A device for utilizing heat energy from solvent refining in the production process of synthetic rubber

Abstract

The utility model discloses a device for utilizing heat energy of solvent refining in the production process of synthetic rubber, which mainly comprises a distillation tower, a reboiler, an absorption heat pump, a condenser, a reflux tank and a reflux pump. The device recovers the heat energy of oil and gas in the upper part of the distillation tower through the absorption heat pump technology to produce steam or hot water, and uses it as a partial heat source required for distillation, thereby reducing the consumption of solvent refining steam and circulating cooling water, achieving the purpose of energy saving and emission reduction, and having good economic and environmental benefits.

Description

Technical Field

[0001] The utility model belongs to the technical field of synthetic rubber production, and relates to a device for utilizing heat energy of solvent refining in the synthetic rubber production process, and specifically relates to an absorption heat pump device for recovering oil and gas heat energy in the synthetic rubber solvent refining production process. Background Art

[0002] In the production process of synthetic rubber by solution polymerization, such as solution styrene butadiene rubber (SSBR), production units of ethylene propylene rubber, butadiene rubber, isoprene rubber and styrene block copolymer SBC (SBS, SIS, SEBS) by solution polymerization, a large amount of solvent is used in the polymerization or condensation stage. A large amount of solvent is circulated in the unit. The unit is equipped with solvent recovery and refining units and related equipment. The main task of solvent refining is to remove water, light components and heavy components from the solvent using one or more distillation towers.

[0003] Chinese patent CN100453587C "Method for recycling solvents and unreacted monomers in the process of producing polymers by solution polymerization"; Chinese patent CN102504066A "Method for refining solvents in the production of isoprene rubber"; both patents use "one-tower solvent refining process" to remove water, light components and heavy components, saving steam and production costs.

[0004] Chinese patent CN100363409C "A solvent refining process for synthetic rubber production" proposes a solvent refining process with multi-effect distillation after a dehydration tower (referred to as "multi-effect solvent refining process" in this patent), which greatly reduces energy consumption.

[0005] Currently in the synthetic rubber industry, only a small portion of the low-grade oil and gas produced from the top or side lines of the solvent refining distillation tower is used for heat exchange with the feed, and most of it is directly cooled with cooling water and not effectively utilized; including the above-mentioned existing "one-tower solvent refining process" and "multi-effect solvent refining process" technologies, although they greatly reduce the energy consumption of the solvent refining process, the above-mentioned technical measures have not proposed measures to recycle the low-grade oil and gas produced from the top or side lines of the tower, so that the energy consumption of solvent refining is still relatively high. Summary of the invention

[0006] The purpose of the present invention is to recover the heat contained in the oil and gas produced from the top or side line of the solvent refining tower, and to provide an energy-saving and water-saving process. The use of this process can significantly reduce the steam consumption of the solvent refining unit and the use of circulating water, and has good economic and environmental benefits.

[0007] The present invention is realized by the following technical scheme, which is mainly composed of an absorption heat pump, a solvent refining system, etc.

[0008] Technical solution of the present invention

[0009] The technical solution of the present invention is:

[0010] The device for utilizing heat energy of solvent refining in the production process of synthetic rubber mainly consists of a temperature-raising absorption heat pump, a solvent dehydration distillation tower (or a solvent deheavy distillation tower, a solvent delight distillation tower), a tower top condenser, a tower bottom reboiler, a tower top reflux tank, and a reflux pump. The gas phase pipeline produced from the top or side line of the solvent dehydration distillation tower (or a solvent deheavy distillation tower, a solvent delight distillation tower) passes through the evaporator of the absorption heat pump unit, and then passes through the generator of the absorption heat pump, and is connected to the inlet of the condenser, and the outlet of the condenser is connected to the inlet of the reflux tank; the steam condensed water (or soft water) passes through the steam-water separator (or absorber) of the absorption heat pump to recover heat energy and generate secondary steam (or hot water).

