CN107983092A - Residual neat recovering system and exhaust heat recovering method - Google Patents
Residual neat recovering system and exhaust heat recovering method Download PDFInfo
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- CN107983092A CN107983092A CN201711408200.0A CN201711408200A CN107983092A CN 107983092 A CN107983092 A CN 107983092A CN 201711408200 A CN201711408200 A CN 201711408200A CN 107983092 A CN107983092 A CN 107983092A
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- lean solution
- heat
- unit
- solvent
- waste heat
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- 238000000034 method Methods 0.000 title claims abstract description 71
- 239000002904 solvent Substances 0.000 claims abstract description 102
- 238000011084 recovery Methods 0.000 claims abstract description 98
- 239000002918 waste heat Substances 0.000 claims abstract description 83
- 239000007789 gas Substances 0.000 claims abstract description 60
- 230000008929 regeneration Effects 0.000 claims abstract description 50
- 238000011069 regeneration method Methods 0.000 claims abstract description 50
- 239000007788 liquid Substances 0.000 claims abstract description 27
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000012530 fluid Substances 0.000 claims abstract description 22
- 238000005516 engineering process Methods 0.000 claims abstract description 12
- 239000011593 sulfur Substances 0.000 claims abstract description 12
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 94
- 229910001868 water Inorganic materials 0.000 claims description 94
- 238000001816 cooling Methods 0.000 claims description 48
- 238000007701 flash-distillation Methods 0.000 claims description 45
- 230000008569 process Effects 0.000 claims description 44
- 238000010521 absorption reaction Methods 0.000 claims description 36
- 230000003020 moisturizing effect Effects 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 6
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Chemical compound [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 claims description 6
- IIPYXGDZVMZOAP-UHFFFAOYSA-N lithium nitrate Chemical compound [Li+].[O-][N+]([O-])=O IIPYXGDZVMZOAP-UHFFFAOYSA-N 0.000 claims description 6
- IPLONMMJNGTUAI-UHFFFAOYSA-M lithium;bromide;hydrate Chemical compound [Li+].O.[Br-] IPLONMMJNGTUAI-UHFFFAOYSA-M 0.000 claims description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 3
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- LUMVCLJFHCTMCV-UHFFFAOYSA-M potassium;hydroxide;hydrate Chemical compound O.[OH-].[K+] LUMVCLJFHCTMCV-UHFFFAOYSA-M 0.000 claims description 3
- VXJIMUZIBHBWBV-UHFFFAOYSA-M lithium;chloride;hydrate Chemical compound [Li+].O.[Cl-] VXJIMUZIBHBWBV-UHFFFAOYSA-M 0.000 claims description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims 1
- 229910052708 sodium Inorganic materials 0.000 claims 1
- 239000011734 sodium Substances 0.000 claims 1
- 239000005864 Sulphur Substances 0.000 abstract description 10
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 241000196324 Embryophyta Species 0.000 description 35
- 239000000498 cooling water Substances 0.000 description 22
- 230000008676 import Effects 0.000 description 9
- 239000000463 material Substances 0.000 description 9
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- 230000008901 benefit Effects 0.000 description 6
- 238000006477 desulfuration reaction Methods 0.000 description 6
- 230000023556 desulfurization Effects 0.000 description 6
- 239000006096 absorbing agent Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 238000010025 steaming Methods 0.000 description 4
- 238000003795 desorption Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- JBJWASZNUJCEKT-UHFFFAOYSA-M sodium;hydroxide;hydrate Chemical compound O.[OH-].[Na+] JBJWASZNUJCEKT-UHFFFAOYSA-M 0.000 description 2
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- ZZVUWRFHKOJYTH-UHFFFAOYSA-N diphenhydramine Chemical compound C=1C=CC=CC=1C(OCCN(C)C)C1=CC=CC=C1 ZZVUWRFHKOJYTH-UHFFFAOYSA-N 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 125000001967 indiganyl group Chemical group [H][In]([H])[*] 0.000 description 1
- 230000002045 lasting effect Effects 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000008234 soft water Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B30/00—Heat pumps
- F25B30/06—Heat pumps characterised by the source of low potential heat
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention provides a kind of residual neat recovering system and exhaust heat recovering method, and for carrying out waste heat recovery to the lean solution in recovery technology of sulfur, which includes gas absorbing unit, solvent regeneration unit and waste heat recovery unit.Gas absorbing unit absorbs gas and is formed rich solution using solvent.Solvent regeneration unit is used to rich solution is carried out solvent reclamation and forms lean solution, and solvent regeneration unit is fluidly connected with gas absorbing unit, and forms poor liquid fluid line and rich solution streamline.Waste heat recovery unit is arranged on poor liquid fluid line, and the lean solution of solvent regeneration unit output is delivered to waste heat recovery unit and carries out waste heat recovery, the thermal energy thermal energy of lean solution being partially converted into solvent regeneration unit.The residual neat recovering system of the present invention can fully in Recovered sulphur recovery process lean solution low temperature exhaust heat, the low grade heat energy of lean solution is converted into the energy of internal system, the utilization rate of energy is improved, reduces production cost.
Description
Technical field
The present invention relates to technical field of energy saving and environmental protection, and relate more specifically to a kind of residual neat recovering system and a kind of waste heat time
Receiving method.
Background technology
In known recovery technology of sulfur, generally use Claus method or improvement Claus method are to containing H2The sour gas of S
Sulphur recovery is carried out, and generally requires and tail gas is handled and is purified.In large and medium-sized sulfur recovery facility, processing mode
The predominantly method of reduction+absorption, i.e., first by the SO in tail gas2With S hydrogenating reductions into H2S, then using all in absorption tower
The selective desulfurization solvent of such as hydramine is to H2S carries out chemical absorbing.
