US2545389A - Method for increasing the sulfur dioxide content of the cooking acid used in the manufacture of sulfite pulp - Google Patents
Method for increasing the sulfur dioxide content of the cooking acid used in the manufacture of sulfite pulp Download PDFInfo
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- US2545389A US2545389A US706008A US70600846A US2545389A US 2545389 A US2545389 A US 2545389A US 706008 A US706008 A US 706008A US 70600846 A US70600846 A US 70600846A US 2545389 A US2545389 A US 2545389A
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- United States
- Prior art keywords
- sulfur dioxide
- manufacture
- cooking acid
- aminocymene
- sulfur
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- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 title claims description 94
- 239000002253 acid Substances 0.000 title claims description 20
- 238000000034 method Methods 0.000 title claims description 20
- 238000010411 cooking Methods 0.000 title claims description 14
- 238000004519 manufacturing process Methods 0.000 title claims description 11
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 title claims description 3
- IBDUWDDUJSWRTJ-UHFFFAOYSA-N 5-methyl-2-propan-2-ylaniline Chemical compound CC(C)C1=CC=C(C)C=C1N IBDUWDDUJSWRTJ-UHFFFAOYSA-N 0.000 claims description 14
- 239000000203 mixture Substances 0.000 claims description 14
- 238000010521 absorption reaction Methods 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 9
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 7
- 229910052717 sulfur Inorganic materials 0.000 claims description 6
- 239000011593 sulfur Substances 0.000 claims description 6
- 239000000047 product Substances 0.000 claims description 5
- 230000003647 oxidation Effects 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 3
- 239000013589 supplement Substances 0.000 claims description 2
- XLYOFNOQVPJJNP-PWCQTSIFSA-N Tritiated water Chemical compound [3H]O[3H] XLYOFNOQVPJJNP-PWCQTSIFSA-N 0.000 claims 1
- 239000007789 gas Substances 0.000 description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 16
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 239000003513 alkali Substances 0.000 description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 5
- 230000002745 absorbent Effects 0.000 description 4
- 239000002250 absorbent Substances 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 229930007927 cymene Natural products 0.000 description 3
- HFPZCAJZSCWRBC-UHFFFAOYSA-N p-cymene Chemical compound CC(C)C1=CC=C(C)C=C1 HFPZCAJZSCWRBC-UHFFFAOYSA-N 0.000 description 3
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 229920001131 Pulp (paper) Polymers 0.000 description 1
- BUGBHKTXTAQXES-UHFFFAOYSA-N Selenium Chemical compound [Se] BUGBHKTXTAQXES-UHFFFAOYSA-N 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- -1 amino compound Chemical class 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 150000004679 hydroxides Chemical class 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229910052711 selenium Inorganic materials 0.000 description 1
- 239000011669 selenium Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 1
Images
Classifications
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C3/00—Pulping cellulose-containing materials
- D21C3/04—Pulping cellulose-containing materials with acids, acid salts or acid anhydrides
- D21C3/06—Pulping cellulose-containing materials with acids, acid salts or acid anhydrides sulfur dioxide; sulfurous acid; bisulfites sulfites
Definitions
- the gas obtained in this way usually contains only 9-12% by volume of sulfundioxide, and often even less than that, whereas it is possible to obtain gas mixtures containing 17-18% by volme of sulfur dioxide by burning elementary sulfur.
- the present invention is concerned with obtaining the advantages that would accompany the use of liquid sulfur dioxide for preparing the cooking acid in the manufacture of sulte pulp by concentrating a part ofthe pyrites oven gases 3 Claims. (Cl. 23 ⁇ -129) to a strength of nearly sulfur dioxide (the rest being water vapor).
- the concentrated sul'- fur dioxide gas thus obtained is Amixed in suitableproportions with, for example, the main portion of the 9-12% gases from the pyrites oven or with the tower or cooking acid. In this manner it is possible to adjust the sulfur 'dioxide content of the cooking acid to whatl the chips or, respectively, the finished pulp demands.
- the method presented in this invention does not involve any great expense for construction or operation. There is usually enough space already available, considering the normal high constructionv of pyrites ovens, and it is leasy to make the apparatus automatic in operations necessitating onlyv a minimum amount of manuallabor'.