[0011] There are three main specific solutions:

[0012] The first is a device for utilizing heat energy from solvent refining in the production process of synthetic rubber, comprising a rectification tower, a reboiler, a steam absorption heat pump, a condenser, a reflux tank, and a reflux pump; the device is characterized in that:

[0013] The gas phase pipeline at the top of the distillation tower is first connected to the evaporator of the absorption heat pump unit, then to the generator of the heat pump unit, and then connected to the external condenser inlet, and the condenser outlet is connected to the reflux tank inlet; the reflux tank liquid phase outlet is connected to the reflux pump, and the reflux pump outlet is respectively connected to the upper part of the distillation tower and the solvent extraction pipeline, and the distillation tower reboiler is arranged at the lower part of the distillation tower; the steam condensate or other soft water pipeline is fed into the steam-type absorption heat pump steam-water separator, the steam outlet of the steam-water separator is connected to the ejector, and the ejector outlet is connected to the reboiler or other steam-using equipment.

[0014] The second is a device for utilizing heat energy from solvent refining in the production process of synthetic rubber, comprising a rectification tower, a reboiler, a hot water absorption heat pump, a condenser, a reflux tank, and a reflux pump; the device is characterized in that:

[0015] The gas phase pipeline at the top of the distillation tower is first connected to the evaporator of the absorption heat pump unit, then to the generator of the heat pump unit, and then connected to the external condenser inlet, and the condenser outlet is connected to the reflux tank inlet; the reflux tank liquid phase outlet is connected to the reflux pump, and the reflux pump outlet is respectively connected to the upper part of the distillation tower and the solvent extraction pipeline, and the distillation tower reboiler is arranged at the lower part of the distillation tower; the low-grade medium pipeline passes through the hot water absorption heat pump absorber, and is heated to become a high-grade medium before being led out to the use equipment.

[0016] The low-grade medium for heating is hot water, soft water, steam condensate, or other heat media for directly or indirectly transferring heat.

[0017] The third is a device for utilizing heat energy from solvent refining in the production process of synthetic rubber, comprising a distillation tower, a reboiler, a steam absorption heat pump, a condenser, a reflux tank, a reflux pump, a side condenser, a buffer tank, and a discharge pump; the device is characterized in that:

[0018] The side-line gas phase pipeline of the distillation tower is first connected to the evaporator of the absorption heat pump unit, and then to the generator of the heat pump unit, and then connected to the inlet of the external side-line condenser, and the condenser outlet is connected to the inlet of the buffer tank; the liquid phase outlet of the buffer tank is connected to the discharge pump; the gas phase pipeline at the top of the distillation tower is connected to the external condenser inlet, and the condenser outlet is connected to the inlet of the reflux tank; the reflux pump outlet is respectively connected to the upper part of the distillation tower and the solvent extraction pipeline, and the distillation tower reboiler is arranged at the lower part of the distillation tower; the steam condensate or other soft water pipeline is connected to the steam-type absorption heat pump steam-water separator, the steam outlet of the steam-water separator is connected to the ejector, and the ejector outlet is connected to the reboiler or other steam-using equipment.

[0019] The steam absorption heat pump is mainly composed of an evaporator, a generator, an absorber, a cooler, a steam-water separator and a pump.

[0020] The hot water absorption heat pump is mainly composed of an evaporator, a generator, an absorber, a cooler and a pump.

[0021] When the solvent recovery tower system adopts the two-tower solvent refining process technology (consisting of a dehydration tower and a deweighting tower), the top gas phase of the distillation tower is separately connected to a temperature-raising absorption heat pump to recover most of the heat energy of the oil and gas produced from the top gas phase of the distillation tower.

[0022] When the solvent recovery tower adopts a one-tower solvent refining process technology (a distillation tower realizes the dehydration and deweighting functions), the gas phase produced from the top or side of the tower is separately connected to a temperature-raising absorption heat pump to recover most of the heat energy of the gas-phase produced oil and gas.

[0023] When the solvent recovery tower adopts the dehydration distillation tower + double-effect de-heavy distillation tower process, the dehydration distillation tower and the top gas phase of the last de-heavy distillation tower are separately connected to a temperature-raising absorption heat pump to recover most of the heat energy in the oil and gas produced by the dehydration distillation tower and the top gas phase of the last de-heavy distillation tower.

