CN106635214A - Rich-liquid desorption technique and device for vacuum carbonate desulfuration - Google Patents

Rich-liquid desorption technique and device for vacuum carbonate desulfuration Download PDF

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Publication number
CN106635214A
CN106635214A CN201710049681.4A CN201710049681A CN106635214A CN 106635214 A CN106635214 A CN 106635214A CN 201710049681 A CN201710049681 A CN 201710049681A CN 106635214 A CN106635214 A CN 106635214A
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CN
China
Prior art keywords
liquid
desorber
rich solution
vacuum
rich
Prior art date
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Pending
Application number
CN201710049681.4A
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Chinese (zh)
Inventor
李昊阳
郝鹏
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Acre Coking and Refractory Engineering Consulting Corp MCC
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Acre Coking and Refractory Engineering Consulting Corp MCC
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Application filed by Acre Coking and Refractory Engineering Consulting Corp MCC filed Critical Acre Coking and Refractory Engineering Consulting Corp MCC
Priority to CN201710049681.4A priority Critical patent/CN106635214A/en
Publication of CN106635214A publication Critical patent/CN106635214A/en
Pending legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/103—Sulfur containing contaminants
    • 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
    • B01D53/1456—Removing acid components
    • B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/104—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/44—Deacidification step, e.g. in coal enhancing
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/541—Absorption of impurities during preparation or upgrading of a fuel

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Organic Chemistry (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

The invention discloses a rich-liquid desorption technique for vacuum carbonate desulfuration and a device for vacuum carbonate desulfuration; the device comprises a desorption tower, a rich-liquid tank, a heat exchanger, a condenser, a cooler A, a gas fluid separator, a vacuum condensate tank, a cooler B, and a barren liquor pump; the rich-liquid tank is connected with the heat exchanger through the rich-liquid pump, a rich-liquid outlet of the heat exchanger is connected to the inlet of the middle part of the desorption tower; a gas phase outlet at the top part of the desorption tower is orderly connected with the vacuum condensate tank through the condenser, the cooler A and the gas liquid separator; the condensate pump in the vacuum condensate tank is connected to the inlet at the top part of the desorption tower; the liquid phase outlet at the bottom part of the desorption tower is connected with the heat exchanger through the barren liquor pump, and then connected with the absorbing tower through the cooler B. The device and method can effectively improve the rich-liquid desorption efficiency prevent the condensed and cooled hydrogen sulfide saturated solution from directly returning to the rich-liquid tank, avoid backmixing, improve the desulfuration barren liquor quality, and finally reach the purpose of improving the desulfuration efficiency; the technique can improve the desulfuration efficiency while not add other device and land; thereby facilitating the worker operation.