- the expenses incurred for heat are small, for it is possible to utilize for the purpose, forexample, the excess of low-grade heat always available in a pulp mill.
- the loss of heat in the method presented in this invention is quite insignificant, inasmuch as it is easy to install heat exchangers to recover the heat liberated in the/process.
- an absorption tower I equipped with plates or grates and lled with Raschig rings or the like or in some other way so arranged as to bring about as great a contacct surface as possible between gas and liquid.
- the gas mixture coming from the pyritesoven containing, for example, 10% sulfur dioxide gas, is'introduced into the bottom of the absorption tower 2.
- rmeansof a pump 3 a mixture of wateriand absorbent at suitably 30 C; is pumped from -container 4 through the pipeline 5to the top ofthe absorption tower, where the absorption mixture sulfur dioxide, is conducted through pipeline 6 to container 1.
- the absorbent used according to this invention is Z-aminocymene, suitably mixed with water in the proportion of 1:1.
- the aggregate is so dimensioned and the flow of gas and absorbent mixture so regulated that the gas mixture issuing from the upper end of the tower through pipeline 8 has a residual sulfur dioxide content of about 0.1% and can thus be released into the air without causing trouble.
- the gas stream carries with it small amounts of amine, corresponding to the partial pressure of the latter. These latter are recovered in a scrubber 9 by the aid of sulfuric acid (which forms solid compounds with them), alkali bisulte, or oily substances.
- the aminocymene may be separated in separator 9a by heating with alkali, and from the last-named it may be separated, depending on the nature of the oil, by fractional distillation or some other known method. After separation, the sulfuric acid, bisulte solution, or oil is transferred to container 28 and thence put into the process again by pump 29 via pipeline 30.
- the sulfur dioxide solution received in container 1 is suitably at ⁇ a temperature of about 30 C. and contains 100-130 gm. sulfur dioxide (that can be boiled 01T) per 1 liter absorption mixture (water: aminocymene in proportion of 1:1).
- the sulfur dioxide solution is pumped by a pump I I through pipeline I2 through the heat exchangers I3, I4 and I5 to the regeneration tower I5, which is -llled with, for example, Raschig rings.
- the sulfur dioxide containing mixture of aminocymene and water is here met in its downward passage by a stream of steam (and liberated SO2) generated in the boiler I'I and injected through pipeline I8.
- pipeline I 9 issues a mixture Vof sulfur dioxide and steam including some amino compound, the heat liberated by the condensing steam ⁇ being recovered in I4.
- Heat exchanger I5 utilizes partly the heat from the aminocymenewater mixture freed of sulfur dioxide and returning from the regenerating tower through pipeline :20 to boiler II and partly heat obtained from the water of condensation in the steam coil of boiler I 'I through pipe 2I.
- the boiler I1 is coupled below to a separatory funnel 22, in which the water and aminocymene 4 are separated from one another after removal of the sulfur dioxide.
- the water contains sulfur troxide, the product of oxidation of sulfur dioxide, in the form of for example, sodium sulfate, thio-acids as sodium salts, and the excess alkali, which was changed to bisulte in the absorption tower, has almost entirely changed to sulite during the boiling.
- the aminocymene is returned through pipeline 23 to container 4 to take part in the circulation again.
- a portion of the water solution is transferred through pipeline 24 from 22 to apparatus 25, which is equipped with a reflux condenser and a mixer, and to which is .piped also through line 26 the aminocymene recovered from scrubber 9 in separator 9a.
- apparatus 25 which is equipped with a reflux condenser and a mixer, and to which is .piped also through line 26 the aminocymene recovered from scrubber 9 in separator 9a.
- the gas coming from heat exchanger I4 is further cooled in condenser tower 3
- the absorbing substance used according to this invention is aminocymene.
- Cymene the raw material for this substance, is .obtained as ra side-product in the production of sulte pulp and has so far found no other considerable use.
- the yield of aminocymene in synthesis from cymene is about About OF5-1.5 kg. of aminocymene are lost per ton of sulfur dioxide concentrated. Calculated as NaOH about 9-12 kg. of soda are used per ton of sulfur dioxide and about 1.0-1.3 tons of normal steam.