[0024] Application of solvent refining heat energy utilization device in synthetic rubber production process:

[0025] This solution is a continuous production process. The 80-100℃ oil gas evaporated from the distillation tower is condensed in the evaporative absorption heat pump evaporator, and then continues to pass through the absorption heat pump generator for heat exchange cooling, and then enters the condenser for condensation, and then enters the reflux tank for oil-water separation (when it contains water), discharges water, and the oil phase refluxes to the top of the tower;

[0026] a. The steam condensate from outside the boundary, or the steam condensate condensed in the reboiler of this unit is pressurized by a pump and enters the absorption heat pump steam-water separator for heating to produce 100-130℃ secondary steam; the produced 100-130℃ steam can be sent out of the boundary area for use in other equipment; the produced 100-130℃ steam can also (or be pressurized by steam injection) enter the bottom reboiler of the tower and be directly used as the heat source of the tower kettle.

[0027] b. Steam condensate (or soft water) from outside the boundary enters the absorption heat pump absorber for heating, and produces 100-130℃ superheated hot water which can be sent out of the boundary area for use in other equipment.

[0028] c. The post-processed hot water from outside the boundary enters the absorption heat pump absorber for heating, produces 100-130℃ superheated hot water, and then returns to the condensation unit for use.

[0029] The heating type absorption heat pump is mainly composed of an evaporator, a generator, an absorber, a cooler, a steam-water separator (steam type absorption heat pump), a pump, etc.

[0030] The oil gas is condensed into oil phase in the absorption heat pump evaporator and generator, cooled in the condenser and enters the reflux tank at the top of the tower.

[0031] The solvent refining tower system can be a three-tower system in series (one dehydration and weight removal tower, and two weight removal towers), a two-tower system in series (dehydration and weight removal towers), or a single-tower system (dehydration and weight removal).

[0032] Beneficial effects of the utility model:

[0033] 1) Using absorption heat pump technology, the heat in the low-grade oil and gas of the synthetic rubber refining system is recovered and used to heat steam condensate or other soft water to generate secondary steam for use in the tower kettle reboiler, thereby reducing the steam consumption of the refining system;

[0034] 2) By recovering part of the latent heat in the oil and gas, the cooling water consumption of the solvent refining unit can be reduced.

[0035] 3) The economic benefits are obvious. BRIEF DESCRIPTION OF THE DRAWINGS

[0036] Figure 1 Comparative Example 1 Schematic diagram of solvent refining system

[0037] Figure 2 Flow chart of a solvent refining heat energy utilization device in a synthetic rubber production process of the present invention

[0038] Figure 3 One-tower solvent refining process

[0039] Figure 4 One-tower solvent refining + thermal energy utilization process

[0040] Figure 5 Multi-effect solvent refining process

[0041] Figure 6 Multi-effect solvent refining process + thermal energy utilization process

[0042] In the figure: 1-distillation tower, 2-reboiler, 3-condenser, 4-reflux tank, 5-reflux pump, 6-bottom pump, 7-first side line product condenser, 8-second side line product condenser, 9-discharge pump, 10-absorption heat pump, 11-steam-water separator, 12-ejector.

[0043] LS-steam, SC-steam condensate (or other soft water), CW-circulating cooling supply water, CWR-circulating cooling return water. DETAILED DESCRIPTION

[0044] The present invention is further described below in conjunction with the accompanying drawings, but does not constitute a limitation of the present invention. The "rectifier" in this specification refers to a rectifying tower used in the rectification process of the general industrial field, and the rectifying tower can be equipped with each or all of a condenser and / or a heat exchanger (or a reboiler). According to the needs of the rectifying tower, the condenser and / or the heat exchanger (or the reboiler) can be optionally configured or not configured.

[0045] The "distillation tower system" or "distillation system" in this specification refers to a system consisting of one or more distillation towers and the related facilities they need to be equipped with, such as reboilers, condensers, reflux tanks, pumps and pipelines, all or part of these facilities, or one or more of a certain facility, which can complete the specified separation function. In addition, unless otherwise specified, condensers, heat exchangers, pumps and pipes may be omitted facilities or components even if they are shown in the drawings.

