CN110408443B - Biogas desulfurization system - Google Patents
Biogas desulfurization system Download PDFInfo
- Publication number
- CN110408443B CN110408443B CN201810394483.6A CN201810394483A CN110408443B CN 110408443 B CN110408443 B CN 110408443B CN 201810394483 A CN201810394483 A CN 201810394483A CN 110408443 B CN110408443 B CN 110408443B
- Authority
- CN
- China
- Prior art keywords
- solvent
- product
- tank
- storage tank
- liquid product
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
- B01D53/82—Solid phase processes with stationary reactants
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- 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
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/602—Oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
- B01D2256/245—Methane
Abstract
The invention relates to a biogas desulfurization system, comprising: a contact reaction tank having an adsorbent for absorbing hydrogen sulfide to produce a product; a first solvent storage tank having a first solvent for reacting with the product in the contact reaction tank to produce a first liquid product; a first liquid product treatment tank for receiving the first liquid product and cooling and separating the first liquid product to produce a first solvent product and a solid sulfur product, wherein the separated first solvent product can flow back to the first solvent storage tank; the solid sulfur recovery tank is used for recovering and storing the separated solid sulfur product; a second solvent storage tank for storing a second solvent for reacting with the first solvent remaining in the contact reaction tank to produce a second liquid product; and a second liquid product treatment tank, wherein a heating device is used for heating and separating the received second liquid product to generate a first solvent product and a second solvent product, the first solvent product can flow back to the first liquid product treatment tank, and the evaporated second solvent product flows back to the second solvent storage tank.
Description
Technical Field
The invention relates to the technical field of hydrogen sulfide gas removal, in particular to a biogas desulfurization system, which is a designed system for closed cycle regeneration without replacing an adsorbent by mainly performing cycle regeneration on the adsorbent so that the adsorbent can be reused.
Background
The livestock farm waste water contains bivalent sulfur poisoned matters which pollute the environment, and when livestock farmers discharge the excrement into the environment randomly, the environment is polluted and damaged. At present, the livestock farm waste water is mainly used for processing the excrement by generating electricity through biogas, although the livestock farm waste water can be converted into energy, the produced biogas contains other gases (such as hydrogen sulfide and the like) which are corrosive to metals, so the biogas must be purified by desulfurization equipment.
The main components of the biogas are methane (about 60-80%), carbon dioxide (about 20%) and other gases (including hydrogen sulfide, nitrous oxide, volatile organic acid, etc.). Methane, carbon dioxide and nitrous oxide are main greenhouse gas indexes, so if hydrogen sulfide in the methane can be removed in an economic and effective mode, the utilization of the methane can be greatly improved, the emission of greenhouse gas can be reduced, and the methane has environmental protection value.
The general treatment method for removing hydrogen sulfide from the biogas comprises the following steps: physical adsorption, water washing and biological treatment.
Physical adsorption method: the adsorbent (such as activated carbon or ferric oxide) is used for adsorbing gas components to convert pollutants from gas phase to solid phase, the effect of hydrogen sulfide adsorption of different adsorbents can reach 50-70%, but the adsorption effect is lost when the adsorption reaches saturation, the adsorbent needs to be replaced, and the problems of adsorbent recovery and regeneration and cost increase are caused.
Water washing method: the gas component in the gas phase is transferred to the liquid phase by the gas-liquid two-phase contact using a washing column. Although the absorption rate is fast, the scrubber must consume a large amount of power and washing water to maintain the repeated circulation in the scrubber, and the circulating water needs to be replaced periodically to maintain the effect of removing hydrogen sulfide in the biogas, so the cost is high, the economy is poor, and the replaced large amount of washing water must be treated before being discharged, otherwise, the environmental pollution is caused. The washing method converts the toxic gas problem of hydrogen sulfide into the problem of waste water for changing the phases of pollutants, but does not really remove the hydrogen sulfide gas.
Biological treatment method: hydrogen sulfide pollutants are decomposed and oxidized into sulfate radicals (SO) through a biological treatment system and microbial bacteria after decomposition, oxidation and conversion4 2-) Carbon dioxide (CO)2) Water (H)2O), and the like. Although the biological treatment method has the characteristic of no secondary pollution, it has no advantages in treatment performance (such as treatment time and treatment concentration), and the environmental conditions (such as humidity, acid-base (pH) value and oxygen-containing concentration) need to be controlled, thereby limiting the development.
