阅读说明：本技术 一种煤气化制合成气脱硫的装置和方法 (Device and method for desulfurizing synthesis gas prepared by coal gasification ) 是由 郝代军 沈方峡 李欣 任潇航 俞安平 刘林娇 李静静 魏小波 李治 刘丹禾 于 2019-10-08 设计创作，主要内容包括：本发明提供了一种煤气化制合成气脱硫的装置和方法,所述煤气化制合成气脱硫的装置,能够实现合成气干法脱硫的连续化,克服了固定床干法脱硫周期性运行的缺点；能够实现合成气干法脱硫更宽的温度范围,克服了湿法脱硫只能在低温、常温运行的缺点。本发明所提供的煤气化制合成气脱硫的方法,工艺过程简单,工艺操作条件范围广,建设投资少,操作费用低。(The invention provides a device and a method for desulfurizing synthesis gas prepared by coal gasification, wherein the device for desulfurizing synthesis gas prepared by coal gasification can realize the continuity of dry desulfurization of synthesis gas and overcome the defect of periodic operation of the dry desulfurization of a fixed bed; the method can realize wider temperature range of the dry desulphurization of the synthesis gas and overcome the defect that the wet desulphurization can only be operated at low temperature and normal temperature. The method for desulfurizing the synthesis gas prepared by coal gasification has the advantages of simple process, wide range of process operation conditions, less construction investment and low operation cost.)

1. An apparatus for desulfurizing a synthesis gas produced by coal gasification, comprising: a fluidized bed adsorption reactor, a spent desulfurizer stripper, a spent desulfurizer regeneration reactor and a regenerated desulfurizer stripper;

the fluidized bed adsorption reactor is connected with the to-be-generated desulfurizer stripper;

the spent desulfurizer stripper is connected with the spent desulfurizer regeneration reactor through a spent desulfurizer circulating pipeline;

the to-be-regenerated desulfurizer regeneration reactor is connected with the regenerated desulfurizer stripper;

the regenerated desulfurizer stripper is connected with the fluidized bed adsorption reactor through a regenerated desulfurizer circulating pipeline.

2. The apparatus for desulfurizing coal gasification syngas according to claim 1, wherein the fluidized bed adsorption reactor is further configured to comprise: a syngas inlet and a syngas outlet.

3. The apparatus for desulfurizing coal gasification syngas according to claim 1, wherein the fluidized bed adsorption reactor further comprises: reactor cyclones and syngas feed distributors.

4. The device for desulfurizing coal gasification syngas according to claim 1, wherein the to-be-generated desulfurizing agent stripper further comprises: a first stripping steam distributor and a first stripping steam inlet.

5. The device for desulfurizing coal gasification syngas according to claim 1, wherein the to-be-generated desulfurizing agent regeneration reactor further comprises: a regenerator cyclone and a flue gas outlet.

6. The device for desulfurizing coal gasification syngas according to claim 1, wherein the to-be-generated desulfurizing agent regeneration reactor further comprises: a regeneration gas distributor and a regeneration gas inlet.

7. The apparatus for desulfurizing coal gasification syngas according to claim 1, wherein the regenerated desulfurizer stripper is further configured to comprise: a second stripping steam distributor and a second stripping steam inlet.

8. The apparatus for desulfurizing coal gasification syngas according to claim 1, wherein the apparatus comprises a cooler, and the cooler is disposed inside or outside the to-be-generated desulfurizing agent regeneration reactor.