[0046] In this specification, the "reboiler" mentioned above refers to a heating device that is provided in conjunction with a distillation tower and is used to reheat and evaporate the liquid flow in the bottom of the tower.

[0047] The "condenser" in this specification refers to a cooling device that is provided in conjunction with a distillation tower and is used to condense and cool the gas phase flow distilled from the top of the distillation tower by indirect contact with the introduced refrigerant (such as circulating cooling water).

[0048] In the present specification, the "upper part of the distillation tower" refers to the relatively higher part of the distillation tower cylinder; the "lower part of the distillation tower" refers to the relatively lower part of the distillation tower cylinder; the "top part of the distillation tower" may refer to the highest part of the distillation tower and may be located at the above-mentioned upper part of the distillation tower; the "bottom part of the distillation tower" may refer to the lowest part of the distillation tower and may be located at the above-mentioned lower part of the distillation tower.

[0049] Comparative Example 1:

[0050] The solvent cyclohexane of the SBS unit is distilled and the solvent processing capacity is 50t / h. The existing process is dehydration first and multi-effect solvent refining process. The dehydration tower process is as follows Figure 1 As shown;

[0051] The crude solvent from the crude solvent tank enters the distillation tower 1 (dehydration tower); the reboiler 2 uses steam as the heating medium; the gas phase solvent heated by the reboiler 2 transfers heat and mass with the top feed and reflux liquid of the distillation tower 1 in the tower; the vapor phase at the top of the dehydration tower 1 is condensed by the top condenser 3 and flows into the reflux tank 4, and is allowed to stand for stratification, and the oil phase returns to the dehydration tower 1 for feeding; the discharge from the bottom of the dehydration tower 1 is sent to the deweight removal tower through the tower kettle pump 6.

[0052] The operating pressure of the dehydration tower is atmospheric pressure, the top temperature is about 80°C, and the bottom temperature is about 90°C.

[0053] Embodiment 1:

[0054] The solvent cyclohexane of the SBS device is distilled and treated, and the solvent treatment capacity is 50 t / h, which is the same as that of Comparative Example 1; the separation requirements, treatment capacity and operating parameters of the distillation tower 1 are the same as those of Comparative Example 1.

[0055] Based on the process of comparative example 1, an absorption heat pump 10, a steam-water separator 11, and an ejector 12 are added to recover the gas phase heat energy at the top of the distillation tower 1. The process is as follows Figure 2 As shown:

[0056] By adopting the technology of the present invention, an absorption heat pump system is newly added, with an investment of 1.5 million yuan; the tower top gas phase heat energy recovery rate is considered to be 50%, and about 1050kg / h of steam can be recovered, the steam consumption of the distillation system is reduced by 1050kg / h, and the consumption of circulating cooling water of the distillation system is reduced by 60t / h.

[0057] Table 1 Comparison of main economic indicators between Example 1 and Comparative Example 1

[0058]

[0059] Among them, the steam price is 160 yuan / t, the cooling water price is 0.22 yuan / t, the electricity price is 0.60 yuan / kw.h, and the investment cost is depreciated over 15 years, saving 1.332 million yuan per year.

[0060] Comparative Example 2:

[0061] The solvent cyclohexane of the SSBR unit is distilled and treated. The solvent treatment capacity is 32t / h. The existing one-tower solvent refining process technology (one distillation tower realizes dehydration and deweighting functions) is adopted. The process is as follows Figure 3 As shown;

