and heat recovery system, heat recovery system includes styrene technology lime set stripping device 1, first heat recovery unit 2, second heat recovery unit 3 and lime set recovery unit 4, styrene technology lime set stripping device 1 be connected with first heat recovery unit 2 and/or second heat recovery unit 3 and/or lime set recovery unit 4, the technology lime set carries out heat recovery through first heat recovery unit 2 and/or second heat recovery unit 3, the technology lime set carries out lime set through lime set recovery unit 4 and retrieves.
The styrene processing technology comprises two main process technology units, namely an ethylbenzene unit and a styrene unit. The ethylbenzene unit flow scheme is as follows: benzene and ethylene are subjected to alkylation and transalkylation reactions, and an intermediate product ethylbenzene is obtained after separation and is supplied to a styrene device for dehydrogenation. The main flow of the styrene unit is as follows: ethylbenzene from the ethylbenzene unit enters a styrene device to undergo dehydrogenation reaction, the product styrene is obtained after separation, the recycle benzene returns to the ethylbenzene device to continue reaction, and finally byproducts of toluene, polyethylbenzene, tar and the like are obtained.
styrene is produced by the ethylbenzene dehydrogenation process and the dehydrogenation reaction must be carried out in the presence of steam, i.e. in the styrene process condensate stripper unit 1, which upon condensation generates a large amount of process condensate. The main component of the process condensate is water and contains trace hydrocarbon organic matters, wherein most of the organic matters are removed after steam stripping in the condensate stripping tower. The condensate temperature of the partial process is very high, and if the partial process is directly discharged, a large amount of heat energy and a large amount of water are lost, so that the production cost is increased.
The styrene stripping device can be a styrene stripping tower, and the ethylbenzene is subjected to dehydrogenation reaction in the styrene stripping tower to generate process condensate. In order to avoid resource waste and save cost, the process condensate can be recycled, the heat energy of the process condensate can be recycled, or the heat energy and the water resource of the process condensate can be recycled simultaneously, so that the recycling rate is further improved.
Specific schemes may include, but are not limited to, the following:
Scheme 1, styrene technology lime set steam stripping device 1 is direct to be connected with lime set recovery unit 4, can avoid technology lime set direct emission, avoids water waste to the water resource recycle of technology lime set.
Scheme 2, styrene technology lime set steam stripping device 1 is connected with first heat recovery unit 2, and first heat recovery unit 2 passes through the tube coupling with lime set recovery unit 4, and the technology lime set carries out heat recovery through first heat recovery unit 2, and the technology lime set carries out lime set through lime set recovery unit 4 and retrieves.
Scheme 3, styrene technology lime set steam stripping device 1 is connected with second heat recovery unit 3, and second heat recovery unit 3 passes through the tube coupling with lime set recovery unit 4, and the technology lime set carries out heat recovery through second heat recovery unit 3, and the technology lime set carries out lime set through lime set recovery unit 4 and retrieves.
Scheme 4, styrene technology lime set steam stripping device 1, first heat reclamation device 2, second heat reclamation device 3 and lime set recovery unit 4 connect gradually, and the technology lime set carries out twice heat recovery through first heat reclamation device 2, second heat reclamation device 3 in proper order, and the technology lime set carries out lime set through lime set recovery unit 4 and retrieves.
In conclusion, the process condensate can be subjected to primary heat recovery or secondary heat recovery, the heat energy of the process condensate is fully utilized, and the water resource of the process condensate can be recycled. The heat energy of the styrene process condensate is recycled, the heat energy utilization rate is improved, the production cost is reduced, the process condensate is recycled, and the cost of water resources is saved.
example two
As shown in fig. 2, in this embodiment, which is a further limitation of the first embodiment, the stripping device 1, the first heat recovery device 2, the second heat recovery device 3, and the condensate recovery device 4 of the styrene process condensate in this embodiment are sequentially connected, the process condensate sequentially passes through the first heat recovery device 2 and the second heat recovery device 3 for heat recovery, and the process condensate passes through the condensate recovery device 4 for condensate recovery.