Desulfurization solvent absorbs H2S-shaped becomes rich solution, then is delivered to regenerator；Regenerator uses steam stripped mode by rich solution
In H2S is desorbed from desulfurization solvent, obtains purer H2S gases are simultaneously delivered in sulfur recovery facility.Desulfurization after desorption
Solvent is formed as lean solution, i.e. regenerated solvent, reenters absorption tower after cooling, so far completes H2The absorption of S is drawn through with solution
Journey.
The lean solution temperature usually exported from the bottom of towe of regenerator is generally 120~130 DEG C.It is being delivered to the process on absorption tower
In, it is necessary to be handled by Multi-stage cooling so that the lean solution for entering to absorption tower reaches suitable temperature, so as to ensure absorption tower
Interior assimilation effect is preferable.Wherein, one of Multi-stage cooling processing is that lean solution and rich solution are carried out heat exchange process, after exchanging heat
The temperature of lean solution is substantially down to 90~100 DEG C.
Since the heat source within the temperature range of 90~100 DEG C is difficult directly to be used by other techniques or user again, the heat
Usually via water cooling and/or the air-cooled waste for being immediately discharged to environment, largely causing system capacity.Water cooling dress at the same time
Put and/or air cooling device can consume a large amount of cooling waters and/or expend a large amount of electric energy so that cause the increase of production cost.
Thus, the low grade heat energy that this part of lean solution not directly utilizes how is fully recycled, and produce more high-grade
Heat source realizes the economy and environmental benefit of energy-saving and emission-reduction, becomes the important topic studied at present to meet the needs of production technology.
Therefore, it is necessary to a kind of residual neat recovering system and a kind of exhaust heat recovering method, to solve the prior art at least in part
Present in problem.
The content of the invention
A series of concept of reduced forms is introduced in Summary, this will in specific embodiment part into
One step describes in detail.The Summary of the present invention is not meant to attempt to limit technical solution claimed
Key feature and essential features, do not mean that the protection domain for attempting to determine technical solution claimed more.
In order to solve the above problems at least in part, according to an aspect of the invention, there is provided a kind of waste heat recovery system
System, for carrying out waste heat recovery to the lean solution in recovery technology of sulfur, which includes gas absorbing unit, solvent
Regeneration unit and waste heat recovery unit.
The gas absorbing unit absorbs gas and is formed rich solution using solvent.
Solvent regeneration unit, the solvent regeneration unit are used to the rich solution is carried out solvent reclamation and formed described poor
Liquid, to be fluidly connected as the solvent absorbed to gas, the solvent regeneration unit with the gas absorbing unit,
And form poor liquid fluid line and rich solution streamline.
The waste heat recovery unit is arranged on the poor liquid fluid line, and the lean solution of the solvent regeneration unit output is defeated
Send to the waste heat recovery unit and carry out waste heat recovery, the thermal energy of the lean solution is partially converted into the solvent reclamation list
Thermal energy in member.
According to this programme, residual neat recovering system can fully in Recovered sulphur recovery process lean solution low temperature exhaust heat, will be poor
The low grade heat energy of liquid is converted into the energy of internal system, improves the utilization rate of energy, reduces production cost.Due to waste heat
The effect of recovery unit is so that the temperature of lean solution is lowered, so as to provide the bar of energy-saving and emission-reduction for the follow-up cooling processing of lean solution
Part.
Preferably, the heat exchange unit being arranged on the poor liquid fluid line and the rich solution streamline is further included, the waste heat returns
The lean solution and the rich solution of gas absorbing unit output for receiving unit output carry out hot friendship via the heat exchange unit
Change processing.
According to this programme, first carry out waste heat recovery from the lean solution of solvent regeneration unit output and carried out again with rich solution at heat exchange
Reason, so can fully recycle the low grade heat energy of lean solution, while enable waste heat recovery unit to produce high-grade heat
Energy.Preferably, the waste heat recovery unit includes heat pump, and the heat pump is fluidly connected with the solvent regeneration unit, so that institute
The thermal energy for stating lean solution via the heat-pump part is absorbed.
According to this programme, the low grade heat energy of lean solution can be recycled using heat pump.
Preferably, the waste heat recovery unit further includes flash distillation plant, and the flash distillation plant is connected with the heat pump fluid,
And the conveying streamline of hot water is formed, the hot water is converted into steam via the flash distillation plant, and is delivered to the solvent reclamation
Unit is as heat source.
According to this programme, the low grade heat energy of lean solution can be converted into the high-grade thermal energy of steam, using as solvent again
The heat source of raw unit, reduces the consumption of the steam of former process system, realizes the economic benefit and Environmental Effect of energy-saving and emission-reduction
Benefit.
Preferably, the hot water of the heat pump output is superheated water, and the temperature of the superheated water is described higher than being delivered to
The temperature of the lean solution of heat pump.
According to this programme so that the low grade heat energy of lean solution can be converted into the high-grade thermal energy of superheated water, so as to improve
The economic benefit of residual neat recovering system.
Preferably, the waste heat recovery unit further includes water replanishing device, the water replanishing device and the flash distillation plant fluid
Connection, to carry out moisturizing to the flash distillation plant.
According to this programme so that the liquid level of water maintains certain height in flash distillation plant.
Preferably, the solvent regeneration unit includes solvent regeneration tower and reboiler, and the reboiler and the solvent are again
Raw tower is connected with the heat pump fluid, respectively to convey the lean solution to the solvent regeneration tower and the heat pump, and institute
State steam and be delivered to the reboiler, using the heat source boiled again as the lean solution.
According to this programme, part heat load can be provided for reboiler so that the low grade heat energy of lean solution is converted into lean solution
The thermal energy boiled again.
Preferably, the heat pump includes generator and evaporator, and the lean solution is delivered to the steaming with cascade successively
Device and the generator are sent out, continuously to carry out heat exchange process, or the lean solution is respectively delivered to institute with parallel form
Generator and the evaporator are stated, respectively to carry out heat exchange process.