[0062] The wet solvent containing impurities from the upstream and the refined solvent produced from the side line are heat exchanged through the first side line product condenser 7, and then enter the top of the distillation tower 1 (corresponding to its dehydration and deheaving distillation tower); the reboiler 2 uses steam as the heating medium; the gaseous solvent heated by the reboiler 2 transfers heat and mass with the feed and reflux liquid at the top of the distillation tower 1 in the tower; the refined and qualified solvent is produced from the side line of the stripping section of the distillation tower 1 in the form of gas phase, and the gaseous solvent product produced from the side line is condensed by the first side line product condenser 7 and the second side line product condenser 8 in turn, and then sent out of the distillation system through the solvent pump 9; the crude solvent is distilled out of the top of the distillation tower 1, and the oil and gas flows into the condenser 3, is condensed by the circulating cooling water, and the condensate is discharged into the reflux tank 4; a small amount of non-condensable gas that has not been condensed by the condenser 3 in the reflux tank 4 is discharged to the tail gas treatment system. The condensate is separated into oil and water in the reflux tank 4. The lower layer is the water layer and is discharged from the distillation system. The upper layer is the oil phase solvent, which is pressurized by the reflux pump 5 as the reflux liquid and sent to the top of the distillation tower 1 after heat exchange in the first side product condenser 7. The heavy component impurities in the crude solvent are enriched in the kettle liquid at the bottom of the distillation tower 1, and are pressurized by the kettle liquid pump 6 and sent out of the distillation tower system or to other facilities for further treatment.

[0063] The operating pressure of the distillation tower 1 is atmospheric pressure, the tower top temperature is about 81°C, and the tower bottom temperature is about 102°C.

[0064] Embodiment 2:

[0065] The solvent cyclohexane of the SSBR unit is distilled and treated, and the solvent treatment capacity is 32 t / h. The separation requirements, treatment capacity and operating parameters of the distillation tower 1 are the same as those of Comparative Example 2.

[0066] Based on the process of comparative example 2, an absorption heat pump 10, a steam-water separator 11, and an ejector 12 are added to recover the gas phase heat energy extracted from the side line of the distillation tower 1. The process is as follows Figure 4 As shown:

[0067] The gas phase extracted from the side line of the distillation tower 1 passes through the absorption heat pump 10 to recover heat, and heats the steam condensate or soft water in the steam-water separator 11 to generate secondary steam. The secondary steam is pressurized by the ejector 12 and sent to the steam heating side of the reboiler of the distillation tower for heating the reboiler.

[0068] The operating conditions of the distillation tower 1 are the same as those of the comparative example 2.

[0069] By adopting the technology of the present invention, an absorption heat pump system is newly added with an investment of 3 million yuan; considering the gas phase heat energy recovery rate at the top of the tower as 50%, about 2700kg / h of steam can be recovered, the steam consumption of the distillation system is reduced by 2700kg / h, and the consumption of circulating cooling water of the distillation system is reduced by 160t / h.

[0070] Table 3 Comparison of main economic indicators of Example 2 and Comparative Example 2

[0071]

[0072] Among them, the steam price is 160 yuan / t, the cooling water price is 0.22 yuan / t, the electricity price is 0.60 yuan / kw.h, and the investment cost is depreciated over 15 years, saving 3.495 million yuan per year.

[0073] Comparative Example 3:

[0074] The solvent cyclohexane of the SBS unit is distilled and treated with a solvent treatment capacity of 50t / h. The existing dehydration and multi-effect solvent refining process (two-effect co-current deweighting process) is adopted. The process is as follows Figure 5 As shown;

[0075] The solvent that meets the quality requirements is in the form of gas phase from the top of the first effect distillation tower to the shell side of the reboiler 2 of the distillation tower 1 (corresponding to the second effect distillation tower in the second effect distillation), and is used as the heating medium of the reboiler 2. Most of it is condensed and flows to the reflux tank 4 by gravity. The solvent containing heavy components is pressed into the distillation tower 1 from the bottom of the first effect distillation tower by the pressure difference between the first and second effect towers (or the first effect tower bottom pump 6), and is refined in the distillation tower 1. The refined qualified solvent enters the condenser 3 from the top of the tower in the form of gas phase, and is cooled to below about 50°C by the circulating cooling water. The gas phase solvent is almost completely condensed and enters the reflux tank 4, and the remaining non-condensable gas is discharged to the tail gas treatment system. The reflux tank 4 contains the refined qualified solvent, which is sent to the top of the first effect distillation tower and the top of the distillation tower 1 respectively by the reflux pump 5 in a certain proportion, and a part of it is sent as reflux liquid to the top of the first effect distillation tower and the top of the distillation tower 1, and the rest is sent out of the distillation tower system as a product. The bottom liquid is the heavy component enriched with solvent and is sent out of the distillation tower system or other facilities for treatment via the distillation tower bottom liquid pump 6.