The technology lime set of this embodiment carries out heat recovery through first heat reclamation device 2, second heat reclamation device 3, also is exactly through twice heat recovery, can increase the recycle ratio of heat energy, further reduces the waste of heat energy, has improved the utilization ratio of technology lime set heat energy. Meanwhile, the process condensate is subjected to condensate recovery through the condensate recovery device 4, and water resources of the process condensate can be simultaneously recycled, so that the cost is further saved.
In a further scheme, the first heat recovery device 2 comprises a benzene storage device 21 and a circulating water station 5 for heating the benzene storage device 21, process condensate discharged from the styrene process condensate stripping device 1 enters the circulating water station 5, and at least part of heat energy of the process condensate is transferred to a medium in the benzene storage device 21.
The benzene storage unit 21 is used for storing the raw material benzene, and the crystallization point of the benzene is high and is 5.5 ℃. In order to prevent benzene from crystallizing and ensure normal reaction, heat tracing is required to be carried out on the benzene storage device 21 to ensure that benzene is in a dissolved liquid state. The benzene storage unit 21 may be a benzene storage tank.
in the scheme, the benzene storage device 21 is not heated independently, but the heat energy of the process condensate discharged by the styrene process condensate stripping device 1 is fully utilized for heat tracing. After the process condensate is discharged by the styrene process condensate stripping device 1, the temperature is higher, generally above 90 ℃, a proper amount of heat energy of the styrene process condensate can be transferred to benzene in the benzene storage device 21 according to the amount required by the benzene storage device 21, after the styrene process condensate passes through the benzene storage device 21, the temperature of the styrene process condensate is reduced to 80 ℃, the heat energy can be recycled, and the need of additionally carrying heat to the benzene storage device 21 is avoided.
in a further aspect, the second heat recovery device 3 includes a heat exchange device 31, the heat exchange device 31 includes a desalted water pipeline 6 for circulating desalted water and a heat exchange medium pipeline 7 for circulating a heat exchange medium, and when the process condensate flows through the heat exchange medium pipeline 7, at least part of heat energy of the process condensate is transferred to the desalted water.
Desalted water is water that has had the strong electrolyte removed or reduced to some extent, which is easily removed. The desalinated water needs to be heated with steam in a deaerator to remove dissolved oxygen before entering the boiler. The temperature through the technology lime set behind first heat recovery unit 2 is still higher in this scheme, utilizes this high temperature technology lime set to preheat the desalinized water to the temperature when improving the entering deaerator. Thus, the temperature of the process condensate after passing through the benzene storage device 21 and the heat exchange device 31 is greatly reduced to 45 ℃, and the desalted water is heated to 41 ℃ from 25 ℃. Therefore, the heat energy of the process condensate can be recycled, the environmental heat energy pollution is avoided, and a large amount of steam for heating desalted water can be saved, so that the cost is greatly reduced, and the production benefit is improved.
In a further scheme, a water inlet of the heat exchange medium pipeline 7 is connected with a water outlet of the circulating water station 5, and a water outlet of the heat exchange medium pipeline 7 is connected with circulating water through a pipeline;
Preferably, the system further comprises a desalted water storage device of the thermal power plant, and the water outlet of the desalted water pipeline 6 is connected with the desalted water storage device.
In a further scheme, a filtering device 8 is arranged between the styrene process condensate stripping device 1 and the first heat recovery device 2, and at least one part of process condensate discharged from the styrene process condensate stripping device 1 enters the benzene storage device 21 after passing through the filtering device 8.
The filtering device 8 arranged between the styrene process condensate stripping device 1 and the first heat recovery device 2 is used for filtering impurities, and a part of the filtered process condensate enters the benzene storage device 21 to preheat benzene therein, so that the condensate resource of the process condensate is recovered after the heat energy of the process condensate is used.