9. A method for desulfurizing coal gasification synthesis gas, which is applied to the apparatus for desulfurizing coal gasification synthesis gas according to any one of claims 1 to 8, comprising the steps of:

the synthesis gas prepared by coal gasification enters a fluidized bed adsorption reactor to perform desulfurization adsorption reaction with a desulfurizing agent to obtain a desulfurizing agent to be generated and desulfurized synthesis gas, and the desulfurizing agent to be generated is subjected to steam stripping and then is subjected to desulfurizing agent regeneration reaction with regeneration gas to obtain a regenerated desulfurizing agent and SO₂The regenerated desulfurizer is returned to the fluidized bed adsorption reactor after being stripped and continues to react with the undesulfurized gasCarrying out desulfurization reaction on the prepared synthesis gas;

preferably, the temperature of the desulfurization adsorption reactor is 25-600 ℃, more preferably 250-500 ℃;

preferably, the gauge pressure of the fluidized bed adsorption reactor is 0-8MPa, more preferably 0-2 MPa;

preferably, the volume space velocity of the synthesis gas prepared by coal gasification is 100-^-1More preferably 1000-^-1；

Preferably, the coal is gasified to produce H in the synthesis gas₂S content of 50-5000mg/m³More preferably 1000-2000mg/m³；

Preferably, the temperature of the desulfurizing agent regeneration reaction is 400-700 ℃, and more preferably 500-600 ℃;

preferably, the gauge pressure of the desulfurizing agent regeneration reaction is 0-8MPa, and more preferably 0-2 MPa.

10. The method for desulfurizing coal gasification syngas according to claim 9, wherein the desulfurizing agent comprises a metal oxide based desulfurizing agent;

preferably, the regeneration gas is an oxygen-containing gas, more preferably, the regeneration gas is selected from oxygen and/or air.

Technical Field

The invention relates to the technical field of desulfurization, in particular to a device and a method for desulfurizing synthesis gas prepared by coal gasification.

Background

The synthesis gas (containing fuel gas) prepared by coal gasification is the basis of novel coal chemical industry, is mainly used for synthesizing ammonia in the prior art, is mainly used for producing methanol, glycol, natural gas, special oil products and the like at present, and is also used for synthesizing fine chemicals.

The sulfur-containing compounds in the synthesis gas produced by coal gasification not only can cause corrosion of production equipment and pipelines and influence production safety, but also can cause poisoning and inactivation on the catalyst of subsequent chemical reaction and directly influence the yield and quality of the final product. The sulfur-containing compounds in the synthesis gas are removed, so that the safety production can be improved, the subsequent reaction efficiency can be guaranteed, and important sulfur resources can be recovered from the sulfur-containing compounds.

The coal gasification synthesis gas desulfurization mainly comprises two modes of wet desulfurization and dry desulfurization. The wet desulfurization comprises three processes of chemical absorption, physical absorption and physical and chemical absorption, and has the advantages that the desulfurizer can be continuously circulated for desulfurization and regeneration, is suitable for large-scale production and can recover sulfur. The wet desulphurization has the disadvantages that the wet desulphurization is generally used in the normal-temperature and low-temperature desulphurization process, and the operation energy consumption is too high for medium-temperature or high-temperature synthesis gas. The dry desulfurization includes adsorption reaction methods such as zinc oxide, iron oxide, manganese oxide, activated carbon method and the like, and particularly, the zinc oxide desulfurization is the most extensive. Dry desulfurization has many advantages of both inorganic sulfur removal and organic sulfur removal, both high temperature desulfurization and low temperature desulfurization, and high desulfurization accuracy, but dry desulfurization cannot be recycled, can only be periodically operated, and is not suitable for removing a large amount of sulfides.

In view of the above, the present invention is particularly proposed.

Disclosure of Invention

The first purpose of the invention is to provide a device for desulfurizing synthesis gas by coal gasification, which is used for solving the problems that a desulfurizing agent can not be regenerated circularly and the technological process can not be operated continuously in the prior fixed bed dry desulfurization technology, wherein the device comprises a fluidized bed adsorption reactor, a desulfurizing agent stripper to be generated, a desulfurizing agent regeneration reactor to be generated and a desulfurizing agent regeneration stripper, can realize the continuity of the dry desulfurization of the synthesis gas and overcomes the defect of the periodic operation of the dry desulfurization of the fixed bed; meanwhile, the wider temperature range of the synthesis gas dry desulphurization can be realized, and the defect that the wet desulphurization can only be operated at low temperature and normal temperature is overcome.

The second purpose of the invention is to provide the method for desulfurizing the coal gasification synthesis gas, which has the advantages of simple process, wide range of process operation conditions, less construction investment and low operation cost.