According to this programme, the low-grade heat in lean solution can be enabled fully to be utilized, and can caused and heat
The temperature that pump carries out the lean solution after heat exchange is relatively low.
Preferably, the heat pump include circulation working medium pair, the working medium to for lithium bromide-water, ammonia-water, lithium chloride-
Any of water, lithium chloride and lithium bromide-water, potassium hydroxide-water, sodium hydroxide-water, lithium nitrate amine-ammonia.
Preferably, the cooling unit between the heat exchange unit and the gas absorbing unit is further included, with cooling
The lean solution.
According to this programme so that lean solution can be cooled to the feeding temperature of gas absorbing unit.Due to waste heat recovery unit
Setting so that effectively reducing energy expenditure in cooling unit.
According to another aspect of the present invention, there is provided a kind of exhaust heat recovering method, in recovery technology of sulfur
Lean solution carries out waste heat recovery, which includes the following steps：
Gas absorption step, absorbs gas using solvent and forms rich solution；
Solvent reclamation step, carries out solvent reclamation to the rich solution and forms the lean solution, to be absorbed as the gas
The solvent in step；And
Waste heat recovery step, waste heat recovery is carried out to the thermal energy of the lean solution, and by the thermal energy of the lean solution partly
The thermal energy being converted into the solvent reclamation step.
According to this programme, exhaust heat recovering method can fully in Recovered sulphur recovery process lean solution low temperature exhaust heat, will be poor
The low grade heat energy of liquid is converted into the energy of internal system, improves the utilization rate of energy, reduces production cost.Due to lean solution
Heat exchange is carried out in waste heat recovery step, thus the temperature of lean solution is lowered, so as to be carried for the follow-up cooling processing of lean solution
The condition of energy-saving and emission-reduction is supplied.
Preferably, heat exchange step is further included after the waste heat recovery step, in the heat exchange step, by waste heat
The lean solution of recycling carries out heat exchange process with the rich solution.
Preferably, in the waste heat recovery step, the thermal energy of the lean solution via heat-pump part is absorbed.
Preferably, in the waste heat recovery step, the thermal energy of absorption is used for heat hot water by the heat pump, to institute
State the hot water after heating to carry out flash distillation process and be converted into steam, to be used as the heat source in the solvent reclamation step.
Preferably, the hot water after the heating is superheated water, and the temperature of the superheated water of the heat pump output, which is higher than, to be delivered to
The temperature of the lean solution of the heat pump.
Preferably, in the waste heat recovery step, to the flash distillation process during carry out moisturizing.
Preferably, in the waste heat recovery step, the lean solution is delivered to the steaming of the heat pump with cascade successively
Device and generator are sent out, continuously to carry out heat exchange process twice, or the lean solution via the heat pump with parallel form point
The evaporator and generator of the heat pump are not delivered to, respectively to carry out heat exchange process via the heat pump.
Preferably, between the heat exchange step and the gas absorption step, lean solution cooling step is further included, in lean solution
In cooling step, cooling treatment is carried out to the lean solution Jing Guo the heat exchange process.
Brief description of the drawings
The drawings below of the present invention is used to understand the present invention in this as the part of the present invention.Shown in the drawings of this hair
Bright embodiment and its description, device used to explain the present invention and principle.In the accompanying drawings,
Fig. 1 is the structure diagram according to the residual neat recovering system of the preferred embodiment of the present invention；
Fig. 2 is the structure diagram of the first embodiment of the residual neat recovering system shown in Fig. 1；
Fig. 3 is the structure diagram of the second embodiment of the residual neat recovering system shown in Fig. 1；And
Fig. 4 is the structure diagram according to the exhaust heat recovering method of the preferred embodiment of the present invention.
Embodiment
In the following description, a large amount of concrete details are given in order to provide more thorough understanding of the invention.So
And it is obvious to the skilled person that the present invention may not need one or more of these details and be able to
Implement.In other examples, in order to avoid with the present invention obscure, for some technical characteristics well known in the art not into
Row description.
In order to thoroughly understand the present invention, detailed structure will be proposed in following description, to explain the present invention.It is aobvious
So, execution of the invention is not limited to the specific details that the those skilled in the art are familiar with.The preferable reality of the present invention
Example is applied to be described in detail as follows, but in addition to these detailed descriptions, the present invention can also have other embodiment, should not solve
It is interpreted as being confined to embodiments presented herein.
It should be appreciated that the purpose of term as used herein is only that description specific embodiment and not as the present invention
Limitation, " one " of singulative, "one" and " described/should " be also intended to include plural form, unless context is expressly noted that
Other mode.When the term " comprising " and/or " including " is used in this specification, its indicate there are the feature, entirety,
Step, operation, element and/or component, but do not preclude the presence or addition of other one or more features, entirety, step, operation,
Element, component and/or combinations thereof.Term " on ", " under ", "front", "rear", "left", "right" used in the present invention with
And similar statement is for illustrative purposes only, not limits.
The cited such as ordinal number of " first " and " second " is only to identify in the present invention, without any other
Implication, such as specific order etc..Moreover, for example, term " first component " itself does not imply that the presence of " second component ", art
Language " second component " does not imply that the presence of " first component " in itself.
Hereinafter, the specific embodiment of the present invention is described in more detail with reference to the accompanying drawings, those figures show this
The representative embodiment of invention, is not to limit the present invention.
A preferred embodiment of the invention, there is provided a kind of residual neat recovering system, for sulphur recovery work
Lean solution in skill carries out waste heat recovery.