Disclosure of Invention
The invention discloses a biogas desulfurization system, which mainly aims to: the design system can be used for circularly regenerating the adsorbent, so that the adsorbent can be repeatedly used, and the purpose of closed cyclic regeneration without replacing the adsorbent is achieved.
In order to achieve the above object, the present invention provides a biogas desulfurization system, comprising: the contact reaction tank is filled with an adsorbent and is used for absorbing hydrogen sulfide in gas to generate a product; a first solvent storage tank filled with a first solvent which can contact and react with the product in the contact reaction tank to produce a first liquid product; a first liquid product treatment tank for receiving the first liquid product generated in the contact reaction tank and cooling, filtering and separating the first liquid product to generate a first solvent product and a solid sulfur product, wherein the separated first solvent product can flow back to the first solvent storage tank for the next operation; the solid sulfur recovery tank is used for recovering and storing the separated solid sulfur product in the first liquid product treatment tank; the second solvent storage tank is filled with a second solvent, and the second solvent can contact and react with the residual first solvent in the contact reaction tank to generate a second liquid product; and the second liquid product processing tank is provided with a second heating device and is used for receiving the second liquid product generated in the contact reaction tank and carrying out heating, evaporation, filtration and separation processing through the second heating device to generate a first solvent product and a second solvent product, the separated first solvent product can flow back to the first liquid product processing tank and then is cooled, filtered and separated, and the evaporated second solvent product flows back to the second solvent storage tank and is stored for the next operation.
In the above-mentioned biogas desulfurization system of the present invention, the gas is biogas.
In the biogas desulfurization system of the present invention, the adsorbent may be one selected from iron oxide, iron oxyhydroxide, and cobalt-iron oxyhydroxide; iron oxyhydroxide has a large specific surface area due to a large number of pores having a small pore size, and thus has a higher desulfurization activity, and therefore, is preferably iron oxyhydroxide.
In the biogas desulfurization system according to the present invention, the first solvent is selected from polar solvents, preferably dipropylene glycol methyl ether.
In the above-mentioned biogas desulfurization system of the present invention, the second solvent is selected from ethanol.
In the biogas desulfurization system of the present invention, the system further comprises a delivery pump, and the delivery pump can respectively deliver the first solvent in the first solvent storage tank or the second solvent in the second solvent storage tank into the contact reaction tank to perform the first and second washing treatments with the adsorbent.
In the biogas desulfurization system of the present invention, the first solvent storage tank further comprises a first heating device for heating the first solvent, so that the first solvent can be fully mixed with the adsorbent for reaction.
In the biogas desulfurization system of the present invention, the heat source of the first heating device in the first solvent storage tank can be selected from recovered heat or electric heat, and the recovered heat is preferred because the electric heat needs to use extra electric power.
In the biogas desulfurization system of the present invention, the heat source of the second heating device in the second liquid product treatment tank can be selected from recovered heat or electric heat, and the recovered heat is preferred because the electric heat requires additional electric power.
In the biogas desulfurization system according to the present invention, the first liquid product treatment tank may be cooled, filtered and separated by natural cooling or a condenser, and natural cooling is preferred because the condenser must use additional electric power.
In the above-mentioned biogas desulfurization system of the present invention, further comprising: the gas storage tank is used for storing gas generated by anaerobic reaction and inputting the gas into the contact reaction tank so that hydrogen sulfide in the gas is absorbed by the adsorbent to carry out conversion reaction; the buffer gas storage tank is used for receiving and storing the sulfur-removing gas treated by the contact reaction tank; and the power generation device is used for receiving the gas from the buffer gas storage tank to perform combustion power generation, and tail gas generated by the combustion power generation can be provided for the first heating device of the first solvent storage tank and the second heating device of the second liquid product treatment tank to be used.
The invention relates to a biogas desulfurization system, which mainly uses an adsorbent in a contact reaction tank to adsorb hydrogen sulfide in biogas to generate a product; then washing and separating the product by a first solvent (dipropylene glycol methyl ether) so that the hydrogen sulfide is converted into solid sulfur and can be recovered; washing and separating the first solvent remained in the contact reaction tank by using a second solvent, so that the adsorbent in the contact reaction tank is recovered to the original adsorption efficiency; therefore, the adsorbent can be repeatedly used by circularly regenerating the adsorbent, and a design system of closed cyclic regeneration without replacing the adsorbent is achieved.