- This heat may, however, as already mentioned be supplied by utilizingthe low-grade heat usually abundantly available in connection with pulp manufacture. .Inasmuch as the whole process ,according to this invention can also easily be made to operate automatically, this method offers many advantages in solving the problem of a strong cooking acid.
- the method of .concentrating sulfur dioxide gases by means of a mixture of aminocymene and water can naturally be applied in all industries inwhich gases containing sulfur dioxide are available, for instance themetallurgic industries.
- a method of increasing the sulfur dioxide content of the cooking acid in connection with the manufacture of sulte pulp which comprises, diverting a portion of the gas supply, concentrating the sulfur dioxide in the said diverted ⁇ portion ⁇ of -said gas supply by means of absorbing in a mixture of 2-aminocymene and water, boiling ofi the sulfur dioxide and retaining oxidation products of sulfur dioxide in the absorption liquid, and thereafter introducing said concentrated sulfur dioxide to supplement the sulfur dioxide content of thecooking acid.
- a method according to claim 1 wherein the 2-aminocymene used is prepared by synthesis from cymene obtained in the production of sulte pulp.
Landscapes
- Gas Separation By Absorption (AREA)
Description
Patented Mar.J 13, 1951 METHOD FOR INCREASING THE SULFUR DIOXIDE CONTENT OF THE COOKING ACID USED IN THE `MANUFACTURE OF SULFITE PULP Vin Herman Somer, Lauritsala, and Tor Erik Brehmer, Jarvenpaa, Finland, assignors, by direct and mesne assignments, of one-half to said Somer and one-half to Aktiebolage Kaukas Fabrik, Lauritsala, Finland v Application october 26, 1946, serial No. 706,008 In Finland January 30, 1946 The present tendency in the manufacture of 'chemical pulp by the sulflte method is to use as strong a cooking acid as possible, i. e., an acid with a high content of sulfur dioxide. This is because a strong acid impregnates the chips better than a weak one, and the time required for the cook can thus be shortened appreciably. The pulp thus obtained is better and, before all,
Y more even in quality, which is of great importance particularly in view of the growing demand for high grade pulp of the articial fiber industry. A contributory cause for the increased necessity for a stronger cooling acid lies in the fact that the pulp mills are nowadays for various reasons seldom in a position to use dry and seasoned logs andhave mostly to `content themselves with such that are green or recently floated. As a result the water content of theA chips may rise as high as 55-57%, whereas seasoned logs generally contain but approximately 20-25% of water.
It is more difficult nowadays to secure a stronger cooking acid due to the fact that the Finnish sulte pulp mills are at present obliged to produce their sulfur dioxide by roasting pyrites. The gas obtained in this way usually contains only 9-12% by volume of sulfundioxide, and often even less than that, whereas it is possible to obtain gas mixtures containing 17-18% by volme of sulfur dioxide by burning elementary sulfur.
Outside of the usual gasification in which the gaseous products are cooled and conducted into the tower acid for increasing the sulfur dioxide content of the cooking acid, several other methods have been developed based on the utilization of the gasification products. However, these methods are neither sufficiently flexible nor fast enough, the apparatus needed is often expensive, and only a limited variation of the cooking vacid sulfur dioxide content is possible. Naturally, the use of liquid sulfur dioxide to add to the tower acid would give unlimited possibilities for varying the cooking acid strength, but such a method could hardly be economically carried out in view of the expense in production and transportation of the liquid sulfur dioxide involved (drying the sulfur dioxide gas, liquifyi'ng, storage in pressure containers, transfer to 'l atm. pressure tank cars, shipping, etc.).
The present invention is concerned with obtaining the advantages that would accompany the use of liquid sulfur dioxide for preparing the cooking acid in the manufacture of sulte pulp by concentrating a part ofthe pyrites oven gases 3 Claims. (Cl. 23`-129) to a strength of nearly sulfur dioxide (the rest being water vapor). The concentrated sul'- fur dioxide gas thus obtained is Amixed in suitableproportions with, for example, the main portion of the 9-12% gases from the pyrites oven or with the tower or cooking acid. In this manner it is possible to adjust the sulfur 'dioxide content of the cooking acid to whatl the chips or, respectively, the finished pulp demands.