Preferably, the system also comprises a boiler water deoxygenation device 9 connected with the filtering device 8, wherein after the process condensate discharged by the styrene process condensate stripping device 1 passes through the filtering device 8, one part of the process condensate enters the benzene storage device 21, and the other part of the process condensate enters the boiler water deoxygenation device 9.
In a further scheme, the condensate recovery device 4 comprises a circulating water station 41, the first heat recovery device 2 and/or the second heat recovery device 3 are/is connected to a water path of the circulating water station 41 through a pipeline, and recovered process condensate is used for supplementing water to circulating water.
The circulating water station 41 is used for providing circulating water for all places as required, and the condensate recovery device 4 in the scheme is the circulating water station 41. The temperature of the process condensate after passing through the first heat recovery device 2 and the second heat recovery device 3 is greatly reduced, and the heat energy of the process condensate is fully recycled. The temperature of the process condensate after the two heat recoveries is reduced to about 45 ℃, and the process condensate can be directly used as circulating water after entering a circulating water station 41. Due to the low temperature, the evaporation amount of the process condensate in the process of conveying the process condensate to the circulating water station 41 is small, and water resources are further saved.
in a further scheme, the first heat recovery device 2 and the second heat recovery device 3 are further provided with accident pools, and the accident pools are respectively communicated with the first heat recovery device 2 and the second heat recovery device 3. And under special conditions, discharging the process condensate to an accident water tank for improving the production safety.
In addition, the embodiment also provides a control method of the styrene process condensate and heat energy recovery system.
The method comprises the following steps: the heat energy of the process condensate discharged from the styrene process condensate stripping device 1 is subjected to twice heat recovery through the first heat recovery device 2 and the second heat recovery device 3 in sequence, and the process condensate is recovered through the condensate recovery device 4.
In a further scheme, the process condensate is subjected to heat exchange with a medium in a benzene storage device 21 through a first heat recovery device 2, the temperature is reduced to 80 ℃, and then the process condensate enters a second heat recovery device 3 to be subjected to heat exchange with desalted water, and the desalted water is heated to 41 ℃ from 25 ℃. And cooling the process condensate passing through the second recovery device to 45 ℃, and then feeding the process condensate into a circulating water station 41 for supplementing water by circulating water and recovering the process condensate.
More specifically, the process condensate generated in the styrene process condensate stripping tower is conveyed to the filtering device 8 by the stripping tower liquid pump 10 for filtering. And (3) conveying a part of the filtered and impurity-removed process condensate to a boiler water deoxygenation device 9, and conveying a part of the filtered and impurity-removed process condensate to a first heat recovery device 2, namely carrying out heat tracing on a benzene storage tank. The temperature of the process condensate after heat exchange of the benzene storage tank is reduced to 80 ℃, and then the process condensate enters the second heat recovery device 3, namely the heat exchange medium pipeline 7 of the heat exchange device 31 to exchange heat with desalted water in the desalted water pipeline 6, and the desalted water is heated to 41 ℃ from 25 ℃. The temperature of the process condensate flowing out of the heat exchange device 31 is reduced to 45 ℃, and then the process condensate enters the circulating water station 41 to be used for supplementing circulating water.
Therefore, the control method of the embodiment not only recycles the heat energy of the styrene process condensate, improves the heat energy utilization rate, but also reduces the steam quantity required by the benzene storage device 21 and the heating desalted water, reduces the production cost, and recycles the process condensate to be used as circulating water for supplementing water, thereby saving the circulating water supplementing cost and improving the production benefit.