Description

A kind of rich solution desorption technique and equipment of vacuum carbonate desulfurization
Technical field
The present invention relates to coke oven gas purification field, more particularly to a kind of vacuum carbonate desulfurization rich solution desorption technique and Equipment.
Background technology
Coke-stove gas removing hydrogen sulfide is the important system of gas cleaning device.Vacuum carbonate desulphurization technique is a kind of The common technology of hydrogen sulfide in for removing raw coke oven gas.The processing range is：Desulfurization is carried out to the coal gas into this device, is being inhaled Receive and washed using potassium carbonate lean solution in tower, remove the hydrogen sulfide and partial CO 2 in coal gas.In absorption tower, dioxy Change carbon and hydrogen sulfide to be at war with absorption, lean solution to absorb and become rich solution after hydrogen sulfide and partial CO 2, laggard through heat exchange Enter desorber.Desorption column overhead adopts negative-pressure operation, rich solution to be desorbed into desorber by tower top, hydrogen sulfide and carbon dioxide Condensate cooler is escaped and enter by tower top with gas phase Jing after desorption, liquid phase returns rich solution groove after cooling, gas phase enters true Empty pump, bottom of towe lean solution returns to absorption tower.
Vacuum carbonate sulfur removal technology has the advantages that energy consumption is low, flow process is short compared to other sulfur removal technologies.But, by Limit in its absorption and the mechanism for desorbing, its desulfurization index should be had certain limitations.The desorption that the present invention passes through improvement rich solution Method to reduce lean solution in do not remove the content of hydrogen sulfide, so as to improve technique desulfuration efficiency.
See Fig. 2, in existing rich solution desorption technique, the overhead gas of desorber 3 enter the liquid produced after condensate cooler Mutually enter after vacuum condensation liquid bath 7, through the most of return rich solution groove 1 of condensate pump 8, enter with the rich solution at absorption tower bottom after mixing Enter the desorption again of desorber 3.Condensate cooler produce liquid be hydrogen sulfide under this operating condition saturated aqueous solution, the liquid Body returns the concentration that rich solution groove 1 not only improves hydrogen sulfide in rich solution, and forms " back-mixing " in separation, is unfavorable for hydrogen sulfide Desorption.Due to the part coolant, to contain concentration of hydrogen sulfide higher, if individually set up separating-purifying equipment not only flow process it is longer, Occupation of land is bigger than normal, and causes to be difficult to operate continuously because its total amount is on the low side, is that execute-in-place workman brings great inconvenience.This Existing process by this part cooling liquid directly return rich solution groove again air lift the reason for.
The content of the invention
The invention provides the rich solution desorption technique and equipment of a kind of vacuum carbonate desulfurization, the technique can effectively improve richness Liquid desorption efficiency, prevents from condensing the hydrogen sulfide saturated solution back-mixing of cooling, so as to improve desulfurization lean solution quality, and is finally reached Improve the purpose of desulfuration efficiency；The technique does not additionally increase while desulfuration efficiency is improved takes up an area, and facilitates operative.
In order to achieve the above object, the present invention employs the following technical solutions realization：
A kind of rich solution desorption technique of vacuum carbonate desulfurization, the technique comprises the steps：
1) the sulfur removing pregnant solution Jing rich solution pumps conveying in rich solution groove, after exchanging heat in heat exchanger with the lean solution of desorber bottom of towe, Desorbed into desorber middle part；
2) after the condensed device of gas phase of desorber top extraction, cooler A coolings, into gas-liquid separator, Jing gas-liquids point Gas phase from device goes to vacuum system, and the liquid phase being separated enters vacuum condensation liquid bath；
3) liquid in vacuum condensation liquid bath, conveys via condensate pump, and major part returns to desorber top, and fraction is defeated Deliver to treatment unit for waste water；
4) desorber bottom of towe liquid phase Jing lean pump conveying, after exchanging heat with the rich solution for entering tower, enters Jing after cooler B coolings and inhales Receive tower.
The equipment that a kind of rich solution desorption technique of vacuum carbonate desulfurization is adopted, including desorber, rich solution groove, heat exchanger, Condenser, cooler A, gas-liquid separator, vacuum condensation liquid bath, cooler B, lean pump, rich solution groove is changed by rich solution pump connection Hot device, heat exchanger rich solution outlet is connected with the entrance in the middle part of desorber；Gaseous phase outlet at the top of desorber sequentially pass through condenser, Cooler A and gas-liquid separator connection vacuum condensation liquid bath, at the top of the condensate pump connection desorber in vacuum condensation liquid bath Entrance；The liquid-phase outlet of desorption tower bottom connects heat exchanger, then Jing coolers B connections absorption tower by lean pump.