[0076] The operating pressure of the first effect distillation tower is 0.25 MPa (gauge), the tower top temperature is 121°C, and the tower bottom temperature is about 128°C. The operating pressure of distillation tower 1 is atmospheric pressure, the tower top temperature is about 81°C, and the large tower bottom temperature is about 102°C.

[0077] Embodiment 3:

[0078] The solvent cyclohexane of the SBS device is distilled and treated, and the solvent treatment capacity is 50 t / h. The separation requirements, treatment capacity and operating parameters of the distillation tower 1 are the same as those of Comparative Example 3.

[0079] Based on the process of comparative example 3, an absorption heat pump 10 is added to the top of the second-effect distillation tower in the corresponding second-effect distillation to recover the gas phase heat energy at the top of the distillation tower 1. The process is as follows Figure 6 As shown:

[0080] The gas phase at the top of the distillation tower 1 passes through the absorption heat pump 10 to recover heat and heat the circulating hot water returned from the post-processing unit to the condensation unit.

[0081] The operating conditions of the distillation tower 1 are the same as those of Comparative Example 3.

[0082] Adopting the technology of the present invention, an absorption heat pump system is newly added, with an investment of RMB 2.8 million. Considering the gas phase heat energy recovery rate at the top of the tower as 50%, about 1480KW of heat can be recovered per hour, which is converted into about 2300kg / h of steam, and the 100m3 of the post-processing unit can be returned to the condensation unit. 3 / h circulating hot water, heated from 95℃ to 108℃, the condensing steam consumption can be reduced by 2300kg / h, and the circulating cooling water consumption of the distillation system is reduced by 140t / h.

[0083] Table 3 Comparison of main economic indicators of Example 3 and Comparative Example 3

[0084]

[0085] Among them, the recovered heat is converted into the amount of saved condensing steam, the steam price is 160 yuan / t, the cooling water price is 0.22 yuan / t, the electricity price is 0.60 yuan / kw.h, and the investment cost is depreciated for 15 years, saving 2.967 million yuan per year.

[0086] Embodiment 4:

[0087] The solvent cyclohexane of the SBS device is distilled and treated, and the solvent treatment capacity is 50 t / h, which is the same as that of Comparative Example 1; the separation requirements, treatment capacity and operating parameters of the distillation tower 1 are the same as those of Comparative Example 1.

[0088] Based on the process of comparative example 1, an absorption heat pump 10 and a steam-water separator 11 are added to recover the gas phase heat energy at the top of the distillation tower 1. The steam generated by the steam-water separator 11 is directly used in the tower reboiler. The process is roughly as follows: Figure 2 (The difference is that there is no ejector) as shown:

[0089] By adopting the technology of the present invention, an absorption heat pump system is newly added, with an investment of 1.45 million yuan; the tower top gas phase heat energy recovery rate is considered to be 50%, and about 1050kg / h of steam can be recovered, the steam consumption of the distillation system is reduced by 1050kg / h, and the consumption of circulating cooling water of the distillation system is reduced by 60t / h.

[0090] Table 1 Comparison of main economic indicators of Example 4 and Comparative Example 1

[0091]

[0092] Among them, the steam price is 160 yuan / t, the cooling water price is 0.22 yuan / t, the electricity price is 0.60 yuan / kw.h, and the investment cost is depreciated over 15 years, saving 1.335 million yuan per year.

[0093] The above is only a preferred implementation of the technology of the present invention. It should be pointed out that for ordinary technicians in this technical field, several improvements and substitutions can be made without departing from the technical principles of the present invention. These improvements and substitutions should also be regarded as the scope of protection of the present invention.