The methane desulfurization system has the following advantages:
firstly, the hydrogen sulfide in the biogas is reacted by using an adsorbent in a contact reaction tank to generate a product and a sulfur removal gas, when the adsorbent is saturated (the dosage of the adsorbent can be designed and used for 30 days or a detector is used for measuring the concentration value of the hydrogen sulfide), the product is washed by using a first solvent (dipropylene glycol methyl ether) to generate a first liquid product, the first liquid product is cooled and separated to generate a first solvent product and a solid sulfur product, the first solvent product can be recovered for recycling, the solid sulfur can be safely recovered, and the adsorbent in the contact reaction tank can recover the original adsorption efficiency, so that the purposes of recycling and reusing the adsorbent and not needing to be replaced are achieved.
Two or more groups of contact reaction tanks can be used in series or in parallel, when the contact reaction tanks are operated and used for 30 days, the contact reaction tanks can be washed once by using a first solvent (dipropylene glycol methyl ether), the washing time is about one day, and the washing only needs one group of electric power of a delivery pump, so that a large amount of electric power is not needed; in addition, when one group of contact reaction tanks is washed, the other group of contact reaction tanks can be used for carrying out desulfurization treatment operation without interruption. In addition, when the concentration is more than 2,000ppm, the washing frequency of the first solvent can be increased (reduced to one time of washing for 20 days or 15 days), so the invention can freely set and control the washing frequency, time and frequency, and achieve the aim of rapidly treating high-concentration hydrogen sulfide.
And thirdly, the first liquid product washed by the first reaction can be cooled and filtered by the first product treatment tank to separate a first solvent product and a solid sulfur product, the first solvent product can flow back into the first solvent storage tank to be stored for the next operation, and the solid sulfur can be safely recovered and stored, so that the cooling, filtering and separating treatment of the first product treatment tank can be completed without using any electric power.
The first solvent remained in the contact reaction tank is washed by the second solvent (ethanol), so that the adsorption efficiency of the adsorbent for adsorbing the hydrogen sulfide pollutants is recovered, the second liquid product generated by the contact reaction of the second solvent (ethanol) and the first solvent is heated and evaporated to separate the first solvent product and the second solvent product, and the heat source used for heating and evaporation separation is the heat recovered from the combustion tail gas of the combustion power generation device.
Fifthly, the invention can automatically detect the gas concentration through the controller to carry out automatic washing treatment, and can also set the washing times and time through the operation of the controller, thereby achieving the purpose of rapidly treating the high-concentration (more than 2000 ppm) hydrogen sulfide-containing H2The purpose of the S gas.
Therefore, the biogas desulfurization system can regenerate the adsorbent repeatedly, does not need to replace and treat the recovered adsorbent, has simple operation procedure, and does not need to consume a large amount of electric energy and water resources, so that the biogas desulfurization system can improve the pollution of organic wastewater discharge of animal farms (or other sewage treatment plants) to the environment, improve the utilization of biogas, and achieve the aims of resource reuse and environmental protection.
Drawings
FIG. 1 is a system diagram illustrating a first embodiment of the present invention.
FIG. 2 is a schematic diagram of a system for cooling and separating a first liquid product treatment tank by using a condenser according to a second embodiment of the present invention.
FIG. 3 is a schematic diagram of a system for returning the first solvent product separated from the second liquid product treatment tank to the first solvent storage tank according to a third embodiment of the present invention.
FIG. 4 is a schematic diagram of a system for performing desulfurization operation by using two sets of contact reaction tanks connected in series according to the present invention.
FIG. 5 is a system diagram of the first and second scrubbing operations (removal of the internally adsorbed products) performed by the first contact reactor and the desulfurization operation performed by the second contact reactor according to the present invention.
FIG. 6 is a system diagram of the second contact reactor performing the first and second scrubbing operations (to remove the internally adsorbed products) and the first contact reactor performing the desulfurization operation according to the present invention.
FIG. 7 is a schematic diagram of a system for performing desulfurization operation in parallel using two sets of contact reaction tanks according to the present invention.