In order to achieve the above purpose of the present invention, the following technical solutions are adopted:

an apparatus for desulfurizing a synthesis gas produced by coal gasification, comprising: a fluidized bed adsorption reactor, a spent desulfurizer stripper, a spent desulfurizer regeneration reactor and a regenerated desulfurizer stripper;

the fluidized bed adsorption reactor is connected with the to-be-generated desulfurizer stripper;

the spent desulfurizer stripper is connected with the spent desulfurizer regeneration reactor through a spent desulfurizer circulating pipeline;

the to-be-regenerated desulfurizer regeneration reactor is connected with the regenerated desulfurizer stripper;

the regenerated desulfurizer stripper is connected with the fluidized bed adsorption reactor through a regenerated desulfurizer circulating pipeline.

Preferably, the fluidized bed adsorption reactor is further provided with: a syngas inlet and a syngas outlet.

Preferably, the fluidized bed adsorption reactor is further provided with: reactor cyclones and syngas feed distributors.

Preferably, the spent desulfurizer stripper further comprises: a first stripping steam distributor and a first stripping steam inlet.

Preferably, the spent desulfurizer regeneration reactor further comprises: a regenerator cyclone and a flue gas outlet.

Preferably, the spent desulfurizer regeneration reactor further comprises: a regeneration gas distributor and a regeneration gas inlet.

Preferably, the regenerated desulfurizer stripper is further provided with: a second stripping steam distributor and a second stripping steam inlet.

Preferably, the device comprises a cooler, and the cooler is arranged inside or outside the to-be-generated desulfurizer regeneration reactor.

The method for desulfurizing the coal gasification synthesis gas is suitable for the device for desulfurizing the coal gasification synthesis gas, and comprises the following steps of:

the synthesis gas prepared by coal gasification enters a fluidized bed adsorption reactor to perform desulfurization adsorption reaction with a desulfurizing agent to obtain a desulfurizing agent to be generated and desulfurized synthesis gas, and the desulfurizing agent to be generated is subjected to steam stripping and then is subjected to desulfurizing agent regeneration reaction with regeneration gas to obtain a regenerated desulfurizing agent and SO₂And after steam stripping, the regenerated desulfurizer returns to the fluidized bed adsorption reactor to continue to perform desulfurization reaction with the synthesis gas prepared by coal gasification without desulfurization.

Preferably, the temperature of the desulfurization adsorption reactor is 25-600 ℃, more preferably 250-500 ℃.

Preferably, the fluidized bed adsorption reactor has a gauge pressure of 0 to 8MPa, more preferably 0 to 2 MPa.

Preferably, the volume space velocity of the synthesis gas prepared by coal gasification is 100-^-1More preferably 1000-^-1。

Preferably, the coal is gasified to produce H in the synthesis gas₂S content of 50-5000mg/m³More preferably 1000-2000mg/m³。

Preferably, the temperature of the desulfurizing agent regeneration reaction is 400-700 ℃, and more preferably 500-600 ℃.

Preferably, the gauge pressure of the desulfurizing agent regeneration reaction is 0-8MPa, and more preferably 0-2 MPa.

Preferably, the desulfurizing agent comprises a metal oxide-based desulfurizing agent.

Preferably, the regeneration gas is an oxygen-containing gas, more preferably, the regeneration gas is selected from oxygen and/or air.

Compared with the prior art, the invention has the beneficial effects that:

(1) the device for desulfurizing the synthesis gas by coal gasification provided by the invention can realize the continuity of the dry desulfurization of the synthesis gas and overcome the defect of periodic operation of the fixed bed dry desulfurization.

(2) The device for desulfurizing the synthesis gas prepared by coal gasification can realize wider temperature range of dry desulfurization of the synthesis gas and overcome the defect that wet desulfurization can only operate at low temperature and normal temperature.

(3) The method for desulfurizing the synthesis gas prepared by coal gasification has the advantages of simple process, wide range of process operation conditions, low construction investment and low operation cost.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.