The method presented in this invention does not involve any great expense for construction or operation. There is usually enough space already available, considering the normal high constructionv of pyrites ovens, and it is leasy to make the apparatus automatic in operations necessitating onlyv a minimum amount of manuallabor'. The expenses incurred for heat are small, for it is possible to utilize for the purpose, forexample, the excess of low-grade heat always available in a pulp mill. Moreover the loss of heat in the method presented in this invention is quite insignificant, inasmuch as it is easy to install heat exchangers to recover the heat liberated in the/process.
The expenditures for chemicalsconstitute only a small fraction ofthe total costs Yin the production of liquid sulfur dioxide, and this item of expense is the only onev that remains unchanged for the production of highly concentrated sulfur dioxide gasin accordance with the present invention. l
We will explain the method according to this invention with reference to the. accompanying drawing, which is a schematic representation of a plant for concenrtation of sulfur dioxide gas.
In connection with the pyrites oven there is erected an absorption tower I equipped with plates or grates and lled with Raschig rings or the like or in some other way so arranged as to bring about as great a contacct surface as possible between gas and liquid. The gas mixture coming from the pyritesoven, containing, for example, 10% sulfur dioxide gas, is'introduced into the bottom of the absorption tower 2. -By
rmeansof a pump 3 a mixture of wateriand absorbent at suitably 30 C; is pumped from -container 4 through the pipeline 5to the top ofthe absorption tower, where the absorption mixture sulfur dioxide, is conducted through pipeline 6 to container 1.
The absorbent used according to this invention is Z-aminocymene, suitably mixed with water in the proportion of 1:1. The aggregate is so dimensioned and the flow of gas and absorbent mixture so regulated that the gas mixture issuing from the upper end of the tower through pipeline 8 has a residual sulfur dioxide content of about 0.1% and can thus be released into the air without causing trouble. The gas stream carries with it small amounts of amine, corresponding to the partial pressure of the latter. These latter are recovered in a scrubber 9 by the aid of sulfuric acid (which forms solid compounds with them), alkali bisulte, or oily substances. From the two rst-named of these scrubber substances the aminocymene may be separated in separator 9a by heating with alkali, and from the last-named it may be separated, depending on the nature of the oil, by fractional distillation or some other known method. After separation, the sulfuric acid, bisulte solution, or oil is transferred to container 28 and thence put into the process again by pump 29 via pipeline 30..
The heat developed in the absorption tower by the solution of the sulfur dioxide is removed by means of a cooling arrangement I inserted between the diierent units of the tower. In this man-ner it is possible to avoid the expense attendant on the otherwise necessary numerous conduits for gas and absorbent fluid between a plurality of towers.
The sulfur dioxide solution received in container 1 is suitably at `a temperature of about 30 C. and contains 100-130 gm. sulfur dioxide (that can be boiled 01T) per 1 liter absorption mixture (water: aminocymene in proportion of 1:1).
Wherever sulfur dioxide comes into contact with water sulfur trioxide is formed. This reaction is catalysed by a number Vof substances, such as arsenic and selenium. There are also other substances that retard this reaction. We may reckon with an oxidation of k0.5-1.5% .of the sulfur dioxideV gas streaming through the absorption tower to sulfur troxide, in addition to which some thioacids are also formed. In order to bind these we may add to the tower liquid alkali or alkali earth hydroxides or carbonates. It is, however, not so advantageous to use the latter of these as their use leads to the formation of insoluble alkaline earth sulfates. Y
From container I the sulfur dioxide solution is pumped by a pump I I through pipeline I2 through the heat exchangers I3, I4 and I5 to the regeneration tower I5, which is -llled with, for example, Raschig rings. The sulfur dioxide containing mixture of aminocymene and water is here met in its downward passage by a stream of steam (and liberated SO2) generated in the boiler I'I and injected through pipeline I8. Through pipeline I 9 issues a mixture Vof sulfur dioxide and steam including some amino compound, the heat liberated by the condensing steam `being recovered in I4. Heat exchanger I5 utilizes partly the heat from the aminocymenewater mixture freed of sulfur dioxide and returning from the regenerating tower through pipeline :20 to boiler II and partly heat obtained from the water of condensation in the steam coil of boiler I 'I through pipe 2I.