Test example 1
The experimental example calculates the investment cost for scheme reconstruction and the cost saved after reconstruction, and the cost is greatly saved in the reconstructed scheme. The specific calculation process is as follows:
1. Investment cost:
(1) Material cost: pipeline: DN200SCH40 price: 19.5 ten thousand yuan; rock wool: 10 ten thousand yuan; 27 ten thousand yuan of waterproof polyurethane coiled materials; 0.3mm stainless steel plate: 15.5 ten thousand yuan; the cost of pipeline installation: 4.7 ten thousand yuan; and (3) pressure test: 1.2 ten thousand yuan; washing: 5 thousand yuan; supporting: 2 ten thousand yuan; and (3) corrosion prevention: 3.5 ten thousand yuan; derusting: 4 ten thousand yuan)
(2) Plate heat exchanger: 3 thousands (Heat exchange area 36m2)
(3) A valve: 5.5 ten thousand (DN200 stainless steel ball valves 2, DN200 carbon steel ball valves 5)
totaling: the reconstruction cost is about: 96.4 ten thousand
2. the cost is saved:
(1) the benzene storage device saves the cost by heat tracing:
the original design is that the temperature of the benzene tank is maintained at 40 ℃ by using steam (143 ℃) and heat tracing, and the temperature of the benzene tank is maintained at 40 ℃ by using condensate liquid heat tracing in the prior art. (specific enthalpy of steam at 143 ℃ 653.9 kcal/kg; specific enthalpy of water at 80 ℃ 80.1 kcal/kg; specific enthalpy of water at 82 ℃ 82.1 kcal/kg; specific enthalpy of water at 143 ℃ 143.8kcal/kg)
The heat energy that can be recovered is therefore:
(82.1-80.1)kcal/kg×100000kg/h＝200000kcal
The amount of steam consumed is therefore reduced:
200000kcal/h÷(653.9kcal/kg-143.8kcal/kg)＝392kg/h
savings can be calculated in terms of 130 dollars per ton of steam:
0.392X 130X 8000 ═ 40.7 ten thousand yuan/year
(2) The desalted water preheating saves the cost:
The original design was to heat the desalinated water from 25 ℃ to 120 ℃ using steam (200 ℃), and the desalinated water can now be preheated to 41 ℃ via condensate preheating. (specific enthalpy of steam at 200 ℃ 667.1 kcal/kg; specific enthalpy of water at 120 ℃ 120.3 kcal/kg; specific enthalpy of water at 25 ℃ 25.03 kcal/kg; specific enthalpy of water at 41 ℃ 41.00kcal/kg)
the heat energy that can be recovered is therefore:
(41-25.03)kcal/kg×220000kg/h＝3513400kcal/h
The amount of steam consumed is therefore reduced:
3513400kcal/h÷(667.1kcal/kg-120.3kcal/kg)＝6425kg/h
therefore, the steam consumption can be reduced by 6.4t/h if the preheating is carried out to 41 ℃. Savings can be calculated in terms of 130 dollars per ton of steam:
6.4X 130X 8000 (665.6 ten thousand yuan/year)
(3) The water replenishing cost for saving the circulating water is as follows:
the original design is to supplement water to the circulating water station through tap water, and now part of water supplement can be performed through recycling condensate.
The condensate amount which can be recovered every year is as follows:
100X 8000 ═ 800000 t/year
The savings can be calculated according to a price of 5 yuan per ton of tap water:
800000 × 5 ═ 400 ten thousand yuan/year
In conclusion, the cost saved by heat tracing of the benzene storage device, the cost saved by preheating desalted water and the water replenishing cost saved by circulating water can reach 1106.3 ten thousand yuan per year in total, the modification cost is removed by 96.4 ten thousand, and the cost saved per year is also ten million, so the cost is greatly saved, and the benefit is improved.
Although the present invention has been described with reference to a preferred embodiment, it should be understood that various changes, substitutions and alterations can be made herein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (10)
1. The utility model provides a styrene technology lime set and heat recovery system, its characterized in that, heat recovery system includes styrene technology lime set steam stripping device, first heat recovery unit, second heat recovery unit and lime set recovery unit, styrene technology lime set steam stripping device be connected with first heat recovery unit and/or second heat recovery unit and/or lime set recovery unit, the technology lime set carries out heat recovery through first heat recovery unit and/or second heat recovery unit, the technology lime set carries out lime set through lime set recovery unit and retrieves.