Fig. 1 is a schematic connection diagram of an apparatus according to an embodiment of the present invention.

Reference numerals:

1-a syngas inlet; 2-syngas feed distributor; 3-a fluidized bed adsorption reactor;

4-cyclone separation of the reactor 5-outlet of the synthesis gas; 6-spent desulfurizer stripper;

separating from the device;

7-stripping steam distribution 8-first stripping steam inlet; 9-spent desulfurizing agent circulating pipe

A machine; a lane;

10-regeneration of a desulfurizer to be regenerated 11-a cyclone separator of a regenerator; 12-a flue gas outlet;

a raw reactor;

13-a cooler; 14-a regeneration gas distributor; 15-a regeneration gas inlet;

16-regenerated desulfurizer steam 17-steam stripping steam distributor; 18-second stripping steam in

Lifting a device; a mouth;

19-regeneration of the desulfurization agent cycle

And (4) surrounding the pipeline.

Detailed Description

The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings and the detailed description, but those skilled in the art will understand that the following described embodiments are some, not all, of the embodiments of the present invention, and are only used for illustrating the present invention, and should not be construed as limiting the scope of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.

In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.

In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.

The invention provides a device for desulfurizing synthesis gas produced by coal gasification, which comprises: a fluidized bed adsorption reactor 3, a spent desulfurizer stripper 6, a spent desulfurizer regeneration reactor 10 and a regenerated desulfurizer stripper 16;

the fluidized bed adsorption reactor 3 is connected with the to-be-generated desulfurizer stripper 6;

the spent desulfurizer stripper 6 is connected with the spent desulfurizer regeneration reactor 10 through a spent desulfurizer circulating pipeline 9;

the to-be-regenerated desulfurizer regeneration reactor 10 is connected with the regenerated desulfurizer stripper 16;

the regenerated desulfurizer stripper 16 is connected with the fluidized bed adsorption reactor 3 through a regenerated desulfurizer circulating pipeline 19.

The device for desulfurizing the synthesis gas by coal gasification provided by the invention can realize the continuity of the dry desulfurization of the synthesis gas and overcome the defect of periodic operation of the fixed bed dry desulfurization. The method can realize wider temperature range of the dry desulphurization of the synthesis gas and overcome the defect that the wet desulphurization can only be operated at low temperature and normal temperature.

In some preferred embodiments of the present invention, the fluidized bed adsorption reactor 3 is further configured to include: a syngas inlet 1 and a syngas outlet 5.

In some preferred embodiments of the present invention, the fluidized bed adsorption reactor 3 further comprises: a reactor cyclone 4 and a syngas feed distributor 2.

In some preferred embodiments of the present invention, the spent desulfurizer stripper 6 is further configured to include: a first stripping steam distributor 7 and a first stripping steam inlet 8.

In some preferred embodiments of the present invention, the spent desulfurizer regeneration reactor 10 is further configured to include: the regenerator cyclone separator 11 and the flue gas outlet 12, and the other rich sulfur dioxide is discharged from the flue gas outlet 12 and recovered to prepare sulfur.

In some preferred embodiments of the present invention, the spent desulfurizer regeneration reactor 10 is further configured to include: a regeneration gas distributor 14 and a regeneration gas inlet 15.

In some preferred embodiments of the present invention, the apparatus includes a cooler 13, and the cooler 13 is disposed inside or outside the to-be-generated desulfurizing agent regeneration reactor 10.

In some preferred embodiments of the present invention, the spent desulfurizer regeneration reactor 10 is further provided with a cooler 13, and the cooler 13 is disposed inside or outside the spent desulfurizer regeneration reactor 10.

In order to take out the excess heat, the desulfurizer regeneration reactor 10 to be regenerated is further provided with a cooler 13, the cooler 13 can be an internal heat collector arranged inside the regeneration reactor or an external heat collector arranged outside the regenerator, and the heat-taking medium is usually water, nitrogen, heat-conducting oil and the like, and preferably water is used as the heat-taking medium.