Description of the symbols
10a, 10 b-contact reaction tank
11a, 11 b-adsorbents
20-first solvent storage tank
21-first heating device
30-first liquid product treatment tank
31-condenser
40-solid sulfur recovery tank
50-second solvent storage tank
60-second liquid product treatment tank
61-second heating device
70-gas storage tank
71. 72, 73, 74, 75, 76, 77, 78 control valve
80-buffer gas storage tank
90-power generation device
100-delivery pump
101. 102, 103-detector
200-control panel
201-detection line
202-control lines.
Detailed Description
The embodiments of the present invention are described below with reference to specific embodiments so that those skilled in the art can understand the advantages and effects of the present invention from the disclosure of the present specification. The invention is capable of other and different embodiments and of being practiced or of being carried out in various ways, and its several details are capable of modification in various respects, all without departing from the spirit and scope of the present invention.
The drawings in the embodiments of the invention are all simplified schematic drawings. The drawings show only those elements that are pertinent to the present invention, and the elements shown are not necessarily in the actual implementation, and the number, shape, proportion, and arrangement of the elements may be varied as desired. The following description specifically describes the operation mode of a set of contact reactors and two sets of contact reactors.
Referring to fig. 1, a system schematic diagram of a first embodiment of the present invention is shown, wherein a biogas desulfurization system comprises: a contact reaction tank 10a, a first solvent storage tank 20, a first liquid product treatment tank 30, a solid sulfur recovery tank 40, a second solvent storage tank 50, and a second liquid product treatment tank 60; wherein the contact reaction tank 10a is filled with an adsorbent 11a, the adsorbent 11a can be selected from granular or blocky iron oxide, iron oxyhydroxide and cobalt-iron oxyhydroxide, in this embodiment, cobalt-iron oxyhydroxide is used; the first solvent storage tank 20 has a first heating means 21, the second liquid product treatment tank 60 has a second heating means 61; as shown in fig. 4, the first heating device 21 uses the exhaust gas waste heat of the combustion power generation device 90 as a heat source, and the second heating device 61 also uses the exhaust gas waste heat of the combustion power generation device 90 as a heat source.
According to the invention, through the system, gas (methane containing hydrogen sulfide) is input into the contact reaction tank 10a, the hydrogen sulfide is adsorbed by the adsorbent 11a to generate a product, so that the aim of removing the hydrogen sulfide in the gas is achieved, the removal rate of the iron oxide can reach more than 95 percent, and the desulfurized gas can be output and provided for the power generation device to be combusted and generate power.
In addition, the first solvent storage tank 20 is filled with a first solvent selected from dipropylene glycol methyl ether, the first solvent storage tank 20 is provided with a first heating device 21, the first heating device 21 can heat the first solvent in the first solvent storage tank 20 to 60-70 ℃ by using the exhaust heat of the combustion power generation device as a heat source, and then the first solvent is fed into the contact reaction tank 10a by a delivery pump 100 to contact and react with the product (hydrogen sulfide is adsorbed by the adsorbent 11a to generate a product) to generate a first liquid product, and the first liquid product flows into the first liquid product treatment tank 30 again to repeatedly regenerate the adsorbent 11a in the contact reaction tank 10 a.
Then, the first liquid product flowing into the first liquid product treatment tank 30 is naturally cooled, filtered and separated at the normal temperature of 25-30 ℃ to generate a first solvent product and a solid sulfur product, the separated first solvent product can flow back into the first solvent storage tank 20 to be stored for next recycling, and the separated solid sulfur is recovered and stored in the solid sulfur recovery tank 40; therefore, the purposes of sulfur recovery and storage and repeated recovery and use of the first solvent can be achieved.
Fig. 2 shows a schematic system diagram of the first liquid product processing tank 30 according to the second embodiment of the present invention, in which the condenser 31 is disposed above the first liquid product processing tank 30, and the condenser 31 may first cool the first liquid product and then perform the filtering separation process.