2. The styrene process condensate and heat energy recovery system according to claim 1, wherein the styrene process condensate stripping device is respectively connected with the first heat recovery device and the second heat recovery device, the first heat recovery device and the second heat recovery device are connected through pipelines, the first heat recovery device and the second heat recovery device are respectively connected with the condensate recovery device through pipelines, the process condensate is subjected to heat recovery through the first heat recovery device and/or the second heat recovery device, and the process condensate is subjected to condensate recovery through the condensate recovery device.
3. The styrene process condensate and heat energy recovery system according to claim 1 or 2, wherein the styrene process condensate stripping device, the first heat recovery device, the second heat recovery device and the condensate recovery device are sequentially connected, the process condensate sequentially passes through the first heat recovery device and the second heat recovery device for heat recovery, and the process condensate passes through the condensate recovery device for condensate recovery.
4. a styrene process condensate and heat energy recovery system according to any one of claims 1 to 3, wherein the first heat recovery unit comprises a benzene storage unit and a first heating line for heating the benzene storage unit, wherein the process condensate discharged from the styrene process condensate stripping unit enters the first heating line, and at least part of heat energy of the process condensate is transferred to the medium in the benzene storage unit.
5. The styrene process condensate and heat energy recovery system of any one of claims 1 to 4, wherein the second heat recovery unit comprises a heat exchange unit including a desalted water line for circulating desalted water and a heat exchange medium line for circulating a heat exchange medium, wherein at least a portion of the heat energy of the process condensate is transferred to the desalted water as the process condensate flows through the heat exchange medium line.
6. The styrene process condensate and heat energy recovery system of claim 5, wherein a water inlet of the heat exchange medium pipeline is connected with a water outlet of the first heating pipeline, and a water outlet of the heat exchange medium pipeline is connected with circulating water through a pipeline;
Preferably, the system further comprises a desalted water storage device of the thermal power plant, and the water outlet of the desalted water pipeline is connected with the desalted water storage device.
7. The system for recycling the technical condensate and heat energy of the styrene according to any one of claims 1 to 6, wherein a filtering device is arranged between the stripping device of the technical condensate of the styrene and the first heat recovery device, and at least one part of the technical condensate discharged by the stripping device of the technical condensate of the styrene enters the first heat recovery device after passing through the filtering device;
Preferably, the system also comprises a boiler water deoxygenation device connected with the filtering device, wherein after the process condensate discharged by the styrene process condensate stripping device passes through the filtering device, one part of the process condensate enters the first heat recovery device, and the other part of the process condensate enters the boiler water deoxygenation device.
8. The styrene process condensate and heat energy recovery system according to any one of claims 1 to 7, wherein the condensate recovery device comprises a circulating water station, the first heat recovery device and/or the second heat recovery device are/is connected to a water path of the circulating water station through a pipeline, and the recovered process condensate is used for supplementing circulating water.
9. A method of controlling a styrene process condensate and heat energy recovery system as claimed in any one of claims 1 to 8, the method comprising: the heat energy of the process condensate discharged by the styrene process condensate stripping device is subjected to twice heat recovery by the first heat recovery device and the second heat recovery device in sequence, and the process condensate is recovered by the condensate recovery device.
10. the method of claim 9, wherein the process condensate is heat exchanged with the medium in the benzene storage unit via the first heat recovery unit to reduce the temperature to 80 ℃, and then enters the second heat recovery unit to exchange heat with desalted water to reduce the temperature to 41 ℃, and then enters the circulating water station for replenishing water with circulating water to recover the process condensate.
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| US3527699A (en) * | 1965-08-20 | 1970-09-08 | Badger Co | Condensate recovery system |
| CN103274562A (en) * | 2013-06-24 | 2013-09-04 | 天津大沽化工股份有限公司 | Thermal energy recovery and pure water preparation device for phenethylene process condensate |
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