'The boiler I1 is coupled below to a separatory funnel 22, in which the water and aminocymene 4 are separated from one another after removal of the sulfur dioxide. The water contains sulfur troxide, the product of oxidation of sulfur dioxide, in the form of for example, sodium sulfate, thio-acids as sodium salts, and the excess alkali, which was changed to bisulte in the absorption tower, has almost entirely changed to sulite during the boiling. Giving on' its heat in exchanger I3, the aminocymene is returned through pipeline 23 to container 4 to take part in the circulation again.
Either continuously or at intervals determined 'by analysis a portion of the water solution is transferred through pipeline 24 from 22 to apparatus 25, which is equipped with a reflux condenser and a mixer, and to which is .piped also through line 26 the aminocymene recovered from scrubber 9 in separator 9a. By adding lye and heating the small quantities of aminocymene contained in the water are liberated, rise to the surface, and are then returned to .circulation through pipeline 2,'I.. The remaining water solution goes to the drain, possibly after recover- .ing the sodium sulfate still contained therein.
The gas coming from heat exchanger I4 is further cooled in condenser tower 3|, from which it issues .as about 99% sulfur dioxide.
As mentioned before, the absorbing substance used according to this invention is aminocymene. Cymene, the raw material for this substance, is .obtained as ra side-product in the production of sulte pulp and has so far found no other considerable use. The yield of aminocymene in synthesis from cymene is about About OF5-1.5 kg. of aminocymene are lost per ton of sulfur dioxide concentrated. Calculated as NaOH about 9-12 kg. of soda are used per ton of sulfur dioxide and about 1.0-1.3 tons of normal steam. This heat may, however, as already mentioned be supplied by utilizingthe low-grade heat usually abundantly available in connection with pulp manufacture. .Inasmuch as the whole process ,according to this invention can also easily be made to operate automatically, this method offers many advantages in solving the problem of a strong cooking acid.
The methods described above can, of course, easily be suited also to the use of a sulte pulp mill burning elemental sulfur for its sulfur dioxide supply. In a like manner the concentration of sulfur dioxide can also be carried through with the gases that at the decompression flow to the acid tower after having passed` through the acid cistern, and which often .exert a disturbine influence `on the operation of the tower, or with the blow-oi gases.
The method of .concentrating sulfur dioxide gases by means of a mixture of aminocymene and water can naturally be applied in all industries inwhich gases containing sulfur dioxide are available, for instance themetallurgic industries.
What is claimed is:
1. A method of increasing the sulfur dioxide content of the cooking acid in connection with the manufacture of sulte pulp which comprises, diverting a portion of the gas supply, concentrating the sulfur dioxide in the said diverted `portion `of -said gas supply by means of absorbing in a mixture of 2-aminocymene and water, boiling ofi the sulfur dioxide and retaining oxidation products of sulfur dioxide in the absorption liquid, and thereafter introducing said concentrated sulfur dioxide to supplement the sulfur dioxide content of thecooking acid.
2. A method according to claim 1 wherein the absorption liquid mixture is substantially one part of water and one part of Z-aminocymene.
3. A method according to claim 1 wherein the 2-aminocymene used is prepared by synthesis from cymene obtained in the production of sulte pulp.
VIN HERMAN SOMER. TOR ERIK BREHMER.
REFERENCES CITED The following references are of record in the file of this patent:
Number OTHER REFERENCES Lucas: Organic Chemistry, American Book Co., N. Y., 1935, page 350.