As shown in Figure 1, the residual neat recovering system includes gas absorbing unit 10, solvent regeneration unit 20 and waste heat recovery list
Member 30.Gas absorbing unit 10 absorbs gas and is formed rich solution using solvent, and is delivered to solvent regeneration unit 20.It is molten
Agent regeneration unit 20 is used to rich solution is carried out solvent reclamation and forms lean solution, and lean solution return is delivered to gas absorbing unit 10 and makees
For the solvent absorbed to gas.Waste heat recovery unit 30 is used to carry out waste heat time to the lean solution that solvent regeneration unit 20 exports
Receive, the low grade heat energy of lean solution can so be recycled.The residual neat recovering system of this preferred embodiment can fill
Divide the low temperature exhaust heat of lean solution in Recovered sulphur recovery process, improve the utilization rate of energy.Also, due to waste heat recovery unit
Effect is so that the temperature of lean solution is lowered, so as to provide the condition of energy-saving and emission-reduction for the follow-up cooling processing of lean solution.
The thermal energy of the lean solution of this preferred embodiment solvent in future regeneration unit 20 is partially converted into solvent reclamation list
Heat source in member 20, so that solvent regeneration unit 20 and waste heat recovery unit 30 are improved there are the relation between supply and demand of energy
The economic benefit of the energy-saving and emission-reduction of residual neat recovering system, reduces production cost.It is understood that if necessary to and/or the phase
Hope, the thermal energy of above-mentioned waste heat recovery is also provided to other techniques or heat source user, for example as heating source.
Further, solvent regeneration unit 20 is fluidly connected with gas absorbing unit 10, and forms poor liquid fluid line L1 and richness
Liquid fluid line L2.Waste heat recovery unit 30 is arranged on poor liquid fluid line L1, and the lean solution that solvent regeneration unit 20 exports is returned via waste heat
Receive unit 30 and carry out waste heat recovery.It should be noted that " streamline " that is referred in text, which is defined to fluid, passes through pipeline, device and pipe
The fluid passage formed during one or more in part.Specifically, " poor liquid fluid line L1 " refers to lean solution from solvent regeneration unit 20
After output, the lean solution passage formed during unit 10 receives is actually taken up by gas." rich solution streamline L2 " refers to rich solution from gas
After absorptive unit 10 exports, the rich solution passage that is formed during being received by solvent regeneration unit 20.
In order to which gas absorbing unit 10 can reach preferable assimilation effect, then control is needed to enter to gas absorbing unit
The temperature of 10 lean solution is in suitable scope.In order to which solvent regeneration unit 20 can reach preferable regeneration effect, then need
Control enters to the temperature of the rich solution of solvent regeneration unit 20 in suitable scope.Thus, alternatively, residual neat recovering system is also
Including heat exchange unit 40 and cooling unit 50, heat exchange unit 40 is arranged on poor liquid fluid line L1 and rich solution streamline L2, waste heat recovery
The lean solution that unit 30 exports carries out heat exchange process with the rich solution that gas absorbing unit 10 exports via heat exchange unit 40.So may be used
So that the temperature of rich solution is in suitable scope.Cooling unit 50 is arranged on poor liquid fluid line L1, and is located at heat exchange unit
Between 40 and gas absorbing unit 10, so that after lean solution cools down via heat exchange unit 40, carried out again via cooling unit 50
Cooling, so as to reach suitable feeding temperature.
Preferably, gas absorbing unit 10 includes absorption tower 11.It is gentle that the tower top on absorption tower 11 is provided with lean solution import 12
Body outlet 13, bottom of towe is provided with containing H2The gas feed 14 of the tail gas of S and rich solution outlet 15.Contain H2The tail gas of S from gas into
Mouth 14 enters, in absorption tower 11, the H in tail gas2S is absorbed by lean solution, and unabsorbed gases is discharged from gas vent 13, is inhaled
Receive H2The lean solution of S is formed as rich solution and is exported from rich solution outlet 15.
It should be noted that " lean solution " and " rich solution " that is mentioned above is relative to H2The solute of S and limit, lean solution is
To H2S has absorbent solution, and rich solution refers to absorb H2After S, solvent and solute reach substantial equilibrium in solution.This
The solvent of preferred embodiment is preferably desulfurization solvent.
Preferably, solvent regeneration unit 20 include solvent regeneration tower 21, positioned at solvent regeneration tower 21 bottom of towe reboiler
22 and the condenser 23 positioned at tower top.The rich solution that absorption tower 11 exports enters to solvent regeneration tower 21.In solvent regeneration tower 21
Solvent reclamation processing is carried out to rich solution by steam stripped mode.Reboiler 22 is fluidly connected with solvent regeneration tower 21 so that is formed
Bottom of towe flows back, and condenser 23 is fluidly connected with solvent regeneration tower 21 so that forms overhead reflux, thus, 21 energy of solvent regeneration tower
It is enough that there is higher column efficiency.Desorb obtained H2S gases are delivered to sulfur recovery facility, carry out sulphur recovery.What is obtained is poor
Liquid exports from reboiler 22 and is delivered to absorption tower 11 via after the processing of the grade of waste heat recovery unit 30 Multi-stage cooling.In addition, reboiler
22 generally use steam are as heat source.
Since the lean solution temperature exported from reboiler 22 is usually 120~130 DEG C, in order to reasonably utilize this portion of lean solution
Divide thermal energy, the system is provided with waste heat recovery unit 30.Further, waste heat recovery unit 30 includes heat pump 31 and flash distillation plant
32.Heat pump 31 is fluidly connected with reboiler 22, and the lean solution exported from reboiler 22 is via Pipeline transport to heat pump 31, the heat of lean solution
Can partly it be absorbed via heat pump 31.Flash distillation plant 32 is fluidly connected with heat pump 31, the liquid water (heat in flash distillation plant 32
Water) it is transported to heat pump 31, and the thermal energy of the lean solution of absorption is converted into energy for heat hot water via heat pump 31, with
Hot water is set to become high-temperature-hot-water and be exported from heat pump 31.High-temperature-hot-water is back to flash distillation plant 32 and is converted into steaming by flash distillation process
Vapour, the steam are delivered to reboiler 22, and using the heat source boiled again as lean solution, thermic load is provided for reboiler 22.It is mentioned above
" high temperature " can be understood as temperature of the temperature higher than the hot water of input heat pump 31 of the hot water of the output of heat pump 31, and can dodge
Steam the temperature that device 32 is partially converted to steam.Above-mentioned steam is usually saturated vapor, and steam pressure substantially 0.3~
0.4Mpag。
Preferably, high-temperature-hot-water is superheated water.Heat pump 31 is temperature-boosting absorption heat pump, is made using Absorption heat-transformer technology
The temperature for obtaining superheated water is higher than the temperature for the lean solution for being delivered to heat pump 31.And the temperature of superheated water is enabled to be not less than 100
℃.The heat pump 31 can provide other driving heat sources by the use of low temperature exhaust heat possessed by lean solution as driving heat source without the external world,
It just may be such that the whole unit operation of heat pump 31.Heat pump 31 usually mainly includes generator, evaporator, absorber and condenser,
And low temperature exhaust heat possessed by lean solution is converted into the heat of hot water to realizing that the heat in unit shifts using the working medium of circulation
Energy, improves the grade of the part of waste heat of lean solution.