In the process of using the device provided by the present application, please refer to fig. 1, the synthesis gas produced by coal gasification enters the dense phase region of desulfurizing agent of fluidized bed adsorption reactor 3 from synthesis gas inlet 1 through synthesis gas feeding distributor 2 from the outside of the device, and H in the crude synthesis gas in the dense phase region₂S and the metal oxide on the desulfurizer are subjected to adsorption reaction, so that the aim of desulfurizing the synthesis gas is fulfilled, and the equation is MO + H₂S→MS+H₂O (MO: represents a metal oxide contained in the desulfurizing agent). The desulfurized synthesis gas is in a fluidized bed adsorption reactor 3The purified synthesis gas is separated from desulfurizer particles in the dilute phase zone of the desulfurizer by a reactor cyclone separator 4, and the purified synthesis gas is sent to a downstream device through a synthesis gas outlet 5.

In the fluidized bed adsorption reactor 3, with H₂And after the desulfurization activity of the desulfurizer is lost after the S reaction, the desulfurizer enters a to-be-generated desulfurizer stripper 6, and steam or nitrogen passes through a first stripping steam distributor 7 from a first stripping steam inlet 8 and then is stripped, so that trace synthesis gas carried by the to-be-generated desulfurizer is removed.

The stripped desulfurizer to be generated is conveyed to a dense phase region of a desulfurizer regeneration reactor 10 through a desulfurizer circulation pipeline 9, and in the dense phase region of the regenerator, the desulfurizer to be generated reacts with regeneration gas (air and/or oxygen) from a regeneration gas distributor 14 to burn sulfide on the desulfurizer to be generated, so that the desulfurization activity of the desulfurizer is recovered. The equation is MS + O₂→MO+SO₂(MS: represents a metal sulfide contained in the desulfurizing agent).

The combustion gas in the regenerator is enriched in SO by the regenerator cyclone 11₂The flue gas is separated from the desulfurizer particles, and the flue gas is sent to a downstream sulfur device through a flue gas outlet 12 to prepare sulfur and recover resources.

The regenerated desulfurizer with recovered activity enters a regenerated desulfurizer stripper 16, and steam or nitrogen passes through a second steam stripping steam distributor 17 from a second steam stripping steam inlet 18 to strip the regenerated desulfurizer, so that trace oxygen-containing gas carried by the regenerated desulfurizer is removed. The stripped regenerated desulfurizer is conveyed to a dense phase region of the fluidized bed adsorption reactor 3 through a regenerated desulfurizer circulating pipeline 19 and is re-mixed with H in the undesulfurized synthesis gas₂S adsorption reaction and desulfurization.

The regeneration reaction of the spent desulfurizer in the spent desulfurizer regeneration reactor 10 is an exothermic process, and in order to take out excess heat, a cooler 13 is arranged on the spent desulfurizer regeneration reactor 10, the cooler 13 can be an internal heat collector arranged inside the spent desulfurizer regeneration reactor 10 or an external heat collector arranged outside the spent desulfurizer regeneration reactor 10, the heat-taking medium is usually water, nitrogen, heat-conducting oil and the like, and preferably water is used as the heat-taking medium.

The invention provides a method for desulfurizing synthesis gas prepared by coal gasification, which comprises the following steps:

the synthesis gas prepared by coal gasification enters a fluidized bed adsorption reactor 3 to perform desulfurization adsorption reaction with a desulfurizing agent to obtain a desulfurizing agent to be generated and the synthesis gas after desulfurization, and the desulfurizing agent to be generated is subjected to steam stripping and then performs desulfurizing agent regeneration reaction with a regeneration gas to obtain a regenerated desulfurizing agent and SO₂And after steam stripping, the regenerated desulfurizer returns to the fluidized bed adsorption reactor 3 to continue to perform desulfurization reaction with the synthesis gas prepared by coal gasification without desulfurization.

In some preferred embodiments of the present invention, the temperature of the desulfurization adsorption reactor is in a wide range, and may be normal temperature or high temperature, and the temperature is 25-600 ℃, more preferably 250-500 ℃.