Claims (1)
1. A METHOD OF INCREASING THE SULFUR DIOXIDE CONTENT OF THE COOKING ACID IN CONNECTION WITH THE MANUFACTURE OF SULFITE PULB WHICH COMPRISES, DIVERTING A PORTION OF THE GAS SUPPLY, CONCENTRATING THE SULFUR DOIXIDE IN THE SAID DIVERTED PORTION OF SAID GAS SUPPLY BY MEANS OF ABSORBING IN A MIXTURE OF 2-AMINOCYMENE AND WATER, BOILING OFF THE SULFUR DIOXIDE AND RETAINING OXIDATION PRODUCTS OF SULFUR DIOXIDE IN THE ABSORPTION LIQUID, AND THEREAFTER INTRODUCING SAID CONCENTRATED SULFUR DIOXIDE TO SUPPLEMENT THE SULFUR DIOXIDE CONTENT OF THE COOKING ACID.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI2545389X | 1946-01-30 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2545389A true US2545389A (en) | 1951-03-13 |
Family
ID=8566492
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US706008A Expired - Lifetime US2545389A (en) | 1946-01-30 | 1946-10-26 | Method for increasing the sulfur dioxide content of the cooking acid used in the manufacture of sulfite pulp |
Country Status (2)
| Country | Link |
|---|---|
| US (1) | US2545389A (en) |
| ES (1) | ES174684A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2922735A (en) * | 1956-12-18 | 1960-01-26 | Texas Gulf Sulphur Co | Method of producing pulping liquor |
| US3059995A (en) * | 1960-05-11 | 1962-10-23 | Chemical Construction Corp | Production of sulfur dioxide |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1740342A (en) * | 1925-10-08 | 1929-12-17 | Ig Farbenindustrie Ag | Recovery of sulphurous acid from waste gases |
| US1893385A (en) * | 1929-05-15 | 1933-01-03 | Soc Of Chemical Ind | Process for obtaining concentrated sulphur dioxide |
| US1941592A (en) * | 1931-11-21 | 1934-01-02 | Raymond F Bacon | Roasting pryites fines |
| US2009757A (en) * | 1930-08-12 | 1935-07-30 | William Blythe & Company Ltd | Treatment of toluidine bases |
| US2014775A (en) * | 1929-10-01 | 1935-09-17 | Ralph H Mckee | Process of preparing sulfite cooking liquor |
| US2047032A (en) * | 1934-09-28 | 1936-07-07 | Brown Co | Process of correlating chemical recovery in pulp mills operating with different kinds of liquors |
| US2047819A (en) * | 1932-10-27 | 1936-07-14 | Maitland C Boswell | Process of separating sulphur dioxide from gaseous mixtures |
| US2186453A (en) * | 1938-01-17 | 1940-01-09 | Guggenheim Brothers | Recovery of sulphur dioxide |
-
1946
- 1946-08-21 ES ES174684A patent/ES174684A1/en not_active Expired
- 1946-10-26 US US706008A patent/US2545389A/en not_active Expired - Lifetime
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1740342A (en) * | 1925-10-08 | 1929-12-17 | Ig Farbenindustrie Ag | Recovery of sulphurous acid from waste gases |
| US1893385A (en) * | 1929-05-15 | 1933-01-03 | Soc Of Chemical Ind | Process for obtaining concentrated sulphur dioxide |
| US2014775A (en) * | 1929-10-01 | 1935-09-17 | Ralph H Mckee | Process of preparing sulfite cooking liquor |
| US2009757A (en) * | 1930-08-12 | 1935-07-30 | William Blythe & Company Ltd | Treatment of toluidine bases |
| US1941592A (en) * | 1931-11-21 | 1934-01-02 | Raymond F Bacon | Roasting pryites fines |
| US2047819A (en) * | 1932-10-27 | 1936-07-14 | Maitland C Boswell | Process of separating sulphur dioxide from gaseous mixtures |
| US2047032A (en) * | 1934-09-28 | 1936-07-07 | Brown Co | Process of correlating chemical recovery in pulp mills operating with different kinds of liquors |
| US2186453A (en) * | 1938-01-17 | 1940-01-09 | Guggenheim Brothers | Recovery of sulphur dioxide |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2922735A (en) * | 1956-12-18 | 1960-01-26 | Texas Gulf Sulphur Co | Method of producing pulping liquor |
| US3059995A (en) * | 1960-05-11 | 1962-10-23 | Chemical Construction Corp | Production of sulfur dioxide |
Also Published As
| Publication number | Publication date |
|---|---|
| ES174684A1 (en) | 1946-10-01 |
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