Claims

1. A device for utilizing heat energy from solvent refining in the production process of synthetic rubber, comprising a distillation tower, a reboiler, a steam absorption heat pump, a condenser, a reflux tank, and a reflux pump; characterized in that: The gas phase pipeline at the top of the distillation tower is first connected to the evaporator of the absorption heat pump unit, then to the generator of the heat pump unit, and then connected to the external condenser inlet, and the condenser outlet is connected to the reflux tank inlet; the reflux tank liquid phase outlet is connected to the reflux pump, and the reflux pump outlet is respectively connected to the upper part of the distillation tower and the solvent extraction pipeline, and the distillation tower reboiler is arranged at the lower part of the distillation tower; the steam condensate or other soft water pipeline is connected to the steam-type absorption heat pump steam-water separator, the steam outlet of the steam-water separator is connected to the ejector, and the ejector outlet is connected to the reboiler or other steam-using equipment.

2. The device for utilizing heat energy from solvent refining in the production process of synthetic rubber according to claim 1, characterized in that The steam absorption heat pump is mainly composed of an evaporator, a generator, an absorber, a cooler, a steam-water separator and a pump.

3. The device for utilizing heat energy from solvent refining in the production process of synthetic rubber according to claim 1, characterized in that The outlet of the steam-water separator is directly connected to the reboiler or other steam-using equipment without being pressurized by an ejector.

4. A device for utilizing heat energy from solvent refining in the production process of synthetic rubber, comprising a distillation tower, a reboiler, a hot water absorption heat pump, a condenser, a reflux tank, and a reflux pump; characterized in that: The gas phase pipeline at the top of the distillation tower is first connected to the evaporator of the absorption heat pump unit, then to the generator of the heat pump unit, and then connected to the external condenser inlet, and the condenser outlet is connected to the reflux tank inlet; the reflux tank liquid phase outlet is connected to the reflux pump, and the reflux pump outlet is respectively connected to the upper part of the distillation tower and the solvent extraction pipeline, and the distillation tower reboiler is arranged at the lower part of the distillation tower; the low-grade medium pipeline passes through the hot water absorption heat pump absorber, and is heated to become a high-grade medium before being led out to the use equipment.

5. The device for utilizing heat energy from solvent refining in the production process of synthetic rubber according to claim 1 or 4, characterized in that The distillation tower refers to a dehydration distillation tower for removing water from the tower top in the existing refining process technology, or a light removal distillation tower after dehydration in the solvent refining process.

6. The device for utilizing heat energy from solvent refining in the production process of synthetic rubber according to claim 1 or 4, characterized in that The distillation tower is a de-heaving distillation tower in a single-effect solvent refining process, or a dehydration and de-heaving distillation tower in a one-tower solvent refining process, or a last-effect de-heaving distillation tower in a multi-effect solvent refining process.

7. The device for utilizing heat energy from solvent refining in the production process of synthetic rubber according to claim 4, characterized in that The hot water absorption heat pump is mainly composed of an evaporator, a generator, an absorber, a cooler and a pump.

8. The device for utilizing heat energy from solvent refining in the production process of synthetic rubber according to claim 4, characterized in that The low-grade medium used for heating is hot water, soft water, steam condensate, or other heat media used to transfer heat directly or indirectly.

9. A device for utilizing heat energy from solvent refining in the production process of synthetic rubber, comprising a distillation tower, a reboiler, a steam absorption heat pump, a condenser, a reflux tank, a reflux pump, a side condenser, a buffer tank, and a discharge pump; characterized in that: The side-line gas phase pipeline of the distillation tower is first connected to the evaporator of the absorption heat pump unit, and then to the generator of the heat pump unit, and then connected to the inlet of the external side-line condenser, and the condenser outlet is connected to the inlet of the buffer tank; the liquid phase outlet of the buffer tank is connected to the discharge pump; the gas phase pipeline at the top of the distillation tower is connected to the external condenser inlet, and the condenser outlet is connected to the inlet of the reflux tank; the reflux pump outlet is respectively connected to the upper part of the distillation tower and the solvent extraction pipeline, and the distillation tower reboiler is arranged at the lower part of the distillation tower; the steam condensate or other soft water pipeline is connected to the steam-type absorption heat pump steam-water separator, the steam outlet of the steam-water separator is connected to the ejector, and the ejector outlet is connected to the reboiler or other steam-using equipment.

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