TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The condensation catalyst comprises a zeolite. The slurry catalyst comprises a poison-tolerant catalyst (preferably sulfided catalyst).    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Components: The dried glycol comprises water ( less than or equal to 35 wt.%). The digestion solvent comprises an organic solvent and water (preferably glycerol and water). The organic solvent comprises at least one solvent selected from ethanol, ethylene glycol, propylene glycol and/or glycerol. The digestion solvent or solvent further comprises a monohydric alcohol. The organic component further comprises a methoxyphenol or methanol.    TECHNOLOGY FOCUS - POLYMERS - In the method (M1), at least 5 wt.% of the cellulosic biomass solids are converted into the glycol. The method (M1) further involves separating the dried glycol from the dried reaction product; exposing the dried glycol or a product formed from it to a condensation catalyst; and converting the dried glycol into a higher molecular weight compound using the condensation catalyst. Converting the cellulosic biomass solids into the reaction product takes place in a hydrothermal digestion unit in the presence of a digestion solvent and a slurry catalyst capable of activating molecular hydrogen. At least partially drying the reaction product takes place external to the hydrothermal digestion unit. The slurry catalyst is distributed in the cellulosic biomass solids using fluid flow. The slurry catalyst is circulated through a fluid circulation loop external to the hydrothermal digestion unit. Converting the cellulosic biomass solids into the reaction product further involves heating the cellulosic biomass solids in the presence of the digestion solvent to form a liquor phase comprising soluble carbohydrates, and performing a first catalytic reduction reaction on the soluble carbohydrates to at least partially form the reaction product. The method further involves: removing at least a portion of the liquor phase from the hydrothermal digestion unit and recirculating at least a portion of the removed liquor phase to it, the removed liquor phase also containing at least a portion of the slurry catalyst; performing a second catalytic reduction reaction on the liquor phase external to the hydrothermal digestion unit so as to increase a quantity of the glycol in the reaction product; and returning at least a portion of the dried glycol to the hydrothermal digestion unit. The cellulosic biomass solids are converted into the reaction product in the presence of a solvent (preferably organic solvent and water). At least partially drying the reaction product includes a distillation to separate water from the glycol. The method (M1) preferably involves: providing cellulosic biomass solids and a slurry catalyst in a hydrothermal digestion unit, the slurry catalyst is capable of activating molecular hydrogen; heating the cellulosic biomass solids in the hydrothermal digestion unit in the presence of the slurry catalyst, a digestion solvent, and molecular hydrogen, thus forming a liquor phase comprising soluble carbohydrates; and performing a first catalytic reduction reaction on the soluble carbohydrates within the hydrothermal digestion unit, thus at least partially converting the soluble carbohydrates into a reaction product comprising a glycol. Preferred Composition: The composition further comprises cellulosic biomass solids; and hydrogen. EXAMPLE - A reactor was charged with deionized water (60.16 ml), potassium carbonate buffer (0.195 g), and DC-2534 (RTM: nickel-oxide promoted cobalt molybdate catalyst containing 1-10% cobalt oxide and molybdenum trioxide (up to 30 wt.%) on alumina, and less than 2% nickel) (0.754 g) was added. The catalyst was previously sulfided. The reactor was charged with southern pine mini-chips (39% moisture) (5.1 g) having nominal dimensions of 3 mmx 5 mmx 5 mm, before pressurizing with 53 bars of hydrogen. The stirred reactor was heated to 190 degrees C for 1 hour before ramping over 15 minutes to a temperature of 250 degrees C and holding to complete a 5-hour cycle. At the end of a reaction cycle, aqueous product (5 g) was withdrawn via a sample line fitted with a 0.5 micron sintered metal filter, to retain catalyst in the reactor. Wood ( approximately 5 g) was added to the reactor to initiate another reaction cycle, along with buffer (0.05-0.15 g) as needed to maintain the pH of 5-6. This process was repeated over multiple cycles. After 4 cycles, the reaction product was analyzed by gas chromatography using a 60 mx 0.32 mm ID DB-5 column of 1 mu m thickness, with 50:1 split ratio, 2 ml/minute helium flow, and column oven at 40 degrees C for 8 minutes, followed by a ramp to 285 degrees C at 10 degrees C/minute, and a hold time of 53.5 minutes. The injector temperature was set at 250 degrees C, and the detector temperature was set at 300 degrees C. A range of alkanes, monooxygenated aldehydes and ketones, glycols, and polyols were observed in the aqueous phase, each with volatility greater than 6C sugar alcohol sorbitol. The observed product (29.4 wt.%) yield comprised ethylene glycol and 1,2-propylene glycol, while another 8.8 wt.% comprised glycerol. The digestion process was repeated, except the digestion solvent comprised 45% propylene glycol and 5% ethylene glycol in deionized water. In this case, the reaction sequence was repeated over 20 cycles without plugging of the sintered metal filter occurring, thus showing that greater solubility was achieved in the presence of an organic solvent.