In some preferred embodiments of the present invention, the fluidized bed adsorption reactor 3 has a wide range of pressure (gauge pressure) from 0 to 8MPa, more preferably from 0 to 2 MPa.

In some preferred embodiments of the invention, the volume space velocity of the coal gasification synthesis gas is 100-^-1More preferably 1000-^-1。

In some preferred embodiments of the invention, the coal is gasified to produce H in the synthesis gas₂S content of 50-5000mg/m³More preferably 1000-2000mg/m³。

In some preferred embodiments of the present invention, the temperature of the desulfurization agent regeneration reaction is 400-700 ℃, more preferably 500-600 ℃.

In some preferred embodiments of the present invention, the pressure (gauge pressure) of the desulfurizing agent regeneration reaction is 0 to 8MPa, more preferably 0 to 2 MPa.

In some preferred embodiments of the present invention, the desulfurizing agent is selected from metal oxide desulfurizing agents.

In some preferred embodiments of the present invention, the regeneration gas is an oxygen-containing gas, and more preferably, the regeneration gas is selected from oxygen and/or air.

Further, the metal oxide desulfurizer comprises the following components in parts by mass:

30-80 parts of zinc oxide, 5-20 parts of one or more of manganese oxide, iron oxide, cobalt oxide, copper oxide and gallium oxide, 1-5 parts of phosphorus pentoxide and 20-40 parts of aluminum oxide.

In the desulfurizer, the zinc oxide-based desulfurizer has high desulfurization precision and large sulfur capacity; the zinc oxide-based desulfurizer is modified by metal and phosphorus, and the activity attenuation of the desulfurizer is not obvious after the desulfurizer is regenerated for multiple times, and the zinc oxide-based desulfurizer is particularly suitable for desulfurizing synthesis gas with high water vapor content so as to keep the desulfurization activity of the desulfurizer; the zinc oxide-based desulfurizer prepared by using the pseudo-boehmite as a catalyst carrier and the alumina sol as a binder has strong wear resistance, large specific surface area and pore volume, and is particularly suitable for the working conditions of fluidized bed adsorption desulfurization and regeneration; the zinc oxide based microsphere desulfurizer prepared by utilizing the spray drying and forming technology is particularly suitable for the working conditions of fluidized bed adsorption desulfurization and regeneration.

Two kinds of metal oxide desulfurizing agents used in examples of the present application are illustrated.

The desulfurizing agent DS1 is prepared by the following method: 715g of alumina sol (Al)₂O₃21%) and 2285g of deionized water were added, 192g of pseudo-boehmite (32% weight loss) was slowly added with stirring, and after stirring for 2.0 hours, 32g of ammonium dihydrogen phosphate, 235g of copper nitrate and 2520g of basic zinc carbonate were slowly added with stirring, followed by further stirring for 5.0 hours. Spray drying and forming under the conditions of the hearth temperature of 400 ℃, the outlet temperature of 200 ℃ and the spray pressure of 4.0 MPa. The formed adsorbent is dried for 5.0 hours at 150 ℃ and roasted for 5.0 hours at 600 ℃ to obtain the desulfurizing agent DS 1.

The desulfurizing agent DS2 is prepared by the following method: 715g of alumina sol (Al)₂O₃21%) and 2285g of deionized water were added, 192g of pseudo-boehmite (32% weight loss) was slowly added with stirring, and after stirring for 2.0 hours, 32g of ammonium dihydrogen phosphate, 206g of copper nitrate and 2520g of basic zinc carbonate were slowly added with stirring, followed by further stirring for 5.0 hours. Spray drying and forming under the conditions of the hearth temperature of 400 ℃, the outlet temperature of 200 ℃ and the spray pressure of 4.0 MPa. The formed adsorbent is dried at 150 DEG CDrying for 5.0 hours, and roasting for 5.0 hours at 600 ℃ to obtain the desulfurizing agent DS 2.

The physical properties of the desulfurizing agent DS1 and the desulfurizing agent DS2 are shown in Table 1.

TABLE 1 physical Properties of desulfurizing agent