When the adsorbent 11a in the contact reaction tank 10a is washed with the first solvent, a part of the first solvent, usually 5% or less, remains in the contact reaction tank 10 a; therefore, through the above system design of the present invention, the second solvent storage tank 50 is filled with the second solvent, the second solvent is ethanol, the second solvent is then fed into the contact reaction tank 10a by the delivery pump 100 to contact and react with the residual first solvent to generate the second liquid product, and the generated second liquid product flows into the second liquid product treatment tank 60, so that the residual first solvent in the contact reaction tank 10a is almost completely removed, usually the removal rate can reach more than 95% (5% of the residual internal is removed and 0.25% remains after 95%) and the adsorbent 11a can approach to the efficiency of complete regeneration, thereby providing reuse; in addition, the second liquid product flowing into the second liquid product processing tank 60 can be heated, evaporated, filtered and separated by the second heating device 61 at a temperature of 70-80 ℃ to generate a first solvent product and a second solvent product, the second solvent (ethanol) product is evaporated, separated and then returned to the second solvent storage tank 50 for storage, and is provided for the next operation; the separated first solvent product may be returned to the first liquid product treatment tank 30, and the cooling, filtering and separating treatment may be repeated again.
The separated first solvent product can also be directly returned to the first solvent storage tank 20 for storage, and then used for next operation, as shown in fig. 3, which is a schematic diagram of a system for returning the separated first solvent product from the second liquid product treatment tank 60 to the first solvent storage tank 20 in the third embodiment of the present invention shown in fig. 3.
Generally, the removal rate of the adsorbent 11a inside the contact reaction tank 10a is about 95-97%, so that other embodiments of the biogas desulfurization system of the present invention can be modified to increase the removal rate of hydrogen sulfide, such as: FIGS. 4 and 7 are schematic views illustrating a system for performing desulfurization operation in series using two sets of contact reaction tanks according to a preferred embodiment of the present invention in FIG. 4; FIG. 7 is a schematic diagram of a system for performing desulfurization operation in parallel using two sets of contact reaction tanks according to a preferred embodiment of the present invention; therefore, the present invention is not limited to the two sets of contact reactors operating in series and in parallel.
Referring to fig. 4 again, fig. 4 is a schematic view of a system for performing desulfurization operation by using two sets of contact reaction tanks connected in series according to the present invention, wherein the biogas desulfurization system of the present invention comprises: a first contact reaction tank 10a, a second contact reaction tank 10b, a first solvent storage tank 20, a first liquid product treatment tank 30, a solid sulfur recovery tank 40, a second solvent storage tank 50, a second liquid product treatment tank 60, a gas storage tank 70, a buffer gas storage tank 80, and a power generation device 90; wherein the first contact reaction tank 10a is filled with an adsorbent 11a, and the adsorbent 11a is selected from granular iron oxyhydroxide; the second contact reaction tank 10b is filled with an adsorbent 11b, and the adsorbent 11b is also selected from granular iron oxyhydroxide; the first solvent storage tank 20 is provided with a first heating device 21, the first solvent is filled in the first solvent, dipropylene glycol methyl ether is used as the first solvent, and the first heating device 21 can receive the waste heat of the tail gas generated by the combustion of the power generation device 90 as a heat source; the second solvent storage tank 50 is filled with a second solvent, and ethanol is used as the second solvent; the second liquid product treating tank 60 is provided with a second heating device 61, and the second heating device 61 can receive the waste heat of the tail gas generated by the combustion of the power generation device 90 as a heat source.
The process steps of the system operation of the present invention are as follows, wherein:
step 1-3: FIG. 4 is a schematic diagram of a system for performing desulfurization operation by using two sets of contact reaction tanks connected in series according to the present invention.
Step 4-6: FIG. 5 is a schematic diagram of a system in which a first contact reaction tank 10a performs a first washing operation and a second washing operation (removing internal adsorbed products), and a second contact reaction tank 10b performs a desulfurization operation according to the present invention; FIG. 6 is a system diagram illustrating the first and second washing operations (removing the adsorbed products inside) performed by the second contact reaction tank 10b and the desulfurization performed by the first contact reaction tank 10a according to the present invention.
Step 1: as shown in fig. 4, the gas storage tank 70 receives and stores the gas generated from the anaerobic reaction, and the gas can enter the interior of the first contact reaction tank 10a through opening the control valve 71 to contact with the adsorbent 11a to react to generate a product and a gas, wherein the product is adsorbed on the adsorbent 11a, and the gas can be discharged out of the first contact reaction tank 10 a; the system can be provided with a detector 101 at the front end of the control valve 71 at the inlet end of the first contact reaction tank 10a, and can provide a detection port for measuring the concentration of hydrogen sulfide contained in the input gas, and the detector 101 can also be provided with a detection port for manual sampling.