Working medium to be preferably lithium bromide-water, ammonia-water, lithium chloride-water, lithium chloride and lithium bromide-water, potassium hydroxide-water,
Any of sodium hydroxide-water, lithium nitrate amine-ammonia, or other meet the working medium of heat pump 31 to desired material.
Waste heat recovery unit 30 further includes circulating water device 33, to provide lasting recirculated cooling water for heat pump 31, follows
Ring water installations 33 can be public work pipe network or other the device of recirculated cooling water can be provided.Preferably, recirculated water
The temperature of recirculated cooling water in device 33 is no more than 50 DEG C, to the working medium in sorption type heat pump 31 to being put in cyclic process
The partial heat gone out.
Preferably, the hot water in flash distillation plant 32 is via hot water circulating pump 35 and Pipeline transport to heat pump 31, after heat exchange
High-temperature-hot-water is back to flash distillation plant 32 via pipeline, carries out flash distillation process.The driving that hot water circulating pump 35 is flowed as hot water
Source, is used for realization circulation of the hot water between heat pump 31 and flash distillation plant 32.Convey and be provided with decompression on the pipeline of high-temperature-hot-water
Valve 36, for adjusting the pressure in flash distillation plant 32, enters after being depressurized from the high-temperature-hot-water that heat pump 31 exports via pressure reducing valve 36
Flash distillation plant 32.It is one that hot water circulating pump 35 is shown in figure, and flash distillation plant 32 is flash tank, if desired and/or it is expected,
Hot water circulating pump 35 can set it is multiple, it is spare to make, flash distillation plant 32 can be other have the function of flash distillation device.
Further, waste heat recovery unit 30 further includes water replanishing device 34, and water replanishing device 34 connects with 32 fluid of flash distillation plant
Connect, to carry out moisturizing to flash distillation plant 32, so as to maintain the liquid level of water in flash distillation plant 32.Water replanishing device 34 can be public work
The steam condensation grid of journey, or the device or system of other offer soft water.
Further, heat exchange unit 40 is used to the rich solution of 11 bottom of towe of absorption tower output being heated to suitable temperature, so as to
Reach the feeding temperature of solvent regeneration tower 21.Heat exchange unit 40 includes an at least heat exchanger.A kind of preferred feelings are shown in Fig. 1
Condition, heat exchange unit 40 include 41 and second heat exchanger 42 of First Heat Exchanger that is sequentially connected in series so that lean solution and rich solution continuously into
Row two-stage exchanges heat.Cooling unit 50 is used to lean solution being cooled to suitable temperature, so as to reaching the feeding temperature on absorption tower 11.It is cold
But unit 50 includes air cooling device 51 and/or water cooling plant 52, the lean solution after being exchanged heat by heat exchange unit 40 and rich solution
Air-cooled and/or water cooling can be carried out in cooling unit 50, continues to carry out cooling processing to lean solution, so that lean solution can reach
Into the suitable temperature on absorption tower 11.Preferably, water cooling plant 52 is located at the downstream of air cooling device 51, so that lean solution can be successively
Air-cooled and water cooling is carried out, to save the dosage of the cooling water of water cooling plant 52.
It should be noted that if lean solution is via the temperature energy after heat pump 31,41 and second heat exchanger 42 of First Heat Exchanger
Enough satisfactions enter to the requirement on absorption tower 11, and air cooling device 51 and water cooling plant 52 can be omitted or the deactivation of selectivity.By
This, the waste heat recovery unit 30 of this preferred embodiment can significantly reduce air cooling device 51 and the heat of water cooling plant 52 is born
Lotus, so as to save energy consumption, reduce production cost, and avoids a large amount of losses of the low grade heat energy of lean solution.
Further, although waste heat recovery unit 30 is capable of providing steam and gives heat source of the reboiler 22 as a part,
It is in addition steam supplying device 24 can also be set, to convey steam to reboiler 22, to ensure the demand of 22 thermal energy of reboiler.Steam supply
Device 24 is connected with reboiler 22 via steam supply pipeline 25, so that both fluidly connect.Regulating valve is provided with steam supply pipeline 25
26 and steam converter valve 27.Steam converter valve 27 is arranged at the upstream of regulating valve 26, so that steam first carries out pressure and temperature reducing, then passes through
The adjusting of flow is carried out by regulating valve 26.The pipeline of steam for conveying flash distillation plant 32 is connected with steam supply pipeline 25, so that
Two parts steam is delivered to reboiler 22 jointly after collecting.Two parts steam is collected after regulating valve 26, so can be with
The amount of the steam of the output of steam supplying device 24 is adjusted according to the amount of the steam of the output of flash distillation plant 32.The steaming that flash distillation plant 32 produces
Vapour can be that reboiler 22 provides part heat load, reduce the steam consumption of steam supplying device 24.