Entrance at the top of the desorber and filler is provided between the entrance at middle part, below the entrance in the middle part of desorber It is provided with filler.
Compared with prior art, the invention has the beneficial effects as follows：
A kind of rich solution desorption technique and equipment of vacuum carbonate desulfurization, the technique can effectively improve rich solution desorption efficiency, Prevent the hydrogen sulfide saturated solution for condensing cooling from directly returning rich solution groove, it is to avoid back-mixing, so as to improve desulfurization lean solution quality, and It is finally reached the purpose for improving desulfuration efficiency；Compared with existing technique, the technique does not additionally increase while desulfuration efficiency is improved Oil (gas) filling device and occupation of land, facilitate operative.
Description of the drawings
Fig. 1 is a kind of flow chart of the rich solution desorption technique of vacuum carbonate desulfurization of the invention.
Fig. 2 is the flow chart of rich solution desorption technique in prior art.
In figure：1- rich solution grooves, 2- heat exchangers, 3- desorbers, 4- condensers, 5- cooler A, 6- gas-liquid separators, 7- are true Air cooling condensate tank, 8- condensate pumps, 9- reboilers, 10- lean pumps, 11- cooler B, 12- rich solution pumps.
Specific embodiment
The specific embodiment of the present invention is described further below in conjunction with the accompanying drawings：
As shown in figure 1, a kind of rich solution desorption technique of vacuum carbonate desulfurization, the technique comprises the steps：
1) the sulfur removing pregnant solution Jing rich solution pumps 12 in rich solution groove 1 are conveyed, and are changed in heat exchanger 2 with the lean solution of the bottom of towe of desorber 3 After heat, desorbed into the middle part of desorber 3；
2) after the condensed device 4 of gas phase of the top of desorber 3 extraction, cooler A5 coolings, into gas-liquid separator 6, Jing gas The gas phase of liquid/gas separator 6 goes to vacuum system, and the liquid phase being separated enters vacuum condensation liquid bath 7；
3) liquid in vacuum condensation liquid bath 7, conveys via condensate pump 8, and major part returns to the top of desorber 3, little portion Divide and be delivered to treatment unit for waste water；
After returning the first configured filler desorption thereunder of vacuum condensation liquid at the top of desorber 3, then with enter middle part The rich solution mixing of entrance, the filler below Jing centre entrances is further desorbed, and desulfurization lean solution flows into the bottom of desorber 3.
4) the bottom of towe liquid phase Jing lean pump 10 of desorber 3 is conveyed, after exchanging heat with the rich solution for entering tower, Jing after cooler B11 coolings Into absorption tower.
The equipment that a kind of rich solution desorption technique of vacuum carbonate desulfurization is adopted, including desorber 3, rich solution groove 1, heat exchanger 2nd, condenser 4, cooler A5, gas-liquid separator 6, vacuum condensation liquid bath 7, cooler B11, lean pump 10, rich solution groove 1 is by richness Liquid pump 12 connects heat exchanger 2, and the rich solution outlet of heat exchanger 2 is connected with the entrance at the middle part of desorber 3；The gas phase at the top of desorber 3 goes out Mouth sequentially passes through condenser 4, cooler A5 and gas-liquid separator 6 connection vacuum condensation liquid bath 7, cold in vacuum condensation liquid bath 7 The entrance at the top of the connection of lime set pump 8 desorber 3；The liquid-phase outlet of the bottom of desorber 3 connects heat exchanger 2 by lean pump 10, then Jing coolers B11 connects absorption tower.
The bottom of desorber 3 is provided with self-circulation pipeline, and reboiler 9 is arranged in self-circulation pipeline, lean to the bottom of desorber 3 Liquid is heated.
Filler is provided between the entrance and the entrance at middle part at the top of the desorber 3, under the entrance at the middle part of desorber 3 Side is provided with filler.
By increasing desorber packing, individually the vacuum condensation liquid to flowing back is desorbed the present invention, it is to avoid vacuum is cold Lime set is sufficiently mixed and forms " back-mixing " with rich solution, effectively raises the acid gas concentration for finally going vacuum system, improves The desorption efficiency of desorber, reduces the hydrogen sulfide content in lean solution, is finally reached the purpose of optimization desulfurized effect.Effectively carrying Again without newly added equipment while liter desulfuration efficiency, occupation of land is not increased.