Step 2: as shown in fig. 4, the gas discharged from the first contact reaction tank 10a enters the second contact reaction tank 10b through the open control valves 73 and 72 to contact with the adsorbent 11b for reaction to generate a product and a gas, wherein the product is adsorbed on the adsorbent 11b, and the gas can be discharged from the second contact reaction tank 10 b; the front end of the control valve 73 of the first contact reaction tank 10a is provided with a detector 102 for measuring the concentration of hydrogen sulfide contained in the gas output from the first contact reaction tank 10 a.
And step 3: as shown in fig. 4, the gas discharged from the second contact reaction tank 10b is stored in a buffer gas storage tank 80 by opening a control valve 74, the gas stored in the buffer gas storage tank 80 enters the power generation device 90 through the opening control valve 75 to provide combustion power generation, the waste heat of the tail gas generated by the power generation device 90 through combustion power generation can enter the first heating device 21 of the first solvent storage tank 20 and the second heating device 61 of the second liquid product treatment tank 60 through the opening control valves 77 and 78, the first heating device 21 can heat the first solvent in the first solvent storage tank 20 to a preferred operation temperature (about 60-70 ℃), the second heating means 61 can heat the second liquid product (about 70 to 80 ℃) which has flowed into the second liquid product treating tank 60, the front end of the control valve 74 of the second contact reaction tank 10b is provided with a detector 103 for measuring the concentration of hydrogen sulfide contained in the output gas of the second contact reaction tank 10 b.
And 4, step 4: as shown in fig. 5, when the first contact reaction tank 10a is operated for 30 days or when the detector 102 measures that the concentration of hydrogen sulfide in the output gas is too high, the control valve 71 is closed, and the control valve 72 is opened separately, so that the gas in the gas storage tank 70 enters the second contact reaction tank 10b through the control valve 72, and the desulfurization operation is performed separately in the second contact reaction tank 10 b.
And 5: in the first washing operation of the first contact reaction tank 10a, as shown in fig. 5, the first solvent in the first solvent storage tank 20 is heated to a preferred operation temperature (about 60-70 ℃), the first solvent (dipropylene glycol methyl ether) is conveyed into the first contact reaction tank 10a by the conveying pump 100 to contact and react with the product adsorbed on the adsorbent 11a to generate a first liquid product, the first liquid product can flow into the first liquid product treatment tank 30, and the first liquid product is precipitated and filtered by a natural cooling method to separate a first solvent product (dipropylene glycol methyl ether) and a solid sulfur product, the solid sulfur product can be recovered and stored in the solid sulfur collection tank 40, and the first solvent product (dipropylene glycol methyl ether) can flow back into the first solvent storage tank 20 to be stored for the next operation.
Step 6: a second washing operation of the first contact reaction tank 10a, as shown in fig. 5, the second solvent (ethanol) stored in the second solvent storage tank 50 is conveyed into the first contact reaction tank 10a by the conveying pump 100 to contact and react with the first solvent remaining from the first washing operation to generate a second liquid product, and the second liquid product flows into the second liquid product treatment tank 60, and then the second liquid product is heated by the second heating device 61 to evaporate and separate the first solvent product (dipropylene glycol methyl ether) and the second solvent product (ethanol), wherein the second solvent product (ethanol) is evaporated and separated to flow back into the second solvent storage tank 50 to be cooled to normal temperature (about 30 ℃) for storage, so as to provide for the next operation; the separated first solvent product (dipropylene glycol methyl ether) may be returned to the first liquid product-treating tank 30 and again subjected to cooling, precipitation, filtration and separation treatment
Referring again to FIG. 6, a system diagram of the first and second scrubbing operations (removal of the adsorbed products) performed by the second contact reactor 10b and the desulfurization performed by the first contact reactor 10a according to the present invention is shown.
Referring again to FIG. 7, a schematic diagram of a system for performing desulfurization using two sets of contact reactors 10a, 10b in parallel according to the present invention is shown. In the figure, the system can close the control valve 73, separately open the control valves 71 and 72, and then the gas in the gas storage tank 70 is simultaneously fed into the first contact reaction tank 10a and the second contact reaction tank 10b through the control valves 71 and 72, and simultaneously desulfurized in the first contact reaction tank 10a and the second contact reaction tank 10b, the gas treated in the first contact reaction tank 10a can be output by opening the control valve 76, and the gas treated in the second contact reaction tank 10b can be output by opening the control valve 74 and fed into the buffer gas storage tank 80 for storage, and the gas stored in the buffer gas storage tank 80 can be fed into the power generation device 90 through opening the control valve 75 for combustion power generation. In addition, the operation of the system for performing the first and second washing operations of the desulfurization operation in parallel of FIG. 7 is the same as that of the series connection of FIG. 4.