If desired and/or it is expected, the waste heat recovery unit 30 in the residual neat recovering system of the present invention can be arranged at
Existing H2In the absorption and desorption process system of S.Since waste heat recovery unit 30 is arranged on lean solution pipeline so that without big
Amplitude transforms the arrangement of pipeline, it is possible to is reasonably installed each device in waste heat recovery unit 30, component.It is if logical
Transformation formation and the residual neat recovering system same structure of the present invention of process system are crossed, due to through waste heat recovery list
Lean solution after the heat exchange of member 30 is reduced relative to the lean solution temperature of original heat-exchange system, when using the original for including poor rich liquid heat exchanger
When having heat-exchange system to lean solution progress Multi-stage cooling, in order to make the relatively former heat exchange of the temperature of the rich solution of poor rich liquid heat exchanger output
System remains unchanged, and can increase the heat exchange area of poor rich liquid heat exchanger.Increasing heat exchange area can be by replacing heat exchange area
Big heat exchanger, or increase the other modes such as quantity of heat exchanger to realize.
Residual neat recovering system provided by the invention is applied in recovery technology of sulfur, fully Recovered sulphur can recycle work
The low temperature exhaust heat of the lean solution of 21 bottom of towe of solvent regeneration tower in skill, reduces the follow-up cooling load of lean solution, effectively reduces cooling water
With the consumption of electric power in air cooling device 51.Although absorption heat pump 31 needs to consume a certain amount of recirculated cooling water in itself, this
Invention substantially reduces in the total flow of recirculated cooling water.In addition, heat pump 31 has produced above-mentioned high warm by waste heat recovery
Water, hot water flashes in flash distillation plant 32 and generates steam, by the way that steam to be linked into the steam pipe network of reboiler 22, can attach most importance to
Boil device 22 and part heat load is provided, self-produced personal, effectively reduces the steam consumption of public work.
First embodiment
The residual neat recovering system provided according to above-mentioned preferred embodiment, the present invention provides according to first embodiment remaining
Heat recovery system, as shown in Fig. 2, the residual neat recovering system of the present embodiment and the residual neat recovering system of above-mentioned preferred embodiment
Structure is roughly the same, the difference is that the present embodiment further defines the mode that heat pump 31 receives lean solution.For brevity, originally
Identical part will not be described in great detail in embodiment, and the unit identical with preferred embodiment, device carry out herein it is identical
Numbering.
The lean solution that reboiler 22 exports is delivered to evaporator 311 and generator 312 with cascade successively via pipeline, with
Continuously carry out heat exchange process.Delivery in flash distillation plant 32 to heat pump 31 absorber 313, to carry out at heat exchange
Reason.Recirculated cooling water in circulating water device 33 is delivered to the condenser 314 of heat pump 31, to carry out heat exchange process.
Further, as shown in Fig. 2, heat pump 31 includes four material inlets and four material outlets, four material inlets
Respectively the first lean solution import A1, the second lean solution import B1, hot water inlet C1 and cooling water inlet D1.Four material outlet difference
A2 is exported for the first lean solution, the second lean solution exports B2, hot water outlet C2 and cooling water outlet D2.Lean solution is via the first lean solution import
A1 is delivered to evaporator 311, is exported after carrying out heat exchange process from the first lean solution outlet A2, then poor from second via pipeline again
Liquid import B1 is delivered to generator 312, exports to heat exchange unit 40, completes from the second lean solution outlet B2 after carrying out heat exchange process
Heat exchange of the lean solution in heat pump 31.
The hot water of output is delivered to absorber 313 via hot water inlet C1 in flash distillation plant 32, after carrying out heat exchange process
The heat exchange for flash distillation plant 32, completing hot water in heat pump 31 is exported from hot water outlet C2.
Recirculated cooling water in circulating water device 33 is delivered to condenser 314 via cooling water inlet D1, carries out heat exchange
The heat exchange for circulating water device 33, completing recirculated cooling water in heat pump 31 is exported after processing from cooling water outlet D2.
The evaporator 311 and generator 312 of the present embodiment are arranged on lean solution pipeline in series so that lean solution can
To pass sequentially through evaporator 311 and generator 312, heat exchange process is continuously carried out.The present embodiment is suitable for solvent regeneration tower
The less situation of the lean solutions of 21 bottom of towe.
Second embodiment
The residual neat recovering system provided according to above-mentioned preferred embodiment, the present invention provides according to second embodiment remaining
Heat recovery system, as shown in Fig. 2, the knot of the residual neat recovering system of the present embodiment and the residual neat recovering system of above-mentioned first embodiment
Structure is roughly the same, the difference is that the heat pump 31 of the present embodiment receives the mode of lean solution.For brevity, it is identical in the present embodiment
Part will not be described in great detail, and the unit identical with first embodiment, device are identically numbered herein.
The lean solution that reboiler 22 exports respectively is delivered to evaporator 311 and generator 312 with parallel form via pipeline,
Respectively to carry out heat exchange process.Delivery in flash distillation plant 32 to heat pump 31 absorber 313, to carry out heat exchange
Processing.Recirculated cooling water in circulating water device 33 is delivered to the condenser 314 of heat pump 31, to carry out heat exchange process.
Further, as shown in figure 3, heat pump 31 includes four material inlets and four material outlets, four material inlets
Respectively the first lean solution import A1, the second lean solution import B1, hot water inlet C1 and cooling water inlet D1.Four material outlet difference
A2 is exported for the first lean solution, the second lean solution exports B2, hot water outlet C2 and cooling water outlet D2.Lean solution is via two pipes in parallel
Road is respectively delivered to evaporator 311 and generator 312 from the first lean solution import A1 and the second lean solution import B1, two-part poor
Liquid respectively carries out heat exchange process in evaporator 311 and generator 312, then poor from first via two pipelines in parallel
Liquid exports A2 and the second lean solution outlet B2 exports the heat exchange for heat exchange unit 40, completing lean solution in heat pump 31.
The hot water of output is delivered to absorber 313 via hot water inlet C1 in flash distillation plant 32, after carrying out heat exchange process
The heat exchange for flash distillation plant 32, completing hot water in heat pump 31 is exported from hot water outlet C2.
Recirculated cooling water in circulating water device 33 is delivered to condenser 314 via cooling water inlet D1, carries out heat exchange
The heat exchange for circulating water device 33, completing recirculated cooling water in heat pump 31 is exported after processing from cooling water outlet D2.
The evaporator 311 and generator 312 of the present embodiment are arranged on lean solution pipeline in parallel so that lean solution can
At the same time by evaporator 311 and generator 312, respectively to carry out heat exchange process.The present embodiment is suitable for solvent regeneration tower
The situation of the lean solution abundance of 21 bottom of towe.
According to another aspect of the present invention, a kind of exhaust heat recovering method is additionally provided, in recovery technology of sulfur
Lean solution carry out waste heat recovery.Specifically, as shown in figure 4, the exhaust heat recovering method includes the following steps：
S1：Gas absorption step, absorbs gas using solvent and forms rich solution.
S2：Solvent reclamation step, carries out solvent reclamation to rich solution and forms lean solution, using as molten in gas absorption step
Agent.
S3：Waste heat recovery step, waste heat recovery is partly carried out to the thermal energy of lean solution, and by the thermal energy of lean solution partly
The heat source being converted into solvent reclamation step S2.
Enable the low temperature of lean solution in exhaust heat recovering method fully Recovered sulphur recovery process by using above-mentioned steps
The low grade heat energy of lean solution, is converted into the energy of internal system by waste heat, is improved the utilization rate of energy, is reduced and be produced into
This.Since lean solution has carried out heat exchange in waste heat recovery step, thus the temperature of lean solution is lowered, so that follow-up for lean solution
Cooling handles the condition for providing energy-saving and emission-reduction.
Specifically, gas absorption step S1 can be containing H2H in the tail gas of S2S is absorbed into such as desulfurization solvent
In solvent, do not discharged by the gas of solvent absorption, absorb H2The solvent of S is formed as rich solution and carries out solvent reclamation step S2.
Further, exhaust heat recovering method further includes S4：Heat exchange step, in heat exchange step S4, by waste heat recovery
Lean solution carries out heat exchange process with rich solution.Since the temperature of rich solution can influence the effect of solvent reclamation, therefore, it is necessary to rich solution into
Row heating treatment.Lean solution and rich solution are carried out the mode of heat exchange to heat rich solution by this preferred embodiment, so as to ensure solvent
Regenerated effect.
Solvent reclamation step S2 causes the H in rich solution2S is desorbed, the H of formation2S is transported to recovery technology of sulfur progress
Sulphur recovery, the lean solution of formation are delivered in gas absorption step S1, continue as solvent again after Multi-stage cooling is handled.So
So that save the input cost of solvent in exhaust heat recovering method.
In order to enable H2The desorption effect of S is more preferable, in solvent reclamation step S2, to H2S gases are carried out at condensing reflux
Reason, and reflow treatment is boiled again to lean solution.Lean solution partial reflux after boiling again, partly by carry out waste heat recovery, with reasonably
Utilize the low temperature exhaust heat of lean solution.
Further, in waste heat recovery step S3, the thermal energy of lean solution via heat-pump part is absorbed.And heat pump will
The thermal energy of absorption is used for heat hot water, and to form superheated water, superheated water carries out flash distillation process and is converted into steam, using as solvent again
Heat source in raw step S2.
Preferably, heat pump uses temperature-boosting absorption heat pump.Thus, the temperature of the superheated water of heat pump output can be higher than defeated
Send to the temperature of the lean solution of heat pump so that the low grade heat energy in lean solution can be converted into the high-grade thermal energy of superheated water, improve
The economic benefit of residual neat recovering system.
In waste heat recovery step S3, lean solution can use different mode of movement and enter heat pump.Alternatively, lean solution with
Cascade is delivered to the evaporator and generator of the heat pump successively, continuously to be carried out via heat pump twice at heat exchange
Reason.Alternatively, alternatively, lean solution is respectively delivered to the evaporator and generator of the heat pump, respectively to be carried out via heat pump
Heat exchange process.
Since the steam that flash distillation process produces is output as the part heat load that lean solution boils again, in order to enable hot water can
Continuously carry out heat exchange process with heat pump, then in waste heat recovery step S3, it is necessary to carrying out moisturizing during flash distillation process,
So that the amount control of hot water is within the specific limits.
Between heat exchange step S4 and gas absorption step S1, S5 is further included：Lean solution cooling step, in lean solution cooling step
In S5, cooling treatment is carried out to the lean solution Jing Guo heat exchange process.Cooling treatment can use air-cooled and/or water cooling to lean solution into
Cool down to one step, so that lean solution meets the suitable temperature for carrying out solvent absorption step.
Exhaust heat recovering method provided by the invention can use above-mentioned residual neat recovering system and realize, for brevity, tool
The waste heat reclaiming process process of body is referred to the partial content of residual neat recovering system.
Unless otherwise defined, the those skilled in the art of technical and scientific term used herein and the present invention
Normally understood implication is identical.Term used herein is intended merely to describe specifically to implement purpose, it is not intended that limitation is originally
Invention.The term such as herein presented " portion ", " part " can both represent single part, can also represent multiple parts
Combination.The term such as herein presented " installation ", " setting " can both represent that a component was attached directly to another portion
Part, can also represent that a component is attached to another component by middleware.Describe in one embodiment herein
Feature can be applied to another embodiment in combination individually or with other features, unless this feature is in another implementation
Do not apply to or be otherwise noted in mode.
The present invention is illustrated by above-described embodiment, but it is to be understood that, above-described embodiment is only intended to
Citing and the purpose of explanation, and be not intended to limit the invention in the range of described embodiment.In addition people in the art
Member is it is understood that the invention is not limited in above-described embodiment, teaching according to the present invention can also be made more kinds of
Variants and modifications, these variants and modifications are all fallen within scope of the present invention.Protection scope of the present invention by
The appended claims and its equivalent scope are defined.
Claims (18)
- A kind of 1. residual neat recovering system, for carrying out waste heat recovery to the lean solution in recovery technology of sulfur, it is characterised in that bag Include：Gas absorbing unit, the gas absorbing unit absorb gas and are formed rich solution using solvent；Solvent regeneration unit, the solvent regeneration unit are used to the rich solution is carried out solvent reclamation and forms the lean solution, with As the solvent absorbed to gas, the solvent regeneration unit is fluidly connected with the gas absorbing unit, and shape Into poor liquid fluid line and rich solution streamline；AndWaste heat recovery unit, the waste heat recovery unit are arranged on the poor liquid fluid line, the solvent regeneration unit output The lean solution carries out waste heat recovery by the waste heat recovery unit, the thermal energy of the lean solution is partially converted into described molten Thermal energy in agent regeneration unit.
- 2. residual neat recovering system according to claim 1, it is characterised in that further include and be arranged at the poor liquid fluid line and institute State the heat exchange unit on rich solution streamline, the lean solution and the gas absorbing unit output of the waste heat recovery unit output The rich solution carries out heat exchange process via the heat exchange unit.
- 3. residual neat recovering system according to claim 1, it is characterised in that the waste heat recovery unit includes heat pump, institute State heat pump to fluidly connect with the solvent regeneration unit, so that the thermal energy of the lean solution via the heat-pump part is absorbed.
- 4. residual neat recovering system according to claim 3, it is characterised in that the waste heat recovery unit further includes flash distillation dress Put, the flash distillation plant is connected with the heat pump fluid, and forms the conveying streamline of hot water, and the hot water is filled via the flash distillation Put and be converted into steam, and be delivered to the solvent regeneration unit as heat source.
- 5. residual neat recovering system according to claim 4, it is characterised in that the hot water of the heat pump output is overheat Water, the temperature of the superheated water are higher than the temperature for the lean solution for being delivered to the heat pump.
- 6. residual neat recovering system according to claim 4, it is characterised in that the waste heat recovery unit further includes moisturizing dress Put, the water replanishing device is fluidly connected with the flash distillation plant, to carry out moisturizing to the flash distillation plant.
- 7. residual neat recovering system according to claim 4, it is characterised in that the solvent regeneration unit includes solvent reclamation Tower and reboiler, the reboiler are connected with the solvent regeneration tower and the heat pump fluid, respectively to convey the lean solution To the solvent regeneration tower and the heat pump, and the steam is delivered to the reboiler, using what is boiled again as the lean solution Heat source.
- 8. residual neat recovering system according to claim 3, it is characterised in that the heat pump includes generator and evaporator, The lean solution is delivered to the evaporator and the generator with cascade successively, continuously to carry out heat exchange process；Or PersonThe lean solution is respectively delivered to the generator and the evaporator with parallel form, respectively to carry out at heat exchange Reason.
- 9. residual neat recovering system according to claim 3, it is characterised in that the heat pump includes the working medium pair of circulation, institute State working medium to for lithium bromide-water, ammonia-water, lithium chloride-water, lithium chloride and lithium bromide-water, potassium hydroxide-water, sodium hydroxide- Any of water, lithium nitrate amine-ammonia.
- 10. residual neat recovering system according to claim 2, it is characterised in that further include positioned at the heat exchange unit and institute The cooling unit between gas absorbing unit is stated, to cool down the lean solution.
- A kind of 11. exhaust heat recovering method, for carrying out waste heat recovery to the lean solution in recovery technology of sulfur, it is characterised in that bag Include following steps：Gas absorption step, absorbs gas using solvent and forms rich solution；Solvent reclamation step, carries out solvent reclamation to the rich solution and forms the lean solution, to be used as the gas absorption step In solvent；AndWaste heat recovery step, partly carries out the thermal energy of the lean solution waste heat recovery, and by the thermal energy part of the lean solution Ground is converted into the thermal energy in the solvent reclamation step.
- 12. exhaust heat recovering method according to claim 11, it is characterised in that also wrapped after the waste heat recovery step Heat exchange step is included, in the heat exchange step, the lean solution by waste heat recovery carries out heat exchange process with the rich solution.
- 13. exhaust heat recovering method according to claim 11, it is characterised in that described in the waste heat recovery step The thermal energy of lean solution via heat-pump part is absorbed.
- 14. exhaust heat recovering method according to claim 13, it is characterised in that described in the waste heat recovery step The thermal energy of absorption is used for heat hot water by heat pump, is carried out flash distillation process to the hot water after the heating and is converted into steam, To be used as the heat source in the solvent reclamation step.
- 15. exhaust heat recovering method according to claim 14, it is characterised in that the hot water after the heating is superheated water, The temperature of the superheated water of the heat pump output is higher than the temperature for the lean solution for being delivered to the heat pump.
- 16. exhaust heat recovering method according to claim 14, it is characterised in that in the waste heat recovery step, to institute State and carry out moisturizing during flash distillation process.
- 17. exhaust heat recovering method according to claim 13, it is characterised in that described in the waste heat recovery step Lean solution is delivered to the evaporator and generator of the heat pump with cascade successively, to carry out heat exchange twice via the heat pump Processing；OrThe lean solution is respectively delivered to the evaporator and generator of the heat pump with parallel form, to distinguish via the heat pump Ground carries out heat exchange process.
- 18. exhaust heat recovering method according to claim 12, it is characterised in that inhaled in the heat exchange step and the gas Between receiving step, lean solution cooling step is further included, in the lean solution cooling step, to by described in the heat exchange process Lean solution carries out cooling treatment.
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