Claims (3)

1. a kind of rich solution desorption technique of vacuum carbonate desulfurization, it is characterised in that the technique comprises the steps：
1) the sulfur removing pregnant solution Jing rich solution pumps conveying in rich solution groove, after exchanging heat in heat exchanger with the lean solution of desorber bottom of towe, enters Desorber middle part is desorbed；
2) after the condensed device of gas phase of desorber top extraction, cooler A coolings, into gas-liquid separator, Jing gas-liquid separators Gas phase go to vacuum system, the liquid phase being separated enter vacuum condensation liquid bath；
Liquid in vacuum condensation liquid bath, conveys via condensate pump, and major part returns to desorber top, and fraction is delivered to useless Unit for treating water；
4) desorber bottom of towe liquid phase Jing lean pump conveying, after exchanging heat with the rich solution for entering tower, enters Jing after cooler B coolings and absorbs Tower.
2. the equipment that a kind of rich solution desorption technique of vacuum carbonate desulfurization as claimed in claim 1 is adopted, it is characterised in that Including desorber, rich solution groove, heat exchanger, condenser, cooler A, gas-liquid separator, vacuum condensation liquid bath, cooler B, lean solution Pump, rich solution groove connects heat exchanger by rich solution pump, and heat exchanger rich solution outlet is connected with the entrance in the middle part of desorber；Desorber top Gaseous phase outlet sequentially pass through condenser, cooler A and gas-liquid separator connection vacuum condensation liquid bath, in vacuum condensation liquid bath Entrance at the top of condensate pump connection desorber；The liquid-phase outlet of desorption tower bottom is cold by lean pump connection heat exchanger, then Jing But device B connects absorption tower.
3. the equipment that a kind of rich solution desorption technique of vacuum carbonate desulfurization according to claim 2 is adopted, its feature exists In, entrance at the top of the desorber and filler is provided between the entrance at middle part, is provided with below the entrance in the middle part of desorber Filler.
CN201710049681.4A 2017-01-23 2017-01-23 Rich-liquid desorption technique and device for vacuum carbonate desulfuration Pending CN106635214A (en)

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2004135579A (en) * 2002-10-17 2004-05-13 Mitsubishi Heavy Ind Ltd Biodesulfurization system for biogas
KR20130027191A (en) * 2011-09-07 2013-03-15 한국전력공사 Acidic gas capture system for treating heat stable salt
CN103555375A (en) * 2013-10-31 2014-02-05 袁磊 Coking gas secondary deep desulphurization device and coking gas secondary deep desulphurization method
CN104368232A (en) * 2014-10-22 2015-02-25 陕西华陆化工环保有限公司 Sulfuric acid tail gas recovery device
CN105112110A (en) * 2015-08-19 2015-12-02 攀钢集团西昌钢钒有限公司 Coal gas vacuum potassium carbonate desulfurization and alkali-washing apparatus and method

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2004135579A (en) * 2002-10-17 2004-05-13 Mitsubishi Heavy Ind Ltd Biodesulfurization system for biogas
KR20130027191A (en) * 2011-09-07 2013-03-15 한국전력공사 Acidic gas capture system for treating heat stable salt
CN103555375A (en) * 2013-10-31 2014-02-05 袁磊 Coking gas secondary deep desulphurization device and coking gas secondary deep desulphurization method
CN104368232A (en) * 2014-10-22 2015-02-25 陕西华陆化工环保有限公司 Sulfuric acid tail gas recovery device
CN105112110A (en) * 2015-08-19 2015-12-02 攀钢集团西昌钢钒有限公司 Coal gas vacuum potassium carbonate desulfurization and alkali-washing apparatus and method

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Title
夏征农: "《大辞海 化工轻工纺织卷》", 31 August 2009 *
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Application publication date: 20170510