In the above embodiments, when the system is implemented in series, when the detector at the gas outlet of the first set of contact reaction tanks detects that the concentration of hydrogen sulfide is too high, the second contact reaction tank may be opened for desulfurization, and if the concentration detected by the second contact reaction tank does not meet the emission standard or the set standard, the third contact reaction tank may be opened for desulfurization, and so on, until the concentration of hydrogen sulfide in the treated gas meets the set (emission) standard, the gas may be stored in the buffer gas storage tank and then supplied to the power generation device for combustion and power generation.
As illustrated in the above embodiments and examples, the biogas desulfurization system of the present invention can effectively reduce the concentration of hydrogen sulfide in biogas, convert the removed sulfur into solid sulfur and safely recover the solid sulfur, and can recycle and regenerate the adsorbent, so that the adsorbent can be reused, and the adsorbent does not need to be replaced and recovered.
Claims (10)
1. A biogas desulfurization system, comprising: a contact reaction tank filled with an adsorbent for absorbing hydrogen sulfide in the gas to produce a product; a first solvent storage tank filled with a first solvent which can contact and react with the product in the contact reaction tank to produce a first liquid product; a first liquid product treatment tank for receiving the first liquid product generated in the contact reaction tank and cooling, filtering and separating the first liquid product to generate a first solvent product and a solid sulfur product, wherein the separated first solvent product can flow back to the first solvent storage tank for the next operation; the solid sulfur recovery tank is used for recovering and storing the separated solid sulfur product in the first liquid product treatment tank; a second solvent storage tank filled with a second solvent, wherein the second solvent can contact and react with the residual first solvent in the contact reaction tank to generate a second liquid product; and the second liquid product processing tank is provided with a heating device and is used for receiving the second liquid product generated in the contact reaction tank, heating, evaporating, filtering and separating the second liquid product by the heating device to generate a first solvent product and a second solvent product, the separated first solvent product can flow back to the first liquid product processing tank and then is cooled, filtered and separated, and the evaporated second solvent product flows back to the second solvent storage tank and is stored for the next operation.
2. The biogas desulfurization system of claim 1, wherein the adsorbent is selected from one of iron oxide, iron oxyhydroxide, and cobalt-iron oxyhydroxide.
3. The biogas desulfurization system according to claim 1, wherein the first solvent is selected from dipropylene glycol methyl ether.
4. Biogas desulphurisation system according to claim 1 wherein the second solvent is selected from ethanol.
5. The biogas desulfurization system according to claim 1, further comprising a transfer pump for transferring the first solvent in the first solvent storage tank and the second solvent in the second solvent storage tank into the contact reaction tank.
6. The biogas desulfurization system of claim 1, wherein the first solvent storage tank further comprises a heating device.
7. The biogas desulfurization system according to claim 1, wherein the cooling, filtering and separating process of the first liquid product treatment tank is one of natural cooling and condenser cooling.
8. The biogas desulfurization system of claim 1, further comprising: the gas storage tank is used for storing gas generated by anaerobic reaction and inputting the gas into the contact reaction tank so that hydrogen sulfide in the gas is absorbed by the adsorbent to carry out conversion reaction; the buffer gas storage tank is used for receiving and storing the sulfur-removing gas treated by the contact reaction tank; and the power generation device is used for receiving the gas from the buffer gas storage tank to perform combustion power generation, and the tail gas generated by the combustion power generation can be provided for the heating device of the first solvent storage tank and the heating device of the second liquid product treatment tank to be used.
9. The biogas desulfurization system according to claim 1, wherein the gas inlet and outlet of the contact reaction tank are provided with detectors.
10. The biogas desulfurization system according to any one of claims 1 to 9, further comprising a control panel for controlling the operation of the contact reaction tank, the first solvent storage tank, the heating device, the first liquid treatment tank, the second solvent storage tank, the second liquid product treatment tank, the heating device, the gas storage tank, the buffer gas storage tank and the power generation device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810394483.6A CN110408443B (en) | 2018-04-27 | 2018-04-27 | Biogas desulfurization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810394483.6A CN110408443B (en) | 2018-04-27 | 2018-04-27 | Biogas desulfurization system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110408443A CN110408443A (en) | 2019-11-05 |
| CN110408443B true CN110408443B (en) | 2021-06-04 |
Family
ID=68346742
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810394483.6A Expired - Fee Related CN110408443B (en) | 2018-04-27 | 2018-04-27 | Biogas desulfurization system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110408443B (en) |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8323603B2 (en) * | 2004-09-01 | 2012-12-04 | Sud-Chemie Inc. | Desulfurization system and method for desulfurizing a fuel stream |
| CN101224999B (en) * | 2008-01-16 | 2010-10-27 | 宝林 | Anaerobic digestion handling method for restaurant garbage |
| CN101327396A (en) * | 2008-07-31 | 2008-12-24 | 深圳市龙澄高科技环保有限公司 | Method and device for removing hydrogen sulfide from gas containing hydrogen sulfide and recovering sulfer using catalytic oxidation |
| CA2709722A1 (en) * | 2010-07-15 | 2012-01-15 | Alakh Prasad | Integrated biogas cleaning a system to remove water, siloxanes, sulfur, oxygen, chlorides, and volatile organic compounds |
| CN202430217U (en) * | 2012-01-04 | 2012-09-12 | 逢甲大学 | Reaction chamber for generation of hydrogen or mathane |
| CN103320193B (en) * | 2013-07-05 | 2015-03-25 | 苏州苏净保护气氛有限公司 | Device and method for manufacturing high quality natural gas by purifying methane |
| KR101728809B1 (en) * | 2014-09-25 | 2017-04-21 | 한국화학연구원 | Nanoporous inorganic-organic hybrid materials with nitrogen sorption selectivity and a method for selective separation of nitrogen-containing gas mixtures using the same |
| CN207760298U (en) * | 2018-01-24 | 2018-08-24 | 青岛利德恒业机械有限公司 | A kind of methane desulfurizing tank |
-
2018
- 2018-04-27 CN CN201810394483.6A patent/CN110408443B/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN110408443A (en) | 2019-11-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR100985911B1 (en) | System for preprocessing of bio-gas | |
| CN106430244B (en) | A method of it is recycled from ammonia nitrogen waste water and purifies ammonia | |
| CN203853005U (en) | VOCs (Volatile Organic Compounds) waste gas purification device | |
| KR101207532B1 (en) | Apparatus for performing drying and removing impurities process of bio-methane at high purity bio-methane purification system | |
| JP2011523671A (en) | Biogas purification method and system for methane extraction | |
| CN102814103B (en) | Four-stage sludge drying tail gas treatment system | |
| KR101427599B1 (en) | The purification method and the purification device refining as low density bio-methane | |
| CN111151094A (en) | Regeneration and purification method for organic polluted waste gas | |
| CN102688671B (en) | Synthesis method for removing nitric oxide in flue gas | |
| CN109078459A (en) | A kind of device and technology of absorption-adsorption-desorption cycle resource utilization volatile organic gases | |
| CN206730825U (en) | A kind of system for handling foul gas | |
| CN205613263U (en) | Reation kettle tail gas processing apparatus | |
| CN208449008U (en) | A kind of combined type organic waste-gas purification and recyclable device | |
| CN201482379U (en) | High-efficiency combined type foul smell and VOC waste gas treatment device | |
| CN107670478A (en) | A kind of waste water station waste gas treatment process | |
| CN103145244A (en) | Synergistic biological treatment method for washing waste water and amine salt waste liquor produced by capturing CO2 in smoke of coal-fired power plant | |
| CN110408443B (en) | Biogas desulfurization system | |
| CN202751933U (en) | Four-section type sludge drying off-gas treatment system | |
| TWI701076B (en) | Biogas desulfurization system | |
| CN103230737A (en) | Device and process for performing purification treatment on stinky tail gas in waste water of gas production | |
| CN107174922A (en) | A kind of closed waste gas circulation processing system of air film | |
| CN209885520U (en) | Organic waste gas treatment device | |
| CN205073862U (en) | VOCs exhaust treatment device | |
| CN212790409U (en) | Waste gas treatment device for coal chemical industry sewage treatment | |
| CN212309611U (en) | Saturated activated carbon regeneration treatment device for absorbing VOCs gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20210604 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |